WO2017031624A1 - Cracking process for producing light oil and fuel gas from coal slime - Google Patents

Abstract

A cracking process for producing light oil and fuel gas from coal slime comprises: blending coal slime to obtain a coal slime solution; culturing flora, mixing a thickened and acidified coal slime solution with the flora to obtain a mixture, and then fermenting the mixture to obtain carbon phagocytizing bacteria; decomposing water in the presence of catalytic ions to obtain a hydrogen component; cleaving a carbon bond in a carbon group in the presence of super-strong ammonium ion NH₄ ⁺*4; then mixing the hydrogen component with the broken carbon bond, and carrying out primary reaction while stirring to obtain a mixed oil product; and then carrying out second hydrogen component generation, second carbon bond cleavage, second carbon hydrogen combination reaction, and second carbon hydrogen ionization reaction to obtain light oil and fuel gas. The coal slime can be reasonably utilized and converted into fuel, and the conversion ratio can reach up to 95%.

Description

Slime production of light oil, gas cracking process Technical field

The invention relates to a coal slurry producing light oil and gas cracking process, belonging to the technical field of chemical and bio-energy.

Background technique

What is not destroyed in the universe is carbon, which is filled with hydrogen, and the atomic number of carbon is 6, the atomic weight is 12.01115; the atomic number of hydrogen is 1, and the atomic weight is 1.00797; thus, the difference between the two is large, but Nature has created both of them into a multitude of materials. This is also a puzzling thing for human beings for tens of thousands of years. The essence of carbon is an emitter and an absorber. Just because carbon is an absorber, carbon is immortal.

At present, hydrocarbons are manufactured by nature machinery, and human activities that can be grasped and known after occurrence are also unknown. This is why the production of so many residues is made. In the prior art, carbon dioxide is recovered to produce methanol. The process of coking water gas can be mastered; the carbon dioxide can be recovered by using lead, zinc or copper as the catalyst. The lead, zinc or copper base is obtained by thermal decomposition of sulfide ore. It is chemically feasible to decompose carbon. Another method of producing hydrocarbons is to obtain hydrocarbons by alcoholization using an aqueous solution of carbonic acid produced by carbon itself in water. In summary, hydrocarbons must first be completed by means of less carbon, that is, the carbon bonds are shortened. In the prior art, super acid (fluorinated acid) can decompose carbon bonds, but can not control the subsequent process, nature can use natural process combination, then in theory can also be artificially synthesized; first from carbon carbon extinction research, After being absorbed by organic plants, the carbon dioxide in the atmosphere is synthesized into the energy required for plant growth through the temperature difference in the organic plants. In addition, the algae in the water grows through carbon, which shows that carbon can be decomposed at low and medium temperatures. This is extremely consistent with the decomposition conditions of carbon in the negative pressure and zero absorption (energy).

At present, all production and life are inseparable from fuel, which also leads to fuel imbalance, and the use of fuel needs to be safe, manageable, maneuverable, large-scale, low-priced, and the natural world is filled with fuel materials. The key lies in the use of means and cognition, but from the analysis of hydrocarbons, hydrogen is ubiquitous throughout the Earth's atmosphere, and it is inexhaustible; while carbon is always produced, hydrogen can be taken from the air. , water, etc.; and carbon can be natural carbon, which can come from pollution recovery.

Coal slime is a kind of pollution recovery material, which is the material obtained after the sewage generated by coal washing in the coal washing plant is recovered. In China, there are tens of thousands of coal washing yards. These coal washing yards produce millions of tons of coal every day. Coal slime is a source of pollution and therefore needs to be solved. According to statistics, at present, there are hundreds of millions of tons of untreated coal slime in China. The direction of slime regeneration is limited to coal-dried stone materials mixed with coal slurry to produce fuel for low-calorie coal-fired power generation boilers, but due to process, cost and efficiency. Wait The problem has led to limited development; in addition, in backward areas, residents mix coal briquettes for small daily life, although they can be used in small amounts in open areas, but they may cause poisoning in densely populated areas.

Therefore, it is an urgent problem to be solved in the art to explore a reasonable utilization mode of coal slime.

Summary of the invention

In order to solve the above technical problems, an object of the present invention is to provide a process for producing light oil and gas cracking of coal slime.

In order to achieve the above object, the present invention provides a coal slurry producing light oil and gas cracking process, the process comprising the steps of: adjusting the slime liquid to obtain a slime solution, and then thickening and acidifying the slime solution. , obtaining a thickened and acidified coal slime solution;

Bacterial culture: the root mold is mixed with the yeast, and then mixed into the plant culture material for cultivation to obtain a flora;

Mixing: mixing the thickened and acidified slime solution with the flora to obtain a mixture;

Fermentation: fermenting the mixture obtained after mixing to obtain a carbonaceous bacterium which separates the carbon group from the carbon support;

The first hydrogen component formation: under the action of catalytic ions, the water is decomposed to obtain a hydrogen component;

First carbon bond cleavage: under the action of super ammonium ion NH ₄ ⁺ × 4, the carbon bond in the carbon group is cut off; preferably, the carbon bond in the carbon group is cut off at 150-200 ° C;

