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WO2001058244A2 - Systeme comprenant un appareil et un procede, destine a generer de l"energie a partir de biomasse - Google Patents

Systeme comprenant un appareil et un procede, destine a generer de l"energie a partir de biomasse Download PDF

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Publication number
WO2001058244A2
WO2001058244A2 PCT/NL2001/000077 NL0100077W WO0158244A2 WO 2001058244 A2 WO2001058244 A2 WO 2001058244A2 NL 0100077 W NL0100077 W NL 0100077W WO 0158244 A2 WO0158244 A2 WO 0158244A2
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WO
WIPO (PCT)
Prior art keywords
manure
heat
reactor
biomass
gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
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PCT/NL2001/000077
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English (en)
Other versions
WO2001058244A3 (fr
Inventor
Gilbertus Gualtherus Schoonderbeek
Joannes Jozef Gerardus Opdam
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Cooperatief Advies En Onderzoeksburo Ua Ecofys
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Cooperatief Advies En Onderzoeksburo Ua Ecofys
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Priority to AU37789/01A priority Critical patent/AU3778901A/en
Publication of WO2001058244A2 publication Critical patent/WO2001058244A2/fr
Publication of WO2001058244A3 publication Critical patent/WO2001058244A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F23G5/46—Recuperation of heat
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/026—Dust removal by centrifugal forces
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/20—Purifying combustible gases containing carbon monoxide by treating with solids; Regenerating spent purifying masses
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/10—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of field or garden waste or biomasses
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0909—Drying
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1643—Conversion of synthesis gas to energy
    • C10J2300/165—Conversion of synthesis gas to energy integrated with a gas turbine or gas motor
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/20—Waste heat recuperation using the heat in association with another installation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/40—Intercepting solids by cyclones
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/12—Heat utilisation in combustion or incineration of waste

Definitions

  • Livestock farms have to contend with a manure surplus which causes commercial and environmental problems.
  • the entire poultry farming sector in the Netherlands for instance generates an annual production of about 1.2 million tons of manure, which results in a problem of ammonia emission.
  • a system of apparatus is provided as claimed in claims 1-13.
  • a very efficient processing of biomass can result from using a Torbed reactor to incinerate and/or gasify the biomass, wherein the preferred use of the Torbed reactor, as described inter alia in US 4479920, ensures that, compared with for instance a vortex reactor, less carcinogenic tar is created.
  • Generated energy can fully cover the energy demand and a possible surplus of electricity can be sold as green energy to a utility company.
  • a method is provided for genera ;ing energy from biomass using the above stated system as claimed in claims 14 -17.
  • the set-up can be as follows:
  • manure At the poultry farm a quantity of manure is dried to 85% dry substance (the manure can optionally be pelletized in simple and inexpensive manner to manure pellets) .
  • the manure can be stored without dust formation and emission (ammonia) for a long period (for instance in large bags) .
  • the manure can be supplied directly to a glasshouse market gardener, but also via a distribution/mixing centre.
  • a distribution and mixing centre may be important to the glasshouse market gardener in guaranteeing supply and quality of the manure.
  • the complete Torbed installation (1800 k , including flue gas purification) is built at a glasshouse market garden (with about 5 ha.) .
  • the produced heat will (with use of heat buffer) fully satisfy the heat demand.
  • the produced electricity will be supplied in large part as green energy to a power company.
  • the market gardener saves about 30% to 40% on his energy consumption.
  • a Torbed reactor for incinerating and/or gasifying a biomass, particularly animal manure, and more particularly chicken manure.
  • the quantity of manure per animal depends mainly on the size of the animal.
  • the wet manure, without any drying, is less suitable for direct incineration.
  • the dry substance content (% d.s.) of the manure is increased by means of drying. This drying process can take place in the house as well as outside. Pre-drying of the manure in the house results in a % d.s. of 40 to 60%, depending on the drying system. A possible further drying of the manure takes place outside the house. Different processes can be applied for this purpose, wherein the % d.s. increases to a maximum of about 85%.
  • the manure is produced in a continuous process.
  • the manure is discharged batch-wise to the optional further drying. To maintain the progress of a continuously running manure processing the storage of manure is sometimes necessary.
  • Preprocessing has for its purpose to keep the emission of ammonia as low as possible and to make the manure suitable for incineration in the Torbed. Dry granular manure is very suitable for incineration in the Torbed. In order to obtain such a manure it is necessary to dry the manure further in a further drying system for manure. The manure is certainly suitable for storing for a longer period as a result of this further drying.
