Method and system of obtaining synthesis-gas from biomass by carbonisation |
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IPC classes for russian patent Method and system of obtaining synthesis-gas from biomass by carbonisation (RU 2525491):
 Method for production of pyrolysis resin-free combustible gas during condensed fuel gasification and gas generators for method realisation / 2520450
Group of inventions may be used in the field of condensed and solid fuel processing to generate power. The method for production of pyrolysis resin-free combustible gas during gasification of condensed fuel includes fuel delivery through a loading unit (1) installed in the upper part of the gas generator and loading of a solid incombustible material through a separate loading unit (4) which ensures material staying in the counter-flow of gaseous products. Oxygen-containing gas is delivered to the lower part of the gas generator, pyrolysis and fuel combustion in the gas counter-flow are made. Solid residue is unloaded from the lower part of the gas generator. Gaseous products from the upper part of the gas generator are outputted from a layer of the solid incombustible material not mixed with the fuel. Gaseous products form in result of pyrolysis and drying are separated from the fuel layer and fed to the combustible area (9) placed below the area where fuel and solid incombustible material are mixed (8). The used gas generators are represented by multiple-bedded furnaces, a shaft reactor, and a rotating drum.
 Technology and device for obtaining synthesis gas from biomass by pyrolysis / 2519441
To obtain synthesis-gas from biomass performed is preliminary processing of biomass, including biomass crushing until particles with size 1-6 mm are obtained and drying raw material to moisture 10-20 wt %. After that, pyrolysis of biomass is carried out by means of fast pyrolysis technology, with temperature of pyrolysis layer being 400-600°C, and time of location of gaseous phase on pyrolysis layer being 0.5-5 s. Product of pyrolysis layer is pyrolysis gas and coal powder. Pyrolysis gas is separated from coal powder and solid heat carrier by means of cyclone separator. After that, coal powder and solid heat carrier are separated in separator to separate solid phases, coal powder is charged into coal powder bin for accumulation, solid heat carrier is heated in chamber of boiling layer heating and solid heat carrier is supplied to pyrolysis layer for re-use. After that, pyrolysis gas is supplied to condensate accumulator to condense aerosol and condensation of condensable part of pyrolysis gas is carried out to form bio-oil, after that formed bio-oil is pumped by high pressure oil pump and supplied to gasification furnace for gasification. One part of non-condensed pyrolysis gas is supplied on combustion layer for combustion with air, and the other part of non-condensed pyrolysis gas is supplied on pyrolysis layer as fluidising medium.
 Method and device for obtaining synthesis-gas with low content of resins from biomass / 2516533
Inventions can be used in power engineering and chemical synthesis. Method of obtaining synthesis-gas with low content of resins from biomass includes biomass decomposition n the first fluidised bed reactor (3) into pyrolysis gas and pyrolysis coke. Obtained pyrolysis gas is supplied as gas for formation of fluidised bed (5) in the following fluidised bed reactor (11). Pyrolysis coke in form of small particles is removed together with gas and supplied into the following fluidised bed reactor (11) through nozzle bottom (4).
 Method and device for biomass pyrolysis and gasification using two intercommunicated kilns / 2515307
Solid high heat capacity particles are used as heat carrier while saturated water steam is used as an oxidiser. First, biomass is subjected to low-temperature pyrolysis at 500-800°C to produce unpurified synthetic gas not containing alkaline metal oxides and coke. Then said unpurified synthetic gas and coke are subjected to high-temperature gasification at 1200-1600°C to produce synthetic gas not containing resin. Produced synthetic gas is cooled, de-dusted, deoxidised and dewatered. Proposed device comprises gasification kiln and pyrolysis kiln arranged one on the other. Note here that their chambers are communicated. Besides it comprises heater of particles, heater with plasma flame, draught fan, first heat exchanger, water tank for production of saturated water steam, water feed pump, second heat exchanger, dust catcher, deoxidiser tower and dewatering device.
 Method of producing synthesis gas from wood wastes / 2507238
Wood wastes are dried and heated to temperature of 250-350°C. The heated wood wastes are fed into a pyrolysis chamber where temperature rises to 700°C. The obtained charcoal is fed into a gas-generation chamber where it undergoes steam reforming at temperature of 700-1000°C.