The first carbonation reaction: mixing the hydrogen component obtained by the first hydrogen component formation reaction with the carbon bond which is cleaved after the first carbon bond cleavage, and undergoing a hydrocarbon reaction under stirring to obtain a crude oil Product

The first hydrocarbon ionization reaction: the hydrocarbon product is subjected to hydrocarbon ionization reaction to obtain a mixed oil product;

The second hydrogen component formation: under the action of catalytic ions, the water is decomposed to obtain a hydrogen component; preferably, the water is decomposed at a temperature of 700 ° C or higher;

The second carbon bond cleavage: under the action of the super-strong ammonium ion NH ₄ ⁺ × 4, the carbon bond in the mixed oil product is cut off; preferably, the carbon bond in the mixed oil product is cut off at 150-200 ° C;

a second hydrocarbon reaction: mixing the hydrogen component obtained by the second hydrogen component formation reaction with a carbon bond which is cleaved after the second carbon bond cleavage, and undergoing a hydrocarbonation reaction under stirring;

The second hydrocarbon ionization reaction: the product obtained by the second hydrocarbon reaction is subjected to hydrocarbon ionization reaction to obtain the light oil and gas.

According to the process of the present invention, preferably, the slime has a particle size of from 250 to 350 mesh.

According to the process of the present invention, preferably, the slime needs to be pretreated before being subjected to the conditioning liquid state, and the purpose of the pretreatment is to remove various impurities mixed in the slime due to open stacking, Protect the smooth operation of the equipment. The pre-processing process is a conventional technical means in the field, and those skilled in the art can perform on-site operations. To select a suitable pretreatment method, for example, it can be screened by a net according to the size of the coal particles.

According to the process of the present invention, preferably, the conditioned liquid state comprises the steps of: mixing the slime with a tempering liquid to obtain a slime solution;

More preferably, the mass ratio of the slime to the solution is 1:1;

The conditioned solution includes an aqueous solution or seawater containing chloride ions, sodium ions, sulfur ions, magnesium ions, calcium ions, potassium ions, hydrogencarbonate ions, bromide ions, strontium ions, boron ions, and fluoride ions;

The pH of the mixed solution is 7.9-8.1.

According to the process of the present invention, preferably, after the slime solution is thickened, the particle size of the slime particles is 2-4 microns.

According to the process of the present invention, the thickening is a conventional technical means in the art, and those skilled in the art can select a suitable thickening method according to the requirements of the field operation. In a preferred embodiment of the present invention, a scissor high-speed grinding can be used. The machine refines the slime particles to 2-4 microns, and the state change after grinding causes the flowable liquid to be converted into a non-flowable poly-thick state, and the purpose of thickening is to facilitate phagocytosis.

Coal is a high-emission absorber and a high-emission body. The formation of carbon needs to absorb magnetic energy (thermal energy), that is, quantum magnetism. It is necessary to refine the force (pressure), and the force (pressure) must generate heat, so it needs to be external. It is resistant to thermal substances. The seawater is alkaline and has an endothermic effect. Under the resistance of the alkali, the carbon is not heated.

According to the process of the present invention, preferably, the acidifying comprises the steps of adding oxalic acid to the thickened slime solution and adjusting the pH of the slime solution to 3.5-3.8.

The pH of the thickened slime is 7.9-8.1. The slime is essentially a vegetable carrier. The carrier is covered with pores. After high-speed grinding, the coal will fill the pores of the halogen in the seawater. The mud is not watery, but this does not meet the conditions for the survival of the cells, so it is necessary to lower the pH of the halogen. The lignin polymerization polymer in the slime is organic, and the pH value of the halogen is relatively lower than that required to use the same property. The oxalic acid, that is, the neutral acid, is the same as the lignin polymerization polymer in the acid. Other acids will cause damage to the lignin polymerization polymer. Therefore, in a preferred embodiment of the present invention, the oxalic acid is used as a neutralizing agent to adjust the slime to a pH environment (pH 3.5-3.8) suitable for the survival of the cells as a nutrient for the cells.

According to the process of the present invention, preferably, the microbial culture comprises the steps of: mixing the Rhizopus and the yeast, mixing it into the plant culture material for cultivation, and obtaining the bacterial source; and mixing the bacterial source into the cooked rice. Stabilize the bacteria, mature, and then add brown sugar water to expand the strong bacteria;

More preferably, the total weight of the mixture of Rhizopus and yeast is 100%, the mass fraction of the Rhizopus is 60%-99%, and the mass fraction of the yeast is 1%-40%;

More preferably, the mass ratio of the mixture of the Rhizopus and the yeast to the plant culture material is 1:3;

More preferably, the method for preparing the plant culture material comprises the steps of: mixing the plant with water and then grinding it into a plant slurry to obtain the plant culture material;

Further preferably, the plant to water mass ratio is 2:1;

The plant comprises a combination of a plant of the genus Polygonaceae, a mulberry leaf, an almond leaf, a Chuanxiong, a white peony, an pineapple, an orange leaf, a large green cinnamon and a fragrant licorice leaf;