  • the different further drying systems currently in use make use of the heat from the house. If necessary some of the heat is recovered with an air-air heat exchanger. The further drying can be accelerated and improved by making use of heat supply from outside and by improving the contact between the wet manure and the warm air.
  • a well-known further drying system is for instance the belt dryer, wherein the manure is spread on a number of long conveyor belts in a closed space. The flow-by air absorbs moisture from the manure. This system produces a % d.s. of a maximum of 85%.
  • a drum drying system has been developed wherein the manure is brought into contact with warm air in a rotating drum. This drum drying system makes use of warm air from the house. It is possible to use the heat of the manure incineration to accelerate the drying process.
  • the capacity of the same drum dryer is hereby increased, or the same quantity of manure can be dried with a smaller drum.
  • the choice of material for the drum depends on the temperature. Owing to the rapid drying the ammonia emission will be further reduced and the % d.s. to be achieved is higher than with a further drying system at low air temperature. The required heat at high temperature could then be supplied by the Torbed reactor.
  • Chicken manure is a biological product .
  • the production and the quality of biological material depends on different variables which often cannot all be controlled equally well.
  • the quantity and composition of the manure will as a result vary, often per house.
  • chicken manure Compared with other organic materials, chicken manure has a relatively high content of different ash- forming substances such as calcium, sodium and potassium.
  • the incineration of chicken manure can involve sintering.
  • Sintering of chicken manure begins at a temperature of about 900 °C.
  • the minimum recommended incineration temperature is 850 °C whereby the margin between incomplete incineration and sintering amounts roughly to only about 50 °C.
  • There are different ways of preventing the occurrence of sintering during incineration Most methods are based on temperature control and realization of a homogeneous temperature in the oven (by preventing hot spots) . In the present invention two preventive methods have been chosen: t.ie pretreatment of the manure and the adjustment of the incinerator.
  • the Torbed reactor is a reactor which can be used as incinerator. By keeping the mass in the reactor small the conditions in the reactor can be regulated rapidly and accurately (better than in a reactor with long residence times and large volume) .
  • the rapid and precise temperature control in the Torbed reactor makes it an interesting installation for the incineration of chicken manure wherein, because of sintering, the temperature must remain within the range of 850 and 900 °C.
  • the rapid and complete incineration in the Torbed reactor is realized by feeding the reactor in counterflow. The air is supplied from below at an angle (whereby a rotating upward flow results) and the fuel (manure) is guided into the reactor from the top. The counterflow and the rotating movement causes the fuel to float as a turbulent ring.
  • the turbulence provides for a homogeneous distribution of temperature and reactants.
  • the size of the input and the particle size distribution determine the thickness of the ring.
  • the input For good management of the Torbed the input must preferably enter the Torbed as small homogeneous particles. This means in practice that the input is preferably injected as liquid or fed as fine solid material.
  • chicken manure has a dry substance content of about 20% and, after pre-drying, a dry substance content of about 60%.
  • Chicken manure with a dry substance content of 20% is a thick slurry and manure with a dry substance content of 60% is a paste- like material which cannot be stored for a long period because emissions of harmful substances are too high.
  • the second possibility, drying the manure improves the properties of the manure (higher net heating value, suitability for storage etc.) and reduces the volume of the manure.
  • the energy costs of manure drying can be covered by effective use of the residual heat of incineration.
  • Incineration of materials is an exothermic oxidation reaction; substances in reduced form are oxidized at a high temperature by oxygen. Owing to the high temperatures and the variety of substances during incineration many different reactions can occur which result in different reaction products. The oxidation produces heat and residual substances: flue gas and ash. Both residual flows are mixtures of the incineration products.
  • the formation of the reaction products can be controlled with the composition of the fuel and the control of the incinerating conditions (temperature, input, air etc.), i.e. the incineration residues (which are emitted) depend on fuel and installation (- adjustment) .
  • Ash is the collection of solid particles which remain after incineration.
  • the composition of incineration ash is characterized by the presence of materials which do not volatilize even at high temperatures, most of these materials being salts. These salts, built up of elements present in the fuel which do not volatilize, accumulate in the ash. Harmless concentrations of elements in the fuel (for instance of zinc) can be concentrated to dangerous concentrations in the ash.
