WO2025235319A1

WO2025235319A1 - Methods and compositions for production of carbohydrates from co2 by a chemolithoautotroph

Info

Publication number: WO2025235319A1
Application number: PCT/US2025/027497
Authority: WO
Inventors: Kenneth Zahn; John S. Reed; Dan E. Robertson
Original assignee: Kiverdi Inc
Current assignee: Kiverdi Inc
Priority date: 2024-05-09
Filing date: 2025-05-02
Publication date: 2025-11-13
Anticipated expiration: 2026-11-09

Abstract

Microorganisms and bioprocesses are provided that convert gaseous C1 containing substrates, such as syngas, producer gas, and renewable H2 combined with CO2, into nutritional and other useful bioproducts. Disclosed herein are microorganisms containing that are capable of growing on gaseous carbon dioxide, gaseous hydrogen, syngas, or combinations thereof. The application describes methods for production of glucose and the glucose polymer starch and other polysaccharides by CO2-fixing chemoautotroph strains. The invention includes a method of production wherein the organisms are cultivated microaerobically or aerobically in a bioreactor using CO2, H2 and O2 in an oxyhydrogen fermentation and methods for recovery and purification of secreted glucose, intracellular starch, and other polysaccharides.

Description

METHODS AND COMPOSITIONS FOR PRODUCTION OF CARBOHYDRATES FROM CO2 BY A CHEMOLITHOAUTOTROPH GOVERNMENT FUNDING [01] This invention was made with government support under Contract No. N66001222C4034 awarded by Defense Advanced Research Projects Agency. The U.S. government may therefore have certain rights in the invention. CROSS-REFERENCE TO RELATED APPLICATIONS [02] This application claims the benefit of US Provisional Application Nos.63/644,905, filed on May 9, 2024, and 63/644,909, filed on May 9, 2024, both of which are incorporated by reference herein in their entireties. FIELD OF THE INVENTION [03] The inventive subject matter relates to the biological production of sugars, starch, carbohydrates, polysaccharides, and other biomass constituents, in a microbial system, using a gaseous substrate such as synthesis gas or producer gas or pyrolysis gas or H₂ and CO2 gas mixtures, as a carbon and energy source. The invention also relates to the use of sugars and/or polysaccharides, alone, or in combination with microbial amino acids, proteins, and other biomass constituents to feed or provide nutrients to other heterotrophic organisms, animals, or humans. Sugars, starch, carbohydrates, polysaccharides, amino acids, proteins, and other biomass constituents produced according to the present invention can be consumed and used as nutrients by other organisms for the production of food and other bio-based products. [04] This disclosure relates to compositions capable of producing and methods of producing sugars, starch, carbohydrates, polysaccharides, and other biomass constituents through cultivating bacteria or other microorganisms that grow on carbon-containing gases such as syngas, producer gas, CO₂, carbon monoxide and mixtures of the same containing hydrogen gas. This disclosure further relates to methods of fixing carbon from gaseous input into useful organic molecules such as sugars, starch, carbohydrates, polysaccharides, and other nutrients. The bacteria and/or microorganisms of the invention can be genetically engineered for use in the methods or other aspects of the invention described herein. In some other aspects of the invention described herein the microorganisms are not genetically engineered. [05] This disclosure further relates to methods of fixing carbon from gas into useful organic molecules such as sugars, starch, carbohydrates, polysaccharides, and other biomass constituents. The present invention further describes mechanisms to confer to an organism the ability to produce, and/or to enhance production by an organism of, carbon-based products, through the conversion of carbon dioxide, or other inorganic carbon sources, and inorganic energy, including chemical energy from an inorganic chemical, or directly from an electrical source, into carbon-based products, and in particular sugars, starch, carbohydrates, polysaccharides, and other biomass constituents of commercial value. [06] The present invention falls within the technical areas of carbon capture, carbon dioxide-to-chemicals, carbon recycling, carbon sequestration, energy storage, syngas conversions, and renewable/alternative and/or low carbon dioxide emission sources of energy. Specifically, the present invention is a unique example of the use of biocatalysts within a biological and chemical process to fix carbon dioxide and/or other forms of inorganic carbon and/or or other C1 carbon sources into organic chemical products in a non- photosynthetic process powered by low carbon emission energy sources and/or waste energy sources. In addition, the present invention involves the production of chemical co- products that are co-generated through carbon-fixation reaction steps as part of an overall carbon capture and conversion process. The bacteria of the invention can be genetically engineered for use in some of the methods or other aspects of the invention described herein. The present invention further describes mechanisms to confer and/or enhance production of carbon-based products of commercial value without dependence upon agriculture. BACKGROUND [07] Great interest and resources have been directed towards developing technologies that use renewable energy or waste energy for the conversion of carbon dioxide, or other low value carbon sources, into useful organic chemicals in order to provide alternatives to chemicals, materials and fuels derived from petroleum or other fossil sources. Most of the focus in the area of CO2 conversion has been placed on biological approaches that utilize photosynthesis to fix CO2 into biomass or end-products, while some effort has been directed at fully abiotic and chemical processes for fixing CO₂. [08] Biologic systems that fix gaseous carbon and particularly CO₂ through natural biochemical metabolic processes are well known and have been utilized for thousands of years. The current agricultural system, based on photosynthesis in higher plant crops, is one primary example. Algal systems have also been developed to create food and other agriculturally derived products from CO₂ through photosynthetic reactions. There are also heterotrophic reactions and productions utilizing fixed carbon feedstocks, such as sugar, which indirectly depend upon photosynthesis. Animal husbandry and aquaculture generally at the present time have as ultimate inputs, the products of photosynthesis, in the form of various feeds. Artificial or compound feeds are commonly used which are mixtures of feedstuffs, and vitamin and mineral premixes that are formulated to contain desired levels of essential nutrients and energy. These feeds are often the products of agriculturally produced crops. Or, in some cases, they are sourced from the harvesting or foraging of wild organisms in nature. At the base of this production is generally a photosynthetic trophic layer of primary producers, which are either consumed directly or indirectly. An example of food production which serves to illustrate the direct consumption of wild photosynthetic primary producers is grazing livestock on uncultivated lands. An example which serves to illustrate food production through the indirect consumption of wild photosynthetic primary producers is the use of fishmeal in aquaculture, derived from wild fish stocks such as sardines and anchovies, which in turn feed on photosynthetic algae. However, a number of problems and limitations are confronting the further expansion and growth of current agricultural, animal husbandry, and aquaculture practices, and the photosynthetically based feeds and energy and carbon sources which are currently utilized. [09] A type of CO2-to-organic chemical and/or biomolecule approach that has received relatively less attention is hybrid chemical/biological processes where the biological step is limited to CO₂ fixation alone, corresponding to the dark reaction of photosynthesis. The potential advantages of such a hybrid CO₂-to-organic chemical process include the ability to combine enzymatic capabilities gained through billions of years of evolution in fixing CO2, with a wide array of abiotic technologies to power the process such as solar PV, solar thermal, wind, geothermal, hydroelectric, or nuclear. A hybrid system combining and integrating an abiotic energy conversion step with a biological CO₂ fixing step can enable an efficient and clean production process converting CO2 and/or other C1 carbon sources into valuable biochemicals and biopolymers. [10] Microorganisms performing carbon fixation without light can be contained in more controlled and protected environments, less prone to water and nutrient loss, contamination, or weather damage, than what can practically be used for culturing photosynthetic microorganisms. Furthermore, an increase in bioreactor capacity can be met with vertical rather than horizontal construction, making it potentially far more land efficient. A hybrid chemical/biological system offers the possibility of a CO2-to-organic chemical process that avoids many drawbacks of photosynthesis while retaining the biological capabilities for complex organic synthesis from CO2 and other simple inorganic inputs. [11] Chemoautotrophic microorganisms represent a little explored alternative to photosynthetic organisms for use in carbon fixation processes that can address many of the unmet needs described in this section, while avoiding the limitations of photosynthesis described herein. [12] Chemoautotrophic microorganisms are generally microbes that can perform CO2 fixation in an equivalent to the photosynthetic dark reaction, but which can get the reducing equivalents needed for CO2 fixation from an inorganic external source, rather than having to internally generate them through the photosynthetic light reaction. The chemosynthetic reactions performed by chemoautotrophs for the fixation of CO₂, and other forms of inorganic carbon, to organic compounds, are powered by potential energy stored in inorganic chemicals, rather than by the radiant energy of light [Shively et al. (1998) Annu. Rev. Microbiol.52:191-230; Smith et al. (1967) J Bacteriol 94(4): 972-983; Hugler et al. (2005) J Bacteriol 187(9): 3020-27; Scott and Cavanaugh (2007) Applied and Environmental Microbiology 73(4):1174-79]. [13] Carbon fixing biochemical pathways that occur in chemoautotrophs include the reductive tricarboxylic acid cycle, the Calvin-Benson-Bassham cycle [Shively et al. supra, van Kaulen, et al. (1998) Annu. Rev. Microbiol., 191-230], and the Wood-Ljungdahl pathway [Ljungdahl (1986) 40:415-50; Lee, et al. (2008) Biotechnology and Bioengineering 101(2): 209-228; Fischer, et al. (2008) Metabolic Engineering 10:295-304]. An energy harvesting step corresponding to, or substituting for, the photosynthetic light reaction must still occur upstream of the chemoautotrophic bioprocess, but it can utilize an abiotic process, such as, for example, harvesting light energy with a photovoltaic or solar thermal technology, and/or tapping into non-light energy sources such a wind, hydroelectric, or nuclear power. [14] Chemoautotrophic organisms are particularly well suited for hybrid chemical/biological processes for the conversion of CO2-to-organic chemicals where the biological step is limited to CO2 fixation alone. [15] It is believed that certain embodiments of the present invention utilizing oxyhydrogen type microorganisms for the chemosynthetic fixation of CO2 under carefully controlled oxygen levels may have advantages for the production of organic compounds and biopolymers such as glucose, carbohydrates, starch, and other polysaccharides. [16] Glucose is a common nutrient, sweetener, flavor enhancer, stabilizer, texture enhancer, humectant, preservative, and coating and bulking agent, as well as an energy and carbon source for aerobic and anaerobic fermentation. Glucose is produced in plants using photosynthesis and in other phyla via gluconeogenesis. [17] Glucose is produced industrially from starch by enzymatic hydrolysis using glucose amylase or by the use of acids. Industrial starch sources include corn, potato, rice and wheat. Annual worldwide production volume in 2019 was 83.5 million tons. The global glucose market size was estimated at USD 42.9 billion in 2020 and is expected to expand at a compound annual growth rate (CAGR) of 5.0% from 2020 to 2028. The escalating demand for confectionery, soft drink, and bakery products in the food and beverages sector that uses glucose (dextrose) as an ingredient is driving the market. Glucose has its demand across varied industry verticals such as food and beverages, pharmaceutical, cosmetic and personal care. [18] Industrial glucose and starch production have a large environmental footprint. Cultivation of a starch source requires water, land, and agricultural chemicals, and production results in large volumes of lignocellulosic waste. On the other hand, chemoautotrophic fermentation uses waste CO2 feedstock or CO2 captured from the air or other environmental sources and the oxyhydrogen type of chemoautotrophy produces no byproducts (e.g., CO2) other than H2O, has a minimal requirement for water, and minimizes carbon footprint. [19] Starch is a homopolymer of D-glucose units made of α-D-glucan chains. Native starch semi-crystalline granules are composed of amylose, a linear glucose chain attached by α-1,4 glucosidase bonds. The primary role of starch is energy storage in plants. In an animal's diet, starch is a source of sugar. Starch is present in the leaves of green plants, stems (sago), roots of the cassava plant, all vegetables, fruits (banana, plantain), tubers (potatoes, cassava), cereals (such as wheat, corn, maize, sorghum and, rice), and some algae. [20] Starch and its derivatives are used in the food industry either as food products or additives for thickening, preservation and a quality enhancer in baked foods, confectioneries, pastas, soups and sauces, and mayonnaises. Starch is also used in numerous industrial applications. This is because of its renewability, biodegradability, abundance, and cohesive film-forming properties. Moreover, the hydroxyl (OH) groups associated with the anhydroglucose units provide it with several modification possibilities. These features have resulted in substantial interests for its use in several advanced functional material applications in addition to the typical consumer plastic applications, electronics, drug delivery, pharmaceuticals, antimicrobial materials to structural materials. The global starch market was valued at US $418 million in 2024 and is anticipated to reach US $545 million by 2031, CAGR of 3.8% during the forecast period 2024-2031. [21] Sustainable and renewable sources of sugars, starch, carbohydrates, polysaccharides, and other nutrients and biomass constituents are needed to help meet growing food and other bioproduct and biomaterial needs. There is also a need to reduce the amount of carbon dioxide and other greenhouse gas (GHG) emissions to the atmosphere, as well as to reduce global energy consumption based upon coal, oil, and natural gas in food production systems. Increased demand in the global economy has placed increasing pressure on land and water resources. Increased pressure has also been placed on traditional fossil hydrocarbon inputs for the production of food and other agriculturally derived products. Many industries, including modern agriculture, rely heavily on the availability of fossil hydrocarbon sources as an input for the production and processing of crops. Cost-effective alternatives to current incumbent practices could help mitigate the upward pressure on land use, natural habitats, water, fossil resource demand, raw material costs, and greenhouse gas emissions. [22] Bacterial and other microbial cells have been applied to process sugar feedstocks into useful organic compounds such as ethanol, proteins, and amino acids in heterotrophic fermentation systems. However, there are significant drawbacks for these systems. Heterotrophic fermentations are vulnerable to contamination because other heterotrophic microorganisms that can grow on fixed carbon nutrients and compete with a production strain are ubiquitous in the immediate environment. Heterotrophic technologies also generally suffer limitations in terms of competition with current modes of food production because you are essentially using one type of food source to make another food source or biobased product. This can lead to numerous negative environmental impacts. [23] In addition to the need for new sugar, starch, carbohydrate, polysaccharide, protein and other nutrient sources for feeding animals, that in turn are either consumed, or kept as pets, or otherwise utilized by humankind, there is a need for alternative sugar, starch, carbohydrate, polysaccharide, protein and other nutrient sources for direct consumption by humans. One future area where this need may become particularly pressing, is in the area of long distance human space flight (e.g, to the Moon, Mars, or other planets), which requires a life-support system that supplies the crew’s needs— O₂. H₂O, and food—and eliminates their wastes—CO2, sewage, and heat. Food supplies represent a major source of weight and volume on longer missions. There is a need for life support systems that will operate for longer periods without resupply. An essential requirement for such systems is the ability to convert human and cabin waste products into useful products such as oxygen, potable water, food, and consumables. There is a need for food production that is edible as grown, and which lends itself to extended reliable automated growth and harvesting. The power penalty of biological systems is an important factor. There is a need for biological systems that efficiently utilize reliable nuclear and/or solar power systems. [24] There are previously described applications of chemoautotrophic microorganisms in the capture and conversion of CO2 gas to fixed carbon. However, many of these approaches have suffered shortcomings that have limited their effectiveness, economic feasibility, practicality and commercial adoption. [25] There is a need to break the bottleneck associated with significantly increasing agricultural outputs sustainably, on a very large scale. There is a need for biological production with compact, vertical scaling as opposed to traditional agricultural operations that scale horizontally and are highly land and water intensive. There is a need to mitigate the food versus nature conflict, and conflicts over land use, and the disruption of natural habitats. [26] Gas-to-chemical (GTC) technologies offer the benefit of allowing the utilization of waste carbon sources in the production of organic molecules. Such potential waste sources include: highly lignocellulosic waste - through the conversion to synthesis gas (syngas) via gasification; and waste CO2, captured from industrial flue gases for example, through the provision of dihydrogen. Syngas is a mix of gases that generally contains H2, CO, and CO2 as major components, which can be generated through steam reforming of methane and/or liquid petroleum gas or biogas or through gasification of any organic, flammable, carbon- based material, including but not limited to biomass, waste organic matter, various polymers, peat, and coal. Many gasification processes are available for the production of syngas. A number of gasification processes subject the carbon-based feedstock to partial oxidation at high temperatures (500-1500°C.), with the oxygen supply restricted to prevent complete combustion, producing syngas with varying composition depending on feedstock and reaction conditions such that the ratio of H2:CO can range from 0.5:1 to 3:1. The hydrogen component of syngas can be raised, and/or the CO component lowered, through the reaction of CO with steam in the water gas shift reaction with a concomitant increase in CO2 in the syngas mix. [27] Some major technologies for syngas conversion to chemicals include chemical catalytic processes such as the Fischer-Tropsch (F-T) as well as processes for the synthesis of methanol or other mixed alcohols, the Haber-Bosch reaction for the production of ammonia and urea, and biological syngas fermentation processes. [28] Using syngas and/or CO2 and/or renewable H2 in a gas bioprocess creates the opportunity to utilize cheaper and more flexible and more scalable sources of energy and/or carbon for the biological synthesis of sustainable chemicals and fuels than is possible through heterotrophic or phototrophic biosynthesis. In a syngas bioprocess, syngas acts as both a carbon and energy source for the microbial culture. [29] A bioprocess based upon a gaseous feedstock such as syngas can allow for far lower negative environmental and food production impacts in the biological synthesis of organic compounds than highly land and water intensive heterotrophic or phototrophic-based technologies. However, current biological GTL and GTC technologies generally yield relatively short chain alcohols, or other short chain organic compounds, as primary products. None of these current biological syngas conversions produce commercially competitive sugars, starch, carbohydrates, polysaccharides, amino acids, proteins, or other biopolymers. The syngas-consuming microorganisms used in current biological GTC technologies are generally poorly suited for the synthesis of mid- to long- carbon chain molecules, or biopolymers, such as most sugars, starch, carbohydrates, polysaccharides, amino acids, proteins, and other biological nutrients. [30] While the abiotic synthesis of sugars, starch, carbohydrates, polysaccharides from simple C1 and inorganic precursors such as H2, CO2, CO, H2O, NH3, CH4, CH3OH, HCOH, is known, such approaches are currently non-competitive in comparison with biological methods for supplying sugars, starch, carbohydrates, and polysaccharides for the diet of humans, animals, and other heterotrophs. Challenges hindering the physicochemical, abiotic approach include low yields and side reactions yielding potentially toxic co-products. [31] There is a need to identify a set of microorganisms that can grow in conventional and scalable contained reaction vessels and that produce commercially viable sets of organic carbon chains, in particular over four carbon atoms long in a commercially feasible method. There is a need to identify microorganisms not limited metabolically by typical fixed carbon inputs such as sugar, and microorganisms that can additionally utilize syngas, producer gas, and also a wide array of abiotic sources of carbon and energy, directed through a H2/CO2 gas mix intermediate, for the synthesis of drop-in molecules. This will lead to a feedstock flexibility that far exceeds comparable heterotrophic systems. There is a need to identify and use microorganisms that can utilize electron donors such as hydrogen, present in syngas, producer gas, and also readily generated through a wide array of abiotic renewable and/or low-CO2 emission energy technologies, for growth and carbon fixation. [32] There is a need for a biological means of producing sugars, starch, carbohydrates, polysaccharides, and other biomass constituents from low-cost or sustainable feedstocks. There is a need for a bioprocess that converts low cost syngas and/or CO₂ into higher value organic chemicals including but not limited to sugars, starch, carbohydrates, polysaccharides, and other biomass constituents. SUMMARY OF THE INVENTION [33] In response to a need in the art that the inventors have recognized in making the invention, a system for the production of organic chemicals including but not limited to sugars, starch, carbohydrates, polysaccharides, and other biomass constituents, and/or biological nutrients from low-cost and sustainable feedstocks is presented herein. In some embodiments, the invention can couple the efficient production of these high value organic compounds with the disposal of waste sources of carbon and/or with the capture of CO2, which can generate additional revenue and/or social value. [34] The present invention allows the use of naturally occurring or engineered microorganisms to convert CO₂ gas and/or syngas and/or producer gas and/or methane to higher value mid- to long- carbon chain length molecules and/or biopolymers including but not limited to sugars, starch, carbohydrates, polysaccharides, and other biomass constituents, and/or biological nutrients. In certain embodiments, the present technology allows the development of new natural or classically bred and/or genetically enhanced strains of microorganisms that can be used for syngas bioprocessing within biological gas- to-chemical (GTC) processes to produce and/or secrete various relatively long chain organic compounds and/or biopolymers such as, but not limited to sugars, starch, carbohydrates, polysaccharides, and other biomass constituents, and/or biological nutrients that are drop-in, and are currently only produced commercially in bulk from higher plant agricultural crops or animal sources. [35] Certain embodiments of the present invention consist of a chemolithoautotrophic bacterium engineered to produce strains that selectively produce the carbohydrates glucose or starch. Certain embodiments of the present invention relate to the engineering of a CO2- fixing chemoautotroph to partition carbon from fixed CO2 to glucose and/or to starch polymer. In certain embodiments, the engineered organism enables a sustainable microaerobic or aerobic gas fermentation process for production and processing of these carbohydrates. [36] The present invention relates to the selection and/or breeding and/or engineering of microorganisms, including but not limited to hydrogen-oxidizing, carbon monoxide- oxidizing, and knallgas microorganisms (also known as oxyhydrogen microorganisms), with a natural capability to grow and synthesize biomass on gaseous carbon sources such as syngas and/or CO2, such that the production microorganisms synthesize targeted chemical products under gas cultivation. The microorganisms and methods of the present invention can enable low cost synthesis of biochemicals, which can compete on price with higher- plant crop derived sugars, starch, carbohydrates, polysaccharides, and other biomass constituents and/or biological nutrients. In certain embodiments, these sugars, starch, carbohydrates, polysaccharides, and other biomass constituents and/or biological nutrients are predicted to have a substantially lower price than the same produced through heterotrophic or microbial phototrophic synthesis. [37] The invention relates to a composition comprising a microorganism that converts syngas and/or gaseous CO2 and/or a mixture of CO2 gas and H2 gas along with a nitrogen source including but not limited to ammonia, ammonium, and/or urea, into one or more glucose, sugars, starch, carbohydrates, polysaccharides, and other biomass constituents and/or biological nutrients. In some embodiments, the composition comprises a microorganism, wherein the microorganism is one or more of the following: a hydrogen- oxidizing chemoautotrophic microorganism; a carbon monoxide-oxidizing microorganism; a knallgas microorganism. Knallgas microbes, hydrogenotrophs, carboxydotrophs, and chemoautotrophs more broadly, are able to capture CO2 or CO as their sole carbon source to support biological growth. In some embodiments, this growth includes the biosynthesis of glucose, sugars, starch, carbohydrates, and/or other polysaccharides. Knallgas microbes and other hydrogenotrophs can use H₂ as a source of reducing electrons for respiration and biochemical synthesis. In some embodiments of the present invention knallgas organisms and/or hydrogenotrophs and/or carboxydotrophs and/or other chemoautotrophic microorganisms are grown on a stream of gasses including but not limited to one or more of the following: CO₂; CO; H₂; along with inorganic minerals dissolved in aqueous solution. In some embodiments knallgas microbes and/or hydrogenotrophs and/or carboxydotrophs and/or other chemoautotrophic and/or methanotrophic microorganisms convert greenhouse gases (GHG’s) into biomolecules including one or more of: glucose, sugars, starch, carbohydrates, polysaccharides, and/or other biomass constituents and/or biological nutrients. [38] In certain embodiments of the present invention, well known drawbacks of photosynthetic systems for capture and conversion of CO₂ such as those based on algae or higher plants are circumvented, while the unique biological capability, evolved over billions of years, for complex organic synthesis from CO2 to produce valuable biochemicals such as but not limited to glucose, sugars, starch, carbohydrates, and/or other polysaccharides, is still leveraged. [39] Certain embodiments of the present invention involve a chemoautotrophic microbial host that uses the Calvin Cycle to fix CO2 to 3-phosphoglycerate that feeds into the canonical glycolysis pathway and, through gluconeogenesis, generates glucose-6-phosphate. In certain such embodiments the said chemoautotrophic microbial host is engineered by addition or deletion of genes coding for the metabolic pathways that can impact the partitioning of carbon from a pool of glucose-6-phosphate to either glucose or starch. [40] In some embodiments, the composition comprises a microorganism, wherein the microorganism is chosen from the genera Xanthobacter. In some embodiments, the composition comprises a microorganism, wherein the microorganism is Xanthobacter autotrophicus. In some embodiments, the composition comprises a microorganism, wherein the microorganism is Xanthobacter autotrophicus (DSM 432) or Xanthobacter autotrophicus (DSM 2267). In some embodiments, the composition comprises a microorganism, wherein the microorganism is chosen from the genera Ralstonia or Cupriavidus. In some embodiments, the composition comprises a microorganism, wherein the microorganism is Cupriavidus necator. In some non-limiting embodiments, the strain of Cupriavidus necator is DSM 531 or DSM 541. [41] In one aspect, a natural or engineered microorganism is provided that is capable of converting a gaseous substrate such as producer gas or synthesis gas or another gas mixture that contains H2 and CO2, and/or CO, and/or CH4 into glucose, sugars, starch, carbohydrates, and/or other polysaccharides. The gaseous substrate is used by the microorganism as a carbon and/or energy source. In some embodiments, microorganisms that are capable of growing on a gaseous substrate are transformed with a polynucleotide that encodes a gene that is required for biosynthesis of one or more of glucose, sugars, starch, carbohydrates, and/or other polysaccharides. In some embodiments, glucose, sugars, starch, carbohydrates, and/or other polysaccharides, or a whole cell product is recovered from the microbial cells or from a microbial growth medium. Producer gas, which may be used in the microbial growth processes described herein, may come from sources that include gasification of waste feedstock and/or biomass residue feedstock, or waste gas from industrial processes or steam reforming of natural gas or biogas. [42] In one aspect, a non-naturally occurring microorganism is provided that is capable of growing on a gaseous substrate as a carbon and/or energy source, and wherein the microorganism includes at least one exogenous nucleic acid. In some embodiments, the microorganism is a bacterial cell. For example, in some embodiments, the bacterial cell is a Cupriavidus sp. or Ralstonia sp., for example, but not limited to, Cupriavidus necator. In some non-limiting embodiments, the microorganism is Cupriavidus necator DSM 531 or DSM 541. In some non-limiting embodiments, the microorganism is Ralstonia eutropha N- 1, DSM 13513. [43] In some embodiments, the gaseous substrate includes CO₂ as a carbon source. In some embodiments, the gaseous substrate includes H₂ and/or O2 as an energy source. In some embodiments, the gaseous substrate includes producer gas, syngas, or pyrolysis gas. In some embodiments, the gaseous substrate includes a mixture of gases, comprising H2 and/or CO₂ and/or CO. [44] In some embodiments, the microorganism produces glucose, sugars, starch, carbohydrates, polysaccharides, and/or other biomass constituents and/or other biological nutrients when cultured in the presence of the gas substrate under conditions suitable for growth of the microorganism and production of bioproducts. [45] In some embodiments, an exogenous gene is encoded by a coding sequence in the non-naturally occurring microorganism that is carried on a broad-host-range plasmid. In some embodiments, the exogenous gene coding sequence is under the control of a non- native inducible promoter. In some embodiments, the inducible promoter is derived from the E. coli ara operon. [46] In some embodiments, the coding sequence (CDS) of the exogenous gene is codon optimized for expression in a microorganism of as described herein, for example, but not limited to a Ralstonia or Cupriavidus species or a Xanthobacter species, for example, Cupriavidus necator or Xanthobacter autotrophicus. [47] In another aspect, methods are provided for producing glucose, sugars, starch, carbohydrates, polysaccharides, and/or other biomass constituents and/or other biological nutrients using an engineered microorganism as described herein that is capable of growing on a gaseous substrate as a carbon and/or energy source, and that includes at least one exogenous nucleic acid. In some embodiments, a non-naturally occurring microorganism as described herein is cultured in a bioreactor that includes a gaseous substrate and a culture medium (e.g., a liquid growth medium) that includes other nutrients for growth and bioproduct production, under conditions that are suitable for growth of the microorganism, wherein the microorganism produces glucose, sugars, starch, carbohydrates, polysaccharides, and/or other biomass constituents and/or other biological nutrients. [48] In some embodiments, the gaseous substrate in the bioreactor includes H₂ and/or CO₂. In some embodiments, the gaseous substrate is producer gas, syngas, or pyrolysis gas. In some embodiments, the gaseous substrate is natural gas or biogas. In some embodiments, the gaseous substrate is derived from municipal solid waste, black liquor, agricultural waste, wood waste, stranded natural gas, biogas, sour gas, methane hydrates, tires, pet coke, sewage, manure, straw, lignocellulosic energy crops, lignin, crop residues, bagasse, saw dust, forestry residue, food waste, waste carpet, waste plastic, landfill gas, and/or lignocellulosic biomass. [49] In some embodiments, glucose, other sugars, starch, carbohydrates, polysaccharides, and/or other biomass constituents and/or other biological nutrients are recovered from the culture medium. [50] In certain embodiments, the invention provides compositions and methods for the recovery, processing, and use of the biochemical products of chemosynthetic reaction step or steps performed by oxyhydrogen microorganisms to fix inorganic carbon into organic compounds, such as but not limited to glucose, other sugars, starch, carbohydrates, polysaccharides, and/or other biomass constituents and/or other biological nutrients; and/or synthetic reaction step or steps performed by oxyhydrogen microorganisms to synthesize organic chemicals including but not limited to glucose, other sugars, starch, carbohydrates, polysaccharides, and/or other biomass constituents and/or other biological nutrients. [51] In another aspect, microorganisms and methods for producing glucose, sugars, starch, carbohydrates, and/or other polysaccharides are provided. In some embodiments, a natural or non-naturally occurring microorganism is provided that is capable of growing on a gaseous substrate as a carbon and/or energy source, wherein the microorganism includes zero or at least one exogenous nucleic acid, and wherein said microorganism biosynthesizes glucose, sugars, starch, carbohydrates, polysaccharides, and/or other biomass constituents and/or other biological nutrients. In some embodiments, a method is provided for producing glucose, sugars, starch, carbohydrates, and/or other polysaccharides in a naturally or non- naturally occurring microorganism as described herein that is capable of growing on a gaseous substrate as a carbon and/or energy source, that includes zero or one or more exogenous nucleic acids, and that biosynthesizes glucose, sugars, starch, carbohydrates, polysaccharides, and/or other biological nutrients, including culturing the naturally or non- naturally occurring microorganism in a bioreactor that includes a gaseous substrate and a culture medium (e.g., a liquid growth medium) that includes other nutrients for growth and bioproduct production, under conditions that are suitable for growth of the microorganism and production of glucose, sugars, starch, carbohydrates, polysaccharides, and/or other biological nutrients, wherein the microorganism produces glucose, sugars, starch, carbohydrates, polysaccharides, and/or other biological nutrients. [52] In some embodiments, the microorganisms of the present invention are used to capture CO₂ from industrial flue gasses, and/or off-gases from bioprocesses and/or fermentations and produce glucose, sugars, starch, carbohydrates, polysaccharides, and/or carbohydrate-rich and/or polysaccharide-rich biomass. In some embodiments, these said products are a commodity. In some embodiments, the glucose, sugars, starch, carbohydrates, polysaccharides, and/or carbohydrate-rich and/or polysaccharide-rich biomass is used as a source of dietary carbohydrates, fiber, and/or calories. In some embodiments, the carbohydrates and/or carbohydrate-rich biomass is used as an animal feed or in an animal or aquaculture feed formulation or in a biofertilizer. In some embodiments, the starch and/or starch-rich biomass is used as a high-carbohydrate substitute in human food and/or ingredients, and/or aquaculture and/or other animal feed and/or plant fertilizer products. In some embodiments the starch and/or starch-rich biomass is used as a replacement for, or an additive to starch derived from one or more of the following plant crop sources: wheat, potatoes, maize (corn), rice, and cassava (manioc). In some non- limiting embodiments, the present invention is used both for GHG reduction and to produce high-carbohydrate products for applications including but not limited to human food and/or ingredients, and/or animal feed and/or replacements or additives to starch derived from one or more of the following plant crop sources: wheat, potatoes, maize (corn), rice, and cassava (manioc). [53] In one aspect, a biological and chemical method is provided for the capture and conversion of an inorganic and/or organic molecules containing only one carbon atom, into organic molecules containing multiple chemically bound carbon atoms produced through anabolic biosynthesis including glucose, sugars, starch, carbohydrates, and/or polysaccharides comprising: introducing inorganic and/or organic molecules containing only one carbon atom, into an environment suitable for maintaining chemoautotrophic microorganisms; introducing a gaseous substrate into an environment suitable for maintaining chemoautotrophic microorganisms; wherein the inorganic and/or organic molecules containing only one carbon atom are used as a carbon source by the microorganism for growth and/or biosynthesis; converting the inorganic and/or organic molecules containing only one carbon atom into the organic molecule products containing multiple chemically bound carbon atoms within the environment via at least one chemosynthetic carbon-fixing reaction and at least one anabolic biosynthetic pathway contained within the chemoautotrophic microorganisms, including but not limited to gluconeogenesis; wherein the chemosynthetic fixing reaction and anabolic biosynthetic pathway are at least partially driven by chemical and/or electrochemical energy provided by electron donors and electron acceptors that have been generated chemically and/or electrochemically and/or thermochemically and/or are introduced into the environment from at least one source external to the environment. [54] In some embodiments, said microorganism is a bacterial cell. In some embodiments, said microorganisms are knallgas microorganisms. In some embodiments, said microorganism is a Cupriavidus sp. or Ralstonia sp. In some embodiments, said microorganism is Cupriavidus necator. In some embodiments, said microorganism is a Xanthobacter sp.. In some embodiments, said microorganism is Xanthobacter autotrophicus. In some embodiments, the microorganisms include microorganisms selected from one or more of the following genera: Cupriavidus sp., Rhodococcus sp., Hydrogenovibrio sp., Rhodopseudomonas sp., Hydrogenobacter sp., Gordonia sp., Arthrobacter sp., Streptomycetes sp., Rhodobacter sp., and/or Xanthobacter sp. [55] In some embodiments, said gaseous substrate comprises CO₂ as a carbon source. In some embodiments, said gaseous substrate comprises H2 and/or O2 as an energy source. In some embodiments, said gaseous substrate comprises pyrolysis gas or producer gas or syngas. In some embodiments, said gaseous substrate comprises a mixture of gases, comprising H₂ and/or CO₂ and/or CO. In some embodiments, said gaseous substrate comprises H2 and/or CO2. [56] In some embodiments, said microorganism produces glucose and/or other sugars and/or starch and/or other carbohydrates and/or other polysaccharides and/or vitamins and/or biomass when cultured in the presence of the gas substrate under conditions suitable for growth of the microorganism and production of bioproducts. In some embodiments, glucose and/or other sugars and/or starch and/or other carbohydrates and/or other polysaccharides and/or amino acids and/or protein and/or vitamins and/or biomass is recovered from the culture medium. [57] In some embodiments, said microorganisms and/or nutrients produced by said microorganisms are used to feed or provide nutrition to one or more other single-cell and/or multicellular organisms. [58] In some embodiments, said gaseous substrate is pyrolysis gas or producer gas or syngas. In some embodiments, said gaseous substrate is derived from municipal solid waste, black liquor, agricultural waste, wood waste, stranded natural gas, biogas, sour gas, methane hydrates, tires, pet coke, sewage, manure, straw, lignocellulosic energy crops, lignin, crop residues, bagasse, saw dust, forestry residue, food waste, waste carpet, waste plastic, landfill gas, kelp, seaweed, and/or lignocellulosic biomass. [59] In some embodiments, said electron donors and/or molecules containing only one carbon atom are generated through a thermochemical process acting upon organic matter comprising at least one of: gasification; pyrolysis; steam reforming; autoreforming. In some embodiments, said electron donors and/or organic molecules containing only one carbon atom are generated through methane steam reforming. In some embodiments, the ratio of hydrogen to carbon monoxide in the output gas from gasification and/or pyrolysis and/or autoreforming and/or steam reforming is adjusted using the water gas shift reaction prior to the gas being delivered to the microorganisms. [60] In some embodiments, said electron donors and/or electron acceptors are generated or recycled using renewable, alternative, or conventional sources of power that are low in greenhouse gas emissions, and wherein said sources of power are selected from at least one of photovoltaics, solar thermal, wind power, hydroelectric, nuclear, geothermal, enhanced geothermal, ocean thermal, ocean wave power, and tidal power. [61] In some embodiments, said electron donors and/or electron acceptors are generated using grid electricity during periods when electrical grid supply exceeds electrical grid demand, and wherein storage tanks buffer the generation of said electron donors and/or electron acceptor, and their consumption in the chemosynthetic reaction. [62] In some embodiments, molecular hydrogen acts as an electron donor and is generated via a method using at least one of the following: electrolysis of water; thermochemical splitting of water; electrolysis of brine; electrolysis and/or thermochemical splitting of hydrogen sulfide. In some embodiments, electrolysis of water for the production of hydrogen is performed using one or more of the following: Proton Exchange Membranes (PEM), liquid electrolytes such as KOH, alkaline electrolysis, Solid Polymer Electrolyte electrolysis, high-pressure electrolysis, high temperature electrolysis of steam (HTES). In some embodiments, thermochemical splitting of water for the production of hydrogen is performed using one or more of the following: the iron oxide cycle, cerium(IV) oxide- cerium(III) oxide cycle, zinc zinc-oxide cycle, sulfur-iodine cycle, copper-chlorine cycle, calcium-bromine-iron cycle, hybrid sulfur cycle. [63] In some embodiments, molecular hydrogen acts as an electron donor and is generated via electrochemical or thermochemical processes known to produce hydrogen with low- or no- carbon dioxide emissions including one or more of the following: carbon capture and sequestration (CCS) enabled methane steam reforming; CCS enabled coal gasification; the Kværner-process and other processes generating a carbon-black product; CCS enabled gasification or pyrolysis of biomass; pyrolysis of biomass producing a biochar co-product. [64] In some embodiments, said electron donors include but are not limited to one or more of the following reducing agents: ammonia; ammonium; carbon monoxide; dithionite; elemental sulfur; hydrocarbons; hydrogen; metabisulfites; nitric oxide; nitrites; sulfates such as thiosulfates including but not limited to sodium thiosulfate (Na₂S₂O₃) or calcium thiosulfate (CaS₂O₃); sulfides such as hydrogen sulfide; sulfites; thionate; thionite; transition metals or their sulfides, oxides, chalcogenides, halides, hydroxides, oxyhydroxides, phosphates, sulfates, or carbonates, in dissolved or solid phases; and conduction or valence band electrons in solid state electrode materials. In some embodiments, said electron acceptors comprise one or more of the following: carbon dioxide; oxygen; nitrites; nitrates; ferric iron or other transition metal ions; sulfates; or valence or conduction band holes in solid state electrode materials. [65] In some embodiments, the biological conversion step is preceded by one or more chemical preprocessing steps in which said electron donors and/or electron acceptors and/or carbon sources and/or mineral nutrients required by the microorganism, are generated and/or refined from at least one input chemical and/or are recycled from chemicals emerging from the carbon-fixing step and/or are generated from, or are contained within, waste streams from other industrial, mining, agricultural, sewage or waste generating processes. [66] In some embodiments, the organic chemical product includes compounds with carbon backbones that are five carbons or longer. In certain such embodiments, the said organic chemical product is a sugar. In certain such embodiments, the said sugar is glucose. In certain such embodiments, the said glucose is the isomer dextrose (d-Glucose). [67] In some embodiments, a method is provided for producing glucose and/or other sugars and/or starch and/or other carbohydrates and/or other polysaccharides and/or amino acids and/or protein and/or vitamins and/or biomass, comprising culturing a microorganism as described herein in a bioreactor that comprises a gaseous substrate and a culture medium that comprises other nutrients for growth and bioproduct production, under conditions that are suitable for growth of the microorganism and production of glucose and/or other sugars and/or starch and/or other carbohydrates and/or other polysaccharides and/or amino acids and/or protein and/or vitamins and/or biomass, wherein said microorganism produces glucose and/or other sugars and/or starch and/or other carbohydrates and/or other polysaccharides and/or amino acids and/or protein and/or vitamins and/or biomass. [68] In some embodiments, at least one chemosynthetic reaction and at least one anabolic biosynthetic pathway results in the formation of biochemicals including at least one of: glucose; sugars; starch; carbohydrates; polysaccharides; amino acids; peptides; proteins; lipids; and/or vitamins. [69] In some embodiments, biomass and/or biochemicals are produced through the said at least one chemosynthetic reaction, and wherein the biomass and/or biochemicals have application as at least one of the following: as an organic carbon and/or nitrogen source for fermentations; as a nutrient source for the growth of other microbes or organisms; as a nutrient source, calorie source, fiber source, or food ingredient for humans; as a feed for animals; as a raw material or chemical intermediate for manufacturing or chemical processes; as sources of pharmaceutical, medicinal or nutritional substances; as a fertilizer; as soil additives; and/or as soil stabilizers. [70] In some embodiments, the carbon and/or nitrogen source from the said chemosynthetic reaction is used in a fermentation to produce biochemicals including least one of: commercial enzymes, antibiotics, amino acids, protein, food, food ingredients; vitamins, lipids, bioplastics, polysaccharides, neutraceuticals, pharmaceuticals. In some embodiments, said feed for animals is used to feed one or more of: cattle, sheep, chickens, pigs, fish, shellfish, insects, invertebrates, coral. [71] Various objects, features, aspects, and advantages of the present invention will become more apparent from the following detailed description of preferred embodiments of the invention, along with the accompanying drawings in which like numerals represent like components BRIEF DESCRIPTION OF THE DRAWINGS [72] Non-limiting embodiments of the present invention will be described by way of example with reference to the accompanying figures, some of which are schematic and are not intended to be drawn to scale. For purposes of clarity, not every component is labeled in every figure, nor is every component of each embodiment of the invention shown where illustration is not necessary to allow those of ordinary skill in the art to understand the invention. [73] Figure 1. Strategy for construction of a chemoautotrophic glucose production organism. Deleted enzymes and pathways are indicated by dotted lines. Carbon flux in the recombinant strain is depicted with heavy arrows; heterologous enzymes coded by recombinant expression of HAD phosphatase and glucose facilitator genes are in bold; deleted enzymes or pathways are shown as dotted lines. Unbolded enzymes are endogenous. Enzymes in in bold italics are heterologous. [74] Figure 2. Strategy for construction of a chemoautotrophic starch production organism. Deleted enzymes and pathways are indicated by dotted lines. Carbon flux in the recombinant strain is depicted with heavy arrows; heterologous enzymes are in bold; deleted enzymes or pathways are shown as dotted lines. Unbolded enzymes are endogenous. Enzymes in in bold italics are heterologous. [75] Figure 3. Glucose growth phenotype expressed in the chemoautotroph. Growth of induced chemoautotroph with glf+ genotype. Arabinose induction of the pBAD glf construct produces a growth+ phenotype in a strain not normally able to facilitate glucose transport, indicating successful expression and assembly of the glucose membrane transporter. [76] Figure 4. Lugol staining of starch produced by a recombinant strain expressing glg genes. Tube 1 is a strain expressing glgA, tube 2 is a strain expressing glgC and tube C is a strain expressing both genes. Staining indicates starch production in the strain expressing both genes. [77] Figure 5. Comparison of starch production by the glgA/glgC recombinant strain grown heterotrophically on fructose or autotrophically on CO2/H2. Media compared for an effect on starch titer were Luria Broth (LB) and Minimal Salts Media (MSM) [78] Figure 5 illustrates metabolic pathways of knallgas microorganisms. [79] Figure 6 shows the growth curve for the knallgas microorganism Cupriavidus necator grown on H₂/CO₂/O₂ in a bioreactor. [80] Figure 7 shows bioreactor growing Hydrogenovibrio marinus on gas. [81] Figure 8 shows a schematic diagram of a two-liter glass fermenter system used to grow Xanthobacter autotrophicus strain DSM 432 on a mixture of H2, CO2, and O2 gases as the sole source of energy and carbon for growth. [82] Figure 9 shows the headplate of the bioreactor depicted in Figure 21, schematically illustrated. [83] Figure 10 shows a schematic diagram of a reactor system used to grow Xanthobacter autotrophicus, including pressure gauges; gas flow meters; safety and check valves; 0.2 micron filters; the bioreactor vessel, sensors, actuators, and controllers; a condenser and foam trap; and outlet vent. [84] Figure 11 shows a schematic diagram of the gas delivery system used to grow X. autotrophicus. [85] Figure 12 shows correlation between OD600 and cell dry weight (CDW) for X. autotrophicus. [86] Figure 13 shows the growth curve for the knallgas microorganism X. autotrophicus grown on H₂/CO₂/O₂. [87] Figure 14 shows a process flow diagram for an embodiment with capture of CO₂ performed by a microorganism capable of performing an oxyhydrogen reaction to produce carbohydrates and/or carbohydrate-rich biomass. DETAILED DESCRIPTION [88] Provided herein are methods and systems for biosynthetic production of glucose, sugars, starch, carbohydrates, polysaccharides, and/or other biomass constituents and/or and other biological nutrients. Certain embodiments provided herein give methods and systems for biosynthetic production of glucose or starch. In certain embodiments, natural or engineered microorganisms are provided that produce glucose, sugars, starch, carbohydrates, polysaccharides, and/or other biomass constituents and/or other biological nutrients, on a gaseous substrate, including, but not limited to producer gas, syngas, tail gas, pyrolysis, knallgas, and gas mixtures containing H2 and CO2, and/or CO and/or CH4. In certain embodiments, engineered microorganisms are provided that produce glucose or starch on a gaseous substrate, including, but not limited to producer gas, syngas, tail gas, knallgas, and gas mixtures containing H2 and CO2, and/or CO and/or CH4. The gaseous substrate may serve as a carbon and/or energy source and/or a source of electron donors and/or electron acceptors for growth of the microorganisms and biosynthesis of bioproducts. [89] The inventive subject matter comprises, in certain embodiments, a wild-type or engineered microorganism capable of growing on syngas, or producer gas, and/or H₂, and/or CO2, and/or CO, and/or CH4, and/or other waste gases, which are capable of producing sugars including but not limited to glucose. [90] In certain embodiments of the present invention glucose, sugars, starch, carbohydrates, polysaccharides, and/or vitamins and/or other biomass constituents and/or other biological nutrients are synthesized from simple C1 and inorganic precursors including but not limited to one or more of the following: H2, CO2, CO, H2O, NH3, CH4, CH₃OH, HCOH, formic acid and/or formate, urea. [91] In some embodiments, the invention relates to a method of producing one or more glucose or other sugars or starch or carbohydrates or polysaccharides or amino acids or proteins or vitamins, comprising exposing a bacterial cell to syngas and/or producer gas and/or gaseous CO₂ and/or H₂ and/or CO and/or CH4; wherein the bacterial cell is capable of fixing gaseous CO₂ and/or other C1 molecules into one or more glucose or other sugars or starch or carbohydrates or polysaccharides or amino acids or proteins or vitamins, and wherein the microorganism comprises zero or at least a first exogenous nucleic acid. In some embodiments, the cell utilizes the said gaseous substrates as a source of reducing equivalents and/or metabolic energy for the synthesis of one or more glucose or other sugars or starch or carbohydrates or polysaccharides or amino acids or proteins or vitamins. In some embodiments, the microorganism through its native machinery produces glucose and/or other sugars and/or starch and/or carbohydrates and/or polysaccharides and/or amino acids and/or proteins and/or vitamins. [92] In some embodiments, the invention relates to a method for producing glucose and/or other sugars and/or starch and/or carbohydrates and/or polysaccharides and/or amino acids and/or proteins and/or carbohydrate-rich biomass and/or vitamins wherein the method comprises culturing natural strain or an engineered microorganism in a bioreactor or solution with a feedstock comprising syngas and/or producer gas and/or CO2 and/or H2 gas and/or CO and/or CH4. In some embodiments, the invention relates to a bioreactor comprising the composition or bacterial or microbial cells described herein. In some embodiments, the invention relates to a system for the production of one or more of glucose, other sugars, starch, carbohydrates,polysaccharides, or nutrients, comprising a bioreactor, which comprises: (a) a microorganism population comprising a cell described herein; and (b) an inlet connected to a feedstock source allowing delivery of a feedstock comprising syngas or producer gas and/or gaseous CO₂ and/or H₂ and/or CO and/or CH₄. [93] In another aspect of the invention, the invention relates to a method of producing a molecule or mixture of molecules in a microorganism population comprising the cell or the composition described herein, wherein the method comprises: culturing a population of microorganisms comprising the cell or the composition described herein in a feedstock comprising syngas or producer gas and/or gaseous CO2 and/or H₂ and/or CO and/or CH₄. [270] In some embodiments the invention relates to a method of producing glucose and/or other sugars and/or starch and/or carbohydrates and/or polysaccharides and/or other nutrients or biopolymers in a microorganism population comprising the cell of the composition described herein, wherein the method comprises: culturing a population of microorganisms comprising the cell or the composition described herein in a feedstock comprising syngas or producer gas and/or gaseous CO2 and/orH2 and/or CO and/or CH4. [94] In some embodiments, the invention relates to a method of manufacturing one or more of glucose, other sugars, starch, carbohydrates,polysaccharides, or other nutrients, comprising (a) culturing a cell described herein in a reaction vessel or bioreactor in the presence of syngas or producer gas and/or gaseous CO2 and/or H2 and/or CO and/or CH4, wherein the cell produces and/or secretes one or more of glucose, other sugars, starch, carbohydrates,polysaccharides, or other nutrients in a quantity equal to or greater than at least 10% of the cell’s total dry cellular mass; and (b) separating the one or more of glucose, other sugars, starch, carbohydrates, polysaccharides, or other nutrients, or a whole cell product from the reaction vessel. In some embodiments, the method further comprises purifying the one or more of glucose, other sugars, starch, carbohydrates, polysaccharides, or other nutrients, or whole cell products after separation from the reaction vessel or bioreactor. In some embodiments, the one or more of glucose, other sugars, starch, carbohydrates, polysaccharides, or other nutrients, or whole cell products are components of, or precursors to, or are included within a feed or nutrient supply or fertilizer provided to another organism. In certain non-limiting embodiments that other organism is a heterotroph, and in certain such embodiments an animal including but not limited to one or more of a: zooplankton, shellfish or other invertebrate, fish, amphibian, insect, reptile, bird, or mammal. [95] In some embodiments, the invention relates to a method of producing one or more glucose molecules and/or other sugar molecules comprising exposing a bacterial cell and/or archaeal cell and/or other microbial cell to syngas and/or gaseous CO₂ and/or H₂ and/or CO and/or CH₄; wherein the cell is capable of fixing gaseous CO₂ and/or other C1 carbon sources into one or more of glucose and/or other sugars and/or starch and/or carbohydrates and/or polysaccharides and/or amino acids and/or proteins and/or vitamins; wherein the compounds are recovered from the bioreactor and fed to a second or more additional reactors and/or process steps wherein the compounds are post-processed to generate products including but not limited to one or more of the following: fertilizer, aquaculture feed, animal feed, human nutrition, or vitamins. [96] In some embodiments the present invention gives compositions and methods for the capture and conversion of carbon dioxide from carbon dioxide-containing gas streams and/or atmospheric carbon dioxide and/or carbon dioxide in dissolved, liquefied or chemically-bound form via a chemical and biological process that utilizes obligate or facultative chemoautotrophic microorganisms and particularly chemolithoautotrophic organisms, and/or cell extracts containing enzymes from chemoautotrophic microorganisms in one or more carbon fixing process steps. The present invention also gives compositions and methods for the recovery, processing, and use of the chemical products of chemosynthetic reactions performed by chemoautotrophs to fix inorganic carbon into organic compounds that are intermediate or finished chemicals, including but not limited to glucose and/or other sugars and/or starch and/or carbohydrates and/or polysaccharides and/or amino acids and/or protein and/or vitamins and/or biomass. The present invention also gives compositions and methods for the generation, processing and delivery of chemical nutrients needed for chemosynthesis and maintenance of chemoautotrophic cultures, including but not limited to the provision of electron donors and electron acceptors needed for chemosynthesis. The present invention also gives compositions and methods for the maintenance of an environment conducive for chemosynthesis and chemoautotrophic growth, and the recovery and recycling of unused chemical nutrients and process water. [97] In some embodiments, the microorganisms disclosed herein are recombinantly engineered to express one or more enzymes for biosynthetic production of glucose and/or other sugars and/or starch and/or carbohydrates and/or polysaccharides and/or amino acids and/or proteins and/or other biological nutrients and/or biopolymers. In some embodiments, substrates or intermediates are diverted to the synthesis of sugars including but not limited to glucose, starch, carbohydrates, polysaccharides, and/or other biological nutrients or biopolymers in the microbial cells, such as, for example, 3-phosphoglycerate, glucose-6- phosphate, acetyl-CoA, pyruvate, or malonyl-CoA. In some non-limiting embodiments, some fraction of carbon flux along the various biosynthesis pathways is directed into the biosynthesis of targeted sugars including but not limited to glucose, starch, carbohydrates, polysaccharides, and other biological nutrients and/or biopolymers. [98] In certain non-limiting embodiments of the present invention construction of a glucose production strain proceeds stepwise using well known methods in the scientific and technological areas of genetic engineering, metabolic engineering, and classical strain improvement, with the goal of the synthesis of a pool of glucose (Figure 1). [99] In some embodiments, the microorganisms disclosed herein use the Calvin Cycle to fix CO₂ to 3-phosphoglycerate that feeds into a glycolysis pathway (Figure 1) and, through gluconeogenesis, generates glucose-6-phosphate. In certain such embodiments, engineering by addition or deletion of genes coding for the metabolic pathways determine the partitioning of carbon from a pool of glucose-6-phosphate to either glucose (Figure 1) or starch (Figure 2). In certain non-limiting embodiments of the present invention, the said species of microorganism that uses the Calvin Cycle to fix CO₂ to 3-phosphoglycerate and/or that converts 3-phosphoglycerate to glucose-6-phosphate via gluconeogenesis is Cupriavidus necator. In other non-limiting embodiments the said species is Xanthobacter autotrophicus. [100] In certain non-limiting embodiments of the present invention, the construction of a chemoautotrophic glucose production organism is accomplished following the strategy diagrammed in Figure 1. In certain non-limiting embodiments, the enablement of glucose production in one or more of the microorganisms disclosed herein involves deleting via genetic engineering and/or mutation one or more of the following enzymes: Glucose kinase; Glucose-6-phosphate dehydrogenase (Figure 1). In certain non-limiting embodiments, deletion of glucose kinase in one or more of the microorganisms disclosed herein, in order to prevent phosphorylation of glucose to glucose-6-phosphate, increases the pool of glucose. In certain such embodiments, the said microorganism is Cupriavidus necator. In other such embodiments, the said microorganism is Xanthobacter autotrophicus. In certain non- limiting embodiments, deletion, in one or more of the microorganisms disclosed herein, of one or more genome copies of the zwf genes coding for glucose-6-phosphate dehydrogenase is performed to eliminate the Enter-Doudoroff pathway to pyruvate. In certain such embodiments deletion of three genome copies of the zwf genes coding for glucose-6- phosphate dehydrogenase is performed to eliminate the Entner–Doudoroff pathway to pyruvate. In certain such embodiments, the said microorganism is Cupriavidus necator. In other such embodiments, the said microorganism is Xanthobacter autotrophicus. [101] In certain non-limiting embodiments, the enablement of glucose production in one or more of the microorganisms disclosed herein involves deleting via genetic engineering and/or mutation the metabolic pathway for polyhydroxybutryrate (PHB) biosynthesis (Figure 1). In certain such embodiments, the said microorganism is Cupriavidus necator. In other such embodiments, the said microorganism is Xanthobacter autotrophicus. In certain such embodiments, the removal of PHB biosynthesis involves deletion of the PHA promoter, pha, to prevent carbon flux to the storage polymer polyhydroxybutyrate. [102] In certain non-limiting embodiments, the enablement of glucose production in one or more of the microorganisms disclosed herein involves the activity of heterologous enzymes coded by recombinant expression of phosphatase and/or glucose facilitator genes (Figure 1). In certain such non-limiting embodiments the said phosphatase is Glucose 6- phosphatase (Figure 1). In certain such non-limiting embodiments the said phosphatase is a haloacid dehydrogenase phosphatase (HAD phosphatase – Figure 1). In certain such embodiments, heterologous expression of the glucose facilitator from, for example, Xymomonas, glf, creates a glucose+ growth phenotype of diffusion of glucose in and out of the cell of one or more of the microorganisms disclosed herein. In certain such embodiments, the said microorganism is Cupriavidus necator. In certain non-limiting embodiments a HAD phosphatase is inserted into in one or more of the microorganisms disclosed herein to convert glucose phosphates into glucose. In certain such embodiments, the said microorganism is Cupriavidus necator. [103] In certain non-limiting embodiments, one or more of the microorganisms disclosed herein have one or more of the following enzymes overexpressed and/or introduced into the microorganism as a heterologous enzyme: Fructose-bisphosphate aldolase; Fructose-1,6- biphosphatase; Glucose-6-phosphate isomerase (Figure 1). In certain embodiments, one or more of the following the enzymes: fructose-bisphosphate aldolase; fructose-1,6- bisphosphatase; glucose-6-phosphate isomerase; are overexpressed in one or more of the microorganisms disclosed herein to increase carbon flux through the gluconeogenesis pathway. In certain non-limiting embodiments, one or more of the following enzymes are endogenous to microorganisms disclosed herein: Phosphoglycerate kinase; Glyceraldehyde 3-phosphate dehydrogenase (Figure 1). In certain such embodiments the said microorganism is Cupriavidus necator. [104] In certain non-limiting embodiments targeting the production of free glucose, genes essential for glucose polymer synthesis, e.g., phosphoglucomutase, are deleted. In other non-limiting embodiments targeting the production of glucose polymers, such as starch for example, genes essential for synthesis of glucose polymers are NOT deleted. ; [105] In certain non-limiting embodiments of the present invention construction of a starch production strain proceeds stepwise using well known methods in the scientific and technological areas of genetic engineering, metabolic engineering, and classical strain improvement, with the goal of the synthesis of a pool of starch (Figure 2). [106] In certain non-limiting embodiments of the present invention, the construction of a chemoautotrophic starch production organism is accomplished following the strategy diagrammed in Figure 2. [107] In certain non-limiting embodiments, the enablement of starch production in one or more of the microorganisms disclosed herein involves deleting via genetic engineering and/or mutation one or more of the following enzymes: Glucose-6-phosphatase; Glucose-6- phosphate dehydrogenase; Gluconolactonase; 1,4-alpha-glucan branching enzyme (Figure 2). In certain non-limiting embodiments targeting starch production, deletion of glucose-6- phosphatase is performed in one or more of the microorganisms disclosed herein in order to to prevent conversion of glucose-6-phosphate to glucose and to prevent carbon flux from glucose-6-phosphate to glucose. In certain such embodiments, the said microorganism is Cupriavidus necator. In other such embodiments, the said microorganism is Xanthobacter autotrophicus. [108] In certain non-limiting embodiments targeting starch production, deletion of glucose-6-phosphatase is performed in one or more of the microorganisms disclosed herein in order to block carbon partitioning to the Entner–Doudoroff pathway. In certain non- limiting embodiments for the construction of a starch strain, deletion, in one or more of the microorganisms disclosed herein, of one or more genome copies of the zwf genes coding for glucose-6-phosphate dehydrogenase is performed to eliminate the Entner–Doudoroff pathway to pyruvate. In certain such embodiments deletion of three genome copies of the zwf genes coding for glucose-6-phosphate dehydrogenase is performed. In certain such embodiments, the said microorganism is Cupriavidus necator. In other such embodiments, the said microorganism is Xanthobacter autotrophicus. [109] In certain non-limiting embodiments, the enablement of starch production in one or more of the microorganisms disclosed herein involves deleting via genetic engineering and/or mutation the metabolic pathway for polyhydroxybutryrate (PHB) biosynthesis (Figure 2). In certain such embodiments, the said microorganism is Cupriavidus necator. In other such embodiments, the said microorganism is Xanthobacter autotrophicus. In certain such embodiments, the removal of PHB biosynthesis involves deletion of the PHA promoter, pha, to prevent carbon flux to PHB. [110] In certain non-limiting embodiments, the enablement of starch production in one or more of the microorganisms disclosed herein involves the activity of heterologous enzymes coded by recombinant expression of glucose-1-phosphate adenylyltransferase, glgC and/or ADP glucose starch synthase, glgA genes (Figure 2). In certain such embodiments, the said microorganism is Cupriavidus necator. In other such embodiments, the said microorganism is Xanthobacter autotrophicus. In certain non-limiting embodiments a HAD phosphatase is inserted into in one or more of the microorganisms disclosed herein to convert glucose phosphates into glucose. In certain such embodiments, the said microorganism is Cupriavidus necator. [111] In certain non-limiting embodiments targeting starch production, one or more of the microorganisms disclosed herein have one or more of the following enzymes overexpressed and/or introduced into the microorganism as a heterologous enzyme: Fructose-bisphosphate aldolase; Fructose-1,6-biphosphatase; Glucose-6-phosphate isomerase (Figure 2). In certain embodiments targeting starch production, one or more of the following the enzymes: fructose-bisphosphate aldolase; fructose-1,6-bisphosphatase; glucose-6-phosphate isomerase; are overexpressed in one or more of the microorganisms disclosed herein to increase carbon flux through the gluconeogenesis pathway. In certain non-limiting embodiments targeting starch production, one or more of the following enzymes are endogenous to microorganisms disclosed herein: Phosphoglycerate kinase; Glyceraldehyde 3-phosphate dehydrogenase (Figure 2). In certain such embodiments the said microorganism is Cupriavidus necator. [112] In certain non-limiting embodiments, the microorganisms disclosed herein are recombinantly engineered to express one or more enzymes for biosynthetic production and secretion of glucose, for example, the glucose facilitator obtained from Escherichia coli or, in other embodiments, for starch synthesis, for example by engineering expression of glucose-1-phosphate adenylyltransferase. [113] In certain non-limiting embodiments, substrates or intermediates are diverted to glucose or starch synthesis in the microbial cells by deletion of genes coding for pathways that divert carbon from the engineered metabolic routes, for example, in the case of glucose engineering, deletion of glucose-6-phosphatase to promote carbon to glucose, or deletion of glucose-6-phosphate dehydrogenase to block carbon flux to the competing native Enter- Doudoroff pathway. [114] In certain non-limiting embodiments, the invention provides for a method of producing glucose by combining, in a bioreactor or solution, a carbon-containing gas and a natural or engineered microorganism that converts a carbon-containing gas such as syngas, producer gas, CO2, carbon monoxide and mixtures of the same containing hydrogen gas; and/or C1 compounds liquid or gaseous including but not limited to methanol or methane, into glucose and encodes one or more genes including but not limited to the heterologous enzyme HAD phosphatase. [115] In certain non-limiting embodiments, the invention provides for a method of producing starch by combining, in a bioreactor or solution, a carbon-containing gas and a natural or engineered microorganism that converts a carbon-containing gas such as syngas, producer gas, CO2, carbon monoxide and mixtures of the same containing hydrogen gas; and/or C1 compounds liquid or gaseous including but not limited to methanol or methane, into starch. [116] One feature of certain embodiments of the present invention is the inclusion of one or more process steps that utilize chemotrophic microorganisms and/or enzymes from chemotrophic microorganisms as a biocatalyst for the conversion of C1 chemicals into longer carbon chain organic molecules (i.e., C2 or longer and, in some embodiments, C5 or longer carbon chain molecules), within an overall process for the conversion of C1 carbon sources including but not limited to carbon monoxide, methane, methanol, formate, or formic acid, and/or mixtures containing C1 chemicals including but not limited to various syngas compositions generated from various gasified, pyrolyzed, or steam- reformed fixed carbon feedstocks and/or methane feedstocks. In some such embodiments C1 containing syngas, or process gas, or C1 chemicals in a liquid form or dissolved in solution are pumped or otherwise added to a vessel or enclosure containing nutrient media and chemotrophic microorganisms. In some such cases chemotrophic microorganisms perform biochemical synthesis to elongate C1 chemicals into longer carbon chain organic chemicals using the carbon and electrons stored in the C1 chemical, and/or electrons and hydrogen from molecular hydrogen and/or valence or conduction electrons in solid state electrode materials and/or one or more of the following list of electron donors pumped or otherwise provided to the nutrient media, which include, but are not limited to one or more of the following: ammonia; ammonium; carbon monoxide; dithionite; elemental sulfur; hydrocarbons; metabisulfites; nitric oxide; nitrites; sulfates such as thiosulfates including but not limited to sodium thiosulfate (Na₂S₂O₃) or calcium thiosulfate (CaS₂O₃); sulfides