The slurry has a particle size of 120-160 mesh;

The mass ratio of the plant, the mulberry leaf, the almond leaf, the Chuanxiong, the white peony, the pineapple, the orange leaf, the big green cinnamon and the fragrant eucalyptus leaves is 1:1:1:1:1:1:1:1:1 ;

More preferably, the culture temperature of the bacterial source is 30-36 ° C, the relative humidity is 80% or more, and the ratio (the ratio is Rhizopus, the yeast accounts for the mass percentage of the plant culture material) is 20%-25%;

More preferably, the mass ratio of the bacterial source to the cooked rice is 10:100-15:100;

More preferably, the time for the stationary culture is 10-14 days;

More preferably, the mass ratio of the brown sugar water to the bacterial source is 15:100;

Further preferably, the brown sugar water is brown sugar water having a mass ratio of brown sugar to water of 1:50 to 1:100.

According to the process of the present invention, the koji is a mixture of Rhizopus koji or Rhizopus koji and yeast, and the Rhizopus koji is the main component of the mixture of Rhizopus koji and yeast, accounting for the total mixture. 60-99% of the quality. The Rhizopus koji can be commercially available, such as: a commercial koji produced by Angel Yeast under the trade name Angeline koji (SAP material number: 84000084); or it can be purchased through commercial channels. Rhizopus species are inoculated into a suitable medium and cultured, and commercially purchased Rhizopus, such as: commercially available Rhizopus Q303, Rhizopus 3.668 of Chengdu Institute of Biology, Chinese Academy of Sciences. The medium of Rhizopus can be selected as a medium, especially a rice medium, a wheat flour medium, a bran medium, or the like. The yeast may be commercially available yeast for koji, including: brewer's yeast (eg, brewer's yeast K), Hansenula, Candida, ascospores, genus, and spores 1308 Saccharomyces Cerevisiae, Chengdu Institute of Biology, Chinese Academy of Sciences.

Rhizopus and yeast can be separately cultured and then mixed, for example:

(1) Preparation of Rhizopus koji: Take rice medium (2 kg of cooked rice and 6 L of water). After sterilization and cooling, the root mold 3.866 which accounts for 1% of dry weight of rice is inoculated into rice medium and cultured at 28-30 ° C for 30 h. Left and right, get the root mold koji;

(2) Yeast culture: take the concentration of 13 ° B × wort, take sulfuric acid to adjust the pH value to 4.1-4.5, sterilize and cool, inoculate 2% inoculation amount of S. cerevisiae K at 28-30 ° C for 20-24 h, Removing the medium to obtain a yeast;

(3) Mixing Rhizopus koji and yeast to obtain koji, in which Rhizopus koji accounts for 60-99% of the total mass of koji.

The culture of Rhizopus koji and yeast can also be carried out by means of mixed culture.

According to the process of the present invention, the bacteria source is mixed with the cooked rice to be sterilized, and after ripening, brown sugar is added. In the process of expanding the strong flora, the temperature is controlled to 30-36 °C.

According to the process of the present invention, the Rhizopus used in the present invention is biologically classified into a single-celled microorganism of the genus Algae, Mucor, Mucor, and Rhizopus.

According to the process of the present invention, the plant is herbaceous, mulberry is woody, and the almond leaf is apricot leaf. The above substances all contain oxalic acid, which has an inhibitory effect on general pathogenic bacteria. The mulberry is the mulberry leaf, and the genus Polygonaceae can be used as the whole plant, the orange is the leaf, the big green laurel is the skin, and the citron is the branch.

According to the process of the present invention, preferably, the mixing is to mix the thickened, acidified slime solution and the flora obtained by the culture of the flora;

More preferably, the mass ratio of the flora obtained by the bacterial culture to the thickened and acidified slime solution is 100:12.2.

According to the process of the present invention, preferably, the fermentation is carried out according to the following steps: fermenting the mixture obtained after mixing to obtain a carbonaceous bacterium;

More preferably, the fermentation temperature is 20-36 ° C, the humidity is 100%, and the fermentation time is 21-90 days.

According to the process of the present invention, the above fermentation needs to be allowed to stand at a temperature of 20-36 ° C and a humidity of 100% for the bacterial population to be 21-90 days, and the flora is adapted to the transition period within 7 days, after 15 The natural flora of the group turned into a carbonaceous bacterium; in 7 days, the quality of reproduction was repeated every 15 minutes, and on the 7th day, there were 672 generations of metamorphic varieties (every 15 minutes of reproductive quality change, the daily qualitative change was 96 generations, the 7th day was 672 generations), a suitable carbonaceous bacterium capable of separating a carbon group from a carbon carrier.

According to the process of the present invention, preferably, the catalytic ions in the first hydrogen component generating step include ions generated by the sulfide ore being heated at 370 ° C;

More preferably, the catalytic ion is a zinc ion or a copper ion.

According to the process of the present invention, preferably, the water is decomposed at a temperature of 700 ° C or higher in the first hydrogen component forming step.