  • the Dutch government has defined which concentrations of substances are permissible in the Designation of Hazardous Substances Decree (BAGA) . If the waste complies with the BAGA standard, the waste is suitable for different applications, such as for instance filler material in cement or asphalt. Ash is subdivided into two types: ground ash and fly ash.
  • the ground ash is the solid material which remains after incineration and is not discharged with the hot gases.
  • Ground ash consists mainly of non-volatile compounds.
  • Fly ash consists of smaller ash particles which are entrained by the incineration gases. The actual composition of fly ash is the same as the composition of the ground ash.
  • contact with the flue gases can result in volatile flue gas compounds being absorbed on the surface of the fly ash. The longer the fly ash is in contact with the flue gases, the higher the concentrations of absorbed substances on the fly ash.
  • the flue gas of incineration is a mixture of gaseous combustion products and solid particles which are carried along with the hot gases.
  • the composition of the flue gas mixture depends on installation and fuel.
  • the composition of the flue gas of chicken manure incineration in a Torbed reactor has been derived from literature values for comparable systems. The difference between these values and the actual flue gas composition will have to be determined on the basis of incineration tests with the Torbed reactor.
  • Figure 1 and figure 2 show the dry and wet flue gas purification lines with SNCR (Selective Non Catalytic Reduction) . These two purification lines illustrate, subject to the flue gas composition, solutions for meeting emission requirements.
  • SNCR Selective Non Catalytic Reduction
  • the dry gas purification will be able to realize the upper limit of the emission requirements if the quantity of NO ⁇ in the flue gas does not far exceed the expected value.
  • the second line the dry gas purification with SNCR
  • the dry purification with an SNCR system complies with the upper limit of emission range, even if the NO in the flue gas is high or if the emission standard for the NO ⁇ is made more stringent.
  • the wet gas purification with SNCR will be able to achieve the lower limit of the emission requirements. Variant without or with limited flue gas purification. This illustrates the investment cost for a situation where less stringent emission standards are in force .
  • the processing of manure has a dual purpose. Firstly, the volume of the manure is greatly reduced to a limited quantity which can be further processed economically and ecologically. Secondly, the processing of manure generates energy in the form of heat. This heat must be used as effectively as possible.
  • the heat demand of a poultry farm is small because the animals themselves produce a large part of the heat demand. Only in the case of broiler chickens is there a considerable heat demand at the beginning of the production cycle. Because supplying heat to third parties is not economically worthwhile, it is interesting to investigate whether the heat can be converted into an economically valuable form such as electricity.
  • the conversion of heat to electricity is possible in different ways, these are: Rankine cycle process with steam, Rankine cycle process with a volatile organic substance, a Stirling engine or a hot air engine.
  • the Rankine cycle process with water as medium (steam cycle) is only economical at outputs greater than 1 MWe.
  • the costs of a small installation are relatively high and the efficiency is low, so there is no demand for this type of installation.
  • the development of a machine with an electrical power between 10 and 100 kWe is not envisaged in the short term.
  • Hot air turbine A hot air turbine is a gas turbine wherein the incinerating chamber is replaced by a high temperature heat exchanger.
  • the British company JET supplies ROVER gas turbines with a heat demand of 400 kW at 700 °C turbine inlet temperature. The full load output amounts to about 10%. This gas turbine can be readily converted to a hot air turbine.
  • the heat comes from the Torbed reactor and is released at a temperature of 800 °C and 1 atm. In a heat exchanger this heat is transferred to the air coming from the compressor. This air has a pressure of about 3.2 atm and is heated isobarically to about 700 °C. The hot air expands in the turbine and thereby drives the compressor and the generator. The air from the turbine has a pressure of 1 atm and a temperature of about 500 °C. This hot air can be used to heat the broiler chicken houses.
  • the heat exchanger is based on counterflow and constructed from tubes and plates. At a fixed power the temperature difference between the ingoing flue gases and the outgoing hot air determines the output, the dimensions and the costs of the heat exchanger.
  • the improvement in the output of the heat exchanger means a reduction of the temperature difference.
  • the heat -exchanging surface is proportional to the temperature difference.
  • the length of the heat exchanger is inversely proportional to the temperature difference.
  • the output of the heat exchanger increases only marginally as the length increases.
  • a temperature difference between the heat flows of 150 °C has been chosen as example.
  • the hot flue gases enter the heat exchanger at a temperature of 850 °C.
  • the air from the compressor leaves the heat exchanger at a temperature of 700 °C.