such as hydrogen sulfide; sulfites; thionate; thionite; transition metals or their sulfides, oxides, chalcogenides, halides, hydroxides, oxyhydroxides, sulfates, or carbonates, in soluble or solid phases. The electron donors can be oxidized by electron acceptors in a chemosynthetic respiratory reaction. In certain embodiments, electron acceptors that are used for respiration by the microorganisms of the present invention include but are not limited to one or more of the following: oxygen, carbon dioxide, ferric iron or other transition metal ions, nitrates, nitrites, oxygen, or holes in solid state electrode materials. In certain non-limiting embodiments, the said chemotrophic microorganism is a knallgas or oxyhydrogen microorganism. [117] In certain embodiments the invention relates to chemotrophic bacterial strains that comprise zero or more exogenous nucleic acid sequences. The present invention arises in part from the discovery that chemotrophic bacteria and particular related microorganisms provide unforeseen advantages in the economic and large scale production of chemicals, sugars, starch, carbohydrates, polysaccharides, proteins, vitamins, nutrients, feeds, fertilizers, monomers, oils, fuels, and other biological substances from gaseous and waste carbon feedstocks, and also from the discovery of genetic techniques and systems for modifying these microorganisms for improved performance in these applications. The glucose, other sugars, starch, carbohydrates, polysaccharides, and other biochemicals synthesized by the microorganisms of the present invention can be applied to uses including but not limited to as: a dietary source of calories and/or fiber, petrochemical substitutes, monomers, feedstock for the production of polymers, lubricants, as ingredients in fertilizer, animal feed, food, personal care, and cosmetic products. In some embodiments of the present invention enzymatic and chemical processes can be utilized to produce vitamins, glucose, other sugars, starch, carbohydrates, polysaccharides, amino acids, and/or proteins. Some embodiments enable the production of food, animal feeds, and/or fertilizers. In addition, the present invention gives methods for culturing and/or modifying chemotrophic bacteria for improved yield of glucose, other sugars, starch, carbohydrates, and/or polysaccharides and/or lower production costs. In some embodiments, a genetically modified bacterium produces more of a certain type or types of: sugar, including but not limited to glucose; starch; carbohydrates; and/or polysaccharides; as compared to the same bacteria that is not genetically modified. [118] The present invention relates to methods and mechanisms to confer production and/or secretion of carbon-based products of interest including but not limited to sugars, starch, carbohydrates, polysaccharides, chemicals, monomers, polymers, amino acids, proteins, vitamins, nutraceutical or pharmaceutical products or intermediates thereof in obligate or facultative chemotrophic organisms such that these organisms convert carbon dioxide and/or other forms of inorganic carbon and/or syngas and/or other C1 compounds such as methanol and/or the liquid, gaseous, and solid products of pyrolytic reactions such as pyrolysis gas and/or oil, into carbon-based products of interest, and in particular the use of such organisms for the commercial production of sugars, including but not limited to glucose, starch, carbohydrates, polysaccharides, chemicals, monomers, polymers, amino acids, proteins, polysaccharides, vitamins, animal feeds, fertilizers, nutraceutical or pharmaceutical products or intermediates thereof. [119] In some embodiments the present invention also gives compositions and methods for chemical process steps that occur in series and/or in parallel with the chemosynthetic reaction steps that: convert unrefined raw input chemicals to more refined chemicals that are suited for supporting the chemosynthetic carbon fixing step; that convert energy inputs into a chemical form that can be used to drive chemosynthesis, and specifically into chemical energy in the form of electron donors and electron acceptors; that direct inorganic carbon captured from industrial or atmospheric or aquatic sources to the carbon fixation step or steps of the process under conditions that are suitable to support chemosynthetic carbon fixation; that further process the output products of the chemosynthetic carbon fixation steps into a form suitable for storage, shipping, and sale, with said products including but not limited to glucose and/or other sugars and/or starch and/or carbohydrates and/or polysaccharides and/or amino acids and/or proteins and/or vitamins and/or biomass. The fully chemical, abiotic, process steps combined with the biological chemosynthetic carbon fixation steps constitute the overall carbon capture and conversion process of the present invention. The present invention utilizes the unique ease of integrating chemoautotrophic microorganisms within a chemical process stream as a biocatalyst, as compared to other lifeforms. While not intending to be limited by theory, this unique capability and facility appears to arise from the fact that chemoautotrophs naturally act at the interface of biology and abiotic chemistry through their chemosynthetic mode of existence. [120] Unless defined otherwise herein, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. Singleton, et al., Dictionary of Microbiology and Molecular Biology, second ed., John Wiley and Sons, New York (1994), and Hale & Markham, The Harper Collins Dictionary of Biology, Harper Perennial, NY (1991) provide one of skill with a general dictionary of many of the terms used in this invention. Any methods and materials similar or equivalent to those described herein can be used in the practice or testing of the present invention. [121] The practice of the present invention will employ, unless otherwise indicated, conventional techniques of molecular biology (including recombinant techniques), microbiology, cell biology, and biochemistry, which are within the skill of the art. Such techniques are explained fully in the literature, for example, Molecular Cloning: A Laboratory Manual, second edition (Sambrook et al., 1989); Oligonucleotide Synthesis (M. J. Gait, ed., 1984; Current Protocols in Molecular Biology (F. M. Ausubel et al., eds., 1994); PCR: The Polymerase Chain Reaction (Mullis et al., eds., 1994); and Gene Transfer and Expression: A Laboratory Manual (Kriegler, 1990). [122] Numeric ranges provided herein are inclusive of the numbers defining the range. [123] Unless otherwise indicated, nucleic acids are written left to right in 5' to 3' orientation; amino acid sequences are written left to right in amino to carboxy orientation, respectively. Definitions [124] “A,” “an” and “the” include plural references unless the context clearly dictates, thus the indefinite articles “a”, “an,”, and “the” as used herein in the specification and in the claims, unless clearly indicated to the contrary, should be understood to mean “at least one.” [125] The phrase “and/or,” as used herein in the specification and in the claims, should be understood to mean “either or both” of the elements so conjoined, i.e., elements that are conjunctively present in some cases and disjunctively present in other cases. Other elements may optionally be present other than the elements specifically identified by the “and/or” clause, whether related or unrelated to those elements specifically identified unless clearly indicated to the contrary. Thus, as a non-limiting example, a reference to “A and/or B,” when used in conjunction with open-ended language such as “comprising” can refer, in one embodiment, to A without B (optionally including elements other than B); in another embodiment, to B without A (optionally including elements other than A); in yet another embodiment, to both A and B (optionally including other elements); etc. [126] The term “about” as used herein when referring to a measurable value such as an amount, a temporal duration, and the like, is meant to encompass variations of ±20%, ±10%, ±5%, ±1%, or ±0.1% from the specified value, as such variations are appropriate to perform the disclosed methods. [127] The terms “amino acid” refer to a molecule containing both an amine group and a carboxyl group that are bound to a carbon, which is, designated the alpha-carbon. Suitable amino acids include, without limitation, both the D- and L-isomers of the naturally occurring amino acids, as well as non-naturally occurring amino acids prepared by organic synthesis or other metabolic routes. In some embodiments, a single “amino acid” might have multiple sidechain moieties, as available per an extended aliphatic or aromatic backbone scaffold. Unless the context specifically indicates otherwise, the term amino acid, as used herein, is intended to include amino acid analogs. [128] The term “biomass” refers to a material produced by growth and/or propagation of cells. Biomass may contain cells and/or intracellular contents as well as extracellular material, including, but not limited to, compounds secreted by a cell. [129] The term “bioreactor” or “fermenter” refers to a closed or partially closed vessel in which cells are grown and maintained. The cells may be, but are not necessarily held in liquid suspension. In some embodiments, rather than being held in liquid suspension, cells may alternatively be growing and/or maintained in contact with, on, or within another non- liquid substrate including but not limited to a solid growth support material. [130] The term “carbohydrate” as used herein refers to biomolecule composed of carbon, hydrogen, and oxygen atoms where the hydrogen to oxygen ratio is often 2:1. [131] The term “catalyst” refers to a chemical actor, such as a molecule or macromolecular structure, which accelerates the speed at which a chemical reaction occurs where a reactant or reactants is converted into a product or products, while the catalyst is not turned into a product itself, or otherwise changed or consumed at the completion of the chemical reaction. After a catalyst participates in one chemical reaction, because it is unchanged, it may participate in further chemical reactions, acting on additional reactants to create additional products. To accelerate a chemical reaction a catalyst decreases the activation energy barrier across the reaction path allowing it to occur at a colder temperature, or faster at a given temperature. In this way a more rapid approach of the system to chemical equilibrium may be achieved. Catalysts subsume enzymes, which are protein catalysts. [132] The term “cellulosic material” refers to any material with a high amount of cellulose, which is a polysaccharide having the formula (C₆H₁₀O₅)_n, that generally consists of a linear chain of hundreds to thousands of ^(1→4) linked D-glucose monomers. Sources of cellulosic material include but are not limited to cardboard, cotton, corn stover, paper, lumber chips, sawdust, sugar beet pulp, sugar cane bagasses, and switchgrass. [133] The term “CoA” or “coenzyme A” refers to an organic cofactor for condensing enzymes involved in fatty acid synthesis and oxidation, pyruvate oxidation, acetyl or other acyl group transfer, and in other acetylation. [134] The term “cofactor” subsumes all molecules needed by an enzyme to perform its catalytic activity. In some embodiments, the cofactor is any molecule apart from the substrate. [135] In the claims, as well as in the specification, all transitional phrases such as “comprising,” “including,” “carrying,” “having,” “containing,” “involving,” “holding,” and the like are to be understood to be open-ended, i.e., to mean including but not limited to. Only the transitional phrases “consisting of” and “consisting essentially of” shall be closed or semi-closed transitional phrases, respectively. [136] The terms “exogenous gene” means a nucleic acid that has been recombinantly introduced into a cell, which encodes the synthesis of RNA and/or protein. In some embodiments, the exogenous gene is introduced by transformation. In some embodiments, the exogenous gene is introduced into the cell by electroporation. A transformed cell may be referred to as a recombinant cell, into which additional exogenous gene(s) may be introduced. The exogenous gene put into the host species may be taken from a different species (this is called heterologous), or it may naturally occur within the same species (this is homologous as defined below). Therefore, exogenous genes subsume homologous genes that are integrated within or introduced to regions of the genome, episome, or plasmid that differ from the locations where the gene naturally occurs. Multiple copies of the exogenous gene may be introduced into the cell. An exogenous gene may be present in more than one copy within the host cell or transformed cell. In some embodiments, the microorganism comprises between and including 1 and 10,000 copies of the nucleic acid that encodes an exogenous protein. In some embodiments, the microorganism comprises between and including 1 and 1,000 copies of the nucleic acid that encodes an exogenous protein. In some embodiments, the microorganism comprises between and including 1 and 10,000 copies of the nucleic acid that encodes an exogenous protein. In some embodiments, the microorganism comprises between and including 1 and 1,000 copies of the nucleic acid that encodes an exogenous protein. In some embodiments, the microorganism comprises between and including 1 and 500 copies of the nucleic acid that encodes an exogenous protein. In some embodiments, the exogenous gene is maintained by a cell as an insertion into the genome or as an episomal molecule. In some embodiments, the microorganism comprises no more than 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 20, 30, 40, 50, 60, 70, 80, 90, 100, or 1000 copies of the one or more nucleic acids that encode one or more exogenous proteins. [137] As used herein, the term “expressible form” refers to gene constructs that contain the necessary regulatory elements operably linked to a coding sequence that encodes an enzyme or fragment thereof capable of conferring enzymatic activity to a cell, such that when present in the cell, the coding sequence will be expressed. In some embodiments of the invention, the composition comprising the microorganisms or bacterial cells of the present invention comprise no more than ten expressible forms of exogenous nucleic acid sequences. [138] Glucose is a sugar having the molecular formula C6H12O6. [139] The term “lignocellulosic material” is any material composed of cellulose, hemicellulose, and lignin where the carbohydrate polymers (cellulose and hemicelluloses) are tightly bound to lignin. Lignocellulosic materials subsume agricultural residues (including corn stover and sugarcane bagasse), most biomass energy crops, wood residues (including sawmill and paper mill discards), and a substantial fraction of municipal waste. [140] The terms “lipids” refers to category of molecules that can be dissolved in nonpolar solvents (such as, but not limited to, chloroform and/or ether) and which also have low or no solubility in water. The hydrophobic character of lipid molecules typically results from the presence of long chain hydrocarbon sections within the molecule. Lipids subsume the following molecule types: hydrocarbons, fatty acids (saturated and unsaturated), fatty alcohols, fatty aldehydes, hydroxy acids, diacids, monoglycerides, diglycerides, triglycerides, phospholipids, sphingolipids, sterols such as cholesterol and steroid hormones, fat-soluble vitamins (such as vitamins A, D, E and K), polyketides, terpenoids, and waxes. [141] The term “lysate” refers to the liquid containing a mixture and/or a solution of cell contents that result from cell lysis. In some embodiments, the methods of the present invention comprise a purification of chemicals or mixture of chemicals in a cellular lysate. In some embodiments, the methods of the present invention comprise a purification of amino acids and/or protein in a cellular lysate. [142] The term “lysis” refers to the rupture of the plasma membrane and if present the cell wall of a cell such that a significant amount of intracellular material escapes to the extracellular space. Lysis can be performed using electrochemical, mechanical, osmotic, thermal, or viral means. In some embodiments, the methods of the present invention comprise performing a lysis of cells or microorganisms described herein in order to separate a chemical or mixture of chemicals from the contents of a bioreactor. In some embodiments, the methods of the present invention comprise performing a lysis of cells or microorganisms described herein, in order to separate an amino acid or mixture of amino acids and/or proteins from the contents of a bioreactor. [143] Polysaccharides are long-chain polymeric carbohydrates composed of monosaccharide units bound together by glycosidic linkages. [144] Starch is a polymer consisting of glucose monomers joined by glycosidic bonds. [145] The term “sugar” as used herein refers to sweet-tasting, soluble carbohydrates. [146] As used herein in the specification and in the claims, “or” should be understood to have the same meaning as “and/or” as defined above. For example, when separating items in a list, “or” or “and/or” shall be interpreted as being inclusive, i.e., the inclusion of at least one, but also including more than one, of a number or list of elements, and, optionally, additional unlisted items. Only terms clearly indicated to the contrary, such as “only one of” or “exactly one of,” or, when used in the claims, “consisting of,” will refer to the inclusion of exactly one element of a number or list of elements. In general, the term “or” as used herein shall only be interpreted as indicating exclusive alternatives (i.e. “one or the other but not both”) when preceded by terms of exclusivity, such as “either,” “one of,” “only one of,” or “exactly one of.” “Consisting essentially of,” when used in the claims, shall have its ordinary meaning as used in the field of patent law. [147] “Titer” refers to amount of a substance produced by a microorganism per unit volume in a microbial fermentation process. For example, biomass titer may be expressed as grams of biomass produced per liter of solution. [148] “Yield” refers to amount of a product produced from a feed material (for example, sugar) relative to the total amount of the substance that would be produced if all of the feed substance were converted to product. For example, amino acid yield may be expressed as % of amino acid produced relative to a theoretical yield if 100% of the feed substance were converted to amino acid. [149] “Productivity” refers to the amount of a substance produced by a microorganism per unit volume per unit time in a microbial fermentation process. For example, biomass productivity may be expressed as grams of biomass produced per liter of solution per hour. [150] As used herein, the term “polynucleotide” refers to a polymeric form of nucleotides of any length and any three-dimensional structure and single- or multi-stranded (e.g., single- stranded, double-stranded, triple-helical, etc.), which contain deoxyribonucleotides, ribonucleotides, and/or analogs or modified forms of deoxyribonucleotides or ribonucleotides, including modified nucleotides or bases or their analogs. Because the genetic code is degenerate, more than one codon may be used to encode a particular amino acid, and the present invention encompasses polynucleotides, which encode a particular amino acid sequence. Any type of modified nucleotide or nucleotide analog may be used, so long as the polynucleotide retains the desired functionality under conditions of use, including modifications that increase nuclease resistance (e.g., deoxy, 2'-O-Me, phosphorothioates, etc.). Labels may also be incorporated for purposes of detection or capture, for example, radioactive or nonradioactive labels or anchors, e.g., biotin. The term polynucleotide also includes peptide nucleic acids (PNA). Polynucleotides may be naturally occurring or non-naturally occurring. The terms “polynucleotide,” “nucleic acid,” and “oligonucleotide” are used herein interchangeably. Polynucleotides may contain RNA, DNA, or both, and/or modified forms and/or analogs thereof. A sequence of nucleotides may be interrupted by non-nucleotide components. One or more phosphodiester linkages may be replaced by alternative linking groups. These alternative linking groups include, but are not limited to, embodiments wherein phosphate is replaced by P(O)S (“thioate”), P(S)S (“dithioate”), (O)NR2 (“amidate”), P(O)R, P(O)OR', CO or CH2 (“formacetal”), in which each R or R' is independently H or substituted or unsubstituted alkyl (1-20 C) optionally containing an ether (--O--) linkage, aryl, alkenyl, cycloalkyl, cycloalkenyl or araldyl. Not all linkages in a polynucleotide need be identical. Polynucleotides may be linear or circular or comprise a combination of linear and circular portions. [151] As used herein, “polypeptide” refers to a composition comprised of amino acids and recognized as a protein by those of skill in the art. The conventional one-letter or three- letter code for amino acid residues is used herein. The terms “polypeptide” and “protein” are used interchangeably herein to refer to polymers of amino acids of any length. The polymer may be linear or branched, it may comprise modified amino acids, and it may be interrupted by non-amino acids. The terms also encompass an amino acid polymer that has been modified naturally or by intervention; for example, disulfide bond formation, glycosylation, lipidation, acetylation, phosphorylation, or any other manipulation or modification, such as conjugation with a labeling component. Also included within the definition are, for example, polypeptides containing one or more analogs of an amino acid (including, for example, unnatural amino acids, etc.), as well as other modifications known in the art. [152] As used herein, a “vector” refers to a polynucleotide sequence designed to introduce nucleic acids into one or more cell types. Vectors include cloning vectors, expression vectors, shuttle vectors, plasmids, phage particles, cassettes and the like. [153] As used herein, the term “expression” refers to the process by which a polypeptide is produced based on the nucleic acid sequence of a gene. The process includes both transcription and translation. [154] As used herein, “expression vector” refers to a DNA construct containing a DNA coding sequence (e.g., gene sequence) that is operably linked to one or more suitable control sequence(s) capable of effecting expression of the coding sequence in a host. Such control sequences include a promoter to effect transcription, an optional operator sequence to control such transcription, a sequence encoding suitable mRNA ribosome binding sites, and sequences that control termination of transcription and translation. The vector may be a plasmid, a phage particle, or simply a potential genomic insert. Once transformed into a suitable host, the vector may replicate and function independently of the host genome, or may, in some instances, integrate into the genome itself. The plasmid is the most commonly used form of expression vector. However, the invention is intended to include such other forms of expression vectors that serve equivalent functions and which are, or become, known in the art. [155] A “gene” refers to a DNA segment that is involved in producing a polypeptide and includes regions preceding and following the coding regions as well as intervening sequences (introns) between individual coding segments (exons). [156] As used herein, the term “host cell” refers to a cell or cell line into which a recombinant expression vector for production of a polypeptide may be transfected for expression of the polypeptide. Host cells include progeny of a single host cell, and the progeny may not necessarily be completely identical (in morphology or in total genomic DNA complement) to the original parent cell due to natural, accidental, or deliberate mutation. A host cell includes cells transfected or transformed in vivo with an expression vector. [157] The term “recombinant,” refers to genetic material (i.e., nucleic acids, the polypeptides they encode, and vectors and cells comprising such polynucleotides) that has been modified to alter its sequence or expression characteristics, such as by mutating the coding sequence to produce an altered polypeptide, fusing the coding sequence to that of another gene, placing a gene under the control of a different promoter, expressing a gene in a heterologous organism, expressing a gene at a decreased or elevated levels, expressing a gene conditionally or constitutively in manner different from its natural expression profile, and the like. Generally recombinant nucleic acids, polypeptides, and cells based thereon, have been manipulated by man such that they are not identical to related nucleic acids, polypeptides, and cells found in nature. [158] The term “derived from” encompasses the terms “originated from,” “obtained from,” “obtainable from,” “isolated from,” and “created from,” and generally indicates that one specified material finds its origin in another specified material or has features that can be described with reference to another specified material. [159] The term "culturing" refers to growing a population of cells, e.g., microbial cells, under suitable conditions for growth, in a liquid or solid medium. [160] The term “introduced,” in the context of inserting a nucleic acid sequence into a cell, includes “transfection,” “transformation,” or “transduction” and refers to the incorporation of a nucleic acid sequence into a eukaryotic or prokaryotic cell wherein the nucleic acid sequence may be incorporated into the genome of the cell (e.g., chromosome, plasmid, plastid, or mitochondrial DNA), converted into an autonomous replicon, or transiently expressed. [161] As used herein, the terms “transformed,” “stably transformed,” and “transgenic” refer to a cell that has a non-native (e.g., heterologous or exogenous) nucleic acid sequence integrated into its genome or as an episomal plasmid that is maintained through multiple generations. [162] The terms “recovered,” “isolated,” “purified,” and “separated” as used herein refer to a material (e.g., a sugar, polysaccharide, nucleic acid, or cell) that is removed from at least one component with which it is naturally associated. For example, these terms may refer to a material that is substantially or essentially free from components which normally accompany it as found in its native state, such as, for example, an intact biological system. [163] As used herein, “wild-type,” “native,” and “naturally-occurring” proteins are those found in nature. The terms “wild-type sequence” refers to an amino acid or nucleic acid sequence that is found in nature or naturally occurring. In some embodiments, a wild-type sequence is the starting point of a protein engineering project, for example, production of variant proteins. “Wild-type” in reference to a microorganism refers to a microorganism as it occurs in nature. [164] “Chemoautotrophic” refers to organisms that obtain energy by the oxidation of chemical electron donors by chemical electron acceptors and synthesize all the organic compounds needed by the organism to live and grow from carbon dioxide. [165] “Lithoautotrophic” refers to a specific type of chemoautotrophy where the organism utilizes the oxidation of inorganic chemical electron donors by inorganic chemical electron acceptors as an energy source. [166] The term “knallgas” refers to the mixture of molecular hydrogen and oxygen gas. A “knallgas microorganism” is a microbe that can use hydrogen as an electron donor and oxygen as an electron acceptor in respiration for the generation of intracellular energy carriers such as Adenosine-5'-triphosphate (ATP). The terms “oxyhydrogen” and “oxyhydrogen microorganism” can be used synonymously with “knallgas” and “knallgas microorganism” respectively. Knallgas microorganisms generally use molecular hydrogen by means of hydrogenases, with some of the electrons donated from H2 being utilized for the reduction of NAD⁺ (and/or other intracellular reducing equivalents) and some of the electrons from H₂ being used for aerobic respiration. Knallgas microorganisms generally fix CO2 autotrophically, through pathways including but not limited to the Calvin Cycle or the reverse citric acid cycle [“Thermophilic bacteria”, Jakob Kristjansson, Chapter 5, Section III, CRC Press, (1992)]. [167] “Heterotrophic” refers to organisms that cannot synthesize all the organic compounds needed by the organism to live and grow from carbon dioxide, and which must utilize organic compounds for growth. [168] “Hydrogen-oxidizer” refers to microorganisms that utilize reduced H₂ as an electron donor for the production of intracellular reducing equivalents and/or in respiration. [169] “Acetogen” refers to microorganisms that generate acetate and/or other short chain organic acids up to C4 chain length as a product of anaerobic respiration. [170] “Methanogen” refers to a microorganism that generates methane as a product of anaerobic respiration. [171] “Methylotroph” refers to microorganisms that can use reduced one-carbon compounds, such as but not limited to methanol or methane, as a carbon source and/or as an electron donor for their growth. [172] “Extremophile” refers to microorganisms that thrive in physically or geochemically extreme conditions (e.g., high or low temperature, pH, or high salinity) compared to conditions on the surface of the Earth or the ocean typically tolerated by most life forms. [173] “Thermophile” refers to a type of extremophile that thrives at relatively high temperatures for life, between 45 and 122°C. [174] “Hyperthermophile” refers to a type of extremophile that thrives in extremely hot environments for life, from 60°C (140 °F) upwards. [175] “Acidophile” refers to a type of extremophile that thrives under highly acidic conditions (usually at pH 2.0 or below). [176] “Halophile” refers to a type of extremophile that thrives in environments with very high concentrations of salt. [177] “Psychrophile” refers to a type of extremophile capable of growth and reproduction in cold temperatures, ranging from 10°C and below. [178] “Producer gas” refers to gas mixture containing various proportions of H2, CO, and CO2, and having heat value typically ranging between one half and one tenth that of natural gas per unit volume under standard conditions. Producer gas can be generated various ways from a variety of feedstocks including gasification, steam reforming, or autoreforming of carbon-based feedstocks. In addition to H2, CO, and CO2, producer gases can contain other constituents including but not limited to methane, hydrogen sulfide, condensable gases, tars, and ash depending upon the generation process and feedstock. The proportion of N₂ in the mixture can be high or low depending upon if air is used as an oxidant in the reactor or not and if the heat for the reaction is provided by direct combustion or through indirect heat exchange. [179] “Syngas” or “Synthesis gas” refers to a type of gas mixture, which like producer gas contains H₂ and CO, but which has been more specifically tailored in terms of H₂ and CO content and ratio and levels of impurities for the synthesis of a particular type of chemical product, such as but not limited to methanol or fischer-tropsch diesel. [180] “Carbon source” refers to the types of molecules from which a microorganism derives the carbon needed for organic biosynthesis. [181] “Energy source” refers to either the electron donor that is oxidized by oxygen in aerobic respiration or the combination of electron donor that is oxidized and electron acceptor that is reduced in anaerobic respiration. [182] “Biphasic growth environment” refers to a growth environment containing two immiscible liquid phases. [183] The term “gasification” refers to a generally high temperature process that converts carbon-based materials into a mixture of gases including hydrogen, carbon monoxide, and carbon dioxide called synthesis gas, syngas or producer gas. The process generally involves partial combustion and/or the application of externally generated heat along with the controlled addition of oxygen and/or steam such that insufficient oxygen is present for complete combustion of the carbon-based material. [184] The term "hydrophobic" refers to matter that has low solubility in water and greater solubility in a hydrophobic phase than in an aqueous phase. [185] The terms “microorganism” and “microbe” mean microscopic single celled life forms, including but not limited to bacteria, fungi, and algae microorganisms. [186] The term “molecule” means any distinct or distinguishable structural unit of matter comprising one or more atoms, and includes for example sugars, hydrocarbons, lipids, polypeptides and polynucleotides. [187] The term “organic compound” refers to any gaseous, liquid, or solid chemical compounds which contain carbon atoms with the following exceptions that are considered inorganic: carbides, carbonates, simple oxides of carbon, cyanides, and allotropes of pure carbon such as diamond and graphite. [188] The term “precursor to” or “precursor of” is an intermediate towards the production of one or more of the components of a finished product. [189] The term “producing” includes both the production of compounds intracellularly and extracellularly, which is to include the secretion of compounds from the cell. [190] Unless otherwise defined herein, scientific and technical terms used in connection with the present disclosure shall have the meanings that are commonly understood by those of ordinary skill in the art. Further, unless otherwise required by context, singular terms shall include pluralities and plural terms shall include the singular. The methods and techniques of the present disclosure are generally performed according to conventional methods well-known in the art. Generally, nomenclatures used in connection with, and techniques of biochemistry, enzymology, molecular and cellular biology, microbiology, genetics and protein and nucleic acid chemistry and hybridization described herein are those well-known and commonly used in the art. The methods and techniques of the present disclosure are generally performed according to conventional methods well known in the art and as described in various general and more specific references that are cited and discussed throughout the present specification unless otherwise indicated. Production of glucose, other sugars, starch, carbohydrates, polysaccharides, and other biological nutrients from gaseous energy and carbon substrates [191] In some embodiments natural or engineered microorganisms are provided that are capable of converting producer gas or a gas mixture containing H2 and/or CO and/or CO2 and/or CH₄ into glucose, other sugars, starch, carbohydrates, polysaccharides, and/or other biological nutrients. In some embodiments, natural or engineered microorganisms are provided that are capable of converting producer gas or a gas mixture containing H2 and/or CO and/or CO2 and/or CH4 into a vitamin. In certain embodiments that vitamin is a B vitamin including but not limited to one or more of the following: vitamin B1, B2, and/or B12. [192] The inventive subject matter comprises, in some embodiments, a natural microorganism capable of growing on syngas, and/or H2 and CO2, and/or CO, and/or CH4, and/or other waste gases and which is capable of producing glucose, other sugars, starch, carbohydrates, polysaccharides and/or other biological nutrients using said gases as a growth substrate. The inventive subject matter comprises, in other embodiments, a natural microorganism capable of growing on syngas, and/or H2 and CO2, and/or CO, and/or CH4, and/or other waste gases and capable of producing vitamin B1, vitamin B2, and/or vitamin B12 and/or other vitamins. [193] In some embodiments, the instant invention provides for a method of producing glucose, other sugars, starch, carbohydrates, polysaccharides, and/or other biological nutrients including but not limited to vitamins, by combining, in a bioreactor or solution, a carbon-containing gas, and a natural or engineered strain microorganism that converts a carbon-containing gas such as syngas, producer gas, CO₂, carbon monoxide and/or mixtures of the same containing hydrogen gas; and/or C1 compounds, gaseous or liquid, including but not limited to methanol or methane, into glucose, other sugars, starch, carbohydrates, polysaccharides, and/or other biological nutrients including but not limited to vitamins. [194] Producer gas used in some embodiments of the process may come from sources that include gasification of waste feedstock and/or biomass residue feedstock, or waste gas from industrial processes, or reforming of methane containing gases including by not limited to natural gas, biogas, landfill gas, stranded natural gas and/or flared natural gas. In some embodiments, methane may be converted to glucose, other sugars, starch, carbohydrates, polysaccharides, and/or other biological nutrients including but not limited to vitamins, using engineered or natural microorganisms and methods described herein. [195] In some embodiments, the inventive subject matter comprises an engineered microorganism with one or more exogenous genes. [196] Chemoautotrophs are capable of performing chemosynthetic reactions that fix CO2, and/or other forms of inorganic carbon, to organic compounds, using the potential energy stored in inorganic chemicals to drive the reaction, rather than radiant energy from light as in microorganisms performing photosynthesis [Shively et al. (1998) supra; Smith et al. (1967) supra; Scott and Cavanaugh (2007) supra]. Carbon fixing biochemical pathways that occur in chemoautotrophs include the reductive tricarboxylic acid cycle, the Calvin- Benson-Bassham cycle [Shively, et al. (1998) supra], and the Wood-Ljungdahl pathway [Ljungdahl (1986) supra; Lee, et al. (2008) supra; Fischer, et al. (2008) supra]. [197] Certain non-limiting embodiments of the invention relate to a wild-type or genetically modified microorganism and compositions comprising such a microorganism, wherein