According to the process of the present invention, preferably, the method for preparing the super-strong ammonium ion NH ₄ ⁺ × 4 in the first carbon bond cleavage step comprises the following steps: at 900-1000 ° C, water is catalyzed by ions The reaction occurs under the action to obtain NH ₄ ⁺ × 4;

More preferably, the catalytic ion is an ion generated by the sulphide ore being heated at 370 ° C;

Further preferred is zinc ion or copper ion.

According to the process of the present invention, the nitrogen required for the preparation of the super-strong ammonium ion NH ₄ ⁺ × 4 is derived from nitrogen in the air and a small amount of nitrogen dissolved in water.

According to the process of the present invention, preferably, the carbon bond in the carbon group in the first carbon bond cleavage step is 150-200 ° C was cut off.

According to the process of the present invention, the above-mentioned super-strong ammonium ion NH ₄ ⁺ × 4 is prepared by compressing ammonium ions by 4 times, and the present invention does not limit the apparatus for preparing super-strong ammonium ions, but only the preparation method thereof. And the reaction conditions are limited: that is, at 900-1000 ° C, water is prepared under the action of catalytic ions (ions produced by the heat of sulfide ore at 370 ° C).

The super-ammonium ion NH ₄ ⁺ × 4 used in the preferred embodiment of the invention is a vapor which is made into steam and then catalyzed by ions (the sulfide ore is heated at 370 ° C, preferably zinc ion or copper). Under the action of ions, the water in the vapor state is decomposed to obtain a hydrogen component and an oxygen component, and the oxygen component is separated to leave a hydrogen component; the obtained hydrogen component is further neutralized with nitrogen (derived from nitrogen and water in the air). The reaction was carried out with a small amount of nitrogen to obtain the above-mentioned super ammonium ion NH ₄ ⁺ × 4.

According to the process of the present invention, preferably, the first hydrocarbon reaction specifically comprises the steps of: hydrogenating the hydrogen component formed by the first hydrogen component from the carbon after being fractured by the first carbon bond in a water bath The bond is mixed, stirred at a speed of 10,000 rpm, and a hydrocarbon reaction occurs to obtain a crude product;

More preferably, the mass ratio of hydrogen to carbon is 1:1.6;

More preferably, the temperature of the hydrocarbon reaction is 70 to 80 ° C, and the reaction time is 10 minutes.

According to the process of the present invention, in the first carbonation reaction process, the high-speed stirring of the reaction system at a rate of 10,000 rpm produces a throwing force, a pressure, a polymerization force, which in turn facilitates hydrocarbon hydrogenation. The reaction proceeds.

According to the process of the present invention, the crude oil product is in a blue-black liquid state, and contains hydrocarbons, organic substances, decays, multi-element polymer, high molecular polymer, lignin, oxide, hydride, carbide. Wait.

According to the process of the present invention, the hydrocarbon ionization reaction is a light oil cracking reaction, which is a technical means well known in the art, and the skilled person can perform the ionization reaction of the hydrocarbon according to the field operation requirements. The reaction parameters are selected and adjusted.

In a preferred embodiment of the invention, the first hydrocarbon ionization reaction is carried out in two stages: first at 120 ° C, then the temperature is raised to 130-140 ° C, the reaction is continued, preferably the reaction time of each reaction is It is 10 minutes.

According to the process of the present invention, preferably, after the first hydrocarbon ionization reaction, a fractionation operation is required, and after the fractionation operation, a mixed oil product is obtained.

According to the process of the present invention, preferably, the catalytic ions in the second hydrogen component generating step include ions generated by the sulfide ore being heated at 370 ° C;

More preferably, the catalytic ion is a zinc ion or a copper ion.

According to the process of the present invention, preferably, the water is decomposed at a temperature of 700 ° C or higher in the second hydrogen component forming step.

According to the process of the present invention, preferably, the method for preparing the super-strong ammonium ion NH ₄ ⁺ × 4 in the second carbon bond cleavage step comprises the following steps: at 900-1000 ° C, water is catalyzed by ions Under the action, NH ₄ ⁺ × 4 is obtained;

More preferably, the catalytic ions include ions generated by the sulfide ore being heated at 370 ° C;

Further preferably, the catalytic ion is a zinc ion or a copper ion.

According to the process of the present invention, preferably, the carbon bond in the carbon group in the second carbon bond cleavage step is cleaved at 150 to 200 °C.

According to the process of the present invention, preferably, the second hydrocarbon reaction specifically comprises the steps of: a hydrogen component formed by the second hydrogen component and a carbon which is cleaved after the second carbon bond is broken in a water bath. The bond is mixed and stirred at a speed of 10,000 rpm to cause a hydrocarbon reaction;

More preferably, the mass ratio of hydrogen to carbon is 1:1.6;

More preferably, the temperature of the hydrocarbon reaction is 70 to 80 ° C, and the reaction time is 10 minutes.

According to the process of the present invention, the hydrocarbon ionization reaction is a light oil cracking reaction, which is a technical means well known in the art, and the skilled person can perform the ionization reaction of the hydrocarbon according to the field operation requirements. The reaction parameters are selected and adjusted.