  • the length of the heat exchangers amounts to about 3 metres. A greater length is realized by folding the heat exchanger ' double' .
  • the characteristics of a Stirling engine are: the operation of a Stirling engine is based on the heating and cooling of a closed quantity of gas. Mechanical energy is herein released which can be converted to electricity.
  • the electrical output greatly depends on the temperature on the warm side of the Stirling engine. Experiments and field tests produce outputs of 25 to 40%, wherein it should be noted that here the reliability and life span decreases as temperature increases. Taking the information of the various manufacturers as starting point, an output of 20% is realistic. This estimate is based on the fact that the temperature on the warm side of the Stirling engine in the application in combination with a Torbed reactor is much lower than applications of a Stirling engine directly heated by fossil fuels or the sun.
  • the heat is fed to a heat exchanger on the warm side of the Stirling engine.
  • the temperature is about 600 to 1000 °C. It is very important here that this heat exchanger is not fouled by the flue gases.
  • the heat is discharged by means of water, the cooling water has a temperature of a maximum of about 80 °C. This heat can be relinquished to the house or the environment by means of a radiator.
  • the ideal Stirling engine for a poultry farm of 50,000 chickens has the following specifications: - Thermal power between 100 and 500 kW; Electrical power between 10 and 50 kW; Feed temperature flue gases about 800 °C; Heat exchanger is suitable for relatively ' dirty' flue gases; - Electrical output is at least 15%.
  • the firm Spilling in Germany supplies a steam engine which at a steam temperature of 180 °C (10.5 atm) has an electrical output of about 7%. At a steam production of 2.3 ton/hour the electrical power amounts to 95 kW. At a steam production of 0.42 ton/hour the electrical power is zero.
  • the use of this steam engine under partial load is possible up to about 0.7 ton/hour (400 kWth) and then produces about 20 kWe at an output of 5%.
  • the hot air turbine offers the best prospects for the time being.
  • the demanded thermal power of 400 kW (after the heat exchanger) requires about 500 kW heat from the Torbed reactor. This heat is (at 7500 full load hours per year) available at farms with 112,500 broiler chickens, 100,000 laying hens or 60,000 parent animals. 40 kW of electricity is then generated continuously with an output of 10%.
  • Figure 3 presents a diagram of the configuration for manure preprocessing, manure incineration, flue gas purification and generation of electricity via a system according to the present invention.
  • Dried manure P coming from a manure dryer 20, is incinerated and/or gasified in a Torbed reactor 22.
  • Ground ash, flow Q is discharged and NH 3 , flow S, is added.
  • the incinerated/gasified manure, flow R is subsequently guided into a cyclone 24 where the greater part of the fly ash, flow T, is captured.
  • Low-dust flue gases, flow G relinquish heat in a heat exchanger 26 to compressed air O coming from a hot air turbine 30, via a compressor 28.
  • This hot air, flow V produces mechanical energy in the turbine 30 for a generator 32 which is connected to the electricity grid via a converter 34.
  • the cooled flue gases W are further purified in a dry washer 38, wherein carbon and calcium, flow X, are injected into flue gases W, and leave the installation via flow Y and chimney 36.
  • the residual heat (flow O) of the turbine is partially used to dry manure from 55% d.s. to 85% d.s.
  • the energy demand of a poultry house is divided into a heat and an electricity demand.
  • a poultry house requires electricity for ventilation, lighting and internal transport of feed, eggs and manure.
  • the heat demand is particularly present in the case of broiler chickens at the beginning of the production cycle. Table 1 shows the orders of magnitude and some characteristics of the energy demand.
  • Drying of the manure to a % d.s. greater than 80% has the advantage that it can be stored without danger of heating up and without emission of ammonia.
  • the present further drying systems for manure can dry the manure with the heat which is recovered from the house.
  • the degree of drying of the manure depends among other things on the temperature and the flow rate and the relative air humidity of the ventilating air. During a moist cold period the drying process progresses slowly, whereby manure with a lower % d.s. remains.
  • the supply of energy is provided by the incineration of manure.
  • Fully dried manure (100% d.s.) has a heating value of 11 to 20 MJ/kg. At 85% d.s. the heating value of manure amounts to 9 to 17 MJ/kg.
  • Table 2 shows the energy supply for the three types of farm. Table 2 Energy supply.
  • the last column shows the amount of electrical energy which can be produced with the released heat. From the comparison with the electricity demand of the farm itself (Table 3) can be seen that the possible electricity production (Table 2) is much higher than the electricity demand of the poultry farm.