Method of conducting pyrolysis / 2502779
Method of conducting pyrolysis involves feeding first starting material into a burning boiler and feeding second staring material into a pyrolysis reactor (a). Energy is obtained from the first starting material in the burning boiler and then transferred from the burning boiler to the pyrolysis reactor by a heat carrier (b). The heat carrier is heated in the burning boiler (c). Gaseous and liquid product fractions are obtained in the pyrolysis reactor from the second starting material via fast rapid pyrolysis (d). The second starting material is mixed with a carrier gas to obtain a mixture, and the heat carrier heated in the burning boiler is fed into said mixture (e). The heat carrier is pumped in a closed system from the burning boiler to the pyrolysis reactor and from the pyrolysis reactor to the burning boiler through a separation step (f). Most of the streams of by-products, residues and wastes are fed into the burning boiler (g).
 Gasification method of solid fuel, and once-through gas generator / 2470990
Method is implemented in once-through gas generator containing fuel bunker 14 for fuel subject to gasification, and at least one combustion chamber 32 by means of pyrolysis, at which fuel is decomposed into pyrolysis products, and further gasification, at which pyrolysis products are gasified to gas. Heat transfer from combustion chamber to fuel bunker is restricted to reduce the fuel heating before the beginning of pyrolysis stage using cooling channel 18 for movement of such medium, as gasification air. Upper surface of cooling channel 18 is formed with upper covering 16a of once-through gas generator, above which fuel bunker 14 is arranged, and lower surface is formed with lower covering 16b of once-through gas generator, under which combustion chamber 32 is located.
Method for obtaining fuels from waste / 2459860
Biowaste is pressed in batches in the form of briquettes and subject to gasification. Processed waste is passed in temperature rise direction through at least one low-temperature zone and at least one high-temperature zone. Synthesis gas is obtained. The obtained synthesis gas is used for obtaining diesel fuel. Some part of synthesis gas, which was not used in Fischer-Tropsch process, is used for covering the consumption of power required for implementation of biowaste utilisation method.
 Method and device for hard fuel gasification / 2333929
Invention is intended for chemical industry, and can also be used in power engineering and municipal economy for production of fuel and synthesisgas by means of hard fuel gasification. The claimed method of hard fuel gasification consists in that carbonisation of hard fuel is carried out in pseudoliquefied layer of heat-carrier material. The obtained fuel gas and hard carbonised residue are separated in device installed in the upper part of the apparatus. Carbonised residue is subjected to gasification by mixture of water vapour and oxygen obtaining synthesis gas. Device for hard fuel gasification consists of two coaxially placed vessels, the outer vessel being used for carbonisation, and the inner one for fuel gasification. In the lower part of the outer vessel, an air-distributing grid, with a layer of pseudoliquefied heat-carrier material arranged on it, is placed. The inner high pressure vessel is placed within the limits of pseudoliquefied layer of heat-carrier material. In the upper part of the outer vessel there is a cyclone for separation of fuel gas from hard carbonised residue, which, under the action of its own weight, flows to gasificator through a vertical pipe.
 Apparatus for obtaining gaseous product from such fuel as biomass / 2467055
Invention relates to solid fuel gasification. A gaseous product containing CO, H2, CH4 is obtained from biomass in an apparatus 1. The apparatus 1 has a reactor 2 which is bounded by a base 5 and reactor walls. The reactor walls have a peripheral wall 10 and a top wall 11. The reactor 2 has an inlet hole 18 for feeding the biomass, a rising pipe 24 for chemical conversion of the biomass to the gaseous product. The rising pipe 24 has an upper end 28 and a lower end 26, as well as an outlet hole 44 for releasing the gaseous product. The rising pipe 24 is attached to the reactor wall 10. The base 5 of the reactor 2 consists of two lower sections 7 and 8. The lower end 26 of the rising pipe 24 lies above the lower section 8 of the base and is at such a distance from the lower section of the base 5 that it can freely move in the longitudinal direction as a result of thermal expansion.
 Method and apparatus for producing biofuel from solid biomass / 2459857
Method includes a gasifying step for gasifying solid biomass (2) in a gasifier (6) to obtain raw synthetic gas (3). Further, conditioning of the raw synthetic gas (3) to purify the raw synthetic gas (3) to obtain purified synthetic gas (4) having a molar ratio of hydrogen to carbon monoxide between 2.5:1 and 0.5:1; one of the conditioning steps is catalytic treatment in a reformer (18). Further, using the purified raw synthetic gas (4) for Fischer-Tropsch synthesis in a Fischer-Tropsch reactor (5) to obtain a liquid hydrocarbon product (1). The invention also relates to apparatus for realising the present method.