In a preferred embodiment of the present invention, the second hydrocarbon ionization reaction is carried out in three stages: first at 120 ° C, then the temperature is raised to 130-140 ° C to carry out the reaction, and then the temperature is raised to 141-350 ° C. The reaction is continued, and it is preferred that the reaction time of each reaction is 10 minutes.

According to the process of the present invention, preferably, a rectification operation is required after the second hydrocarbon ionization reaction, and the light oil and gas are obtained after the end of the rectification operation.

The process of the invention can rationally utilize and convert the coal slurry into fuel, and the conversion rate is high, and can reach 95%.

DRAWINGS

1 is a flow chart of a process for producing light oil and gas cracking of coal slime according to the present invention;

2 is a gas chromatography mass spectrum of samples A, C, and D in an embodiment of the present invention;

3 and FIG. 4 are gas chromatography mass spectra of sample A in an embodiment of the present invention;

5 and FIG. 6 are gas chromatography mass spectra of sample C in an embodiment of the present invention;

7 and 8 are gas chromatographic mass spectra of sample D in an example of the present invention.

detailed description

In order to better understand the technical features, objects, and advantages of the present invention, the embodiments of the present invention and the advantages thereof will be described in detail by the specific embodiments and the accompanying drawings. The spirit and characteristics of the present invention are understood, but are not intended to limit the scope of the invention.

The coal slurry raw material used in the embodiment of the present invention is the slime discharged from the coal slurry water recovered by the coal washing yard of Hongguo County, Guizhou Province. The diameter of the slime is 250-350 mesh, and the calorific value is 2700 calories (C content). ).

Example 1

The embodiment provides a process for producing light oil and gas cracking of coal slime, and the process comprises the following steps:

(1) Sorting and selecting materials: Pre-treatment of the slime by the net according to the size of the coal particles. The purpose of the pre-treatment is to remove the various impurities mixed in the slime due to open stacking to protect the smooth operation of the equipment. .

(2) Reconciling the liquid: the pre-treated slime and the conditioned liquid (seawater) with a mass ratio of 1:1 are mixed and mixed with a mixer to a liquid state to obtain a slime solution; the pH of the slime solution The value is 8.

(3) Thickening: The slime solution obtained in the step (2) is refined into a 2-4 micron particle size by a scissor high speed grinder.

(4) Acidification: The oxalic acid is added to the thickened slime solution, and the pH of the slime solution after acidification is 3.5-3.8.

(5), bacterial culture: Mix the Rhizopus and yeast, and mix it with the plant culture material (the mass ratio of the mixture of Rhizopus and yeast to the plant culture material is 1:3), the culture temperature is 30 -36 ° C, relative humidity is 80% or more, the ratio is 20% -25%, the source of the bacteria is obtained; and the bacterial source is mixed into the cooked rice (the mass ratio of the bacterial source to the cooked rice is 10:100-15:100) After standing for 10-14 days, after ripening, add brown sugar water with a mass ratio of 15:100 (the brown sugar water is brown sugar water with a mass ratio of brown sugar to water of 1:50-1:100). ) to expand the strong flora;

The total weight of the mixture of Rhizopus and yeast is 100%, the mass fraction of the Rhizopus is 60%-99%, and the mass fraction of the yeast is 1%-40%;

The method for preparing the plant culture material comprises the steps of: mixing the plant with water at a mass ratio of 2:1 and then grinding it into a plant slurry to obtain the plant culture material; the particle size of the plant culture material It is 120-160 mesh; the above plants include medlar, mulberry leaf, almond leaf, Chuanxiong, white peony, pineapple, orange leaf, big green cinnamon and fragrant eucalyptus leaves with a mass ratio of 1:1:1:1: A 1:1:1:1 combination.

(6) Mixing: The thickened and acidified slime solution and the flora obtained by the bacterial culture were mixed at a mass ratio of 12.2:100.

(7) Fermentation: after the thickened and acidified slime solution is mixed with the flora obtained by the bacterial culture, the fermentation is carried out for 21-90 days under the conditions of temperature of 20-36 ° C and humidity of 100%. A carbonaceous bacterium is obtained; the carbonaceous bacterium can separate the carbon group from the carbon support.

(8) The first hydrogen component formation: under the action of zinc ions or copper ions (ions generated by the heat of sulphide ore at 370 ° C), water is decomposed at a temperature of 700 ° C or higher to obtain a hydrogen component. .

(9) The first carbon bond cleavage: under the action of super-strong ammonium ion NH ₄ ⁺ × 4, the carbon bond in the fermented carbon group is cut off at 150-200 ° C;

The preparation method of the super-strong ammonium ion NH ₄ ⁺ × 4 comprises the following steps: under the action of zinc ion or copper ion (ion generated by heating of sulfide ore at 370 ° C) at 900-1000 ° C, NH ₄ ⁺ × 4 was obtained.

(10) First hydrocarbonation reaction: the hydrogen component obtained by the first hydrogen component formation reaction is mixed with the carbon bond which is cleaved after the first carbon bond cleavage in a water bath at a mass ratio of 1:1.6. The mixture was stirred at a rate of 10,000 rpm, and a hydrocarbonation reaction was carried out at 70 to 80 ° C for 10 minutes to obtain a crude product.