  • Table 3 compares the energy supply with the total energy demand of the three farms.
  • the total energy demand is the sum of the heat demand and the electrical energy from the hot air turbine.
  • the heat demand for generating electricity is covered by the heat extracted from the flue gases. During this exchange of heat about 20% of the heat is lost. At a conversion efficiency of
  • Table 3 shows that the supply of energy from the manure is more than sufficient to meet the energy demand of the three types of house. This large supply of energy gives some latitude in the design and use of the installations. Because there is a heat surplus the residual heat can also be converted into electricity. The surplus electricity can be supplied to the grid.
  • the further treatment of the flue gases .
  • Connection to the public electricity grid (converting from 400 Hz to 50 Hz, 230 V) Housing of the complete installation.
  • the broiler chickens have an external heat requirement. This heat is extracted from the flue gases after the first heat exchanger with a second heat exchanger .
  • Broiler chicken farm without electricity production An appraisal has been made at the broiler chicken farm as to whether the costs of incinerating the manure can be recovered without the production of electricity.
  • the broiler chicken farm has been chosen for this purpose because there is a considerable heat demand which can be fully covered by the heat production of the Torbed reactor.
  • Table 4 Energy demand and supply without electricity production (112,500 broiler chickens)
  • the heat demand is greater in winter than in summer.
  • the growth cycle of the broiler chickens takes about 7 weeks .
  • the heat demand is greatest and the manure production the lowest.
  • the heat demand is low and the manure production high. That the heat demand and supply do not coincide can be resolved by storing the manure for a period of a maximum of one growth cycle. This will amount to about 50,000 kilos of manure. This manure is incinerated during the first few weeks of the subsequent growth cycle.
  • the energy demand amounts to about 24% of the energy supply.
  • the supply is therefore amply sufficient for heating the house.
  • About 950 GJ/year is required to evaporate the surplus moisture from the pre-dried manure from the house (d.s.% 55%) to a d.s. of 85%. This is only 10% of the surplus heat. There is therefore sufficient heat available for further drying of the manure.
  • the clustering of farms has for its object to improve the economic result of small-scale manure processing.
  • manure, heat and electricity By exchanging manure, heat and electricity, adjacent farms can link their mutual shortfalls and surpluses to each other.
  • Torbed reactor located centrally at one farm. This has the advantage that the installations for incineration, flue gas purification and electricity generation can take a larger form and are thereby cheaper per unit .
  • the clustering of farms also involves additional costs for the transport of manure, heat and electricity.
  • the scenario for a link between the poultry and glasshouse market gardening sectors can be outlined as follows.
  • the manure is dried on the poultry farm to a d.s.% of 85%.
  • This manure can be supplied to a heat- demanding party such as for instance a glasshouse market garden.
  • the quality of the dried manure is such that it has no gaseous emissions, although it does cause dust.
  • An additional step could be pelletizing the dried manure. Transport and long-term storage is then no longer a problem.
  • the poultry farmer supplies dried (optionally pelletized) manure (d.s. 85%) to the glasshouse market garden.
  • the manure is stored.
  • the manure is incinerated in a Torbed reactor and the flue gases are purified.
  • the heat is supplied to the glasshouse. Because a Torbed reactor must be switched on and off as little as possible, a buffering of heat is necessary. This buffer is charged with heat when the heat demand of the glasshouse is lower than the heat production of the Torbed reactor. When the heat demand rises above the capacity of the Torbed reactor, the buffer will supply heat to the glasshouse. If the buffer is empty and the heat demand is higher than the capacity of the Torbed reactor, a gas boiler will supply the required extra heat. If the heat demand is less than the nominal output of the Torbed reactor for a longer period, the Torbed reactor will be switched off and all heat is supplied by the gas boiler.
  • a glasshouse market garden can obtain the dried manure directly from one or more poultry farmers but also via a mixing/distribution centre. Purchase via a mixing/ distribution centre may have advantages for the glasshouse market garden in respect of the guarantee of the quality and supply of the manure. DESCRIPTION OF PURIFICATION EQUIPMENT IN FIGURES 1, 2 and 3
  • Dust removal The larger dust particles must be removed first because at lower rates of flow the particles are deposited and may accumulate (accumulation of dust can disrupt the purification line) . Dust particles are moreover condensation nuclei and reaction surfaces for a wide range of complex reactions . Timely removal of dust prevents these reactions occurring.