 Fluid bed reactor with furnace-type pulsed heat transfer modules / 2448765
Invention may be used in chemical industry. Proposed fluid bed reactor 300 comprises reaction vessel 302 with first wall part and second wall part, first heat transfer module 310 connected to vessel 302. First heat transfer module 310 comprises first pulse furnace 312 connected to first acoustic chamber 311 with first and second faces. First pulse furnace 312 comprises, at least, one exhaust pipe 314 terminating in first acoustic chamber 311 between first and second faces, and multiple heat transfer pipes 326. Every said heat transfer pipes 326 stays in fluid contact with acoustic chamber 311 via said wall part. Combustion products from exhaust pipe 314 along first channel of every heat transfer pipe from first wall part and, then, along second channel toward wall first part. Resonance tube of first pulse furnace 312 does not extend inside reaction vessel 302.
 Gas generator system with coal circulating fluidised bed / 2426769
System includes coal gas generator 2, high-temperature separator 3, heat exchanger 5, low-temperature separator 4 and heat recovery steam generator 6, which are connected in series. Coal gas generator 2 is equipped with primary air inlet 21 and at least one secondary air inlet 22 to supply high-temperature gasifying agent to gas generator 2. Gas generator 2 is also equipped with inlet 23 for circulating coal. Primary air inlet 21 and primary air inlet 22 are connected to heat exchanger 5. Inlet 23 for circulating coal is connected to high-temperature separator 3, low-temperature separator 4 and heat exchanger 5. System can include venturi scrubber 7 connected to HRSG 6, gas cleaning column 8 connected to venturi scrubber 7. At that, sedimentation tank 9 is arranged at the bottom of gas cleaning column 8, and slag removal device 11 is located at the bottom of sedimentation tank 9. Cooling tower 10 is arranged between cooling water inlet and cooling water outlet on gas cleaning column 8.
 Gas generator with boiling layer for gasification of solid fuels / 2341551
Boiling layer is created from coke particles in the grid 11, which is supplied from fuel supply facility 10. Coal is sent to gasification chamber 5, where it is coked with coke gases exhaust. Part of gasification products is discharged through nozzle 14 to consumer, and remaining products are supplied to the top part of layer for afterburning. Air is supplied to boiling layer in burning zone along pipes 9, which are welded into pipe plate 6. Pipes 8, which are welded into pipe plate 7, serve for collection of technological gas supplied to consumer from horizontal section of reactor. To provide proper mixing of some gasification products with supplied air, inhibiting visors 18 are fixed to pipes of secondary air 9 supply.
 Method of pyrolysis and gasification of organic agents or mixtures of organic agents and device for realization of this method / 2272064
Proposed method includes introduction of raw materials in one or several drying and pyrolysis reactors with one or several reactors with movable bed or one or several rotating reactors or one or several rotating reactors and reactors with movable bed for contact with material of fluidized combustion bed containing only ash of organic agent or unburnt carbon residues of organic agents and additional material of fluidized bed for contact with material of fluidized bed and reactor wall of fluidized combustion bed. As a result, water vapor and pyrolysis products containing condensable components and solid carbon residues are formed. Solid carbon residues or solid carbon residues and part of water vapor and pyrolysis gas with condensable components and material of fluidized bed are returned to fluidized combustion layer where carbon reside of organic components is burnt. Material of fluidized bed is heated and is again directed to pyrolysis reactor where pyrolysis residues performing function of stationary fluidized bed are burnt. After drying, water vapor and pyrolysis gases with condensable components are subjected to treatment in additional reaction zones of indirect heat exchanger at addition of vapor, oxygen and air or their mixture to pyrolysis gas or to heat exchanger in order to obtain gaseous product at high calorific power. Device proposed for realization of this method includes pyrolysis reactor, fluidized combustion bead for pyrolysis residue and reaction zone for pyrolysis gases.