(11) First hydrocarbon ionization reaction: the crude oil product obtained by the first hydrocarbon reaction is subjected to hydrocarbon ionization reaction.

The first hydrocarbon ionization reaction was first carried out at 120 ° C for 10 minutes, then the temperature was raised to 130-140 ° C, and the reaction was continued for 10 minutes.

(12) Fractionation: The product obtained by the first hydrocarbon ionization reaction is fractionated to obtain a mixed oil product.

(13), the second hydrogen component formation: under the action of zinc ions or copper ions (the ions generated by the sulphide ore being heated at 370 ° C), the water is decomposed at a temperature of 700 ° C or higher to obtain a hydrogen component. .

(14), the second carbon bond cleavage: under the action of super strong ammonium ion NH ₄ ⁺ × 4, the carbon bond in the mixed oil obtained after fractionation is cut off at 150-200 ° C;

The preparation method of the super-strong ammonium ion NH ₄ ⁺ × 4 comprises the following steps: under the action of zinc ion or copper ion (ion generated by heating of sulfide ore at 370 ° C) at 900-1000 ° C, NH ₄ ⁺ × 4 was obtained.

(15) A second hydrocarbon reaction: mixing a hydrogen component formed by the second hydrogen component with a carbon bond which is cleaved after the second carbon bond is broken in a water bath at a mass ratio of 1:1.6 to 10,000 The mixture was stirred at a speed of rpm, and a hydrocarbon reaction was carried out at 70-80 ° C for 10 minutes.

(16) A second hydrocarbon ionization reaction: the product obtained by the second hydrocarbon reaction is subjected to a hydrocarbon ionization reaction.

The second hydrocarbon ionization reaction was first carried out at 120 ° C for 10 minutes, then the temperature was raised to 130-140 ° C, the reaction was carried out for 10 minutes, and the temperature was raised to 141-350 ° C, and the reaction was continued for 10 minutes.

(17), rectification: after the second hydrocarbon ionization reaction, a rectification operation is required, and the rectification operation comprises the following steps: rectifying the product obtained by the second hydrocarbon ionization reaction to obtain The light oil and gas.

The flow chart of the process for producing light oil and gas cracking of the slime of the invention is shown in FIG. 1 .

The product and product related parameters obtained after fractionation and rectification are shown in Table 1 below:

Table 1 Product and product related parameters obtained after fractionation and rectification

Analysis example

This analysis example provides an analytical test experiment of the hydrocarbon product prepared by the above Example 1, specifically including the following items:

Sample Description: Four samples containing oil slick, emulsion layer and formation, numbered A, B, C, D; samples A and B are respectively prepared for the hydrocarbon product prepared in Example 1 at a temperature below 120 °C. The upper layer and the lower layer distillate obtained by fractional distillation; the samples C and D are the upper layer and the lower layer distillate obtained by fractional distillation of the hydrocarbon product prepared in Example 1 at a temperature above 130 ° C; the analysis experiment is only for oil slick Part of the oil was taken by centrifugation for analysis and analysis. Sample B was rarely analyzed due to little oil slick.

Analytical method:

The content of C and H in the upper oil phase of samples A, C and D was analyzed by ASTM D5291 standard;

The content of S element in the upper oil phase of samples A, C, and D was analyzed by ASTM D5453 standard;

The content of N element in the upper oil phase of samples A, C, and D was analyzed by ASTM D5762 standard;

Analysis of distillation temperature distribution by high temperature GC simulated distillation (ASTM D2887);

The carbon structure characteristics were analyzed by FT-NMR nuclear magnetic resonance spectroscopy: Ca (aromatic carbon), Cp (paraffin carbon), Cn (cycloalkane carbon);

The components in the upper oil phase of samples A, C and D were identified by CC/MSD gas chromatography-mass spectrometry;

The monocyclic, bicyclic and tricyclic aromatic hydrocarbon content (ASTM D6591) was analyzed by HPLC.

The analysis results of the above analysis items are shown in Table 2 - Table 8, wherein the gas chromatographic mass spectra of samples A, C, and D are shown in Figures 2-8;

Table 2 Contents of C, H, S and N in the upper oil phase of samples A, C and D

A C D C, carbon content (wt%) 84.61 86.88 86.63 H, hydrogen content (wt%) 11.37 12.22 12.43

S, sulfur content (wt%) 0.28 0.19 0.17 N, nitrogen content (ppmw) 155 100 110

Table 3 Sample A, C, D distillation temperature distribution data

A C D Initial boiling point (IBP, °C) 224.6 233.8 232.7 5% 271.8 287.4 286.9 10% 292.2 307.3 307.0 20% 313.7 329.6 329.2 30% 328.5 344.1 343.8 40% 340.5 356.5 356.2 50% 352.8 368.1 367.9 60% 366.1 380.5 380.3 70% 383.2 396.7 396.4 80% 410.0 417.3 417.0 90% 434.8 439.4 439.1 95% 449.6 457.7 457.3 Final boiling point (FBP, °C) 503.4 527.7 525.2