  • the two main reasons for placing the heat exchanger at the front of the line are the high temperature at the beginning of the line and the advantages of a rapid cooling.
  • the purification steps which follow limit the minimum and the maximum temperature. It is therefore wise to have the heat exchanger fulfill a dual function: effective utilization of the heat and cooling of the flue gas to within the set temperature limits of the further purification.
  • the placing of the heat exchanger after the cyclone results from the necessity of removing the larger dust particles because it is possible for dust to accumulate in the heat exchanger .
  • Dust particles (up to a determined size) are separated from the residual flow by centrifugal forces. Solid particles have a greater density and mass and thereby a greater inertia. They are driven against the wall of the cyclone whereby they cannot follow the upward flow of the gas. Small dust particles are not removed. In the case of particles smaller than 100 ⁇ m the aerodynamic properties must be taken into account.
  • the choice of material for the filter determines the maximum temperature (and the cost) .
  • the pressure drop is estimated at 1200 Pa.
  • complications may occur (for instance encrusting or clogging of the cloth) .
  • Difference in particle size Operation
  • the filter cloth has holes of a determined size.
  • the gas can penetrate through these holes.
  • the solid particles remain behind on the cloth.
  • the solid particles are removed periodically from the cloth (either pneumatically or mechanically) .
  • the choice of material for the filter and the incineration temperature of the active carbon determine the maximum temperature (and the cost) .
  • the gas is guided at low speed through a space where negatively charged wires are stretched, while the wall of the ESP is positively charged. Dust particles take* on a negative charge and migrate to the wall while the flue gas remains unaffected. The dust on the walls is removed periodically.
  • Flue gas is brought into intensive contact with solvent (packed bed, sprinkler system etc.) .
  • the catalytic de-NO ⁇ must be placed at the end of the purification because of the temperature requirements made by this method and the disruptive effects of components in the gas such as different acids, dust and other components.
  • Design properties Low temperatures 300-450 °C
  • NH 3 is injected into the flue gas and reacts with NO ⁇ to form 2 and H 2 0. Despite the low temperatures reaction can take place owing to the presence of a catalyst.
  • a Torbed reactor can also be used for gasifying biomass. Because of its unique design a Torbed reactor can prevent sintering. Two gas purification steps can be incorporated in order to comply a) with the requirements for the heating gases for the gas engine, and b) with the emission requirements for flue gases in the Netherlands. These tests have demonstrated that a Torbed reactor is in principle suitable for keeping the processing conditions well under control so that the danger of problems occurring (among other things sintering) can be small.
  • the heating gases which are released on gasification can be fed immediately after purification to a gas engine with which electricity can be generated.
  • a good purification of the gases is important for the lifespan of the gas engine.
  • the manure is however important.
  • the manure is preferably pelletized or briquetted. Drying to 85% dry substance in a drum dryer gives a granular structure. This granular structure also appears to be very suitable for gasification. Rapid further drying at the poultry farm to 85% d.s. is taken as starting point because of the resulting granular structure of the manure and because the ammonia production can be considerably reduced.
  • the manure can furthermore be transported without emission to a possible heat-demanding industry such as a glasshouse market garden.
  • heating gases In order to prevent corrosion in the gas engine the heating gases must be purified.
  • Three heating gas purification lines are proposed. The line with a dust removal step, a tar filter and a wet gas washer will almost certainly work well.
  • the ammonia emission can be reduced very considerably if the manure is dried at the poultry farm.
  • the produced heat with high temperature can be used directly for the purpose of a very rapid further drying of the manure.
  • the poultry farmer will also further dry the manure to 85% d.s.
  • the ammonia emission will herein also be reduced, although according to expectations not to the same degree as when use can b* ⁇ made of heat at high temperature.
  • the biomass is gasified with an undermeasure of oxygen (air) , wherein a relatively small volume of hot heating gas (mainly CO, H 2 , CH 4 , ..) is produced.
  • This heating gas can be used for the production of electricity and/or heat by combustion in a gas engine or gas turbine. Since the heating gas must comply with the material requirements, this to prevent corrosion and deposition problems, the heating gas can be purified before leing combusted.
  • An advantage hereof is that contaminants are removed from a relatively small (fuel) gas volume, which is simpler and can take place at lower cost than with a large volume of combustion gases.
  • Electricity production using a gas engine takes place by means of a generator, whereafter the low temperature residual heat can be used for heating purposes.