the microorganism comprises zero or one or more exogenous genes and wherein the microorganism grows on carbon-containing gas or utilizes a gaseous feedstock selected from syngas, CO2, H2, CO, CH4, or mixtures of gas comprising one or more gases selected from syngas, CO2, H2, CO, or CH4. [198] In some embodiments, the microorganism of the inventive subject matter is selected from the Ralstonia microorganisms. In some embodiments, the microorganism is Ralstonia eutropha. In some embodiments, the microorganism is selected from Cupriavidus microorganisms. In some embodiments, the microorganism is Cupriavidus necator. In some embodiments, the microorganism is Cupriavidus necator DSM531 or DSM541. In some embodiments, the microorganism is selected from the genus Hydrogenobacter. In some embodiments, the microorganism is Hydrogenobacter thermophilus. In some embodiments, the microorganism contains the reverse tricarboxylic acid cycle (rTCA), also known as the reverse citric acid cycle or the reverse Krebs cycle. [See, e.g., Miura, A., Kameya, M., Arai, H., Ishii, M. & Igarashi, Y. A soluble NADH- dependent fumarate reductase in the reductive tricarboxylic acid cycle of Hydrogenobacter thermophilus TK-6. J Bacteriol 190: 7170-7177, doi:JB.00747-08 [pii] 10.1128/JB.00747- 08 (2008).; Shively, et al. (1998) supra, which are incorporated herein by reference in their entireties.] [199] In some embodiments the microorganism is Rhodococcus opacus or Rhodococcus jostii or Rhodococcus sp.. In some non-limiting embodiments, the microorganism is Rhodococcus opacus DSM 43205 and/or Rhodococcus sp. DSM 3346. In some embodiments, the natural or engineered strain includes but is not limited to hydrogen utilizing microbes including but not limited to the genera Rhodococcus or Gordonia, Ralstonia or Cupriavidus. [200] The invention relates to a cell and compositions comprising a cell of the class Actinobacteria comprising zero or one or more exogenous genes. The invention also relates to cells and compositions comprising cells of the family of Nocardiaceae comprising zero or one or more exogenous genes. The invention also relates to cells and compositions comprising cells of Corynebacterium, Gordonia, Rhodococcus, Mycobacterium and Tsukamurella comprising zero or one or more exogenous genes. In some embodiments, the invention relates to cells of the family of Nocardiaceae comprising zero or one or more exogenous genes, wherein the cell is not a cell of the genus Mycobacterium. In some embodiments, the invention provides a cell and compositions comprising a cell of the genus Rhodococcus comprising zero or one or more exogenous genes, and in some embodiments the cell is a strain of the species Rhodococcus sp., Rhodococcus opacus, Rhodococcus aetherivorans; Rhodococcus aurantiacus; Rhodococcus baikonurensis; Rhodococcus boritolerans; Rhodococcus equi; Rhodococcus coprophilus; Rhodococcus corynebacterioides; Nocardia corynebacterioides (synonym: Nocardia corynebacterioides); Rhodococcus erythropolis; Rhodococcus fascians; Rhodococcus globerulus; Rhodococcus gordoniae; Rhodococcus jostii; Rhodococcus koreensis; Rhodococcus kroppenstedtii; Rhodococcus maanshanensis; Rhodococcus marinonascens; Rhodococcus opacus; Rhodococcus percolatus; Rhodococcus phenolicus; Rhodococcus polyvorum; Rhodococcus pyridinivorans; Rhodococcus rhodochrous; Rhodococcus rhodnii; (synonym: Nocardia rhodnii); Rhodococcus ruber (synonym: Streptothrix rubra); Rhodococcus sp. RHA1; Rhodococcus triatomae; Rhodococcus tukisamuensis; Rhodococcus wratislaviensis (synonym: Tsukamurella wratislaviensis); Rhodococcus yunnanensis; or Rhodococcus zopfii. In some embodiments, the cell comprising zero or one or more exogenous genes is one or more of the following: strain Rhodococcus opacus DSM number 43205 or 43206; Rhodococcus sp. DSM number 3346. In some embodiments, the invention relates to a Rhodococcus cell or composition comprising a Rhodococcus cell, wherein the cell is not a species selected from Rhodococcus equi or Rhodococcus fascians. [201] In some embodiments the microorganism is from the suborder corynebacterineae or the family burkholderiaceae. In some embodiments, the cell or compositions comprising one of more cells is not E. coli. In some embodiments, the cell of the present invention is not pathogenic to animals or plants. In some embodiments, the cell of the present invention is not pathogenic to humans. In some embodiments, the cell or compositions comprising one of more cells is from the genus Ralstonia. In some embodiments, the cell or compositions comprising one of more cells is from the species Ralstonia eutropha or Cupriavidus necator or Cupriavidus metallidurans. In some embodiments, the cell comprising zero or one or more exogenous genes is strain Cupriavidus necator DSM number 531 or 541. [202] In some embodiments, the composition comprises a microorganism that can naturally grow on H₂/CO₂ and/or syngas, and wherein the microorganism can naturally accumulate polyhydroxybutyrate (PHB) or polyhydroxyalkanoate (PHA) to 50% or more of the cell biomass by weight. In some embodiments, the microorganisms have a native ability to direct a high flux of carbon through the acetyl-CoA metabolic intermediate, which can lead into fatty acid biosynthesis, along with a number of other synthetic pathways including PHA and PHB synthesis, as well as amino acids. In some embodiments, the microorganism exhibiting these traits is Cupriavidus necator (DSM 531 or DSM 541). [203] In some embodiments the natural or engineered strain includes but is not limited to Corynebacterium autotrophicum. In some embodiments, the natural or engineered strain includes but is not limited to Corynebacterium glutamicum. In some embodiments, the microorganism is Hydrogenovibrio marinus. In some embodiments, the microorganism is Rhodopseudomonas capsulata, Rhodopseudomonas palustris, or Rhodobacter sphaeroides. [204] In some embodiments, the microorganism is an oxyhydrogen or knallgas strain. In some embodiments the microorganisms comprise one or more of the following knallgas microorganisms: Aquifex pyrophilus, Aquifex aeolicus, or other Aquifex sp.; Cupriavidus necator, Cupriavidus metallidurans, or other Cupriavidus sp.; Corynebacterium autotrophicum or other Corynebacterium sp.; Gordonia desulfuricans, Gordonia polyisoprenivorans, Gordonia rubripertincta, Gordonia hydrophobica, Gordonia westfalica, and other Gordonia sp.; Nocardia autotrophica, Nocardia opaca, or other Nocardia sp.; purple non-sulfur photosynthetic bacteria including but not limited to Rhodobacter sphaeroides, Rhodopseudomonas palustris, Rhodopseudomonas capsulata, Rhodopseudomonas viridis, Rhodopseudomonas sulfoviridis, Rhodopseudomonas blastica, Rhodopseudomonas spheroides, Rhodopseudomonas acidophila and other Rhodopseudomonas sp. and Rhodobacter sp.; Rhodospirillum rubrum, and other Rhodospirillum sp.; Rhodococcus opacus and other Rhodococcus sp.; Rhizobium japonicum and other Rhizobium sp.; Thiocapsa roseopersicina and other Thiocapsa sp.; Pseudomonas facilis, Pseudomonas flava, Pseudomonas putida, Pseudomonas hydrogenovora, Pseudomonas hydrogenothermophila, Pseudomonas palleronii, Pseudomonas pseudoflava, Pseudomonas saccharophila, Pseudomonas thermophile, and other Pseudomonas sp.; Hydrogenomonas pantotropha, Hydrogenomonas eutropha, Hydrogenomonas facilis, and other Hydrogenomonas sp.; Hydrogenobacter thermophiles, Hydrogenobacter halophilus, Hydrogenobacter hydrogenophilus, and other Hydrogenobacter sp.; Hydrogenophilus islandicus and other Hydrogenophilus sp.; Hydrogenovibrio marinus and other Hydrogenovibrio sp.; Hydrogenothermus marinus and other Hydrogenothermus sp.; Helicobacter pylori and other Helicobacter sp.; Xanthobacter autotrophicus, Xanthobacter flavus and other Xanthobacter sp.; Hydrogenophaga flava, Hydrogenophaga palleronii, Hydrogenophaga pseudoflava and other Hydrogenophaga sp.; Bradyrhizobium japonicum and other Bradyrhizobium sp.; Ralstonia eutropha and other Ralstonia sp.; Alcaligenes eutrophus, Alcaligenes facilis, Alcaligenes hydrogenophilus, Alcaligenes latus, Alcaligenes paradoxus, Alcaligenes ruhlandii and other Alcaligenes sp.; Amycolata sp.; Aquaspirillum autotrophicum and other Aquaspirillum sp.; Arthrobacter strain 11/X, Arthrobacter methylotrophus, and other Arthrobacter sp.; Azospirillum lipoferum and other Azospirillum sp.; Variovorax paradoxus, and other Variovorax sp.; Acidovorax facilis, and other Acidovorax sp.; Bacillus schlegelii, Bacillus tusciae and other Bacillus sp.; Calderobacterium hydrogenophilum and other Calderobacterium sp.; Derxia gummosa and other Derxia sp.; Flavobacterium autothermophilum and other Flavobacterium sp.; Microcyclus aquaticus and other Microcyclus; Mycobacterium gordoniae and other Mycobacterium sp.; Paracoccus denitrificans and other Paracoccus sp.; Persephonella marina, Persephonella guaymasensis and other Persephonella sp.; Renobacter vacuolatum and other Renobacter sp.; Streptomycetes coelicoflavus, Streptomycetes griseus, Streptomycetes xanthochromogenes, Streptomycetes thermocarboxydus, and other Streptomycetes sp.; Thermocrinis ruber and other Thermocrinis sp.; Wautersia sp.; cyanobacteria including but not limited to Anabaena oscillarioides, Anabaena spiroides, Anabaena cylindrica, and other Anabaena sp., and Arthrospira platensis, Arthrospira maxima and other Arthrospira sp.; green algae including but not limited to Scenedesmus obliquus and other Scenedesmus sp., Chlamydomonas reinhardii and other Chlamydomonas sp., Ankistrodesmus sp., Rhaphidium polymorphium and other Rhaphidium sp; as well as a consortiums of microorganisms that include oxyhydrogen microorganisms. [205] Oxyhydrogen or knallgas microorganisms are generally described in Chapter 5, Section III of Thermophilic Bacteria, a book by Jakob Kristjansson, CRC Press, 1992, which is incorporated herein by reference. Generally, oxyhydrogen microorganisms are capable of performing the oxyhydrogen reaction. Oxyhydrogen microorganisms generally have the ability to use molecular hydrogen by means of hydrogenases with some of the electrons donated from H₂ being utilized for the reduction of NAD⁺ (and/or other intracellular reducing equivalents) and the rest of the electrons for aerobic respiration. In addition, oxyhydrogen microorganisms generally are capable of fixing CO2 autotrophically, through pathways such as the reverse Calvin Cycle or the reverse citric acid cycle. [206] In some non-limiting embodiments the invention relates to compositions comprising and methods of using chemoautotrophic metabolism to produce ATP for the support of ATP consuming biosynthetic reactions and cellular maintenance, without the co-production of methane or short chain organic acids such as acetic or butyric acid, by means of energy conserving reactions for the production of ATP, which use inorganic electron donors and electron acceptors, including but not limited to the oxyhydrogen reaction. [207] A number of different microorganisms have been characterized that are capable of growing on carbon monoxide as an electron donor and/or carbon source (i.e. carboxydotrophic microorganisms). In some cases, carboxydotrophic microorganisms can also use H2 as an electron donor and/or grow mixotrophically. In some cases, the carboxydotrophic microorganisms are facultative chemolithoautotrophs. [Biology of the Prokaryotes, edited by J Lengeler, G. Drews, H. Schlegel, John Wiley & Sons, Jul 10, 2009, incorporated herein by reference in its entirety.] In some embodiments the microorganisms comprise one or more of the following carboxydotrophic microorganisms: Acinetobacter sp.; Alcaligenes carboxydus and other Alcaligenes sp.; Arthrobacter sp.; Azomonas sp.; Azotobacter sp.; Bacillus schlegelii and other Bacillus sp.; Hydrogenophaga pseudoflava and other Hydrogenophaga sp.; Pseudomonas carboxydohydrogena, Pseudomonas carboxydovorans, Pseudomonas compransoris, Pseudomonas gazotropha, Pseudomonas thermocarboxydovorans and other Pseudomonas sp.; Rhizobium japonicum and other Rhizobium sp.; Streptomyces G26 Streptomyces thermoautotrophicus and other Streptomyces sp.. In certain embodiments of the present invention a carboxydotrophic microorganism is used. In certain embodiments, a carboxydotrophic microorganism that is capable of chemolithoautotrophy is used. In certain embodiments, a carboxydotrophic microorganism that is able to use H2 as an electron donor in respiration and/or biosynthesis is used. [208] In some embodiments the microorganisms comprise obligate and/or facultative chemoautotrophic microorganisms including one or more of the following: Acetoanaerobium sp.; Acetobacterium sp.; Acetogenium sp.; Achromobacter sp.; Acidianus sp.; Acinetobacter sp.; Actinomadura sp.; Aeromonas sp.; Alcaligenes sp.; Alcaliqenes sp.; Aquaspirillum sp.; Arcobacter sp.; Aureobacterium sp.; Bacillus sp.; Beggiatoa sp.; Butyribacterium sp.; Carboxydothermus sp.; Clostridium sp.; Comamonas sp.; Dehalobacter sp.; Dehalococcoide sp.; Dehalospirillum sp.; Desulfobacterium sp.; Desulfomonile sp.; Desulfotomaculum sp.; Desulfovibrio sp.; Desulfurosarcina sp.; Ectothiorhodospira sp.; Enterobacter sp.; Eubacterium sp.; Ferroplasma sp.; Halothibacillus sp.; Hydrogenobacter sp.; Hydrogenomonas sp.; Leptospirillum sp.; Metallosphaera sp.; Methanobacterium sp.; Methanobrevibacter sp.; Methanococcus sp.; Methanococcoides sp.; Methanogenium sp.; Methanolobus sp.; Methanomicrobium sp.; Methanoplanus sp.; Methanosarcina sp.; Methanospirillum sp.; Methanothermus sp.; Methanothrix sp.; Micrococcus sp.; Nitrobacter sp.; Nitrobacteraceae sp., Nitrococcus sp., Nitrosococcus sp.; Nitrospina sp., Nitrospira sp., Nitrosolobus sp.; Nitrosomonas sp.; Nitrosospira sp.; Nitrosovibrio sp.; Nitrospina sp.; Oleomonas sp.; Paracoccus sp.; Peptostreptococcus sp.; Planctomycetes sp.; Pseudomonas sp.; Ralstonia sp.; Rhodobacter sp.; Rhodococcus sp.; Rhodocyclus sp.; Rhodomicrobium sp.; Rhodopseudomonas sp.; Rhodospirillum sp.; Shewanella sp.; Siderococcus sp.; Streptomyces sp.; Sulfobacillus sp.; Sulfolobus sp.; Thermothrix sp., Thiobacillus sp.; Thiomicrospira sp.; Thioploca sp.; Thiosphaera sp.; Thiothrix sp.; Thiovulum sp.; sulfur-oxidizers; hydrogen-oxidizers; iron- oxidizers; acetogens; and methanogens; consortiums of microorganisms that include chemoautotrophs; chemoautotrophs native to at least one of hydrothermal vents, geothermal vents, hot springs, cold seeps, underground aquifers, salt lakes, saline formations, mines, acid mine drainage, mine tailings, oil wells, refinery wastewater. coal seams, deep sub- surface; waste water and sewage treatment plants; geothermal power plants, sulfatara fields, and soils; and extremophiles selected from one or more of thermophiles, hyperthermophiles, acidophiles, halophiles, and psychrophiles. [209] Such organisms also include but are not limited to extremophiles that can withstand extremes in various environmental parameters such as temperature, radiation, pressure, gravity, vacuum, desiccation, salinity, pH, oxygen tension, and chemicals. They include hyperthermophiles, such as Pyrolobus fumarii; thermophiles, such as Synechococcus lividis; mesophiles, and psychrophiles, such as Psychrobacter. Extremely thermophilic sulfur- metabolizers such as Thermoproteus sp., Pyrodictium sp., Sulfolobus sp., Acidianus sp.. Radiation tolerant organisms include Deinococcus radiodurans. Pressure tolerant organisms include piezophiles or barophiles. Desiccant tolerant and anhydrobiotic organisms include xerophiles; microbes and fungi. Salt tolerant organisms include halophiles, such as Halobacteriacea and Dunaliella salina. pH tolerant organisms include alkaliphiles such as Natronobacterium, Bacillus firmus OF4, Spirulina spp., and acidophiles such as Cyanidium caldarium, Ferroplasma sp. Gas tolerant organisms, which tolerate pure CO2 include Cyanidium caldarium and metal tolerant organisms include metalotolerants such as Ferroplasma acidarmanus, Ralstonia sp. [210] In some embodiments, the invention further provides a composition wherein the microorganism is a hydrogen-oxidizing chemoautotroph and/or a carboxydotroph and/or a methylotroph and/or methanotroph. In some embodiments, the invention further provides a composition wherein the microorganism is capable of growing on syngas and/or producer gas and/or pyrolysis gas as the sole electron donor, and/or source of reduced hydrogen atoms, and/or carbon source. In some embodiments, the invention further provides a composition wherein the microorganism is capable of growing on untreated crude glycerol as the sole electron donor, and/or source of reduced hydrogen atoms, and/or carbon source. [211] In certain embodiments of the present invention the microbes used are naturally occurring and/or non-genetically modified (non-GMO) microorganisms and/or non- pathogenic and/or rely on specific environmental conditions provided by the bioprocesses that are absent from the surrounding environment. [212] Certain embodiments of the present invention utilize a microorganism or consortium of microorganisms, isolated from environmental samples and enriched with desirable microorganisms using methods known in the art of microbiology through growth in the presence of targeted electron donors including but not limited to one or more of: hydrogen and/or CO and/or syngas and/or methane, and electron acceptors including but not limited to one or more of oxygen and/or nitrate and/or ferric iron and/or CO2, and environmental conditions (e.g. temperature, pH, pressure, DO, salinity, the presence of various impurities and pollutants etc.). [213] In some embodiments, the invention further provides a method wherein the electron donors utilized in biosynthesis and/or respiration include but are not limited to one or more of the following reducing agents: ammonia; ammonium; carbon monoxide; dithionite; elemental sulfur; hydrogen; metabisulfites; nitric oxide; nitrites; sulfates such as thiosulfates including but not limited to sodium thiosulfate (Na2S2O3) or calcium thiosulfate (CaS2O3); sulfides such as hydrogen sulfide; sulfites; thionate; thionite. [214] In some embodiments the microorganism is a methanotroph. In some embodiments, the microorganism is in the genus Methylococcus. In some embodiments, the microorganism is Methylococcus capsulatus. In some embodiments, the microorganism is a methylotroph. In some embodiments, the microorganism is in the genus Methylobacterium. In some embodiments, the microorganism is drawn from one or more of the following species: Methylobacterium zatmanii; Methylobacterium extorquens; Methylobacterium chloromethanicum. [215] In some embodiments the microorganism of the claimed invention is not dependent upon light to grow and/or to synthesize one or more of the following: glucose, other sugars, starch, carbohydrates, polysaccharides, amino acids, proteins and/or other nutrients. In some embodiments, the microorganism of the claimed invention does not require any type of sugar or any other type of organic compound or any type of fixed carbon to grow and/or to synthesize one or more of the following: glucose, other sugars, starch, carbohydrates, polysaccharides, amino acids, proteins and/or other nutrients. In some embodiments, the microorganism of the claimed invention is a facultative microorganism. [216] The production of organic molecules with carbon chain lengths longer than C4 is most commonly and efficiently accomplished biologically through anabolic biosynthesis pathways such as fatty acid biosynthesis [Fischer, Klein-Marcuschamer, Stephanolpoulos, Metabolic Engineering (2008) 10, 295-304], gluconeogenesis, and various amino acid biosynthetic pathways. A molecule entering into the gluconeogenesis pathway is glyceraldehyde-3-phosphate (G3P), a central metabolite from which many high value biochemicals can be derived. In some embodiments, the invention utilizes microorganisms with a naturally occurring pathway for the conversion of CO, CO2 and/or H2 and/or CH4 to G3P. In some embodiments, the invention utilizes microorganisms that can fix CO and/or CO₂ through the reductive tricarboxylic acid cycle, the Calvin-Benson-Bassham cycle, and/or the Wood-Ljungdahl pathway. In some embodiments, the invention utilizes microorganisms the fix C1 compounds through a methanotrophic pathway. In some embodiments the microorganisms naturally produce enzymes that catalyze the fixation of gaseous inorganic carbon to produce one or more of acetyl-CoA, pyruvate, G3P, malonyl- CoA, utilizing gaseous electron donors such as are present in syngas and/or producer gas as reducing agents, with such enzymatic proteins including but not limited to acetyl-CoA synthase, acetyl-CoA synthase disulfide reductase, cobalamide corrinoid/iron-sulfur protein, carbon monoxide dehydrogenase, hydrogenase, and methyltransferase. [217] Unlike methanogenic, acetogenic and solventogenic pathways, present in methanogens and acetogens respectively, which can produce short chain organic compounds (C1-C4) with net ATP production or zero net consumption (i.e., ATP neutral), anabolic biosynthetic pathways such as fatty acid synthesis involve net ATP consumption. For example, the following gives the net reaction for synthesis of Palmitic acid (C16) starting from Acetyl-CoA: 8Acetyl-CoA + 7ATP + H2O + 14NADPH + 14H⁺ -> Palmitic acid + 8CoA + 14NADP⁺ + 7ADP + 7P_i [218] A drawback with using an obligate methanogen or acetogen in a GTC process for the production of molecules made via anabolic biosynthesis, such as glucose, other sugars, starch, carbohydrates, polysaccharides, amino acids, proteins, or lipids, is the obligate use of CO₂ as an electron acceptor in anaerobic respiration for the production of ATP, which is needed for anabolic biosynthesis such as fatty acid synthesis, gluconeogenesis, or amino acid synthesis. If H2 is the electron donor, the ATP produced per H2 consumed for respiration in an acetogen or methanogen is relatively low: one ATP per 4H2 for the respiratory production of methane [Thauer, R. K., Kaster, A. K., Seedorf, H., Buckel, W. & Hedderich, R. Methanogenic archaea: ecologically relevant differences in energy conservation. Nat Rev Microbiol 6, 579-591, doi:nrmicro1931 [pii], is incorporated herein by reference in its entirety.] or acetic acid production, and one ATP per 10H2 for butyric acid production. [Papoutsakis, Biotechnology & Bioengineering (1984) 26, 174-187; Heise, Muller, Gottschalk, J. Bacteriology (1989) 5473-5478; Lee, Park, Jang, Nielsen, Kim, Jung, Biotechnology & Bioengineering (2008) 101(2) 209-228, which are incorporated herein by reference in their entireties.] [219] In some embodiments, the invention relates to a microorganism or compositions comprising a microorganism, wherein the microorganism is able to produce ATP from an inorganic electron donor such as but not limited to H₂ and/or CO without the synthesis of methane or short chain organic acids (short chain organic acids comprising carbon chain lengths from two to four carbons long). In some non-limiting embodiments, the invention relates to a microorganism or compositions comprising a microorganism, wherein the microorganism produces ATP from an inorganic electron donor such as but not limited to H2 and/or CO, coupled with an electron acceptor other than CO2 that is used in respiration. [220] Certain embodiments of the present invention apply hydrogen-oxidizing and/or CO- oxidizing and/or CH₄ oxidizing microorganisms that use more electronegative electron acceptors in energy conserving reactions for ATP production, such as but not limited to O₂. For example, hydrogenotrophic oxyhydrogen or knallgas microbes that couple the oxyhydrogen reaction, 2 H2 + O2 -> 2 H2O, to ATP production, can produce more ATP per H₂ and/or other electron donor consumed for respiration, than acetogens or methanogens that use CO₂ as an electron acceptor in respiration. For example, knallgas microorganisms can produce at least two ATP per H2 consumed in respiration [Bongers, J. Bacteriology, (Oct 1970) 145-151, is incorporated herein by reference in its entirety.], which is eight times more ATP produced per H₂ consumed in respiration than what can be produced in microorganisms undergoing methanogenesis or acetogenesis, using H₂ as electron donor and CO2 as electron acceptor in respiration. For this reason, using microorganisms that can utilize more electronegative electron acceptors in respiration and in the production of ATP, such as but not limited to knallgas microbes, for anabolic biosynthesis such as but not limited to the biosynthesis of glucose or other sugars or starch or carbohydrates or polysaccharides or amino acids or protein or fatty acids, from syngas or H2, can be more efficient than using acetogens or methanogens, such as those which are currently used in biological GTC technologies. [221] In certain embodiments, the oxyhydrogen reaction used in respiration is enzymatically linked to oxidative phosphorylation. In certain embodiments, the ATP and/or other intracellular energy carriers thus formed are utilized in the anabolic synthesis of glucose and/or other sugars and/or starch and/or carbohydrates and/or polysaccharides. In some embodiments, the invention relates to a knallgas microorganism or compositions comprising a knallgas microorganism, wherein the microorganism comprises at least zero or one or more exogenous nucleic acid sequences that encodes zero or more enzymes to enable biosynthesis of useful carbon-based products of interest including but not limited to glucose, other sugars, starch, carbohydrates, polysaccharides, chemicals, monomers, polymers, proteins, vitamins, nutraceuticals, antibiotics, or pharmaceutical products or intermediates thereof from a carbon-containing gas feedstock, including but not limited to syngas or producer gas or waste CO2 combined with renewable H2 or CO or methane containing gases. In some non-limiting embodiments, the invention relates to a microorganism or compositions comprising a microorganism, wherein the microorganism requires less than 4H2 to produce one ATP through respiration. In other non-limiting embodiments, the invention relates to a microorganism or compositions comprising a microorganism, wherein the microorganism produces more than one ATP per H₂ consumed through respiration. In other non-limiting embodiments, the invention relates to a microorganism or compositions comprising a microorganism, wherein the microorganism produces at least two ATP per H2 consumed through respiration, or at least 2.5 ATP per H2 consumed through respiration. [222] In some embodiments, the invention relates to a composition comprising a microorganism that converts syngas and/or producer gas and/or gaseous CO2 and/or H2 and/or CO and/or CH4 into one or more organic compounds, wherein less than 10% by weight of the organic compounds produced by the microorganism is methane. In some embodiments, the invention relates to a composition comprising a microorganism that converts said gaseous substrates into one or more organic compounds; wherein less than 10% by weight of the organic compounds produced are free organic acids with carbon chain length of four carbons or less. [223] In certain embodiments of the present invention the microorganism reduces CO₂, producing cell material and H2O. In certain embodiments, the energy needed for the metabolic pathways that perform this reduction is obtained by the oxidation of hydrogen with molecular oxygen. In certain embodiments of the present invention the biological system and/or components function directly as a CO₂ reducer, but not an O₂ producer. In certain embodiments, the O₂ utilized in respiration is obtained from another system and provided to the biological system and/or components. In certain embodiments that other system involves the electrolysis and/or thermolysis of water. [224] An advantage of using oxyhydrogen microorganisms over strictly anaerobic acetogenic or methanogenic microorganisms for carbon capture applications and/or syngas conversion applications is the higher oxygen tolerance of oxyhydrogen microorganisms. In some embodiments of the invention a microorganism is utilized which tolerates aerobic and/or microaerobic conditions. Oxyhydrogen microorganisms generally have an advantage over strict anaerobic acetogenic or methanogenic microorganisms for carbon capture applications from a flue gas due to the higher oxygen tolerance of oxyhydrogen microorganisms. Since industrial flue gas is one intended source of CO2 for certain embodiments of the present invention, the relatively high oxygen tolerance of oxyhydrogen microorganisms, as compared with obligately anaerobic methanogens or acetogens, can allow the O2 content of 2-6% found in typical fluegas to be better tolerated. In certain embodiments of the present invention a 2% or greater O2 content in a CO2 containing flue gas, or any other type of input gas mixture, is tolerated by the microbial culture and/or utilized in microbial respiration. [225] A further advantage of using oxyhydrogen microorganisms for carbon capture applications and/or syngas conversion applications over using acetogens is that the production of ATP through respiration powered by the oxyhydrogen reaction results in a water product, which can readily be incorporated into the process stream, rather than the generally undesirable acetic acid or butyric acid products of acidogenesis, which can harm the microorganisms by dropping the solution pH or accumulating to inhibitory or toxic levels. In some embodiments of the invention the primary product of cellular respiration is water. [226] In some embodiments, the microorganism is capable of growing on untreated crude glycerol and/or glucose and/or fructose and/or methanol and/or acetate as the sole electron donor, and carbon source. In some embodiments, the microorganism is able to grow mixotrophically on an organic carbon source and using inorganic electron donor or carbon source. [227] In certain embodiments, microorganisms provided by the invention comprises a cell line selected from eukaryotic plants, algae, cyanobacteria, green-sulfur bacteria, green non- sulfur bacteria, purple sulfur bacteria, purple non-sulfur bacteria, extremophiles, yeast, fungi, proteobacteria, engineered organisms thereof, and synthetic organisms. In certain embodiments Spirulina is utilized. [228] In certain embodiments purple non-sulfur bacteria are used which include but are not limited to the following genera: Phaeospirillum, Rhodobaca, Rhodobacter, Rhodomicrobium, Rhodopila, Rhodopseudomonas, Rhodothalassium, Rhodospirillum, Rodovibrio, and Roseospira. [229] The liquid cultures used to grow cells associated with the invention can be housed in any of the culture vessels known and used in the art. In some embodiments, large scale production in a bioreactor vessel can be used to produce large quantities of a desired molecule and/or biomass. [230] Another advantage of certain embodiments of the present invention relates to the bioreactor vessels used to contain, isolate, and/or protect the culture environment. Exemplary culture vessels that can be used in some non-limiting embodiments of the present invention to culture and grow microorganisms for production of organic compounds including but not limited to one or more of the following: glucose, other sugars, starch, carbohydrates, polysaccharides, amino acids, proteins, and other nutrients; include those that are known to those of ordinary skill in the art of large scale microbial culturing. Such culture vessels, that may be used in certain embodiments of the present invention include but are not limited to one or more of the following: airlift reactors; biological scrubber columns; bubble columns; stirred tank reactors; continuous stirred tank reactors; counter- current, upflow, expanded-bed reactors; digesters and in particular digester systems such as known in the prior arts of sewage and waste water treatment or bioremediation; filters including but not limited to trickling filters, rotating biological contactor filters, rotating discs, soil filters; fluidized bed reactors; gas lift fermenters; immobilized cell reactors; loop reactors; membrane biofilm reactors; pachuca tanks; packed-bed reactors; plug-flow reactors; static mixers; trickle bed reactors; and/or vertical shaft bioreactors. The vessel base, siding, walls, lining, and/or top in certain embodiments can be constructed out of one or more materials including but not limited to bitumen, cement, ceramics, clay, concrete, epoxy, fiberglass, glass, macadam, plastics, sand, sealant, soil, steels or other metals and their alloys, stone, tar, wood, and any combination thereof. In certain embodiments of the present invention where the microorganisms either require a corrosive growth environment and/or produce corrosive chemicals through the carbon-fixation reaction, corrosion resistant materials known in the art and engineering field can be used to line the interior of the container contacting the growth medium. [231] Microbial culturing in the present invention in certain embodiments is performed for the sake of implementing genetic modifications, and/or for production of organic compounds, and particularly in certain embodiments, one or more of the following: glucose, other sugars, starch, carbohydrates, polysaccharides, amino acids, proteins, and other nutrients. Microbial culturing with the aim of genetic manipulation is generally performed at a small benchtop scale and often under conditions that select for genetically modified traits. [232] Microbial culturing aimed at the commercial production of organic compounds and specifically amino acids, protein, and other nutrients is typically performed in bioreactors at much greater scale (e.g., 500 L, 1,000 L 5,000 L, 10,000 L, 50,000 L, 100,000 L, 1,000,000 L bioreactor volumes and higher). In certain embodiments chemoautotrophs of the present invention are grown in a liquid media inside a bioreactor using the methods of the invention. In some embodiments, the bioreactor containing the microorganisms is constructed of opaque materials that keep the culture in near or total darkness. Bioreactors constructed out of opaque materials such as steel and/or other metallic alloys and/or reinforced concrete and/or fiberglass and/or various high strength plastic materials can be designed to have large working volumes. In some embodiments of the present invention fermenters constructed of steel or other metallic alloys that are 50,000 liters and greater in volume are utilized. In some embodiments of the present invention bioreactors able to contain positive headspace pressures above ambient pressure are utilized. In some embodiments of the present invention egg-shape or cylindrical digesters or vertical shaft bioreactors 3,000,000 liters and greater in volume are utilized. In some embodiments, the bioreactor comprising the microorganism does not allow light to penetrate part or most or all of its contained liquid volume. In some embodiments, the bacterial cell or microbial cell is cultured without significant or any exposure to light. In certain embodiments, converting electricity to light is not required. [233] Following the methods of the present invention, in some embodiments the microorganisms are grown and maintained for the production of amino acids, or proteins, or other nutrients, or whole cell products in a medium containing a gaseous carbon source, such as but not limited to syngas or producer gas or tail gas or pyrolysis gas or H2 and CO2 gas mixtures, in the absence of light; where such growth is known as chemoautotrophic growth. In some embodiments, the invention relates to methods of cultivating cells for the large-scale production of sugars, starch, carbohydrates, polysaccharides, amino acids, or proteins, or other nutrients, or whole cell products. In some embodiments, the invention relates to methods of cultivating cells in bioreactors 50,000 liters or greater in volume, which are conventionally constructed out of low cost, sturdy, and opaque materials such as steel or other metallic alloys or reinforced concrete or earthworks. The size, depth, and construction of such bioreactors dictate that the cells will be grown in near or total darkness. In some embodiments, the microorganisms are cultured for the synthesis of sugars, starch, carbohydrates, polysaccharides, amino acids, or proteins, or other nutrients, or whole cell products in accordance with the methods of the present invention in a medium containing gaseous inorganic carbon as the primary or sole carbon source, and without any exposure to light. This type of growth is known as chemoautotrophic growth. In certain non-limiting embodiments, the microorganism used in the CO₂-fixation step is not photosynthetic. In certain non-limiting embodiments, the bioreactor design does not confine the culture in thin layers, or have transparent walls, so as to make light available throughout the vessel, as is generally necessary with photosynthetic microorganisms. [234] In some embodiments of the present invention, the ability of chemoautotrophs to derive the energy needed for growth directly from redox chemistry rather than sunlight, while consuming CO2 facilitates and/or enables continuous CO2 capture operations, day and night, year-round, in all weather conditions, without the need for any artificial lighting. In contrast, algae and higher plants can become net CO₂ emitters during night or at low-light levels. Because of the lack of light requirement in certain embodiments of the present invention, conventional, proven equipment and infrastructure drawn from commercial bioprocesses that are constructed out of opaque materials, non-transparent to visible light, are applied in certain embodiments of the present invention without the need for any artificial lighting. In certain embodiments of the present invention an increase in system capacity is met by vertical scaling, rather than only scaling horizontally. This is in contrast to phototrophic approaches using algae, cyanobacteria, or higher-plants for CO2 capture. Although various vertical farming schemes have been proposed for photosynthetic systems, practically and economically speaking, phototrophic systems must expand horizontally, for example in shallow ponds or photobioreactors in the case of algae. This results in large geographic footprints and many negative environmental impacts. [235] In cases, such as vertical farming, where artificial