Table 4 Contents of aromatic carbon, paraffin carbon and naphthenic carbon in the upper oil phase of samples A, C and D

A C D Ca aromatic carbon, wt% 24.6 17.7 18.4 Cp paraffin carbon, wt% 38.5 44.7 42.9 Cn naphthenic carbon, wt% 36.9 37.6 38.7

Table 5 Contents of aromatic hydrocarbons of monocyclic, bicyclic and tricyclic rings in the upper oil phase of samples A, C and D

A C D Saturated hydrocarbon, wt% - - 68.5 Monocyclic aromatic hydrocarbon, wt% - - 19.3 Bicyclic aromatic hydrocarbons, wt% - - 6.2 Polycyclic aromatic hydrocarbons, wt% - - 6.1 Total aromatic hydrocarbon, wt% - - 31.5

Table 6 Sample A distillation temperature distribution data

Table 7 Sample C distillation temperature distribution data

Table 8 Sample D distillation temperature distribution data

The invention takes 100kg of coal slurry as raw material, and repeats the reaction twice in one hour, each time after reaching temperature (120 ° C) and 130 ° C, once every 10 minutes, feeding 16.67 kg every 10 minutes, each time can be prepared 15.8kg oil. Therefore, the process of the invention can rationally utilize and convert the coal slurry into a fuel, and the conversion rate is high, and can reach 95%.

The invention can convert carbon into energy source in a short time, and the analysis provided by the invention can clearly prove that 100% carbon element in the slime can be obtained by using the process of the invention; as can be seen from the mass spectrum diagrams 2-8, according to the present invention, The process and the carbon bond structure are basically the same, which in turn confirms that the carbon bond truncation process can be achieved by manual means.

In summary, the process of recovering carbon and decomposing carbon by artificial means is feasible. Preliminary statistics show that the annual global carbon emission has reached 10 billion tons. If it is converted into energy equivalent to 10 billion tons of energy, carbon is still carbon in the process of carbon conversion, in order to convert it into energy (hydrocarbon Compounds need to add hydrogen or other various elements, and hydrogen is ubiquitous in the atmosphere, which is convenient and easy to obtain. For example, energy can be obtained by purifying hydrogen from water and then combining hydrogen with carbon to produce hydrogen. (hydrocarbon). In addition, the present invention rationally utilizes the artificially discharged carbon resources to be converted into hydrocarbons, and at the same time reduces carbon dioxide emissions, thereby alleviating the greenhouse effect.

Claims (41)