 System fuel gasification / 2220187
The invention relates to the gasification furnace for gasification of fuels, including coal, municipal waste, and so on, and to the gasification system, which uses such a gasification furnace
 The method of carrying out endothermic reactions and device for its implementation / 2073064
The invention relates to a thermochemical reactor with indirect heating and to methods for conducting thermochemical reactions, including gasification and steam reforming of heavy oils and toxic organic substances, regeneration of black liquor and energy use and conversion of renewable resources such as biomass and energoresursa waste streams
 Method of producing coal gas / 2434931
Dust coal and high-temperature gasifying agent are fed into a coal gas generator to obtain coal gas. Heat exchange takes place between coal gas coming out of the coal gas generator and the gasifying agent to obtain a high-temperature gasifying agent. After heat exchange between the coal gas and the gasifying agent, heat exchange takes place between coal gas and water to obtain steam. The obtained steam is a component of the gasifying agent. Dust coal is separated and fed back into the coal gas generator. After heat exchange with water and further removal of dust and desulphuration, coal gas is output.
 Process of producing gas from solid fuel / 2321617
Invention relates to processes for production of combustible gases from solid carbon-containing fuel, in particular to gasification of lump and granulated fuel, and can find use in chemical industry and heat-and-power engineering. In the process according to invention, solid fuel (peat, brown coal, or wood) is heated to temperature not higher than 150°C in presence of metal oxide (iron and aluminum oxides) catalyst under blow conditions, which blow is carried out with overheated steam at 150 to 400°C.
Method of pyrolysis and gasification of organic agents or mixtures of organic agents and device for realization of this method / 2272064
Proposed method includes introduction of raw materials in one or several drying and pyrolysis reactors with one or several reactors with movable bed or one or several rotating reactors or one or several rotating reactors and reactors with movable bed for contact with material of fluidized combustion bed containing only ash of organic agent or unburnt carbon residues of organic agents and additional material of fluidized bed for contact with material of fluidized bed and reactor wall of fluidized combustion bed. As a result, water vapor and pyrolysis products containing condensable components and solid carbon residues are formed. Solid carbon residues or solid carbon residues and part of water vapor and pyrolysis gas with condensable components and material of fluidized bed are returned to fluidized combustion layer where carbon reside of organic components is burnt. Material of fluidized bed is heated and is again directed to pyrolysis reactor where pyrolysis residues performing function of stationary fluidized bed are burnt. After drying, water vapor and pyrolysis gases with condensable components are subjected to treatment in additional reaction zones of indirect heat exchanger at addition of vapor, oxygen and air or their mixture to pyrolysis gas or to heat exchanger in order to obtain gaseous product at high calorific power. Device proposed for realization of this method includes pyrolysis reactor, fluidized combustion bead for pyrolysis residue and reaction zone for pyrolysis gases.
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FIELD: chemistry. SUBSTANCE: invention can be used in the chemical industry. To obtain synthesis-gas from biomass by carbonisation, preliminary drying and dehydration of the initial biomass are carried out. After that, low-temperature carbonisation is performed at atmospheric pressure and isolation from oxygen at a temperature in a carbonisation furnace of 200-400°C, rate of the temperature growth 5-20°C/min and the time of the initial biomass keeping of 20-90 min. Products in the form of pyrolytic gas and charcoal are obtained. Charcoal is cooled at an outlet from the carbonisation furnace to a temperature of 60-280°C and transported to a storage tank. Pyrolytic gas is separated from powder-like charcoal. A part of separated pyrolytic gas is supplied into a combustion layer for burning, and the other part is heated by hot smoke gas, formed in the process of burning in the combustion layer. Heated pyrolytic gas is supplied into the carbonisation furnace as a heat source. Discharged hot smoke gas after heat exchange is supplied into a zone of preliminary processing of the initial biomass for drying. Separated powder-like charcoal is supplied into the storage tank. Powder-like charcoal is milled with obtaining a suspension, which is introduced into the furnace for gasification by a high-pressure pump. EFFECT: invention makes it possible to increase gasification efficiency, stability and reliability of the system for obtaining synthesis-gas from biomass. 9 cl, 1 dwg, 1 tbl, 6 ex