lighting would be otherwise be required to grow a photosynthetic organism such as algae or higher plants, in certain vertical farming-like embodiments of the present invention, converting electricity to light is not required for CO2 conversion. In certain non-limiting embodiments of the present invention, electrolysis of water is substituted for the conversion of electricity to light, in supporting autotrophic CO₂ uptake and biosynthesis. In certain non-limiting embodiments of the present invention there is a large energy efficiency advantage in the conversion of electricity to electron donors such as, but not limited to, hydrogen through electrolysis, over the conversion of electricity to light. An algal or higher plant system grown with artificial lighting is challenged by inefficient utilization of light energy by the algae, and by inefficient conversion of electrical energy to light energy. In certain embodiments of the present invention, a comparable, in terms of CO2 capture and/or biomass production, algal or high-plant culture grown under artificial lighting, will require more electrical power than the CO₂ capture and/or biomass production system of the present invention. In certain embodiments of the present invention, a comparable, in terms of CO₂ capture and/or biomass production, algal or higher-plant culture grown under artificial lighting, will require at least ten times more electrical power than the CO2 capture and/or biomass production system of the present invention. For algae or higher-plants grown on artificial lighting the heat rejection requirement is almost in direct proportion to the electrical input. In certain embodiments of the present invention, the heat rejection requirements are lower than for a comparable algal, or higher plant system, in terms of CO2 capture and/or biomass production grown on artificial lighting. In certain embodiments of the present invention, the heat rejection requirements are at least ten times lower than for a comparable algal, or higher plant system, in terms of CO2 capture and/or biomass production, grown on artificial lighting. [236] In certain embodiments of the present invention, a relatively high tolerance for inclement conditions provided by the isolation of the bioprocess from the surrounding environment, enables the bioprocess of the present invention to operate in conditions unfavorable to open algal systems or traditional agriculture. In certain non-limiting embodiments of the present invention, low temperatures in winter are used to reduce process cooling costs incurred because the reaction of H₂ and CO₂ to produce sugars, starch, carbohydrates, polysaccharides, or protein is exothermic. [237] To give an illustration of the application of a bioreactor in certain embodiments of the present invention, a bioreactor containing nutrient medium is inoculated with production cells. Generally, there will follow a lag phase prior to the cells beginning to double. After the lag phase, the cell doubling time decreases and the culture goes into the logarithmic phase. The logarithmic phase is eventually followed by an increase of the doubling time that, while not intending to be limited by theory, is thought to result from either a mass transfer limitation, depletion of nutrients including nitrogen or mineral sources, or a rise in the concentration of inhibitory chemicals, or quorum sensing by the microbes. The growth slows down and then ceases when the culture goes into the stationary phase. In certain embodiments, there is an arithmetic growth phase preceding the stationary phase. In order to harvest cell mass the culture in certain embodiments is harvested in the logarithmic phase and/or the arithmetic phase and/or in the stationary phase. The accumulation of sugars, starch, carbohydrates, or polysaccharides, can be triggered by the depletion of the nitrogen source or another key nutrient excepting the carbon or the electron source (e.g., hydrogen). In a number of species this signals the cells to store carbohydrates produced from the excess carbon and energy sources. [238] The bioreactor or fermenter is used to culture cells through the various phases of their physiological cycle. A bioreactor is utilized for the cultivation of cells, which may be maintained at particular phases in their growth curve. The use of bioreactors is advantageous in many ways for cultivating chemoautotrophic growth. For certain embodiments, carbohydrate-rich cell mass, which is used to produce carbohydrates, ingredients, nutrients, or animal feeds, is grown to high densities in liquid suspension. Generally, the control of growth conditions including control of dissolved carbon dioxide, oxygen, and other gases such as hydrogen, as well as other dissolved nutrients, trace elements, temperature and pH, is facilitated in a bioreactor. [239] In some embodiments process conditions are used to enhance the effect on biosynthesis of native or expressed enzymes. In some embodiments, the process condition used to enhance the effect on the native or expressed enzymes is temperature. [240] Nutrient media as well as gases can be added to the bioreactor as either a batch addition, or periodically, or in response to a detected depletion or programmed set point, or continuously over the period the culture is grown and/or maintained. For certain embodiments, the bioreactor at inoculation is filled with a starting batch of nutrient media and/or gases at the beginning of growth, and no additional nutrient media and/or gases are added after inoculation. For certain embodiments, nutrient media and/or gases are added periodically after inoculation. For certain embodiments, nutrient media and/or gas is added after inoculation in response to a detected depletion of nutrient and/or gas. For certain embodiments, nutrient media and/or gas is added continuously after inoculation. For certain embodiments, the added nutrient media does not contain any organic compounds. [241] In certain embodiments inoculation of the culture into the bioreactor is performed by methods including but not limited to transfer of culture from an existing culture inhabiting another bioreactor, or incubation from a seed stock raised in an incubator. In certain embodiments, the seed stock of the strain may be transported and stored in forms including but not limited to a powder, liquid, frozen, or freeze-dried form as well as any other suitable form, which may be readily recognized by one skilled in the art. In certain non-limiting embodiments, the reserve bacterial cultures are kept in a metabolically inactive, freeze-dried state until required for restart. In certain embodiments when establishing a culture in a very large reactor, cultures are grown and established in progressively larger intermediate scale vessels prior to inoculation of the full-scale vessel. [242] For certain embodiments the bioreactors have mechanisms to enable mixing of the nutrient media that include but are not limited to one or more of the following: spinning stir bars, blades, impellers, or turbines; spinning, rocking, or turning vessels; gas lifts, sparging; recirculation of broth from the bottom of the container to the top via a recirculation conduit, flowing the broth through a loop and/or static mixers. The culture media may be mixed continuously or intermittently. [243] In certain embodiments the microorganism containing nutrient medium may be removed from the bioreactors of the present invention partially or completely, periodically or continuously, and in certain embodiments is replaced with fresh cell-free medium to maintain the cell culture in certain embodiments in an exponential growth phase and/or to replenish the depleted nutrients in the growth medium and/or remove inhibitory waste products. [244] The ports that are standard in bioreactors may be utilized to deliver, or withdraw, gases, liquids, solids, and/or slurries, into and/or from the bioreactor vessel enclosing the microbes of the present invention. Many bioreactors have multiple ports for different purposes (e.g. ports for media addition, gas addition, probes for pH and DO, sampling), and a given port may be used for various purposes during the course of a fermentation run. As an example, a port might be used to add nutrient media to the bioreactor at one point in time and at another time might be used for sampling. Preferably, the multiple use of a sampling port can be performed without introducing contamination or invasive species into the growth environment. A valve or other actuator enabling control of the sample flow or continuous sampling can be provided to a sampling port. For certain embodiments, the bioreactors are equipped with at least one port suitable for culture inoculation that can additionally serve other uses including the addition of media or gas. Bioreactor ports enable control of the gas composition and flow rate into the culture environment. For example, the ports can be used as gas inlets into the bioreactor through which gases are pumped. [245] For some embodiments gases that may be pumped into a bioreactor include but not are not limited to one or more of the following: syngas, producer gas, pyrolysis gas, hydrogen gas, CO, CO₂, O₂, air, air/CO₂ mixtures, natural gas, biogas, methane, ammonia, nitrogen, noble gases, such as argon, as well as other gases. In some embodiments the CO₂ pumped into the system may come from sources including but are not limited to: CO2 from the gasification of organic matter; CO2 from the calcination of limestone, CaCO3, to produce quicklime, CaO; CO₂ from methane steam reforming, such as the CO₂ byproduct from ammonia, methanol, or hydrogen production; CO₂ from combustion, incineration, or flaring; CO2 byproduct of anaerobic or aerobic fermentation of sugar; CO2 byproduct of a methanotrophic bioprocess; CO2 metabolic wastes produced by humans, animals, and/or other heterotropic organisms; CO₂ from waste water treatment; CO₂ byproduct from sodium phosphate production; geologically or geothermally produced or emitted CO₂; CO₂ removed from acid gas or natural gas. In certain embodiments, the carbon source is CO2 and/or bicarbonate and/or carbonate in sea water or other bodies of surface or underground water. In certain embodiments, the carbon source is CO₂ from the atmosphere. In certain embodiments, the carbon source is CO₂ from direct air capture (DAC). In certain non- limiting embodiments, the CO2 has been captured from a closed cabin and/or other closed atmosphere and/or closed aquatic system as part of a closed-loop life support system, using equipment such as but not limited to a CO₂ removal assembly (CDRA), such as is utilized on the International Space Station (ISS). [246] In certain embodiments of the present invention, carbon dioxide containing flue gases or exhaust gases are captured from a smoke stack or exhaust stream at temperature, pressure, and gas composition characteristic of the untreated exhaust, and directed with minimal modification into the reaction vessels where carbon-fixation occurs. In some embodiments in which impurities harmful to organisms are not present in the flue or exhaust gas, modification of the flue gas upon entering the reaction vessels can be limited to the compression needed to pump the gas through the reactor system and/or the heat exchange needed to lower the gas temperature to one suitable for exposure to the microorganisms. In certain embodiments, the CO₂ present in a flue or exhaust gas or other mixed gas stream is purified and/or concentrated prior to introduction into the bioreactor using carbon-capture technologies and processes well known in the art. [247] In embodiments in which carbon dioxide bearing flue gas is transported through a system for dissolving the carbon dioxide into solution (such as is well known in the art of carbon capture and/or microbial conversion), the scrubbed flue or exhaust gas with reduced CO2 content, (which generally primarily includes inert gases such as nitrogen), can in certain embodiments be released into the atmosphere. [248] In certain embodiments of the present invention the carbon source is CO₂ and/or CO contained in industrial flue, exhaust, or off-gases and/or from natural sources including but not limited to geological and geothermal sources. In certain embodiments, the CO2 and/or CO containing flue and/or off gases utilized are emitted from one or more of the following industries or sectors: oil; electricity; natural gas; cement; chemicals; steel; metallurgy; fermentation; agriculture; aquaculture; waste water treatment. In certain non-limiting embodiments of the present invention a relatively small land-footprint, facilitates collocation of the bioprocess with industrial facilities producing CO₂ and/or other carbon wastes including but not limited to one or more of the following: fossil power plants; oil refineries; tar sands upgrading facilities; natural gas or petroleum drilling operations; ethanol distilleries; industrial fermentation and bioprocesses; agricultural and/or aquacultural operations; cement manufactures; aluminum manufactures; chloroalkali manufactures; steel foundries; geothermal power plants. In certain embodiments of the present invention waste-heat associated with industrial flue-gas sources is further utilized in the production process of the present invention for steps including but not limited to in biomass drying. [249] In certain embodiments gases in addition to carbon dioxide, or in place of carbon dioxide as an alternative carbon source, are either dissolved into solution and fed to the culture broth and/or dissolved directly into the culture broth including but not limited to gaseous electron donors and/or carbon sources (e.g., hydrogen and/or CO and/or methane gas). In certain embodiments of the present invention, input gases may include other electron donors and/or electron acceptors and/or carbon sources and/or mineral nutrients such as but not limited to other gas constituents and impurities of syngas (e.g., hydrocarbons); ammonia; hydrogen sulfide; and/or other sour gases; and/or O₂; and/or mineral containing particulates and ash. [250] In certain embodiments of the present invention gases are dissolved into the culture broth of the present invention including but not limited to gaseous electron donors such as but not limited to one or more of the following: hydrogen, carbon monoxide, methane, hydrogen sulfide or other sour gases; gaseous carbon sources such as but not limited to one or more of the following CO₂, CO, CH₄; and electron acceptors such as but not limited to oxygen, either within air (e.g.20.9% oxygen) or as pure O2 or as an O2-enriched gas. In some embodiments, the dissolution of these and other gases into solution is achieved using a system of compressors, flowmeters, and flow valves known to one skilled in the art of fermentation engineering, that feed into one of more of the following widely used systems for dispersing gas into solution: sparging equipment; diffusers including but not limited to dome, tubular, disc, or doughnut geometries; coarse or fine bubble aerators; venturi equipment. In certain embodiments of the present invention surface aeration and/or gas mass transfer may also be performed using paddle aerators and the like. In certain embodiments of the present invention gas dissolution is enhanced by mechanical mixing with an impeller or turbine, as well as hydraulic shear devices to reduce bubble size. Following passage through the reactor system holding microorganisms which uptake the gases, in certain embodiments the residual gases may either be recirculated back to the bioreactor, or burned for process heat, or flared, or injected underground, or released into the atmosphere. In certain embodiments of the present invention utilizing H2 as electron donor, H₂ may be fed to the culture vessel either by bubbling it through the culture medium, or by diffusing it through a hydrogen permeable-water impermeable membrane known in the art that interfaces with the liquid culture medium. [251] In certain embodiments the microorganisms grow and multiply on the H2 and CO2 and other dissolved nutrients under microaerobic conditions. In certain embodiments a C1 chemical such as but not limited to carbon monoxide, methane, methanol, formate, or formic acid, and/or mixtures containing C1 chemicals including but not limited to various syngas compositions generated from various gasified, pyrolyzed, or steam-reformed fixed carbon feedstocks, are biochemically converted into longer chain organic chemicals (i.e. C2 or longer and, in some embodiments, C5 or longer carbon chain molecules) under one or more of the following conditions: aerobic, microaerobic, anoxic, anaerobic, and/or facultative conditions. [252] A controlled amount of oxygen can also be maintained in the culture broth of some embodiments of the present invention, and in certain embodiments, oxygen will be actively dissolved into solution fed to the culture broth and/or directly dissolved into the culture broth. In certain aerobic or microaerobic embodiments of the present invention that require the pumping of air or oxygen into the culture broth in order to maintain targeted DO levels, oxygen bubbles may be injected into the broth at an optimal diameter for mixing and oxygen transfer. This has been reported to be 2 mm in the Environment Research Journal May/June 1999 pgs.307-315. In certain aerobic embodiments of the present invention a process of shearing the oxygen bubbles may be used to achieve this bubble diameter as described in U.S. Pat. No.7,332,077. In certain embodiments bubbles, larger than 7.5 mm average diameter and/or slugging are avoided. [253] In some embodiments, the inventive subject matter converts a fuel gas including but not limited to syngas, producer gas, pyrolysis gas, biogas, tailgas, fluegas, CO, CO₂, H₂, and mixtures thereof. In some embodiments, the heat content of the fuel gas is at least 100 BTU per standard cubic foot (scf). In some embodiments of the present invention, a bioreactor is used to contain and grow the microorganisms, which is equipped with fine-bubble diffusers and/or high-shear impellers for gas delivery. [254] In some embodiments oxygen is used as an electron acceptor in the respiration of the microorganism used for the biosynthesis of sugars, starch, carbohydrates, polysaccharides, amino acids, or proteins, or other nutrients, or whole cell products. In some embodiments, strong electron acceptors including but not limited to O₂ are used to maximize efficiency and yield of products produced via anabolic pathways such as sugars, starch, carbohydrates, polysaccharides, amino acids, proteins, fatty acids, or vitamins. A key challenge with using O2 as an electron acceptor is keeping O2 levels sufficiently adequate to allow aerobic microbes to grow well and efficiently generate anabolic products while also maintaining appropriate and safe levels of inflammable H₂ and O₂ mixtures, as well as other fuel gas/O₂ mixtures, in the bioreactor to minimize the risk of explosion. In some embodiments, custom or specialized reactor designs are used to control O2 in the broth at a level that is optimal for the microbes while avoiding dangerous gas mixes. In some embodiments bioreactor designs are used that avoid dangerous mixtures of H₂ and O₂, while providing the microorganisms with necessary levels of these gases for cellular energy, carbon fixation, and for the production of sugars, starch, carbohydrates, polysaccharides, amino acid, or protein, and/or other nutrients, and/or whole cells. [255] Introducing and/or raising the gas flow rate into a bioreactor can enhance mixing of the culture and produce turbulence if the gas inlet is positioned beneath the surface of the liquid media such that gas bubbles or sparges up through the media. In certain embodiments mixing is enhanced through turbulence provided by gas bubbles and/or sparging and/or gas plugging up through the liquid media. In some embodiments, a bioreactor comprises gas outlet ports for gas escape and pressure release. In some embodiments, gas inlets and/or outlets are preferably equipped with check valves to prevent gas backflow. [256] In certain embodiments where chemosynthetic reactions occur within the bioreactor, one or more types of electron donor and one or more types of electron acceptor are pumped or otherwise added as either a bolus addition, or periodically, or continuously to the nutrient medium containing chemoautotrophic organisms in the reaction vessel. The chemosynthetic reaction driven by the transfer of electrons from electron donor to electron acceptor in cellular respiration fixes inorganic carbon dioxide and/or other dissolved carbonates and/or other carbon oxides into organic compounds, including but not limited to sugars, starch, carbohydrates, polysaccharides, and biomass. [257] In certain embodiments a nutrient media for culture growth and production is used comprising an aqueous solution containing suitable minerals, salts, vitamins, cofactors, buffers, and other components needed for microbial growth, known to those skilled in the art [Bailey and Ollis, Biochemical Engineering Fundamentals, 2nd ed; pp 383-384 and 620- 622; McGraw-Hill: New York (1986)]. [258] In certain embodiments the chemicals used for maintenance and growth of microbial cultures as known in the art are included in the nutrient media of the present invention. In certain embodiments these chemicals may include but are not limited to one or more of the following: nitrogen sources such as ammonia, ammonium (e.g., ammonium chloride (NH₄Cl), ammonium sulfate ((NH₄)₂SO₄)), nitrate (e.g., potassium nitrate (KNO₃)), urea or an organic nitrogen source; phosphate (e.g., disodium phosphate (Na₂ HPO₄), potassium phosphate (KH2PO4), phosphoric acid (H3PO4), potassium dithiophosphate (K3PS2O2), potassium orthophosphate (K3PO4), dipotassium phosphate (K2HPO4)); sulfate; yeast extract; chelated iron; potassium (e.g., potassium phosphate (KH₂PO₄) , potassium nitrate (KNO₃), potassium iodide (KI), potassium bromide (KBr)); and other inorganic salts, minerals, and trace nutrients (e.g., sodium chloride (NaCl), magnesium sulfate (MgSO4 7H2O) or magnesium chloride (MgCl2), calcium chloride (CaCl2) or calcium carbonate (CaCO₃), manganese sulfate (MnSO₄7H₂O) or manganese chloride (MnCl₂), ferric chloride (FeCl₃), ferrous sulfate (FeSO₄7H₂O) or ferrous chloride (FeCl₂4H₂O), sodium bicarbonate (NaHCO₃) or sodium carbonate (Na₂CO₃), zinc sulfate (ZnSO₄) or zinc chloride (ZnCl2), ammonium molybdate (NH4MoO4) or sodium molybdate (Na2MoO42H2O), cuprous sulfate (CuSO4) or copper chloride (CuCl22H2O), cobalt chloride (CoCl26H2O), aluminum chloride (AlCl₃6H₂O), lithium chloride (LiCl), boric acid (H₃BO₃), nickel chloride NiCl₂6H₂O), tin chloride (SnCl₂ H₂O), barium chloride (BaCl₂2H₂O), copper selenate (CuSeO45H2O) or sodium selenite (Na2SeO3), sodium metavanadate (NaVO3), chromium salts). In certain embodiments, the mineral salts medium (MSM) formulated by Schlegel et al may be used [“Thermophilic bacteria”, Jakob Kristjansson, Chapter 5, Section III, CRC Press, (1992)]. [259] Aspects of the invention relate to the growth and/or expression of bacterial cells. Bacterial cells associated with the invention can be cultured in some embodiments in media of any type (rich or minimal), including fermentation medium, and any composition. As would be understood by one of ordinary skill in the art, routine optimization would allow for use of a variety of types of media. The selected medium can be supplemented with various additional components. Some non-limiting examples of supplemental components include glucose, other sugars, antibiotics, IPTG for gene induction, arabinose for gene induction, and ATCC Trace Mineral Supplement. Similarly, other aspects of the medium and growth conditions of the cells of the invention may be optimized through routine experimentation. For example, pH and temperature are non-limiting examples of factors which can be optimized. In some embodiments, factors such as choice of media, media supplements, and temperature can influence production levels of a desired molecule. In some embodiments, the concentration and amount of a supplemental component may be optimized. In some embodiments, how often the media is supplemented with one or more supplemental components, and the amount of time that the media is cultured before harvesting the desired molecule is optimized. [260] In certain embodiments, ash derived from the incineration or gasification of biomass contains mineral nutrients that may be used in the present invention. In certain embodiments, the incinerated or gasified biomass that results in mineral containing ash includes but is not limited to one or more of the following: wood, straw, agricultural residues, aquacultural wastes, dung, fecal matter and/or urine. In certain non-limiting embodiments urine is used as a source of nutrients including but not limited to as a nitrogen source. In certain non-limiting embodiments, the urine is diluted with water. In certain non- limiting embodiments urine and/or the products of incineration and/or gasification are used as nutrients for the biological organism of the present invention. In certain non-limiting embodiments, the primary products of metabolic waste processes and/or biological decomposition and/or incineration and/or gasification including but not limited to CO₂, water vapor, H₂, CO, and/or the inorganic mineral nutrients dissolved in water and/or in ash, can be readily utilized by the biological organisms of the present invention. [261] The final products from metabolic waste processes and/or the aerobic decomposition of organic matter generally are carbon dioxide, water, nitrates, phosphates, sulfates, and similar highly oxidized compounds. In certain embodiments of the present invention CO₂ and/or water and/or inorganic mineral nutrients recovered from a waste stream and/or derived from an activated sludge process is utilized as sources of feedstock and/or nutrients and/or electron acceptors in the present invention. In certain embodiments of the present invention CH₄ and/or CO₂ and/or water and/or ammonia and/or hydrogen sulfide and/or other inorganic mineral nutrients derived from anaerobic sludge digestion is utilized as a feedstock and/or nutrient source in the present invention. In certain embodiments humus is utilized as a carbon source and/or an electron acceptor or donor. [262] Aquacultural pollution, which can include CO₂ as well as nitrogen, in forms including but not limited to ammonia, as well as phosphorus, and dead fish is becoming a widespread hazard, particularly in Asia, where 90 percent of farmed fish are located. In certain embodiments of the present invention aquaculture pollution is utilized as a source of nutrients including but not limited to CO₂ and/or nitrogen and/or phosphorus, by the microorganisms of the present invention. In certain embodiments waste that would normally be emitted to the atmosphere and/or the environment and/or discharged into bodies of water and/or go to a sewage or waste water treatment plant or landfill, instead is utilized for the production of nutrients for the microbial process of the present invention. In certain embodiments, these waste streams include but are not limited to one or more of the following: CO2, ammonia, urea, urine, feces, fish waste, and/or other animal waste. In certain embodiments, the microbial aspect of the present invention enables an increase in the water and/or nutrients that can be recirculated through an aquaculture system, and/or decrease the discharge and/or emissions from an aquaculture system. In certain embodiments electron donors and/or carbon sources including but not limited to one or more of the following: H₂, CO, CH₄, CO₂; and/or other nutrients and/or water are generated and/or captured from metabolic waste and/or fish waste and/or other animal waste and/or microbial cellular processes and/or material. In certain such embodiments organic matter, such as but not limited to organic matter refractive to aerobic waste water treatment, is used to generate electron donors and/or carbon sources including but not limited to one or more of the following: H₂, CO, CH₄, CO₂; and/or other nutrients and/or water through well- known processes including but not limited to one or more of the following: gasification, pyrolysis, incineration, and/or anaerobic digestion. In certain embodiments the H2O and/or CO2 and/or other condensable and non-condensable gases and/or ash residue and/or heat that is captured from a waste stream and/or generated through gasification and/or pyrolysis and/or incineration are utilized as feedstocks or inputs in the present invention such as but not limited to one or more of the following: CO2 as a carbon source; H2O as a process water source; condensable and/or non-condensable gases as feedstocks and nutrient sources; ash as a inorganic mineral nutrient source and/or source of base for pH control; heat as a source of process heat and/or energy. Pathogenic microorganisms can survive the anaerobic waste treatment process. In certain embodiments, all pathogenic microorganisms present in raw waste feedstocks entering the process are killed through a heat treatment such as, but not limited to, steam sterilization and/or the aforementioned gasification and/or pyrolysis and/or incineration step or steps leading into one or more C1 capture and bioconversion steps. [263] Certain embodiments of the present invention utilizing waste derived feedstocks and/or nutrients enable the closing of a food loop and/or enable a closed-loop life support system for humans and/or animals and/or microorganisms. [264] In certain embodiments of the present invention there is no requirement for arable land and/or fresh water and/or pesticides and/or herbicides and/or antibiotics. In certain embodiments, the need for fertilizer (e.g., inorganic minerals or organic nutrients for microbial growth) is partially or entirely met using waste sources including but not limited to one or more of the following: CO₂ and other greenhouse gas emissions, nutrient runoff, ashes, biomass, wastewater, sewage, waste effluents. In certain embodiments of the present invention sea water is used as a source of process water and/or inorganic carbon and/or other mineral nutrients and/or fertilizer. [265] In certain embodiments, the concentrations of nutrient chemicals (e.g., the electron donors and acceptors and carbon sources and various mineral nutrients), are maintained within the bioreactor close to or at their respective optimal levels for optimal carbon uptake and/or fixation and/or conversion and/or production of organic compounds, such as but not limited to sugars, starch, carbohydrates, and/or polysaccharides, which varies depending upon the microorganism utilized but is known or determinable without undue experimentation to one of ordinary skill in the art of culturing microorganisms. [266] In certain embodiments of the present invention one or more of the following parameters are monitored and/or controlled in the bioreactor: waste product levels; pH; temperature; salinity; dissolved oxygen; dissolved carbon dioxide gas; liquid flow rates; agitation rate; gas pressure. In certain embodiments, the operating parameters affecting chemoautotrophic growth are monitored with sensors (e.g., dissolved oxygen probe or oxidation-reduction probe to gauge electron donor/acceptor concentrations), and/or are controlled either manually or automatically based upon feedback from sensors through the use of equipment including but not limited to actuating valves, pumps, and agitators. In certain embodiments, the temperature of the incoming broth as well as of incoming gases is regulated means such as but not limited to coolers, heaters, and/or heat exchangers. [267] In certain embodiments of the present invention, the microbial culture and bioreaction is maintained using continuous influx and removal of nutrient medium and/or biomass, in steady state where the cell population and environmental parameters (e.g., cell density, pH, DO, chemical concentrations) are targeted at a constant level or approximately constant level over time. In certain embodiments that constant level is an optimal level for feedstock conversion and/or production of targeted organic compounds, such as but not limited to sugars, starch, carbohydrates, and/or polysaccharides. In certain embodiments cell densities, can be monitored by direct sampling, by a correlation of optical density to cell density, and/or with a particle size analyzer. In certain embodiments, the hydraulic and biomass retention times can be decoupled so as to allow independent control of both the broth chemistry and the cell density. In certain embodiments dilution rates can be kept high enough so that the hydraulic retention time is relatively low compared to the biomass retention time, resulting in a highly replenished broth for cell growth and/or feedstock conversion and/or production of organic compounds. In certain embodiments dilution rates are set at an optimal technoeconomic trade-off between culture broth and nutrient replenishment and/or waste product removal, and increased process costs from pumping, increased inputs, and other demands that rise with dilution rates. In certain embodiments dilution rates are set at or close to an optimal level for maintaining the culture at or close to an optimal specific growth rate and/or specific production rate (production per time per standing biomass e.g., hr^-1). [268] In certain embodiments of the present invention, the pH of the microbial culture is controlled. In certain embodiments pH is controlled within an optimal range for microbial maintenance and/or growth and/or conversion of feedstock and/or production of organic compounds and/or survival. To address a decrease in pH, in certain embodiments a neutralization step can be performed directly in the bioreactor environment or prior to recycling the media back into the culture vessel through a recirculation loop. Neutralization of acid in the broth of certain embodiments can be accomplished by the addition of bases including but not limited to one or more of the following: limestone, lime, sodium hydroxide, ammonia, ammonium hydroxide, caustic potash, magnesium oxide, iron oxide, alkaline ash. In certain embodiments, the base utilized has been produced from a carbon dioxide emission-free source such as naturally occurring basic minerals including but not limited to one or more of the following: calcium oxide, magnesium oxide, iron oxide, iron ore, olivine containing a metal oxide, serpentine containing a metal oxide, ultramafic deposits containing metal oxides, and liquids from underground basic saline aquifers. If limestone is used for neutralization, then carbon dioxide will generally be released. In certain embodiments, this CO2 can be retained or directed back into the bioreactor for uptake by chemosynthesis and/or utilized and/or sequestered in some other way, rather than released into the atmosphere. [269] In certain embodiments, ash derived from the combustion, incineration, or gasification of biomass is used for pH control. In certain embodiments, the incinerated or gasified biomass that results in basic ash includes but is not limited to one or more of the following: wood, straw, agricultural residues, dung, fecal matter and/or urine. [270] In certain embodiments of the present invention an aqueous suspension of chemoautotrophic microorganisms converts one or more electron donors and CO2 into protoplasm. In certain embodiments, an aqueous suspension of hydrogen-oxidizing microorganisms can be used to convert hydrogen and carbon dioxide into bacterial protoplasm. In certain embodiments, an aqueous suspension of carbon monoxide-oxidizing microorganisms can be used to convert carbon monoxide and hydrogen and/or water into protoplasm. In certain embodiments, an aqueous suspension of methane-oxidizing microorganisms can be used to convert methane into protoplasm. In certain embodiments, the microorganism in suspension is a bacterium or an archaea. In certain non-limiting embodiments, an aqueous suspension or biofilm of H2-oxidizing chemoautotrophic microorganisms converts H₂ and CO₂, along with some other dissolved mineral nutrients, into biochemicals and protoplasm. In certain embodiments, the other dissolved mineral nutrients include but are not limited to a nitrogen source, a phosphorous source, and a potassium source. In certain embodiments, the protoplasm produced is of food value to humans and/or other animals and/or other heterotrophs. In certain embodiments, certain biochemicals may be extracted from the protoplasm and/or extracellular broth, which have nutrient value, and/or value in a variety of organic chemistry or fuel applications. In certain embodiments, the intracellular energy to drive this production of protoplasm is derived from the oxidation of an electron donor by an electron acceptor. In certain non-limiting embodiments, the electron donor includes but is not limited to one or more of the following: H₂; CO; CH₄. In certain non-limiting embodiments, the electron acceptor includes but is not limited to O2. In certain non-limiting embodiments, the product of the energy generating reaction, or respiration, includes but is not limited to water. In certain embodiments, the intracellular energy derived from respiration used to drive this synthesis of biochemicals and protoplasm from CO₂ is stored and carried in biochemical molecules including but not limited to ATP. For the knallgas microbes used in certain embodiments herein the electron acceptor is O2 and the product of respiration is water. [271] In some embodiments the production and distribution of glucose, other sugar, starch, carbohydrate, and/or polysaccharide molecules produced is optimized through one or more of the following: control of bioreactor conditions, control of nutrient levels, genetic modifications of the cells. In certain embodiments of the present invention pathways to glucose, other sugars, starch, carbohydrates, polysaccharides, amino acids, proteins, or other nutrients, or whole cell products are controlled and optimized for the production of targeted biochemical products by maintaining specific growth conditions (e.g. levels of nitrogen, oxygen, phosphorous, sulfur, trace micronutrients such as inorganic ions, and if present any regulatory molecules