A coal slurry producing light oil and gas cracking process, wherein the process comprises the following steps: The coal slurry is conditioned to obtain a slime solution, and the slime solution is thickened and acidified to obtain a thickened and acidified slime solution; Bacterial culture: the root mold is mixed with the yeast, and then mixed into the plant culture material for cultivation to obtain a flora; Mixing: mixing the thickened and acidified slime solution with the flora to obtain a mixture; Fermentation: fermenting the mixture obtained after mixing to obtain a carbonaceous bacterium which separates the carbon group from the carbon support; The first hydrogen component formation: under the action of catalytic ions, the water is decomposed to obtain a hydrogen component; First carbon bond cleavage: under the action of super ammonium ion NH ₄ ⁺ × 4, the carbon bond in the carbon group is cut off; the first carbonation reaction: the first hydrogen component The hydrogen component obtained by the reaction is mixed with the carbon bond which is cleaved after the first carbon bond cleavage, and the hydrocarbon reaction is carried out under stirring to obtain a crude oil product; The first hydrocarbon ionization reaction: the hydrocarbon product is subjected to hydrocarbon ionization reaction to obtain a mixed oil product; The second hydrogen component formation: under the action of catalytic ions, the water is decomposed to obtain a hydrogen component; The second carbon bond cleavage: the carbon bond in the mixed oil product is cut off under the action of super strong ammonium ion NH ₄ ⁺ ×4; a second hydrocarbon reaction: mixing the hydrogen component obtained by the second hydrogen component formation reaction with a carbon bond which is cleaved after the second carbon bond cleavage, and undergoing a hydrocarbonation reaction under stirring; The second hydrocarbon ionization reaction: the product obtained by the second hydrocarbon reaction is subjected to hydrocarbon ionization reaction to obtain the light oil and gas. The process of claim 1 wherein said slime has a particle size of from 250 to 350 mesh. The process of claim 1 wherein said tempering liquid comprises the step of mixing said slime with a conditioned liquid to obtain a slime solution. The process according to claim 3, wherein the mass ratio of the slime to the conditioned liquid is 1:1. The process according to claim 3, wherein the conditioning liquid comprises chlorine ions, sodium ions, sulfur ions, magnesium ions, calcium ions, potassium ions, hydrogencarbonate ions, bromide ions, barium ions, boron ions and fluorine. An aqueous solution of ions or seawater. The process of claim 1 wherein the slime has a particle size of from 2 to 4 microns after thickening. The process of claim 1 wherein said acidifying comprises the step of adding oxalic acid to the thickened slime solution to adjust the pH of the slime solution to 3.5-3.8. The process according to claim 1, wherein the microbial culture comprises the steps of: mixing the Rhizopus and the yeast, mixing the plant culture with the plant culture material to obtain a bacterial source; and mixing the bacterial source into the cooked rice. After standing on the bacteria, after ripening, add brown sugar water to enlarge the strong bacteria. The process according to claim 8, wherein the Rhizopus mass fraction is 60% to 99% and the yeast mass fraction is 1% based on 100% by total weight of the mixture of Rhizopus and yeast. 40%. The process according to claim 8, wherein the mass ratio of the mixture of Rhizopus and yeast to the plant culture material is 1:3. The process according to claim 8, wherein the method for preparing the plant culture material comprises the steps of: mixing the plant with water and then grinding it into a plant slurry to obtain the plant culture material. The process of claim 11 wherein the plant to water mass ratio is 2:1. The process according to claim 11, wherein the plant comprises a combination of a plant of the genus Polygonaceae, a mulberry leaf, an almond leaf, a Chuanxiong, a white peony, an ananas, an orange leaf, a large green cinnamon, and a fragrant eucalyptus leaf. The process of claim 11 wherein said slurry has a particle size of from 120 to 160 mesh. The process according to claim 11, wherein the mass ratio of the plant, the mulberry leaf, the almond leaf, the Chuanxiong, the white peony, the pineapple, the orange leaf, the big green cinnamon and the fragrant eucalyptus leaves is 1:1:1: 1:1:1:1:1:1. The process according to claim 8, wherein the bacterial source is cultured at a temperature of 30 to 36 ° C, a relative humidity of 80% or more, and a ratio of 20% to 25%. The process of claim 8 wherein the ratio of the bacterial source to cooked rice is from 10:100 to 15:100. The process of claim 8 wherein said resting bacteria are for a period of 10-14 days. The process of claim 8 wherein the mass ratio of said brown sugar water to the bacterial source is 15:100. The process according to claim 19, wherein said brown sugar water is brown sugar water having a mass ratio of brown sugar to water of from 1:50 to 1:100. The process of claim 1 wherein said mixing is the mixing of the thickened, acidified slime solution and the flora. The process of claim 21 wherein the mass ratio of the microbial population to the thickened, acidified slime solution is 100:12.2. The process according to claim 1, wherein the fermentation is carried out by fermenting the mixture obtained after mixing to obtain a carbonaceous bacterium. The process according to claim 23, wherein the fermentation has a temperature of 20 to 36 ° C, a humidity of 100%, and a fermentation time of 21 to 90 days. The process according to claim 1, wherein in the first hydrogen component generating step, water is decomposed at a temperature of 700 ° C or higher. The process according to claim 1, wherein in the second hydrogen component generating step, water is decomposed at a temperature of 700 ° C or higher. The process according to claim 1, wherein the catalytic ions described in the first hydrogen component formation and the second hydrogen component formation step include ions generated by the sulfide ore being heated at 370 °C. The process of claim 27 wherein the catalytic ion is a zinc ion or a copper ion. The process according to claim 1, wherein in the first carbon bond cleavage step, the carbon bond in the carbon group is cleaved at 150 to 200 °C. The process according to claim 1, wherein in the second carbon bond cleavage step, carbon bonds in the oil compound are cut off at 150 to 200 °C. The process according to claim 1, wherein said method for preparing said super-strong ammonium ion NH ₄ ⁺ × 4 in said first carbon bond cleavage and second carbon bond cleavage step comprises the steps of: 900-1000 At °C, water reacts under the action of catalytic ions to obtain NH ₄ ⁺ × 4. The process of claim 31 wherein said catalytic ions comprise ions produced by the sulphide ore being heated at 370 °C. The process of claim 32 wherein the catalytic ion is a zinc ion or a copper ion. The process according to claim 1, 27 or 31, wherein said first hydrocarbon reaction specifically comprises the step of: breaking a hydrogen component formed by the first hydrogen component with a first carbon bond after a water bath The carbon bond was cut and mixed, and stirred at a rate of 10,000 rpm to carry out a hydrocarbon reaction to obtain a crude product. The process of claim 34 wherein the mass ratio of hydrogen to carbon is 1:1.6. The process according to claim 34, wherein the temperature of the hydrocarbon reaction is from 70 to 80 ° C and the reaction time is 10 minutes. The process according to claim 1, wherein a fractionation operation is required after the first hydrocarbon ionization reaction, and a mixed oil is obtained after fractional distillation. The process according to claim 1, 27 or 31, wherein said second hydrocarbon reaction specifically comprises the step of: breaking the hydrogen component formed by the second hydrogen component after the second carbon bond by a water bath The carbon bonds that were cut off were mixed and stirred at a rate of 10,000 rpm to cause a hydrocarbon reaction. The process of claim 38 wherein the hydrogen to carbon mass ratio is 1:1.6. The process according to claim 38, wherein the temperature of the hydrocarbon reaction is 70-80 ° C, The time should be 10 minutes. The process according to claim 1, wherein a rectification operation is required after the second hydrocarbon ionization reaction, and the light oil and gas are obtained after rectification.

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