The technical FIELD The present invention relates to the production of synthesis gas, more specifically to a method and system for production of synthesis gas from biomass by coking. The method relates to the technical field of production of synthesis gas or fuel gas using biomass. Synthesis gas is a mixture containing CO, H2and many carbohydrates (carbs), which contain carbon, hydrogen and oxygen. The synthesis gas obtained by the method according to the present invention can be used in gas turbine power plants, fuel cells, synthetic oil, metallurgical and other systems. BACKGROUND of INVENTION Since the reduction of the reserves of traditional fossil fuels (coal, oil and natural gas) and the problems of environmental pollution caused by the use of fossil fuels directly threaten the survival and development of mankind, granting importance to the development of renewable and environmentally friendly energy has become the consensus of the governments of all countries. Biomass, i.e. organic matter, formed by plants in photosynthesis, has many sources and is available in large quantities. It can be converted into a clean gas or liquid fuel for energy generation and production of industrial raw materials the chemical products. As the energy it is a clean and renewable energy with zero carbon dioxide emissions, and has the potential to completely replace fossil fuels as a new energy source that has become a priority for all countries. There are many ways of converting biomass into a clean gas or liquid fuel, including the technology of biomass gasification can be adapted to many species and has good prospects for expansion. Biomass gasification is a thermochemical process, i.e. biomass interacts with the gasification agent (such as air, oxygen, steam, carbon dioxide, etc.) at high temperature to obtain a mixed gas consisting of carbohydrate containing carbon, hydrogen and oxygen. The mixed gas is called synthesis gas. The components of the synthesis gas are determined by the connections of biomass used, the type of the gasification agent, the reaction conditions and the design used installations for the gasification. The purpose of gasification are, on the one hand, to minimize the consumption of materials and agents for gasification, and the resin content in the synthesis gas, and on the other hand, maximizing the efficiency of the gasification and the efficiency of conversion of carbon and the content of active ingredient (CO and H2in the synthesis gas. Goal by opredelyayutsya used gas generator, type the gasification agent, the particle size of the biomass, pressure and temperature gasification, as well as moisture and ash content in biomass, etc. Furnace for gasification used in the gasification process can be divided into three classes: fixed bed, fluidized bed and the furnace for gasification gasification stream. Furnace for gasification fixed bed has a simple structure gasification, it is convenient to operate, it has a flexible mode of operation, a higher proportion of conversion to carbon, wide range of operating load, which can vary from 20% to 110%, and solid fuel remains in the layer for a long period of time. However, temperature is not uniform, and her lower efficiency of heat exchange, low calorific value of the synthesis gas at the outlet, and the synthesis gas contains a large amount of resin. Furnace for gasification fluidized bed comfortable for the introduction of material and separation of the ash and the temperature is uniform, and its easy to adjust. However, it is sensitive to the characteristics of the original materials (raw materials). If you modify adhesion, heat resistance, moisture content or the melting temperature of ash initial materials, mode of operation will be abnormal. In addition, to ensure the normal formation of the fluidized bed in the furnace for gasifica the AI, you want to maintain a lower temperature, and the synthesis gas contains more resin. As in the furnace for gasification with a fixed and fluidized bed is formed a large amount of resin must be installed block for cracking of the resin and purification equipment, which leads to a complex process. Furnace for gasification gasification in the stream has a high and uniform operating temperature, good options, multiplication, and it is especially suitable for large-scale industrial applications. Resin Criciuma completely. However, the furnace for gasification gasification thread has strict requirements for the particle size of raw materials. Based on modern technologies of grinding, there is no way of chipping with a large number of cellulose, to particles of suitable size for gasification in the stream. Accordingly, the furnace for gasification gasification in the stream cannot be used for biomass gasification. Today the main problems in the development process of biomass gasification are cracking and pre-treatment of biomass prior to gasification. Chinese patent application No. 200510043836.0 discloses a method and apparatus for the gasification of biomass with low content of resin. The method includes the independent processes of pyrolysis and gasification, and biomass is and is converted into a synthetic gas with low tar. In this way pyrolytic gas and charcoal is subjected to incomplete combustion in the gasifier and tar krakeroy at high temperature. Although the content of the resin is significantly reduced, consumed a lot of charcoal, which leads to a low content of CO, formed in a subsequent reaction, recovery, and high content of CO2in the synthesis