that might not generally be considered a nutrient or energy source). In certain embodiments of the present invention dissolved oxygen (DO) may be optimized by maintaining the broth in aerobic, microaerobic, anoxic, anaerobic, or facultative conditions depending upon the requirements of organisms. A facultative environment is considered to be one having a gradiant of aerobic layers, microaerobic layers, and anaerobic layers caused by stratification of the water column and/or by consumption of oxygen during passage through the bioreactor system. In certain non-limiting embodiments a facultative environment may consist of one having aerobic upper layers, microaerobic mid layers, and anaerobic lower layers caused by stratification of the water column. In other non-limiting embodiments a facultative environment may consist of one having aerobic lower layers, microaerobic mid layers, and anaerobic upper layers caused by culture consumption of oxygen and/or air introduced at the base of the water column. The biosynthesis of sugars, starch, carbohydrates, polysaccharides, amino acids, or proteins, or other nutrients, or whole cell products by the microbes disclosed in the present invention can happen during the logarithmic phase, and/or during the arithmetic phase, and/or afterwards during the stationary phase when cell doubling has stopped, provided there is sufficient supply of carbon and energy and other nutrient sources. In certain embodiments the biosynthesis of sugars, starch, carbohydrates, polysaccharides, amino acids, proteins, and/or other nutrients, and/or whole cell products by the microbes disclosed in the present invention may occur in a continuous process. [272] The specific examples of bioreactors, culture conditions, heterotrophic and chemotrophic growth, maintenance, and production methods described herein can be combined in any suitable manner to improve efficiencies of microbial growth and/or production of glucose, other sugars, starch, carbohydrates, polysaccharides, amino acids, protein, and/or other nutrient, and/or whole cell production. [273] In certain non-limiting embodiments of the present invention the biosynthetic reduction of CO₂ utilizes O₂ electron acceptor and/or H₂ electron donor which are generated by the electrolysis of water. In certain non-limiting embodiments of the present invention, part of the O2 generated by electrolysis of water, and all of the H2 is fed to an aqueous suspension of microorganisms of the present invention. In certain non-limiting embodiments, the molar ratio of H₂ fed to an aqueous suspension of microorganisms to the moles of O2 is greater than 2:1. In certain non-limiting embodiments where O2 electron acceptor and H2 electron donor are generated by the electrolysis of water, there is a surplus of O₂ remaining after all of the metabolic requirements for H₂ and O₂ of the microorganisms of the present invention have been met. In certain such embodiments the surplus O₂ is supplied to humans and/or other aerobic lifeforms and/or is used to support other aerobic processes, such as but not limited to aerobic waste water treatment, and/or is stored and sold as a chemical co-product. [274] In certain non-limiting embodiments the CO₂ has been removed from an industrial flue gas, exhaust gas, or intercepted from a geological source that would otherwise naturally emit into the atmosphere, or it is removed from another biological process, or from a closed cabin atmosphere or a closed-loop life support system. In certain embodiments, inorganic nutrient salts are fed at the onset of the process and/or simultaneously with the gases. In certain embodiments, the microorganisms grow and multiply on the H₂ and CO₂ and inorganic salts (nutrients) provided. In certain embodiments, the microorganisms oxidize the H2 as an energy source for the synthesis of protoplasm. In certain non-limiting embodiments cells are harvested at some fixed rate: maintaining a steady-state population and gas uptake rate. Certain non-limiting embodiments of the present invention are used in closed-loop life support applications. In certain non-limiting embodiments, the present invention can be used to supplant or displace the Sabatier reaction that converts H2 and CO2 into methane. In certain non-limiting embodiments, instead of producing methane from H₂ and CO₂ through the Sabatier reaction, nutrients including but not limited to one or more of the following: glucose, sugars, starch, carbohydrates, polysaccharides, amino acids, proteins, fats, and vitamins are produced using H2 and CO2. In certain non-limiting embodiments, the invention performs useful functions including but not limited to one or more of the following: CO₂ reduction and removal; synthesis of biomass requiring minimum modification for food use; synthesis of nutrients; and utilization of urea and other nutrients in urine. In certain non-limiting embodiments CO2 and/or CO and/or mineral nutrients in ash, arising from the gasification, reforming, or incineration of liquid and/or solid biological and/or other carbon-based wastes are used in the present invention. Inputs and outputs of a non-limiting example of the process provided for illustrative purposes is shown in Figure 29. A non-limiting schematic flow diagram of a process given for illustrative purposes is shown in Figure 30. [275] In certain non-limiting embodiments of the present invention one or more of the following functions is performed: CO2 reduction and/or removal; synthesis of cellular material that can be utilized as a food or nutrition source; the mitigation of nitrogenous wastes and the utilization of urea, ammonia, ammonium, and/or nitrate. [276] In certain non-limiting embodiments of the present invention a closed culture vessel is used and hydrogen, oxygen, and CO2 under pressure are supplied to the vessel. In certain non-limiting embodiments, the flow of gases to the chamber is controlled by gas sensors to maintain fixed H₂, O₂, and CO₂ concentrations in the chamber. In certain non-limiting embodiments, the gases and culture medium are mixed by mechanical agitation in the vessel to maximize gas diffusion into the liquid. In certain non-limiting embodiments, the hydrogen and oxygen gases are supplied by a water electrolysis cell and/or the CO2 is captured from a waste source or a source normally emitted into the atmosphere or cabin air. In certain embodiments the capture and conversion of CO₂ prevents the build-up of CO₂ in another system where it would prove inhibitory, harmful, or dangerous. [277] In certain non-limiting embodiments, the bioprocess stream flows to a biomass harvest unit. In certain non-limiting embodiments, centrifugal action is used to separate the solids from the liquid. In certain non-limiting embodiments liquid is recycled or sent to water recovery such as a water reclamation unit. In certain embodiments, the water produced through respiration of the microorganisms and/or by heterotrophs fed nutrients produced by the microorganisms, can be recycled to an electrolysis cell and/or back to the bioreactor. In certain embodiments, the water recovered from solid-liquid separations can be recycled to an electrolysis cell and/or back to the bioreactor. In certain embodiments, the water byproduct and/or recovered water can be used to partially offset water demand for electrolytic production of H2 and/or production of H2 and CO2 via SMR and/or gasification. In certain embodiments, the water byproduct is a co-product that may be purified and sold, or provided for the growth of plants or other organisms, or otherwise provided to other water consumers. In certain non-limiting embodiments, undesirable substances which might otherwise build up in the system are removed at the water reclamation unit. In certain non-limiting embodiments, the reclaimed water is re-used in the water electrolysis cell. In certain non-limiting embodiments, nutrient makeup is supplied to the culture vessel to maintain a targeted culture medium composition. In certain non-limiting embodiments urine is provided as a nutrient. In certain embodiments, the biomass generated is processed for use as food or other bio-based products. [278] In certain non-limiting embodiments of the present invention, the continuous culture, or batch or fed batch culture, of one or more microorganisms of the present invention is the intermediate step of a three-step closed life support cycle directed to the conversion of the human and/or animal and/or cellular and/or microbial metabolic wastes: such as but not limited to urea and carbon dioxide, into breathable oxygen and a food or feed source and/or nutritional supplement. In certain embodiments this oxygen and/or food or feed source and/or nutritional supplement may be fed or otherwise recirculated back to the humans and/or animals and/or cells and/or microbial culture that were the source of the said metabolic wastes. In these embodiments of the present invention, in addition to the chemoautotrophic CO2-fixation step, the other two steps of the complete cycle are (1) the collection and recovery of the CO2 removed from a cabin and/or other contained or closed atmosphere and/or aquatic system and (2) the electrolysis of water to produce breathable oxygen for the cabin supply and/or supply and/or refreshment of a contained or closed atmosphere and/or aquatic system, along with by-product hydrogen, which is fed to the gas phase of the closed culture vessel used according to the present invention. In certain non- limiting embodiments, the bacteria use waste urea as a partial or sole nitrogen source during growth together with CO₂ waste as a carbon source. In certain non-limiting embodiments, the harvested excess of cells from a steady-state culture is a potential food for humans, animals, or other heterotrophs and/or a fertilizer for plants. [279] The present invention relates to bioreactors that comprise a cell, which comprises at least one endogenous or exogenous nucleic acid sequence that encodes a pathway enzyme to a sugar, such as but not limited to glucose, or starch, or carbohydrate, or polysaccharide or amino acid, or protein, or other nutrient. In some embodiments, the system comprises two or more, three or more, or four or more bioreactors, at least one of which comprise a cell, which comprises at least one endogenous or exogenous nucleic acid sequence that encodes a pathway enzyme to a sugar, such as but not limited to glucose, or starch, or carbohydrate, or polysaccharide or amino acid, or protein, or other nutrient. In some embodiments, the system of bioreactors comprises at least a first and second bioreactor, wherein the first bioreactor comprises a cell, which comprises at least one endogenous or exogenous nucleic acid sequence that encodes a pathway enzyme to a sugar, such as but not limited to glucose, or starch, or carbohydrate, or polysaccharide or amino acid, or protein, or other nutrient; and wherein the second bioreactor comprises a microorganism derived from a different species, wherein the microorganism from a different species comprises at least one endogenous or exogenous nucleic acid sequence. In some embodiments, the system of bioreactors comprises a first bioreactor that comprises the cell of the present invention and a second bioreactor comprising a zooplankton, and/or a microalgal, yeast, bacterial, fungal, animal, and/or plant cell. In some embodiments, the system comprises a first bioreactor that comprises the cell of the present invention and a second tank or vessel comprising a multicellular animal and/or an aquaculture. [280] In certain non-limiting embodiments of the present invention the microorganisms of the present invention are maintained in a symbiotic relationship and/or a trophic relationship with other living organisms. In certain embodiments the microorganisms and/or multicellular organisms fed glucose, other sugars, starch, carbohydrates, polysaccharides, proteins, and/or and other nutrients produced according to the present invention can be grown in containers of natural or artificial origin including but not limited to bioreactors; biological scrubber columns; packed-bed reactors; plug-flow reactors; vats; tanks and in particular tank systems such as known in the prior arts of aquaculture, aquaponics, and hydroponics; digesters; towers; ponds; pools; reservoirs; wells; lagoons; cisterns; caves; caverns; mine shafts; and quarries. The container walls, boundaries, or lining of the structure containing the organisms can be composed of one or more materials including but not limited to steels, other metals and their alloys, plastics, fiberglass, ceramics, glass, concrete, cement, tar, bitumen, sealant, wood, soil, sand, clay, stone and any combination thereof. In certain non-limiting embodiments, the organisms can also be grown in more open structures such as pens. [281] An additional feature of certain non-limiting embodiments of the present invention regards the source, production, or recycling of the electron donors used by the chemoautotrophic microorganisms to fix carbon dioxide and/or other C1 feedstocks into organic compounds. The electron donors used for carbon dioxide capture and carbon fixation can be produced or recycled in certain embodiments of the present invention electrochemically or thermochemically using power from a number of different renewable and/or low carbon emission energy technologies including but not limited to: photovoltaics, solar thermal, wind power, hydroelectric, nuclear, geothermal, enhanced geothermal, ocean thermal, ocean wave power, tidal power. Many of the reduced inorganic chemicals upon which chemoautotrophs can grow (e.g. H2, CO, H2S, ferrous iron, ammonium, Mn²⁺) can be readily produced using electrochemical and/or thermochemical processes well known in the art and science of chemical engineering that can be powered by a variety carbon dioxide emission-free or low-carbon emission and/or renewable sources of power including but not limited to photovoltaics, solar thermal, wind power, hydroelectric, nuclear, geothermal, enhanced geothermal, ocean thermal, ocean wave power, or tidal power. [282] In certain embodiments of the present invention that use molecular hydrogen as electron donor the H₂ is generated by methods well known to art and science of chemical and process engineering including but not limited to one or more of the following: through electrolysis of water including but not limited to approaches using Proton Exchange Membranes (PEM), liquid electrolytes such as KOH, alkaline electrolysis, Solid Polymer Electrolyte electrolysis, high-pressure electrolysis, high temperature electrolysis of steam (HTES); and/or through the thermochemical splitting of water through methods including but not limited to the iron oxide cycle, cerium(IV) oxide-cerium(III) oxide cycle, zinc zinc- oxide cycle, sulfur-iodine cycle, copper-chlorine cycle, calcium-bromine-iron cycle, hybrid sulfur cycle; and/or electrolysis of hydrogen sulfide; and/or thermochemical splitting of hydrogen sulfide; and/or other electrochemical or thermochemical processes known to produce hydrogen with low- or no- carbon dioxide emissions including but not limited to: carbon capture and sequestration (CCS) enabled methane reforming; CCS enabled coal gasification; the Kværner-process and other processes generating a carbon-black product; CCS enabled gasification or pyrolysis of biomass. In certain embodiments of the present invention the approach to generating H2 includes but is not limited to electrolysis powered by renewable electrical energy and/or electricity from a low-GHG source. In certain embodiments of the present invention electrolysis is powered by one or more of the following: solar including but not limited to photovoltaics and/or solar thermal; wind power, hydroelectric; nuclear; geothermal; enhanced geothermal; ocean thermal; ocean wave power; tidal power. [283] In certain embodiments of the present invention, the microbial bioprocess is integrated with, and provides nutrients, to an agricultural and/or aquacultural process and/or heterotrophic bioprocess and/or fermentation and/or photosynthetic or mixotrophic bioprocess, and/or removes waste products such as but not limited to CO2, nitrogenous wastes, and/or waste water from the same. In certain embodiments, the electricity and/or heat requirements of the said processes receiving nutrients from and/or having wastes removed by the present invention are met using renewable energy and/or energy from a low-GHG source. [284] In certain embodiments of the present invention, renewable power produced during off-peak demand hours for the electrical grid, is used to produce H₂ feedstock for the process. In certain embodiments of the present invention, onsite storage of H2 and CO2 gases enables diversion of power from the grid only during periods when renewable generation exceeds electrical demand. In certain embodiments power is allowed to flow as usual into the grid during periods of higher demand. In certain embodiments of the present invention the process does not disrupt renewable power supply, but rather enables more complete utilization of renewable generation capacity such as but not limited to wind and solar. Certain embodiments of the present invention allow and/or facilitate continued renewable power operation and generation and capacity usage even during periods when electrical generation exceeds grid demand (e.g. off-peak wind or solar generation). [285] In certain embodiment of the present invention hydrogen electron donors are not necessarily generated with low- or no- carbon dioxide emissions, however the hydrogen is generated from waste, sustainable, or low value sources of energy and/or carbon using methods known in to art of chemical and process engineering. Such methods include but are not limited to gasification, pyrolysis, steam-reforming, or autothermal reforming of feedstock such as but not limited to one or more of the following: municipal solid waste, black liquor, agricultural waste, wood waste, stranded natural gas, biogas, sour gas, methane hydrates, liquid petroleum gas, pet coke, tires, sewage, manure, straw, sea weed and kelp, and low value, highly lignocellulosic biomass in general. [286] In certain embodiments of the present invention a synthesis gas or producer gas containing H₂ and/or CO and/or CO₂ is utilized as an electron donor and/or as a carbon source. In certain embodiments, the H₂ and/or CO and/or CO₂ contained in a syngas or producer gas is supplemented by H2 generated using a renewable and/or low-GHG energy source and conversion process such as one or more of those described herein. [287] In certain embodiments, the gasification, pyrolysis, incineration, and/or anaerobic digestions used to generate electron donors and/or carbon sources that are used in the bioprocess of the present invention, also generate useful co-products including but not limited to electricity and/or process heat, which are utilized in the microbial bioprocess, and/or an associated agricultural or aquacultural or fermentation system, and/or provided to a grid or utility, or otherwise provided to surrounding consumers. [288] In certain embodiments, process heat generated as a co-product of the production of hydrogen and/or CO via methods such as gasification, pyrolysis, or steam-reforming is recovered and utilized elsewhere in the conversion process to improve overall energy efficiency. A chemical and/or heat and/or electrical co-product can accompany the generation of molecular hydrogen and/or CO, which can be used to the extent possible elsewhere in the conversion process of certain embodiments of the present invention, for example, in order to improve efficiency. [289] In certain embodiments, additional chemical co-product (e.g., beyond what can be used in internally in the conversion process of certain embodiments of the present invention) can be prepared for sale in order to generate an additional stream of revenue. Excess heat or electrical energy co-product in the production of molecular hydrogen and/or CO (e.g., beyond what can be used internally in the process) can be delivered for sale, for example, for use in another chemical and/or biological process through means known in the art and science of heat exchange and transfer, and electrical generation and transmission, including but not limited to the conversion of process heat to electrical power in a form that can be sold into the electrical grid. [290] In certain embodiments of the present invention that utilize H₂ as an electron donor, there can be a chemical co-product formed in the generation of H2 using a renewable and/or CO2 emission-free energy input. If for example water is used as a hydrogen source, then oxygen can be a co-product of water splitting through processes including but not limited to electrolysis or thermochemical water splitting. In certain embodiments of the present invention using water as a hydrogen source and knallgas microorganisms, some of the oxygen co-product can be used for the production of ATP and/or other intracellular energy carriers through respiration by the oxyhydrogen reaction. In certain embodiments of the present invention, the oxygen produced by water-splitting in excess of what is required for respiration in order to maintain optimal conditions for carbon fixation and organic compound production by the knallgas microorganisms and/or other aerobic organisms in the system, may be processed into a form suitable for sale through process steps known in the art and science of commercial oxygen gas production. [291] The electron donors in certain embodiments of the present invention may also be sourced or refined from pollutants or waste products including but not limited to one or more of the following: process gas; tail gas; enhanced oil recovery vent gas; stranded natural gas; biogas; landfill gas; and sour gases. In certain embodiments of the present invention a tail gas containing H2 and/or CH4 and/or CO is used as a source of electron donor and/or carbon. In certain embodiments tail gases from an oil refinery are used as a source of electron donors and/or carbon. [292] In certain non-limiting embodiments, organic compounds containing only one carbon atom are generated through the gasification and/or pyrolysis of biomass and/or other organic matter (e.g., biomass and/or other organic matter from waste or low value sources); and/or through methane steam reforming of methane or natural gas (e.g., stranded natural gas, or natural gas that would be otherwise flared or released to the atmosphere), or biogas, or landfill gas, and provided as a syngas and/or other gas or streams of C1 compounds to the culture of microorganisms; where in certain embodiments the ratio of hydrogen to carbon monoxide in the syngas or producer gas may be adjusted through means such as the water gas shift reaction, and/or where the ratio of hydrogen to CO₂ may be adjusted through means such as carbon capture, prior to the gases being delivered to the microbial culture. [293] In some embodiments the biomass produced through the present invention is converted to animal feed or incorporated into an animal feed formulation or utilized as a source of human nutrition or is used as a nutrient in another heterotrophic fermentation or cell culture or is used as a nutrient, biostimulant, or biofertilizer in another mixotrophic, photosynthetic and/or agricultural production. [294] A significant fraction of higher plants is inedible to many different animals including but not limited to humans and other non-ruminants. This can lead to numerous disadvantages including the channeling of energy and carbon into undesirable byproducts or waste products. This can lower the yield of desired products and add addition burdens for waste processing and disposal. [295] In certain embodiments of the present invention a greater flux of carbon and/or energy is directed into targeted biomass products than for a comparable, in terms of CO2 capture and/or biomass production, higher plant crop. In certain embodiments, the ratio of inedible to edible parts of the biomass produced in the present invention is lower than for a higher plant crop. [296] In certain embodiments, a higher-plant culture grown under artificial lighting, will require at least thirty times more electrical power per unit weight of edible biomass produced than the present invention. The growth cycle of higher plant crops is relatively long, so that food harvests are periodic, and consumption generally does not match production. This mismatch between production and consumption generally necessitates relatively widespread preservation and storage to prevent wastage. [297] In certain embodiments of the present invention the production of biomass by the microorganisms of the present invention and the consumption of biomass products by animals or other heterotrophs is much more closely matched than for a comparable system based on higher plant crops. In certain embodiments of the present invention, less preservation and/or storage of biomass is required than for a comparable system based on higher plant crops. In certain embodiments of the present invention, there is lower amounts of food wastage than for comparable higher plant crops. [298] In some embodiments, the microorganisms of the present invention produce at least 1 mg of carbon-based product of interest per liter of liquid culture suspension. In some examples, the product is secreted by the organism into culture medium. In other examples, the product is retained in the organism in the course of fermentation. In some cases, the product may be recovered by lysing the cells and separating the product. In other cases, the product may have commercial value in the intact organism without significant preparation or purification of the product from the organism. [299] In certain embodiments recovery of biosynthetic chemical products and/or spent nutrients from the aqueous broth solution can be accomplished using equipment and techniques known in the art of process engineering, and targeted towards the chemical products of particular embodiments of the present invention, including but not limited to: solvent extraction; water extraction; distillation; fractional distillation; cementation; chemical precipitation; alkaline solution absorption; absorption or adsorption on activated carbon, ion-exchange resin or molecular sieve; modification of the solution pH and/or oxidation-reduction potential, evaporators, fractional crystallizers, solid/liquid separators, microfiltration, ultrafiltration, nanofiltration, reverse osmosis, and all combinations thereof. [300] In certain embodiments of the present invention separation of cell mass from liquid suspension is performed. In certain embodiments, this separation is performed by methods known in the art of microbial culturing. Examples of cell mass harvesting techniques are provided, for example, in PCT Application No. WO08/00558, published Jan.8, 1998; U.S. Pat. No.5,807,722; U.S. Pat. No.5,593,886 and U.S. Pat. No.5,821,111, incorporated by reference herein in their entireties, including but not limited to one or more of the following: centrifugation; flocculation; flotation; filtration using a membranous, hollow fiber, spiral wound, or ceramic filter system; vacuum filtration; tangential flow filtration; clarification; settling; hydrocyclone. In certain embodiments where the cell mass may be immobilized on a matrix, it may be harvested by methods including but not limited to gravity sedimentation or filtration, and separated from the growth substrate by scraping or liquid shear forces. [301] In certain embodiments the liquid left over following the removal of cell mass can be pumped to a system for removal and/or recovery of dissolved chemical products of the bioprocess and/or unreacted nutrients. In certain embodiments, unreacted nutrients and/or water are recovered and recycled to the extent possible and/or in certain embodiments sold as a co-product and/or properly disposed of. In certain embodiments, the removal of waste products and/or contaminants and/or any inhibitory and/or deleterious compounds using methods and technologies known in the art is performed prior to returning water and/or unreacted nutrients to the bioreactor/s. [302] In certain embodiments of the present invention involving chemoautotrophic microorganisms a solution of oxidized metal cations can remain following the chemosynthetic reaction step or steps. In other non-limiting embodiments, a solution rich in dissolved metal cations can also result from particulates and impurities carried in certain gas inputs to the process such as from a coal fired plant or gasification of coal or municipal solid waste (MSW). [303] In some embodiments of the present invention where metal cations are present in the process stream that would be advantageous to remove, the process stream can be stripped of metal cations by methods including but not limited to: cementation on scrap iron, steel wool, copper or zinc dust; chemical precipitation as a sulfide or hydroxide precipitate; electrowinning to plate a specific metal; absorption on activated carbon or an ion-exchange resin, modification of the solution pH and/or oxidation-reduction potential, reverse osmosis, and/or solvent extraction. In certain embodiments of the present invention, the recovered metals can be recycled and/or used as nutrient and/or fertilizer for another biological process and/or sold for an additional stream of revenue. [304] In certain embodiments free and/or dissolved organic molecules, such as but not limited to glucose, other sugars, starch, carbohydrates, polysaccharides, and/or polysaccharides can be released into the process stream solution from the microorganisms through means including but not limited to cellular excretion or secretion or cell lysis. [305] In certain embodiments recovery and/or recycling of chemical products and/or unreacted nutrients from the aqueous solution can be accomplished in certain embodiments of the present invention using equipment and techniques known in the art of process engineering, and targeted towards the chemical products of particular embodiments of the present invention, including but not limited to: solvent extraction; water extraction; distillation; fractional distillation; cementation; chemical precipitation; alkaline solution absorption; absorption or adsorption on activated carbon, ion-exchange resin or molecular sieve; modification of the solution pH and/or oxidation-reduction potential, evaporators, fractional crystallizers, solid/liquid separators, microfiltration, ultrafiltration, nanofiltration, reverse osmosis, and all combinations thereof. [306] In certain embodiments, chemical products and/or unreacted nutrients flow into an environment that supports the growth of other organisms. In certain embodiments, effluent water and unreacted nutrients are used to irrigate and fertilize algae and/or higher plants. Tilapia and other aquatic animals, are able to absorb minerals from the culture water. In certain embodiments, unreacted mineral nutrients flow into a grow environment for Tilapia and/or other aquatic animals. In certain embodiments of the present invention inorganic nutrients flow from the chemoautotrophic bioreactor of the present invention to an aquaculture system containing animals including but not limited to tilapia and stimulate the production of live food organisms and plants in the culture system including but not limited to algae and phytoplankton. In certain embodiments inorganic and/or organic nutrients from the bioreactor effluent function as a fertilizer which increase primary production of a pond and/or or other enclosures used in aquaculture and/or aquaponics and/or hydroponics. [307] In certain embodiments, the chemoautotrophically generated biomass of the present invention produced from carbon sources including but not limited to one or more of the following: CO2, CO, CH4, CH3OH; flows or is otherwise applied to an agricultural and/or aquacultural and/or aquaponics and/or hydroponics system and/or fermentation and/or cell culture and/or photosynthetic or mixotrophic system where it supplements and/or displaces organic nutrients in directly stimulating higher trophic levels by supplying organic nutrients such as but not limited to glucose, other sugars, starch, carbohydrates, polysaccharides, amino acids, proteins, and vitamins. [308] The high growth rate attainable by certain chemoautotrophic species can allow them to match or surpass the highest rates of carbon fixation and/or biomass production per standing unit biomass that can be achieved by photosynthetic microbes. In certain embodiments, surplus biomass can be produced. In certain embodiments, surplus growth of cell mass can be removed from the system to produce a biomass co-product. In some embodiments, surplus growth of cell mass can be removed from the system in order to maintain a desirable (e.g., an optimal) microbial population and cell density in the microbial culture for continued high carbon capture and fixation rates and/or feedstock conversion rates. [309] In certain embodiments, the chemicals that are used in processes for the recovery of chemical products and/or the recycling of nutrients and water and/or the removal of waste have low toxicity for humans, and if exposed to the process stream that is recycled back into the bioreactor, low or no toxicity for the particular microorganisms being used in that particular embodiment of the invention. [310] To assist in the processing of the biomass product into useful products, harvested microbial cells in certain embodiments of the invention can be broken open using well known methods including but not limited to one or more of the following: ball milling, cavitation pressure, sonication, homogenization, or mechanical shearing. [311] The harvested biomass in some embodiments may be dried in a process step or steps. Biomass drying can be performed in certain embodiments of the present invention using well known technologies including but not limited to one or more of the following: centrifugation, drum drying, evaporation, freeze drying, heating, spray drying, vacuum drying, and/or vacuum filtration. In certain embodiments of the present invention waste heat can be used in drying the biomass. In certain embodiments heat waste from the industrial source of flue gas used as a carbon source can be used in drying the biomass. In certain embodiments, the heat co-product from the generation of electron donors and/or C1 carbon source as discussed above can be used for drying the biomass. [312] In certain embodiments of the invention, the biomass is further processed following drying, or, without a preceding drying step, in order to aid the separation and production of useful biochemicals. In certain embodiments, this additional processing involves the separation of the glucose, other sugars, starch, carbohydrates, polysaccharides, proteins, lipids and/or vitamins and/or other targeted biochemicals from the microbial biomass. In certain embodiments, the separation of the lipids can be performed by using nonpolar solvents to extract the lipids such as, but not limited to one or more of: hexane, cyclohexane, ethyl ether, alcohol (isopropanol, ethanol, etc.), tributyl phosphate, supercritical carbon dioxide, trioctylphosphine oxide, secondary and tertiary amines, or propane. In certain embodiments, other useful biochemicals can be extracted using solvents including but not limited to one or more of: chloroform, acetone, ethyl acetate, and tetrachloroethylene. [313] In some embodiments, the instant invention provides for a method of producing glucose, sugars, starch, carbohydrates, polysaccharides, amino acids, proteins, and/or vitamins by combining, in a bioreactor or solution, one or more biosynthetic pathways including but not limited to a gluconeogenic pathways and/or an amino acid biosynthetic pathway, a carbon-containing gas, and an engineered or natural microorganism that converts a carbon-containing gas such as syngas, producer gas, CO₂, carbon monoxide and mixtures of the same containing hydrogen gas; and/or C1 compounds, gaseous or liquid, including but not limited to methanol or methane, into glucose, other sugars, starch, carbohydrates, polysaccharides, amino acids, and/or proteins. In some embodiments, glucose, other sugars, starch, carbohydrates, polysaccharides, amino acids and/or proteins are included in a human food or food ingredient and/or an animal feed formulation using processes known in the art and science of chemistry, chemical engineering, and food science. [314] In certain embodiments of the present invention carbohydrate-rich biomass produced through the invention is used as an alternative calorie and/or fiber source. In certain embodiments, it is used as a replacement for or additive to starch and/or other carbohydrates derived from one or more of the following plant crop sources: wheat, potatoes, maize (corn), rice, and cassava (manioc).. In certain non-limiting embodiments, the carbohydrate- rich biomass does not contain significant amounts of anti-nutritional factors. In certain embodiments, the carbohydrate-rich biomass does not contain significant amounts of one or more of the following: gossypol, glucosinolates, saponins, trypsin inhibitors. [315] High productivity bioprocess for the cultivation of knallgas microorganisms is described in in PCT international application number PCT/US2022/029657, filed May 17, 2022, and entitled “HIGH PRODUCTIVITY BIOPROCESSES FOR THE MASSIVELY SCALABLE AND ULTRA-HIGH THROUGHPUT CONVERSION OF CO2 INTO VALUABLE PRODUCTS.” This application is incorporated herein by reference in its entirety for all purposes. [316] The utilization of knallgas bioprocess derived nutrients for the growth of other microorganisms and cell cultures is described in in PCT international application number PCT/US2021/014795, filed January 22, 2021, and entitled “MICROORGANISM- DERIVED PROTEIN HYDROLYSATES, AND METHODS OF PREPARATION AND USE THEREOF.” This application is incorporated herein by reference in its entirety for all purposes. [317] The harvesting, recovery and utilization of knallgas bioprocess derived nutrients for human, animal, and plant nutrition is described in in PCT international application number PCT/US2018/016779, filed February 4, 2018, and entitled “MICROBIAL CONVERSION OF CO, AND OTHER CI