  • the moisture which comes with the manure is converted to water vapour in the gasifier.
  • the calorific value of the gas formed from a mixture of wet and dry bio- fuel is estimated by the inventors at 5 MJ/Nm 3 . Thermally the wet fraction goes through the gasifier as ballast. The energy required for evaporation of the moisture is recovered at a low, but usable temperature level by condensation in the gas washer following the gasifier.
  • gasification processes compared to incineration processes are inter alia: a higher efficiency of generating electricity, contaminants can be removed simply and at low cost from the heating gas, and a non-leac able ground ash fraction is produced which can be employed for commercial purposes.
  • the requirements which the manure has to meet for a good gasification in the Torbed reactor are low. A dry substance content of 55% appears sufficient.
  • the manure is preferably pelletized or briquetted. Drying to 85% dry substance in a drum dryer such as designed by Vencomatic gives a granular structure. This granular structure also appears very suitable for gasification. This study assumes a rapid further drying at the poultry farm to 85% d.s. because of the resulting granular structure of the manure and because ammonia production can thereby be considerably reduced.
  • the manure can moreover be transported without emission to a possible heat -demanding industry such as a glasshouse market garden.
  • the tar production depends on the starting material and on the gasification conditions (particularly the temperature) . It is important to have a good impression of the tar production because the production of tar causes a loss in energy efficiency (hydrocarbons are in the tar instead of in the heating gas) , and tar is moreover categorized as chemical waste.
  • the tar production in the Torbed reactor will be comparable to the tar production in a fluidized bed reactor at a temperature of about 800 °C (sintering will probably not occur at this temperature) .
  • the resulting estimate amounts to 100 mg/Nm 3 in percent by weight.
  • the production of tar can perhaps be minimized by a proper adjustment of the Torbed reactor and feedback of the tar into the Torbed reactor.
  • Table 5 Estimate of the composition (in percent by volume) of the heating gas and the tar production (mg/Nm 3 ) during gasification of chicken manure.
  • Tar can be removed in different ways from the heating gas.
  • Two methods of removal are the sand filter and the tar cracker. With these two methods of tar removal three different heating gas purification lines are proposed for the heating gas.
  • the first purification line is a conventional line. This line consists of a dust removal step, a tar filter and a wet gas washer.
  • the second purification line consists of a dust removal step, a tar cracker (simultaneously also removes NH 3 ) and a dry gas washer.
  • the third and last line is comparable to the second line. In this line the dry gas washer is replaced by a wet one.
  • This purification line is added so as to obviate the possibility of exceeding the NH 3 concentrations .
  • the combustion of purified heating gas can take place in a gas engine.
  • Flue gas can be released during combustion of the heating gas in the gas engine.
  • the composition of this flue gas is not precisely known.
  • the gas will probably be relatively clean and (apart from the NO ⁇ and volatile hydrocarbon emission) will comply with future emission requirements.
  • Table 6 Estimat e of the tar and the flue gas emissions of gasification a fter combustion in the gas engine on the basis of the heating gas composition.
  • the NH 3 emission can be considerably reduced if the manure processing takes place at the poultry farm using heat produced in the Torbed reactor. This reduction will be greater than in the case of processing at a glasshouse market garden because the released heat cannot be employed for a rapid further drying of the manure.
  • an infeed of the manure into the reactor in the form of pellets or briquets is strongly preferred to a moist substance.
  • a granular structure will probably also suffice.
  • a granular structure is obtained by further drying of the manure to about 85% d.s. in for instance a drum dryer.
  • manure in granular structure with d.s.% of 85% (in the economic analysis the further drying of manure has been taken into account) .
  • the heating gases will preferably be purified so as to comply with the specifications for gas feed into the gas engine. This purification step is important for care of the gas engine .
  • a flue gas purification line is preferably employed. Since an earlier purification for the gas engine has preferably taken place, a simple flue gas purification can be performed consisting of only a De-NO ⁇ step (SRC; selective catalytic reduction) . The necessary embodiment of this line depends on the flue gas composition and on the emission standards in force.
  • SRC De-NO ⁇ step
  • ash of the incineration is not expected to produce any hazardous (' chemical' ) waste. An additional ash purification line is therefore in all probability not necessary. If it is found (very likely) that the ash complies with the standards, a useful application for the ash can be sought . Owing to the thermal treatment the ash will not be immediately suitable as manure but will be suitable as raw material for fertilizer. In addition, it is expected that the ash will be suitable as additive in construction materials.