gas. Secondly, due to the low temperature combustion reaction temperature in the subsequent recovery becomes lower, and the average temperature in the reduction zone is less than 700°C, and therefore, the output effective synthesis gas (CO and H2) is significantly reduced (approximately 30%). Thirdly, ash and residue of unreacted carbon from the reaction of recovery are extracted directly, which leads to a low degree of conversion of carbon. Finally, the gasifier used in this way in the form of a fixed bed, as well as the reduction proceeds with the absorption of heat, the temperature difference between the top and bottom (at the top approximately 1000°C, and the bottom approximately 500°C) layers is huge, which is a characteristic lack of gasifiers fixed bed. U.S. patent No. 6863878B2 discloses a method and apparatus for producing synthesis gas from carbonaceous materials. The method includes p is ocessi coking (or pyrolysis and gasification independently from each other. In this way the temperature of the coking maintained at a level less than 450°F thus, to reduce the amount of tar formed as a result of pyrolysis. However, during the stage of hard coking products are crushed before transporting them to the reaction chamber of the gasifier, which would reduce the rate and extent of reaction of gasification. Secondly, since the gasification reaction proceeds in the reaction chamber will require a large amount of carrier gas, but the transport gas will take a lot of heat during transport, and, therefore, the efficiency of gasification is low, the temperature is uneven, and the subsequent regeneration system, waste heat massive. Thirdly, uneconomical, when only that the resulting synthesis gas is used to provide heat for the gasification and coking. Fourth, the products of combustion (mainly CO2and H2A) directly extract and not fully used, resulting in low efficiency of gasification. Finally, ash and residue of unreacted carbon in the synthesis gas also directly extract, which leads to a low degree of conversion of carbon. Chinese patent application No. 200810236639.4 discloses a method for production of synthesis gas from biomass by high temperature gasification. The method also uses to which the combination of carbonization (coking) and high-temperature gasification. However, the method has the following problems: first, heat for carbonizing furnace is supplied from the direct combustion of the external combustible gas and oxygen, introduced a high-quality external fuel gas greatly increases the power consumption of the system; secondly, it involved the supply of powder for the pyrolytic gas is difficult; when pyrolytic gas of high temperature is mixed with powdered carbon, low temperature and loaded into the gasifier, the mixture can easily condense to form resin, causing obstruction and disturbing the normal operation; finally, charcoal high-pressure formed in the carbonizing furnace, loaded into the mill for grinding at normal the pressure after decompression and cooling, in order to convert into powder, and then powdered carbon is compressed and fed into the gasifier pyrolytic gas. The whole process is complicated and consumes a large amount of energy, thus, the feasibility of the project is bad. Of the methods mentioned above traditional gasification of biomass or solid carbonaceous materials can not give synthesis gas with high efficiency at a low cost. Although the technology is independent of pyrolysis and gasification can use different biomass and to reduce the content of the malls in the synthesis gas, but the disadvantages, such as non-uniform temperature, a large investment in equipment waste heat recovery, high material consumption, low efficiency of gasification and low degree of conversion of carbon, limit the application of biomass gasification in the industry. In particular, there is no efficient way gasification of biomass using gasifier gasification in the stream. BRIEF description of the INVENTION In view of the above problems, one of the purposes of the present invention is the provision of a method and system to produce synthesis gas from biomass carbonization, which have high efficiency and low cost. The technical scheme of the present invention are described below: method for production of synthesis gas from biomass carbonization, where the method includes the following stages: 1) pre-processing the source material of the biomass; 2) conduct low-temperature carbonization with the receipt of the products in the form of pyrolytic gas and charcoal, cooling of the charcoal at the output of the carbonizing furnace to a temperature of 60-280°C, and transportation of chilled charcoal in the hopper for storing charcoal; 3) Department of pyrolytic gas from powdered charcoal after the withdrawal of the pyrolytic gas from the top is the second part of the carbonizing furnace to pass through gazoadsorbtsionnoi separator; 4) shipping parts separated pyrolytic gas in the layer of combustion for combustion, heat another part separated pyrolytic gas hot flue gas generated during combustion of a layer of combustion, and then shipping the heated pyrolytic gas carbonizing furnace as a heat source for carbonizing furnace; shipping hot exhaust flue gas after heat exchange in the pre-treatment of raw material biomass for