SUBSTRATES TO VEGAN NUTRIENTS BIOSTIMULANTS, ANDSYSTEMS FOR ACCELERATED SOIL CARBON SEQUESTRATION.” This application is incorporated herein by reference in its entirety for all purposes. [318] Engineering of knallgas microorganisms is described in U.S. Patent Application No. 2013/0089899, filed September 19, 2012, and entitled “INDUSTRIAL FATTY ACID ENGINEERING GENERAL SYSTEM FOR MODIFYING FATTY ACIDS.” This application is incorporated herein by reference in its entirety for all purposes. [319] Use of knallgas microorganisms for the conversion of syngas, producer gas, or other H2 and CO2 and/or CO containing gas mixes in high energy density molecules is described in U.S. Patent Application filed on October 26, 2012 under No.2013/0149755, and entitled USE OF OXYHYDROGEN MICROORGANISMS FOR NON-PHOTOSYNTHETIC CARBON CAPTURE AND CONVERSION OF INORGANIC AND/OR C1 CARBON SOURCES INTO USEFUL ORGANIC COMPOUNDS. This application is incorporated herein by reference in its entirety for all purposes. [320] Use of chemotrophic microorganisms for the conversion of CO2 into useful organic chemicals is described in PCT international application number PCT/US2010/001402, filed 05/12/2010, published in the U.S. as Application No.2013/0078690, and entitled BIOLOGICAL AND CHEMICAL PROCESS UTILIZING CHEMOAUTOTROPHIC MICROORGANISMS FOR THE CHEMOSYTHETIC FIXATION OF CARBON DIOXIDE AND/OR OTHER INORGANIC CARBON SOURCES INTO ORGANIC COMPOUNDS, AND THE GENERATION OF ADDITIONAL USEFUL PRODUCTS. This application is incorporated herein by reference in its entirety for all purposes. [321] Aspects of the invention relate to engineered organisms for use in the production of molecules for industrial application. As used herein, “engineered organisms” and “engineered microorganism” and “non-naturally occurring microorganism” are used interchangeably and refer to organisms that recombinantly express nucleic acids comprising at least one exogenous gene. In some embodiments, such nucleic acids encode enzymes as discussed herein. Homologs and alleles of genes associated with the invention can be identified by conventional techniques. Also encompassed by the invention are nucleic acids, referred to as “primers” or “primer sets,” that hybridize under stringent conditions to the genes described herein. The term “stringent conditions” as used herein refers to parameters with which the art is familiar. Nucleic acid hybridization parameters may be found in references which compile such methods, e.g. Molecular Cloning: A Laboratory Manual, J. Sambrook, et al., eds., Fourth Edition, Cold Spring Harbor Laboratory Press, Cold Spring Harbor, New York, 2012, or Current Protocols in Molecular Biology, F.M. Ausubel, et al., eds., John Wiley & Sons, Inc., New York. [322] An additional feature of some embodiments of the present invention regards modifying microorganisms of the present invention, including but not limited to modifying biochemical pathways in oxyhydrogen microorganisms for the production of targeted organic compounds. This modification can be accomplished by manipulating the growth environment and/or through methods known in the art of artificial breeding including but not limited to accelerated mutagenesis (e.g., using ultraviolet light or chemical treatments), genetic engineering or modification, hybridization, synthetic biology or traditional selective breeding. Possible modifications of the microorganisms include but are not limited to those directed at producing increased quantity and/or quality of glucose, other sugars, starch, carbohydrates, polysaccharides, amino acids, proteins, and/or vitamins. [323] An additional feature of certain embodiments of the present invention relates to modifying biochemical pathways in oxyhydrogen microorganisms for the production of targeted organic compounds. This modification can be accomplished by manipulating the growth environment and/or through methods known in the art of artificial breeding including but not limited to accelerated mutagenesis (e.g. using ultraviolet light or chemical treatments), genetic engineering or modification, hybridization, synthetic biology or traditional selective breeding. Post-process conversions Production of human food or animal or aquacultural feed or microbial or cell culture nutrients [324] In some embodiments carbohydrates and/or carbohydrate-rich biomass produced according to the present invention is then converted to human food, food ingredients, animal feed, or rich-media for microbial growth using methods and processes well known in the art and science of chemistry, chemical engineering, and food science. In certain embodiments, the feed produced through the invention is used to grow organisms including but not limited to one or more of the following: other microorganisms, yeast, fungi, zooplankton, shellfish or other invertebrates; insects; fish; amphibians; reptiles; birds; mammals. In certain non- limiting embodiments, the fish include but are not limited to one or more of: tilapia; salmon; cobia. In certain non-limiting embodiments, the birds include but are not limited to chickens or turkeys. In certain non-limiting embodiments, the mammals include but are not limited to one or more of: rabbits, goats, sheep, pigs, cows. [325] In some embodiments, the microbial cells of the present invention are boiled and/or heat treated prior to feeding to another organism. In other embodiments, the cells are sonicated, or otherwise lyzed or ruptured prior to feeding to another organism. [326] One of the major challenges in utilizing biosystems for food production is obtaining the proper dietary balance between the quantities of protein, carbohydrate, and fat. The microbial systems generally considered for food synthesis tend to produce biomass disproportionately high in protein. In certain embodiments of the present invention an carbohydrate-rich strain is used that produces a higher proportion of carbohydrates relative to protein content. In certain embodiments, the glucose and/or starch production strain described in the present invention is utilized to increase the carbohydrate macronutrient in a diet. [327] In certain embodiments, a carbohydrate or polysaccharide producing strain is utilized that produces a higher proportion of carbohydrates or polysaccharide relative to protein content. In certain embodiments, the carbohydrate or polysaccharide producing strain utilized is Xanthobacter autotrophicus and/or Hydrogenovibrio marinus. [328] This invention is not limited in its application to the details of construction and the arrangement of components set forth in the description or illustrated in the drawings. The invention is capable of other embodiments and of being practiced or of being carried out in various ways. [329] The following examples are intended to illustrate, but not limit, the invention. EXAMPLES Example 1 [330] Production of glucose by C necator engineered for glucose transport Demonstration of functionality of the Zymomonas mobilis glucose facilitator glf in C necator. [331] Growth on glucose by a mutant expressing the glucose facilitator, Glf. C. necator cannot naturally grow on glucose because it lacks a transport system specific for glucose uptake. In this example the glf gene was cloned into Cupriavidus necator. glf codes for the glucose facilitator from Zymomonas mobilis. When the recombinant strain is challenged for its ability to grow on glucose, it shows rapid growth while the glf-minus control does not grow, indicating successful assembly and function of the glucose facilitator. Strain was grown on Luria Broth + Kanamycin 200ug/mL [332] Figure 3 shows the growth of the induced chemoautotroph with glucose facilitator glf+ genotype. Induction of the pBAD glf construct produces a growth+ phenotype indicating successful expression and assembly of the glucose membrane transporter. Example 2 Production of glucose on CO2/H2 by a multiple C necator deletion strain glk, zwf1, zwf2, zwf3 via oxyhydrogen fermentation.. [333] The recombinant strain was inoculated as a seed in Luria broth + kanamycin, 200ug/mL, and incubated with agitation overnight at 30C. The seed culture was transferred to a 1L DASGIP CSTR bioreactor modified for gas delivery. The culture was sampled in 25mL aliquots over 140 hours reaching an OD 600 of 51. Samples were submitted for analytical determination of sugars by GCMS. Glucose titer reached 17mg in the 6-day 25mL sample, extrapolating to 640mg/L produced and secreted. ^{mg Sugars in 25-mL of glucose strain in MSM media, gas-grown, 1-L DASGIP} bioreactor D-(+)- L-(+ Total mg Days D-(+)-Glucose )- L-(+)- Galactose Rhamnose Ribose Sugars in 25- mL culture 1 0 0 0 0 0 2 0.30 0 0 0.60 0.89 3 1.08 0 0 1.58 2.66 4 8.21 0 0 1.12 9.34 5 15.63 0.35 0 0.55 16.53 6 16.00 0.66 0 0.52 17.18 [334] TABLE 1. Carbohydrate composition of the C. necator glucose strain grown in a 1L DASGIP bioreactor under oxyhydrogen fermentation conditions. Example 3 Production of starch by an engineered C necator strain. [335] C necator containing either the glgA (sample 1) or glgC gene (sample 2), or both, glgAC (sample 3). Engineered strains were grown on fructose in MSM medium. Sample 3 staining indicates accumulated starch when both glg genes are heterologously expressed. [336] Figure 4 shows Lugol staining of starch produced by a recombinant strain expressing glg genes. Tube 1 is a strain expressing glgA, tube 2 is a strain expressing glgC and tube C is a strain expressing both genes. Staining indicates starch production in the strain expressing both genes and Lugol background in tubes 1 and 2. [337] Three strains were first constructed using standard transformation of a pBAD plasmid incorporating genes for heterologous expression of either glgA (1), glgC (2) or both genes (3) each driven by an arabinose promoter. Strains were grown in MSM medium at 30. C. necator has an endogenous pathway that directs carbon to ADP-glucose, the precursor for a recombinant pathway for the biosynthesis of starch. Recombinant expression of both glucose-1-P adenylyltransferase (glgC) and/or ADP glucose starch synthase (glgA) (see Figure 1) derived from E. coli MG1655 completes the metabolic pathway to starch as shown by staining of recombinant cells with Lugol solution. Lugol’s reagent is a solution composed of iodine and potassium iodide. The iodine in Lugol’s solution selectively binds to alpha-1,4 glucans found in polysaccharides, starch. After centrifugation, it’s evident that the starch reactive material is in the pellet, i.e., intracellular, and that staining in uncentrifuged samples 1 and 2 represents background in the medium from the Lugol stain. [338] Starch recovery from engineered oxyhydrogen biomass [339] Extractions using hot water or homogenization were used to solubilize starch granules from the engineered oxyhydrogen strain. Systematic trials at different temperatures between 60 and 100C for varying incubation times established optimal conditions for hot water extraction. The best-performing starch extraction method is high pressure homogenization. The extracted crude starch fraction is white in color. Example 4 [340] Cupriavidus necator strain DSM 531 was grown to 38 grams per liter dry cell density on a mixture of H₂, CO₂, and O₂ gases as the sole source of energy and carbon for growth. [341] The following protocol was followed for experiments performed using a mixture of gases including H₂, CO₂, and O₂ in a stirred-tank bioreactor. [342] Apparatus: Culture was grown in batch, using a custom-manufactured 500 mL glass fermenter with PEEK headplate. Temperature and pH were controlled and monitored with a commercial controller (Electrolab, Fermac 360, United Kingdom). A combination of magnetic stir bars and continuous recycle at 280 mL/min were used for mixing. Recycle could be either withdrawn from the bottom liquid section of the reactor and returned to the headspace through sprayers to control foaming or run in reverse to recycle the headspace gas and foam into the bottom of the broth. Gas supply was from compressed H2, compressed CO₂ and house air, each regulated to 20 psi. H₂ and air were delivered to a flow proportioner (Matheson G2-4D151-E401/E401, 20 psi), which set the relative fraction of the gases. The H2/air gas mix was then delivered to each fermenter through a variable area flow meter; the flow rate to each fermenter of the same H2/air composition could be adjusted by the needle valve of the flow meter. CO₂ gas was split and delivered to individual variable area flow meters at each fermenter. The CO₂ and H₂/air lines tee into a single line delivered to the fermenter. A pressure gauge was used to monitor the gas delivery pressure to the fermenter. Gas was mixed into the fermenter broth via four 2- micron diffusion stones (p/n KEG592, http://morebeer.com/products/diffusion-stone-2- micron-oxygen.html), and vented from the reactor via a condenser to a foam-overflow bottle, then to an exhaust system. [343] Medium: The medium used for this experiment is described in Example 1. pH control was performed with 2N NH4OH or 2N NaOH. 2N NH4OH was prepared from 5 M NH₄OH, Fluke 318612 (kept at 4°C) (120 mL) + autoclaved milliQ-H₂O (180 mL). [344] Autotrophic inoculum: Cupriavidus necator DSM 531 inoculum was taken from H2/CO2/O2 grown serum bottle culture. Inoculum was prepared from preserved 0.5 mL glycerol stocks stored at -80C for the DSMZ 531 strain. Revival cultures were started on H₂/CO₂/O₂ gas mix per the serum bottle protocol described in Example 1, with 0.5 mL glycerol stock added to 20 mL minimal salts medium (MSM) in a gas tight serum bottle. This initial serum bottle was then subcultured, 1 mL to 20 mL fresh MSM, into 2 serum bottles under the standard H2/CO2/O2 gas headspace. These serum bottles were incubated at 30°C, 250 RPM. The initial revival from the glycerol stock on gas took 2 days and the subculture took another day to grow. The two serum bottle cultures were provided as inoculum for the bioreactor. Optical density (OD) of inoculum was taken as well as a sample for DNA analysis. The gas grown inoculum had an OD ~1. The fermenter was inoculated to give an initial OD ~0.1. In other words, the serum bottle broth was diluted in the bioreactor at a 1:10 ratio. Inoculum was transferred from serum bottles to the bioreactor using a 60 mL syringe. After inoculation, a T0 OD was taken. Generally, all OD measurements were performed with a Beckman Coulter DU720 UV/Vis spectrophotometer. [345] Fermenter Operation: Base addition - pH was controlled with 2N NH₄OH Foam Control - If foaming filled more than ½ headspace, and was not controlled by headspace spraying or recirculation, then anti-foam was used. (A8011, Sigma Antifoam C Emulsion, www.sigmaaldrich.com/catalog/product/sigma/a8011?lang=en&region=US) Nutrient amendment - In addition to nitrogen nutrient provided by base addition of NH₄OH, other mineral nutrients were added during the run so as to prolong growth and prevent any mineral nutrient limitations from occurring. [346] Figure 6 gives an example of a growth curve for the knallgas microorganism Cupriavidus necator grown on H₂/CO₂/O₂ gas substrate according to this protocol. The final OD measured at 650 nm was 132 and the final dry biomass density was 38 grams/liter from growth on H2/CO2/O2 gas substrate. Log growth lasted the first day and a half; however the biomass was still accumulating at a linear rate at the termination of the run during day five. Example 5 [347] Hydrogenovibrio marinus strain DSM 11271 was grown to over eight grams per liter dry cell density on a mixture of H₂, CO₂, and O₂ gases as the sole source of energy and carbon for growth. The following protocol was followed for experiments performed using a mixture of gases including H2, CO2, and O2 in a stirred-tank bioreactor. [348] Apparatus: Culture was grown in batch, using custom-manufactured 500 mL glass fermenter with PEEK headplate; a sparge tube having one porous glass frit, connected to tubing for gas delivery with a 0.2 ^m filter; a septum port for amendment delivery; a dip- tube to bottom with aseptic sampling assembly, a condenser connected via tubing to an overflow vessel with a 0.2 ^m filter on the gas outlet; a port for base delivery and tubing for base-delivery with a luer fitting to a sterile syringe; a grounding probe; a port for antifoam delivery; a pH/temperature probe; an oxidation/reduction probe (ORP). Temperature was controlled to 37^°C, and pH to 6.5, using a commercial controller (Electrolab, Fermac 360, United Kingdom). The target temperature was maintained by a heating pad on the bottom of the reactor, and an integral glass jacket for cooling water. The pH was maintained at 6.5 using 6N NH₄OH. The reactor sat on a stir-plate (VWR 12365-344) and a magnetic stir bar (cross shape, VWR ‘spinplus’ # 58947-828) was used for mixing. The stirplate was set to 300-400 RPM. The gas flow rate into the bioreactor was 1 VVM. Gas supply was from compressed H2, compressed CO2 and house air, each regulated to 20 psi. H2 and CO2 were delivered to a flow proportioner (Matheson G2-4D151-E401/E401, 20 psi), which set the relative fraction of the gases. Air was delivered to a variable area flow meter (Key Instruments 1G03_R5). The H2/CO2 gas mix from the flow proportioner was tee’d into the air, and then delivered to the fermenter through a variable area flow meter. A pressure gauge was used to monitor the gas delivery pressure to the fermenter. Inlet gas flowed through a 0.2 ^m filter (Pall, p/n 4251), and then was dispersed into the fermenter broth via one porous pyrex frit (40-60 ^m, Sigma-Aldrich CLS3953312-C) and vented from the reactor via a condenser (jacketed and cooled) to a 2 L foam-overflow bottle, then through another 0.2 ^m filter (Pall, p/n 4251) and finally to an exhaust system. CO₂ flow was set to the minimum c.l. =5 (c.l.=centerline of float), and the other gases were set to achieve the targeted gas composition, calculating according to the flow meter tables, measuring composition by GC and adjusting and re-measuring. c.l. H2= 25, c.l. air=45 was used to provide a gas mix having respective proportions of CO₂/O₂/H₂ of 11/6.3/59. Ongoing monitoring of O₂ in influent and effluent lines was done using a Foxy probe. Occasional gas samples were taken for GC analysis (in 1 L foil bags, skcinc.com p/n 262-01). [349] Medium: One liter of the basal medium contained 2.0g K2HPO4, 1.0 g KH2PO4, 5.0 g (NH4)2SO4, 29.3 g NaCl, 0.2 g MgSO4-7H20, 10.0mg CaCl2, 10.0mg FeSO4.7H2O, 0.6 mg NiSO₄.7H₂O, and 2.0 ml of trace element solution. The trace element solution was taken from Thermophilic Bacteria, CRC Press, Boca Raton, FL, Jacob K. Kristjansson, ed., 1992, p.87, Table 4. [350] Autotrophic inoculum: A 10% inoculation gas-grown inoculum was prepared in two 500 ml bottles with stoppers containing 50 mL of liquid media. A volume of 61.5 mL inoculum, OD6000.75, was injected into bioreactor via a dip-tube to below the liquid level to prevent dispersion in headspace. The line was flushed with filtered air after inoculation to remove trapped inoculum in the dip-tube. [351] Fermenter Operation: Base addition - pH was controlled with 6N NH₄OH; Nutrient amendment - In addition to nitrogen nutrient provided by base addition of NH4OH, 0.2 grams FeSO4.7H2O were added when the broth OD=3, and 2 grams MgSO4.7H2O when the broth OD=10. The influent O₂ was measured to be around 5%, and effluent O₂ ranged from 3-4%. Samples were withdrawn from a tube extending to the bottom of the reactor using an aseptic sampling system with 25 mL bottles. The DNA sequencing results confirmed H. marinus and no contamination was observed to grow on agar plates that were streaked daily throughout the run. [352] Table 3 shows the cell dry weight (CDW) density measured at various time points during the run. The CDW density reached over eight grams/liter during day 5. The content of chloroform/methanol soluble lipid, and hexane soluble lipid, respectively, as a percentage of the biomass sampled at various time points, is also given in Table 3. The lipids were analyzed by GC/MS using the methods described above and were found to contain fatty acids ranging from 14 to 20 carbons in length. Table 3 c/m extractable (%) Hexane extractable (%) Sample Days Vol CDW OD n Average S.D. Average S.D. ID (mL) (g/L) T3 2.78 25 4.556 7.068 2 19.34 11.12 6.88 0.72 T4 3.79 25 6.776 11.824 3 18.42 2.83 8.12 0.43 T5 4.79 25 7.492 14.18 3 20.59 6.31 8.99 2.39 T6 5.79 25 8.296 13 3 24.13 6/07 8.26 1.53 Example 6 [353] Xanthobacter autotrophicus strain DSM 432 was grown to 14 grams per liter dry cell density on a mixture of H₂, CO₂, and O₂ gases as the sole source of energy and carbon for growth. The following protocol was adhered to for an experiment performed using a mixture of gases including H2, CO2, and O2 in a stirred-tank bioreactor. [354] Apparatus: Culture was grown in batch, using a two-liter glass fermenter schematically illustrated in Figure 21 with a headplate schematically illustrated in Figure 22. Temperature and pH were controlled and monitored with pH and temperature probes and a commercial controller. pH was adjusted through automatic addition of 2N NaOH. Ports in the bioreactor were available for provision of nutrient supplements and anti-foam; inoculum delivery; base; fresh media; and aseptic sampling. Agitation was provided by a turbine and gases were sparged through a glass frit. The reactor system is illustrated schematically in Figure 23. It comprised pressure gauges; gas flow meters; safety and check valves; 0.2 micron filters; the bioreactor vessel, sensors, actuators, and controllers; a condenser and foam trap; and outlet vent. Gas supply was from compressed H₂, compressed CO₂ and house air, each regulated to 20 psi. A schematic of the gas delivery system is shown in Figure 24. H2 and CO2 were delivered to a flow proportioner (Matheson G2-4D151-E401/E401, 20 psi), which set the relative fraction of the gases. The settings used in the flow proportioner were c.l. H₂ = 35; c.l CO₂=10; and c.l air=55. This resulted in a gas mix being delivered to the bioreactor of 64% H₂, 11% CO₂, 5.4% O₂ as measured by GC (Shimadzu GC-8A, TCD detector, and Alltech CTR I column). [355] Medium: The MSM medium used for this experiment is described in Thermophilic Bacteria, CRC Press, Boca Raton, FL, Jacob K. Kristjansson, ed., 1992, p.87, Table 4. [356] Inoculum: Xanthobacter autotrophicus strain DSM 432 inoculum was started from a single glycerol stock vial stored at -80ºC which was transferred into 200 mL of MSM in a one-liter gas-tight bottle. Gas pressure of the H2/CO2/O2 headspace was 10 psig. The culture bottle was agitated at 150 rpm at 30ºC. [357] Fermenter Operation: Prior to inoculation, 1.3 liters of MSM was transferred into the bioreactor vessel. The pH was adjusted to 6.8 using NaOH. The temperature was set at 30ºC and the agitation was set at 500 RPM. Samples were taken twice per day for OD and lipid analysis through an aseptic sampling assembly. All OD measurements were performed with a Beckman Coulter DU720 UV/Vis spectrophotometer. One time per day samples were examined under the microscope to check cell morphology. All culture broth samples were centrifuged at 12,000 x g. 1 mL of supernatant was stored for NH⁴⁺ analysis at -20ºC. Wet biomass pellets were stored temporarily at -80ºC and then freeze dried. [358] The correlation between OD₆₀₀ and CDW (mg/ml) is shown in Figure 25. The linear fit to this correlation is CDW = 0.9944*(OD₆₀₀) + 0.4101 with an R2=0.957. Figure 26 shows the growth curve for the knallgas microorganism Xanthobacter autotrophicus grown on H2/CO2/O2 gas substrate according to this protocol. The final OD measured at 600 nm was 14.8 and the final CDW was 13.8 grams/liter from growth on H₂/CO₂/O₂ gas substrate. After a brief period of logarithmic growth at the onset of the run, the biomass accumulated at a roughly linear rate until the termination of the run on day six. The lipids were extracted and analyzed by GC/MS using the methods described above, and were found to have a relatively high proportion of fatty acids that are 18 carbons in length. Example 6 [358] Xanthobacter autotrophicus strain DSM 2269 was grown in a bioreactor on a mixture of H2, CO2, and O2 gases. The culture was centrifuged and then the liquid cell- free supernatant dried and analyzed. The dissolved solutes were found to be 22.8% wt% polysaccharide with the polysaccharide completely made up of glucose units. Example 7 [359] Figure 31 illustrates a general process flow diagram for certain non-limiting embodiments of the present invention that have (A) a process step for the generation of electron donors (e.g., molecular hydrogen electron donors) suitable for supporting chemosynthesis from an energy input and raw inorganic chemical input (e.g., water); (B) followed by delivery of generated H₂ electron donors and O₂ electron acceptors, water, mineral nutrients, along with CO₂ captured from a point industrial flue gas, or other CO₂ source, into (C) chemosynthetic reaction step or steps housed with one of more bioreactors (4), which make use of oxyhydrogen microorganisms to capture and fix carbon dioxide, and create carbohydrate-rich biomass through chemosynthetic reactions; (D) in parallel, there is recovery of surplus chemical co-products from the electron donor generation step (e.g. O₂); followed by (E) process steps for the recovery of biomass products from the process stream; and (F) recycling of unused nutrients and process water, as well as optionally cell mass needed to maintain the microbial culture, back into the carbon-fixation reaction steps (i.e., back into the bioreactors). [360] In the particular embodiment diagrammed in Figure 31, the CO2 containing flue gas is captured from a point source or emitter. Such sources or emitters include but are not limited to power plants, refineries, cement producers, or other fermentations or biological processes. Electron donors (e.g., H2) needed for chemosynthesis can be generated from input inorganic chemicals and energy. In certain embodiments, the hydrogen is generated through a carbon dioxide emission-free process. Exemplary carbon dioxide emission-free processes for hydrogen generation include, for example, electrolytic or thermochemical processes known in the art, which are powered by energy sources including but not limited to photovoltaics, solar thermal, wind power, hydroelectric, nuclear, geothermal, enhanced geothermal, ocean thermal, ocean wave power, tidal power. The flue gas can be pumped through bioreactors (4) containing oxyhydrogen microorganisms along with electron donors and acceptors needed to drive chemosynthesis and a medium suitable to support the microbial culture and carbon fixation through chemosynthesis. In the non-limiting set of embodiments diagrammed in Figure 31, hydrogen electron donor and oxygen and carbon dioxide electron acceptors are compressed and added continuously to the growth broth along with other nutrients required for chemosynthesis and culture maintenance and growth, which are pumped into one or more bioreactors containing one or more knallgas microorganisms such as but not limited to one or more of the following: Cupriavidus necator, Rhodococcus opacus and/or other Rhodococcus sp., Hydrogenovibrio marinus, Rhodopseudomonas capsulata, Hydrogenobacter thermophilus, and/or Xanthobacter autotrophicus. In the set of non-limiting embodiments illustrated in Figure 31, oxygen serves as an electron acceptor in the chemosynthetic reaction for the intracellular production of ATP through the oxyhydrogen reaction linked to oxidative phosphorylation. The oxygen can originate from the flue gas and/or it can be generated from the water-splitting reaction used to produce the hydrogen, and/or it can be taken from air. In Figure 31, carbon dioxide from the flue gas serves as an electron acceptor (non-respiratory; anabolic) for the synthesis of organic compounds including through biochemical pathways utilizing the ATP produced through the respiratory oxyhydrogen reaction, and NADH and/or NADPH produced from the intracellular enzymatically catalyzed reduction of NAD⁺ or NADP⁺ by H2. The cell culture may be continuously flowed into and out of the bioreactors. After the cell culture leaves the bioreactors, the cell mass can be separated from the liquid medium (5). Solid- liquid separation can be accomplished using processes and equipment well known in the art such as but not limited to continuous centrifuges or flowing broth through membrane filters to separate the cell mass from the liquid. Cell mass needed to replenish the cell culture population at a desirable (e.g., optimal) level can be recycled back into the bioreactor. Surplus cell mass can be dried (8) to form a dry biomass product which can be further post- processed (9) into various food, feed, protein, nutritional, fertilizer, chemical, or fuel products. Post-processing of carbohydrate-rich biomass into animal feed and/or plant fertilizer formulations can be performed according to methods known to those skilled in the art. Following the cell separation step, extracellular chemical products of the chemosynthetic reaction can be removed from the process flow and recovered. Then, any undesirable waste products that might be present are removed (7). If necessary, replacement water and/or nutrients can be provided to the bioreactor to make-up for any losses to the biomass product and/or other effluent streams. Example 8 Chemoautotrophic strain screening [361] Strains were first screened for chemoautotrophy on plates using Almore’s Vacu- Quick jar system. Promising strains were then tested in liquid culture. [362] A minimal salts medium (MSM) was prepared as described above and combined and added in agarose (1.5%) plates aseptically.162 candidate strains drawn from the following genera were tested: Cupriavidus; Xanthobacter; Dietzia; Gordonia; Mycobacterium; Nocardia; Pseudonocardia; Arthrobacter; Alcanivorax; Rhodococcus; Streptomyces; Rhodopseudomonas; Rhodobacter; and Acinetobacter. [363] Each strain was streaked onto a minimal salts medium (MSM) + agarose (1.5%) plate. All the respective plates were then placed in an Almore’s Vacu-Quick jar system. At the bottom of each chamber was laid a sterile paper towel soaked with sterile water, in order to maintain humidity in the chamber and prevent the plates from drying during incubation. The gas tight chambers filled with plates were then evacuated; followed by supply of a H₂:CO₂:Air (70/10/20) gas mixture. The gases provided the sole source of energy and carbon for growth. The gas chambers were incubated at 30ºC for 7-10 days, purging fresh gas mix every day. [364] For plates that exhibited chemoautotrophic growth/colonies, the colonies were picked and then streaked onto fresh minimal salts medium (MSM) + agarose (1.5%) plates followed by a second incubation in the Almore’s Vacu-Quick jar system supplied with H₂ and CO2 and air (70/10/20). Strains the exhibiting strong colony growth in this second incubation were then subjected to chemoautotrophic testing in liquid mineral salts medium (MSM). [365] Experiments were performed in (Chemglass CLS-4209-10, anaerobic, 18 x 150 mm) Hungate tubes with working volume of 5 mL, capped with solid neoprene rubber stoppers (Wheaton Science Products, No.:224100331), crimped with an aluminum cap. Tubes were purged with a gas mix of H₂:CO₂:Air (70/10/20) using a gas manifold designed for high throughput screening. Tubes were purged with fresh gas mix every day. [366] Tubes were incubated in a Multitron Pro Infors HT shaker at a 45º angle, at 600 rpm and 30ºC for 96 hrs. Optical density at 600 nm was measured by spectrophotometer (Genesys 10S, UV-Vis spectrophotometer, Thermo Scientific) every 24 hours. [367] The following bacterial strains were identified as being chemoautotrophic on the knallgas mix: Arthrobacter methylotrophus DSM 14008; Rhodococcus opacus DSM 44304; Rhodococcus opacus DSM 44311; Xanthobacter autotrophicus DSM 431; Rhodococcus opacus DSM 44236; Rhodococcus ruber DSM 43338; Rhodococcus opacus DSM 44315; Cupriavidus metallidurans DSM 2839; Rhodococcus aetherivorans DSM 44752; Gordonia desulfuricans DSM 44462; Gordonia polyisoprenivorans DSM 44266; Gordonia polyisoprenivorans DSM 44439; Gordonia rubripertincta DSM 46039; Rhodococcus percolatus DSM 44240; Rhodococcus opacus DSM 43206; Gordonia hydrophobica DSM 44015; Rhodococcus zopfii DSM 44189; Gordonia westfalica DSM 44215, Xanthobacter autotrophicus DSM 1618; Xanthobacter autotrophicus DSM 2267; Xanthobacter autotrophicus DSM 3874; Streptomycetes coelicoflavus DSM 41471; Streptomycetes griseus DSM 40236; Streptomycetes sp. DSM 40434; Streptomycetes xanthochromogenes DSM 40111; Streptomycetes thermocarboxydus DSM 44293; Rhodobacter sphaeroides DSM 158. [368] Full proximate analysis was performed on knallgas strains grown in liquid MSM media with a knallgas mixture as the sole carbon and energy source. Both C. necator DSM 531 and DSM 541 were observed to synthesize vitamins, including vitamin B1, vitamin B2, and vitamin B12. [369] Although the foregoing invention has been described in some detail by way of illustration and examples for purposes of clarity of understanding, it will be apparent to those skilled in the art that certain changes and modifications may be practiced without departing from the spirit and scope of the invention. Therefore, the description should not be construed as limiting the scope of the invention, which is delineated in the appended claims. [370] All publications, patents, and patent applications cited herein are hereby incorporated by reference in their entireties for all purposes and to the same extent as if each individual publication, patent, or patent application were specifically and individually indicated to be so incorporated by reference. References 1. J. E. Bailey and D. F. Ollis. Biochemical Engineering Fundamentals. Chemical engineering. McGraw-Hill, 1986. 2. L. Bongers. Energy generation and utilization in hydrogen bacteria. Journal of bacteriology, 104(1):145–151, October 1970. 3. G. L. Drake, C. D. King, W. A. Johnson, and E. A. Zuraw. Study of life support systems for space missions exceeding one year in duration. Technical Report SP-134, NASA, April 1966. 4. Curt R. Fischer, Daniel Klein-Marcuschamer, and Gregory Stephanopoulos. Selection and optimization of microbial hosts for biofuels production. Metabolic Engineering, 10(6):295–304, November 2008. 5. Michele R. Hamester, Palova S. Balzer, and Daniela Becker. Characterization of calcium carbonate obtained from oyster and mussel shells and incorporation in polypropylene. Materials Research, 15:204–208, 2012. 6. R. Heise, V. Müller, and G. Gottschalk. Sodium dependence of acetate formation by the acetogenic bacterium acetobacterium woodii. Journal of Bacteriology, 171(10):5473– 5478, October 1989. 7. Michael Hügler, Carl O. Wirsen, Georg Fuchs, Craig D. Taylor, and Stefan M. Sievert. Evidence for autotrophic CO2 fixation via the reductive tricarboxylic acid cycle by members of the ε subdivision of proteobacteria. Journal of Bacteriology, 187(9):3020– 3027, May 2005. 8. J. K. Kristjansson. Thermophilic Bacteria. Taylor & Francis, 1992. 9. Sang Y. Lee, Jin H. Park, Seh H. Jang, Lars K. Nielsen, Jaehyun Kim, and Kwang S. Jung. Fermentative butanol production by clostridia. Biotechnol. Bioeng., 101(2):209–228, October 2008. 10. J. Lengeler, G. Drews, and H. Schlegel. Biology of the Prokaryotes. Wiley, 2009. 11. L. G. Ljungdahl. The autotrophic pathway of acetate synthesis in acetogenic bacteria. Annual Review of Microbiology, 40(1):415–450, 1986. 12. Akane Miura, Masafumi Kameya, Hiroyuki Arai, Masaharu Ishii, and Yasuo Igarashi. A soluble NADH-dependent fumarate reductase in the reductive tricarboxylic acid cycle of hydrogenobacter thermophilus TK-6. Journal of bacteriology, 190(21):7170–7177, November 2008. 13. Eleftherios T. Papoutsakis. Equations and calculations for fermentations of butyric acid bacteria. Biotechnol. Bioeng., 26(2):174–187, February 1984. 14. Kathleen M. Scott and Colleen M. Cavanaugh. CO2 uptake and fixation by endosymbiotic chemoautotrophs from the bivalve solemya velum. Applied and Environmental Microbiology, 73(4):1174–1179, February 2007. 15. J. M. Shively, G. van Keulen, and W. G. Meijer. Something from almost nothing: carbon dioxide fixation in chemoautotrophs. Annual review of microbiology, 52:191–230, 1998. 16. Arnold J. Smith, Jack London, and Roger Y. Stanier. Biochemical basis of obligate autotrophy in Blue-Green algae and thiobacilli. Journal of Bacteriology, 94(4):972–983, October 1967. 17. F. B. Taub, F. E. Palmer, R. E. Condrey, R. B. Kern, K. A. Ballard, and D. F. Kalamasz. Algal culture as aquaculture feed. Research in fisheries, 1973. 18. Frieda B. Taub. Closed ecological systems. Annual Review of Ecology and Systematics, 5:139–160, 1974. 19. Rudolf K. Thauer, Anne-Kristin Kaster, Henning Seedorf, Wolfgang Buckel, and Reiner Hedderich. Methanogenic archaea: ecologically relevant differences in energy conservation. Nature Reviews Microbiology, 6(8):579–591, June 2008. 20. Gil-Lim Yoon, Byung-Tak Kim, Baeck-Oon Kim, and Sang-Hun Han. Chemical– mechanical characteristics of crushed oyster-shell. Waste Management, 23(9):825–834, January 2003. 21. Hyunsuk Yoon, Sangkyu Park, Kiho Lee, and Junboum Park. Oyster shell as substitute for aggregate in mortar. Waste Management & Research, 22(3):158–170, June 2004. 22. Closed Ecological Systems Annual Review of Ecology and Systematics, Vol.5 (1974), pp.139-160 by Frieda B. Taub, and G. L. Drake, C. D. King, W. A. Johnson, and E. A. Zuraw, "Study of life support systems for space missions exceeding one year in duration," NASA, Tech. Rep. SP-134, Apr.1966 23. Jakob Kristjansson Chapter 5, Section III of Thermophilic Bacteria , CRC Press, 1992, 24. White, J.J., Cain, N., French C.E. (2019) Production of insoluble starch-like granules in Escherichia coli by modification of the glycogen synthesis pathway bioRxiv841023; https://doi.org/10.1101/841023 25. Wang, X., Luo, H., Wang, Y., Wang, Y., Tu, T., Qin, X., Su, X., Huang, H., Bai, Y., Yao, B., Zhang, J. (2022) Direct conversion of carbon dioxide to glucose using metabolically engineered Cupriavidus necator. Biores Tech, 362: 127806, ISSN 0960-8524, 26. https://doi.org/10.1016/j.biortech.2022.127806. 27. Smith A.1999. Making starch. Current Opinion in Plant Biology 2:223-229. 28. Smith A.2001. 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Claims