  • Fig. 4 shows an integral system for processing biomass by means of gasification.
  • Biomass (B) is guided into a storage space (50) and subsequently gasified in a Torbed reactor 52. Ash A, is guided away from reactor 52. Resulting flue gas, S, is guided via a gas purification installation 54 into a gas reactor 56. Resulting flue gas, flow R, is guided to a flue gas purification installation 58, while energy from the gas engine 56 is used to generate electricity E and heat W.
  • the present invention is not limited to the foregoing description; the rights sought are defined by the following claims.

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  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Processing Of Solid Wastes (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Treatment Of Sludge (AREA)

Abstract

L"invention concerne un système permettant de générer de l"énergie à partir de biomasse, consistant à incinérer et/ou à gazéifier la biomasse dans un réacteur d"incinération et/ou de gazéification. Ce système comprend également un générateur d"électricité couplé au réacteur d"incinération et/ou de gazéification, ce réacteur étant un réacteur Torbed.
PCT/NL2001/000077 2000-02-02 2001-02-02 Systeme comprenant un appareil et un procede, destine a generer de l"energie a partir de biomasse Ceased WO2001058244A2 (fr)

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NL1014267 2000-02-02

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005042674A1 (fr) * 2003-10-08 2005-05-12 Banham Poultry Ltd Procede pour gazeifier des dechets
WO2006003454A1 (fr) * 2004-07-07 2006-01-12 Mortimer Technology Holdings Limited Procede pour traiter une matiere carbonee
EP1688475A1 (fr) * 2005-02-03 2006-08-09 Samson Bimatech I/S Méthode de traitement de lisier, produit fibreux résultant de ce traitement et utilisations de ce produit
DE102010022807A1 (de) * 2010-06-05 2011-12-08 Harmanus Tapken Verfahren insbesondere zur Abtötung von Viren, Bakterien und anderen Krankheitserregern im Stallmist
EP2479493A1 (fr) 2011-01-21 2012-07-25 Exploitation Energetique de Sous Produits Industriels et Agricoles - Exedia Dispositif de combustion, unité d'incinération comprenant un tel dispositif de combustion, et procédé de mise en oeuvre d'un tel dispositif de combustion

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP3153091B2 (ja) * 1994-03-10 2001-04-03 株式会社荏原製作所 廃棄物の処理方法及びガス化及び熔融燃焼装置
US3656440A (en) * 1970-10-26 1972-04-18 Morse Boulger Inc Incinerator having means for treating combustion gases
FR2417483A1 (fr) * 1978-02-17 1979-09-14 Chambe Maurice Procede et systeme de cuisson, de deshydratation et de sterilisation des dechets et vegetaux
DK148368C (da) * 1979-03-26 1985-11-04 Henrik Have Fremgangsmaade til udvinding af varme fra staldgoedning, spildevandsslam og andet vaadt affald ved forbraending
FR2484294B1 (fr) * 1980-06-17 1985-06-28 Lejeune Gwenole Procede et dispositif de traitement de produits humides
JPH11515090A (ja) * 1995-10-13 1999-12-21 ナムローゼ・フェンノートシャップ・ケマ 廃棄物処理方法及び設備
FR2758100B1 (fr) * 1997-01-06 1999-02-12 Youssef Bouchalat Procede de traitement et valorisation energetique optimisee des boues de stations d'epuration urbaine et industrielle

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005042674A1 (fr) * 2003-10-08 2005-05-12 Banham Poultry Ltd Procede pour gazeifier des dechets
WO2006003454A1 (fr) * 2004-07-07 2006-01-12 Mortimer Technology Holdings Limited Procede pour traiter une matiere carbonee
EP1688475A1 (fr) * 2005-02-03 2006-08-09 Samson Bimatech I/S Méthode de traitement de lisier, produit fibreux résultant de ce traitement et utilisations de ce produit
DE102010022807A1 (de) * 2010-06-05 2011-12-08 Harmanus Tapken Verfahren insbesondere zur Abtötung von Viren, Bakterien und anderen Krankheitserregern im Stallmist
EP2479493A1 (fr) 2011-01-21 2012-07-25 Exploitation Energetique de Sous Produits Industriels et Agricoles - Exedia Dispositif de combustion, unité d'incinération comprenant un tel dispositif de combustion, et procédé de mise en oeuvre d'un tel dispositif de combustion

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AU3778901A (en) 2001-08-20

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