drying; filing separated powdered charcoal into the hopper for storing charcoal; 5) grinding powdered charcoal to obtain a suspension; and 6) introduction of coal slurry using a high-pressure pump for coal suspension in the furnace for gasification for the implementation of gasification. In the method for production of synthesis-gas low-temperature carbonization is a slow pyrolysis is conducted under conditions of atmospheric pressure and isolation from oxygen in the carbonizing furnace, with the temperature in the carbonizing furnace regulate by changing the proportion of pyrolytic gas and air at the level of 200-400°C, the rate of temperature rise in the carbonizing furnace is maintained at a level of 5-20°C/min and the retention time of the original biomass materials in the chamber supported at the level of 20-90 minutes In the way the AZMOL powdered charcoal to obtain a suspension is provided atmospheric refining, and then in the mill served the water and additive to obtain a suspension of charcoal. In the method for production of synthesis gas content of powdered charcoal in a charcoal suspension is 50-70 wt.%, preferably 60-65 wt.%. In the method for production of synthesis-gas temperature carbonizing furnace is maintained at 250°C±10°C, the rate of temperature rise in the carbonizing furnace is preferably maintained at 15°C/min and holding time of the original biomass materials in the furnace is preferably supported at the level of 50 minutes The gasification system to produce synthesis gas from biomass by pyrolysis section includes pre-processing the source material of biomass carbonizing furnace, furnace for gasification, a connecting pipe connecting the carbonizing furnace and the furnace for gasification, and a pneumatic transport system. The upper part of the carbonizing furnace is connected with a cyclone separator; exit cyclone separator is connected to the layer of combustion and a tank for storing charcoal; the output layer of combustion connected with the heat exchanger to heat the recycled pyrolysis gas; and the output of the heated pyrolytic gas is connected with a carbonizing oven, and the output gave the heat exhaust flue gas is connected to the drying system. The system is unifikacii water-cooled screw conveyor is in the pipeline in the direction from the output of charcoal from the carbonizing furnace to the bunker for storage of charcoal, and water-cooled screw conveyor is used for cooling of the charcoal on the yield of charcoal from the carbonizing furnace to 60-280°C, and then cooled charcoal in the hopper for storing charcoal. In the gasification system, the mill, the capacity for suspension of charcoal and a high pressure pump for the suspension of charcoal are consistently located on the pipeline from the outlet of the hopper for storage of charcoal to carbonizing furnace. In the system of gas supply pipe for supplying gas inlet for the layer of combustion connected with the duct, and the air is used as the gas that supports combustion. The advantages of the present invention is given below. First, using low-temperature technology of slow pyrolysis, on the one hand, wood fiber biomass can significantly destroy the biomass is easily ground, the energy consumption is reduced, and the volumetric energy density of biomass is increased; on the other hand, compared with the method of gasification of a patent application China 200810236639.4 at lower temperatures, particularly at temperatures of 250°C±10°C, can be obtained in higher yield of solids and a higher energy output (the mass yield of charcoal is 60-80%, and the energy output of dreven the th coal is 70-90%), energy consumption is reduced, and the degree of conversion of the carbon of the entire system favorably increases. Secondly, the present invention uses heat reusable pyrolytic gas as a heat source for carbonizing furnace through the use of heat produced by the combustion of spontaneously formed pyrolytic gas. Heating technology carbonizing furnace of the present invention has the following three factors: 1) the heat required for the pyrolysis technology, is provided in the inner part of the system so as to realize thermal equilibrium of the system and not to let external energy; 2) heat to heat the recycled pyrolysis gas is provided by direct combustion of pyrolysis gas and air. In other words, uses the chemical energy pyrolytic gas, and on the other hand, instead of pure oxygen is air, which greatly reduces the cost of the entire system and increases process flexibility carbonizing furnace; 3) the heated recycled pyrolysis gas directly served in a carbonizing furnace for contact with the source material, which not only increases the efficiency of the heating carbonizing furnace, but also supports the normal operation of the d the I the highest yield of charcoal under atmospheric pressure, isolation from oxygen and slow pyrolysis. Thirdly, the present invention uses hot exhaust flue gas generated by the combustion of pyrolysis gas for drying of the raw material, therefore increasing the energy efficiency of the entire system. Fourth, using the technology of suspension atmospheric refining, charcoal output of the carbonizing furnace is introduced into the mill atmospheric operatora, and then mixed with a certain amount of water and additives