CLAIMS We claim: 1. A biological and chemical method for the capture and conversion of an inorganic and/or organic molecules containing only one carbon atom, into organic molecules containing two or more carbon atoms produced through anabolic biosynthesis comprising: introducing inorganic and/or organic molecules containing only one carbon atom, into an environment suitable for maintaining chemoautotrophic microorganisms; introducing a gaseous substrate into an environment suitable for maintaining chemoautotrophic microorganisms; wherein the inorganic and/or organic molecules containing only one carbon atom are used as a carbon source by the microorganism for growth and/or biosynthesis; converting the inorganic and/or organic molecules containing only one carbon atom into the organic molecule products containing two or more carbon atoms within the environment via at least one chemosynthetic carbon-fixing reaction and at least one anabolic biosynthetic pathway contained within the chemoautotrophic microorganisms; wherein the chemosynthetic fixing reaction and anabolic biosynthetic pathway are at least partially driven by chemical and/or electrochemical energy provided by electron donors and electron acceptors that have been generated chemically and/or electrochemically and/or thermochemically and/or are introduced into the environment from at least one source external to the environment.

2. The method according to claim 1, wherein said microorganism is a bacterial cell.

3. The method according to claim 1, wherein said gaseous substrate comprises CO₂ as a carbon source.

4. The method according to claim 1, wherein said gaseous substrate comprises H2 and/or O2 as an energy source.

5. The method according to claim 1, wherein said gaseous substrate comprises pyrolysis gas or producer gas or syngas.

6. The method according to claim 1, wherein said gaseous substrate comprises a mixture of gases, comprising H2 and/or CO2 and/or CO.

7. The method according to claim 1, wherein said microorganism produces glucose and/or other sugars and/or starch and/or polysaccharides and/or vitamins and/or biomass when cultured in the presence of the gas substrate under conditions suitable for growth of the microorganism and production of bioproducts.

8. The method according to claim 1 or 7, wherein said microorganism is a Cupriavidus sp. or Ralstonia sp. or Xanthobacter sp.

9. The method according to claim 1 or 7, wherein said microorganism is Cupriavidus necator or Xanthobacter autotrophicus.

10. The method according to claim 1 or 7, wherein said microorganisms and/or nutrients produced by said microorganisms are used to feed or provide nutrition to one or more other organisms.

11. The method according to claim 1 or 7, wherein said microorganisms are knallgas microorganisms.

12. The method according to claim 11, wherein said gaseous substrate comprises H2 and/or CO2.

13. The method according to claim 11, wherein said gaseous substrate is pyrolysis gas or producer gas or syngas.

14. The method according to claim 1 or , wherein glucose and/or other sugars and/or starch and/or polysaccharides and/or and/or vitamins and/or biomass is recovered from the culture medium.

15. The method according to claim 1 or 7, wherein the microorganisms include microorganisms selected from one or more of the following genera: Cupriavidus sp., Rhodococcus sp., Hydrogenovibrio sp., Rhodopseudomonas sp., Hydrogenobacter sp., Gordonia sp., Arthrobacter sp., Streptomycetes sp. Rhodobacter sp., and/or Xanthobacter sp..

16. The method according to claim 1 or 7, wherein said electron acceptors comprise one or more of the following: carbon dioxide; oxygen; nitrites; nitrates; ferric iron or other transition metal ions; sulfates; or valence or conduction band holes in solid state electrode materials.

17. The method according to claim 1 or 7, wherein said electron donors and/or electron acceptors are generated or recycled using renewable, alternative, or conventional sources of power that are low in greenhouse gas emissions, and wherein said sources of power are selected from at least one of photovoltaics, solar thermal, wind power, hydroelectric, nuclear, geothermal, enhanced geothermal, ocean thermal, ocean wave power, and tidal power.

18. The method according to claim 1, wherein the organic chemical product includes compounds with carbon backbones that are five carbons or longer including glucose and/or other sugars.

19. The method according to claim 1 or 7, wherein molecular hydrogen acts as an electron donor and is generated via a method using at least one of the following: electrolysis of water; thermochemical splitting of water; electrolysis of brine; electrolysis and/or thermochemical splitting of hydrogen sulfide.

20. The method according to claim 26, wherein electrolysis of water for the production of hydrogen is performed using one or more of the following: Proton Exchange Membranes (PEM), liquid electrolytes such as KOH, alkaline electrolysis, Solid Polymer Electrolyte electrolysis, high-pressure electrolysis, high temperature electrolysis of steam (HTES).

21. A method for producing glucose and/or other sugars and/or starch and/or polysaccharides and/or and/or vitamins and/or biomass, comprising culturing a microorganism according to claim 1 in a bioreactor that comprises a gaseous substrate and a culture medium that comprises other nutrients for growth and bioproduct production, under conditions that are suitable for growth of the microorganism and production of glucose and/or other sugars and/or starch and/or polysaccharides and/or and/or vitamins and/or biomass, wherein said microorganism produces glucose and/or other sugars and/or starch and/or polysaccharides and/or and/or vitamins and/or biomass.

22. The method according to claim 1, wherein at least one chemosynthetic reaction and at least one anabolic biosynthetic pathway results in the formation of biochemicals including at least one of: glucose; other sugars; starch; polysaccharides; and/or vitamins.

23. The method according to claim 1, wherein biomass and/or biochemicals are produced through the said at least one chemosynthetic reaction, and wherein the biomass and/or biochemicals have application as at least one of the following: as an organic carbon and/or nitrogen source for fermentations; as a nutrient source for the growth of other microbes or organisms; as a nutrient source or food ingredient for humans; as a feed for animals; as a raw material or chemical intermediate for manufacturing or chemical processes; as sources of pharmaceutical, medicinal or nutritional substances; as a fertilizer; as soil additives; and/or as soil stabilizers.

24. The method according to claim 23, wherein the said carbon and/or nitrogen source from the said chemosynthetic reaction is used in a fermentation to produce biochemicals including least one of: commercial enzymes, antibiotics, amino acids, protein, food, food ingredients; vitamins, lipids, bioplastics, polysaccharides, neutraceuticals, pharmaceuticals.

25. The method according to claim 23, wherein said feed for animals is used to feed one or more of: cattle, sheep, chickens, pigs, fish, shellfish, insects, invertebrates, and coral.

26. A method according to claim 1, 7, 21, or 22 for production of a carbohydrate by a chemoautotrophic organism engineered to produce the carbohydrate in an oxyhydrogen process wherein the microorganism converts gaseous CO₂ and/or gaseous H₂ and/or syngas into glucose.

27. The engineered microorganism of claim 26, wherein the microorganism is a hydrogen- oxidizing chemoautotroph.

28. The engineered chemoautotroph of claim 26 is Cupriavidus necator DSM 531 or DSM 541.

29. The engineered chemoautotroph of claim 26 produces and/or secretes glucose in a quantity that is 10% or more of the dry cell mass.

30. A method for metabolic engineering of the host microorganism of claim 1, 7, or 26 to promote carbon flux from fixed CO2 to create an intracellular pool of glucose that includes deletion of metabolic pathways competing for carbon with glucose, and addition of heterologous enzymes for directing carbon to glucose.

31. The method of claim 30 wherein deletion of the glucose kinase gene glk from the C necator genome is performed to prevent phosphorylation of glucose.

32. The method of claim 30 wherein deletion of the EntnerDoudoroff pathway genes zwf1, zwf2, zwf3 from the C necator genome is performed to prevent glucose phosphate metabolism to pyruvate and to increase carbon flux to glucose.

33. The method of claim 30 wherein deletion of the polyhydroxybutyrate synthetic operon pha is performed to prevent carbon diversion to PHB.

34. The method of claim 30 wherein heterologous expression of HAD1 phosphatase is performed to catalyze the dephosphorylation of glucose-6-phosphate and glucose-1- phosphate to produce glucose.

35. The method of claim 30 wherein incorporation of a glucose facilitator gene , glf, is performed to enable glucose secretion to the medium.

36. A method for metabolic engineering of the host microorganism of claim 1, 7, or 26 wherein the microorganism converts gaseous CO₂ and gaseous H₂ and/or syngas into starch.

37. The engineered microorganism of claim 36, wherein the microorganism is a hydrogen- oxidizing chemoautotroph.

38. The engineered chemoautotroph of claim 37 is Cupriavidus necator DSM 541 or Xanthobacter autotrophicus.

39. The engineered chemoautotroph of claim 37 produces starch in a quantity that is 10% or more of the dry cell mass.

40. The method of claim 36 for metabolic engineering of the host microorganism to promote carbon flux from fixed CO2 to create an intracellular pool of glucose-1-phosphate to supply a heterologous starch pathway that includes deletion of metabolic pathways competing for carbon with glucose-1-phosphate, and addition of heterologous enzymes for directing carbon to starch.

41. The method of claim 40 wherein deletion of glucose-6-phosphatase is performed to prevent glucose synthesis from glucose-6-phosphate.

42. The method of claim 40 wherein deletion of three copies of genes for glucose-6- phosphate dehydrogenase (zwf 1,2,3) is performed to prevent carbon flux from glucose-6- phosphate to gluconolactone-6-phosphate.

43. The method of claim 40 wherein deletion of the polyhydroxyalkanoate pathway promoter, phaD is performed to prevent carbon flux to the storage polymer polyhydroxybutyrate (PHB).

44. The method of claim 40 wherein overexpression of phosphoglucomutase maintains a pool of glucose-1-phosphate.

45. The method of claim 40 wherein a heterologous pathway from glucose-1-phosphate to starch is constructed to produce a pool of ADP-glucose by heterologous expression of gene glgC of glucose-1-phosphate adenylyltransferase.

46. The method of claim 40 wherein the starch pathway is completed with heterologous expression of ADP glucose starch synthase, glgA.

47. The method claim 36 or 40 for metabolic engineering of the host microorganism to promote carbon flux from endogenous UDP glucose to starch.

48. The method of claim 47 wherein heterologous expression of UDP glucose starch synthase completes a starch pathway from the C necator native UDP glucose pathway with insertion of UDP glucose starch synthase derived from Thermoanaerobacter tengcongensis 49. The method of claim 36, 40, or 47 wherein endogenous 1,4-alpha-glucan branching enzyme is deleted to limit chain branching. 50 A method for claim 1, 7, or 26 for increasing carbon flux from fixed CO2 to glucose or starch that overexpresses one or more of the native, rate-limiting enzymes of gluconeogenesis. 51. A method for claim 50 wherein those enzymes are fructose-bisphosphate aldolase, fructose-1,6-bisphosphatase and glucose-6-phosphate isomerase 52. A method for claim 50 wherein those enzymes include pyruvate carboxylase (PC), phosphoenolpyruvate carboxykinase (PEPCK; pck genes), fructose-1,6-bisphosphatase (FBPase; fpb gene), and glucose-6-phosphatase (G6Pase; G6pc genes)