to obtain coal suspension. This process is simple and effective. Compared with the method of gasification of a patent application China No. 200810236639.4 downloading from the input method according to the present invention significantly reduces the energy consumption of the input source material and increases the stability, reliability and technical implementation of the system. Fifthly, the present invention uses compression technology and transportation of coal slurry pump. Compared with the method of gasification of the patent 200810236639.4 this method avoids the technical problems associated with pneumatic transport of powder and clogging of the resin when loading dry powdered coal, and also increases the stability, reliability and technical Rea is Itachi system. Briefly, the present invention aims to implement a simple, reliable, energy-saving, cost-effective project with a high possibility of technical implementation. At the same time, the present invention increases the efficiency of the gasification reduces the number of effective synthesis gas and increases the rate of conversion of energy in the system. BRIEF DESCRIPTION of DRAWINGS In Fig. 1 shows the diagram of a method and system for production of synthesis gas from biomass by carbonization in accordance with one embodiments of the present invention. DETAILED DESCRIPTION of embodiments of the INVENTION Preferred examples of the technological scheme of the method and system of the present invention is described on the attached drawing. As shown in figure 1, the gasification system of the present invention includes an inlet 1 for delivery of the original biomass material, the drying system 2, a hopper 3 for storing biomass carbonizing furnace 4, a cyclone separator 5, the duct 6 for the layer burning, layer 7 combustion, the compressor 8, the heat exchanger 9 for heating the recycled pyrolysis gas duct 10 for exhaust of hot flue gas for drying, water-cooled screw conveyor 11, a hopper 12 for storing charcoal, mill 13, in which aproved 14 to obtain a suspension for mills, additional pipeline 15 to the mill, capacity 16 for the coal slurry, the pump 17 high pressure coal suspension, the pipeline 18 to oxygen for injection burner furnace for gasification, the nozzle 19 of the nozzle furnace for gasification furnace 20 for gasification, water-cooled wall 21 of the furnace for gasification, line 22 to the synthesis-gas piping 23 for residual ash, pipeline 24 for desalted and deoksigenirovanii water pipeline 25 for saturated steam, the pipeline N1 for external fuel and exhaust manifold N2. In the gasification system, the upper part of the carbonizing furnace 4 is connected with a cyclone separator 5, and the outlet end of the cyclone separator 5 is connected to the layer 7 of the combustion chamber with the hopper 12 for storing charcoal respectively. The outlet end of the layer 7 of the combustion chamber is connected to the heat exchanger 9 for heating reusable pyrolytic gas. The outlet for the heated pyrolytic gas is connected with a carbonizing oven 4, and an outlet for exhaust heated flue gas is connected to the system 2 drying. Water-cooled screw conveyor 11 is in the pipeline from the outlet for charcoal carbonizing furnace 4 to the hopper 12 for storing charcoal and is used for cooling the charcoal output for charcoal carbonization the Oh furnace to 60-280°C, and then for the chilled charcoal in the hopper 12 for storing charcoal. Mill 13, the container 16 for the coal slurry and pump 17 high pressure coal suspension is located on the pipeline sequentially from the exit of the hopper 12 for storing charcoal to the furnace 20 for gasification. Pipe for supplying gas inlet for the layer 7 of the combustion chamber is connected to the duct 6, and the air used to support combustion of the gas. Method for production of synthesis gas from biomass carbonization process involves the following stages: 1) pre-processing the source material of the biomass; 2) conduct low-temperature carbonization with obtaining products - pyrolytic gas and charcoal, cooling of the charcoal at the output of the carbonizing furnace to a temperature of 60-280°C, and transportation of chilled charcoal in the hopper for storing charcoal; 3) Department of pyrolytic gas from powdered charcoal after the withdrawal of the pyrolytic gas from the upper part of the carbonizing furnace to pass through gazoadsorbtsionnoi separator; 4) shipping parts separated pyrolytic gas in the layer of combustion for combustion, heat another part separated pyrolytic gas hot flue gas formed by burning layer combustion in Teploobmen is nick, and then the delivery of heated pyrolytic gas carbonizing furnace as the heat source for carbonizing furnace; shipping hot exhaust flue gas after heat exchange in the pre-treatment of raw material biomass for drying; filing separated powdered charcoal into the hopper for storing charcoal; 5) grinding powdered charcoal to obtain a suspension; and 6) introduction of coal slurry into the furnace for gasification using high-pressure pump for coal suspension, for the implementation of gasification. Low-temperature carbonization is slow pyrolysis is conducted under conditions of atmospheric pressure and isolation from oxygen in the carbonizing furnace, with the temperature of the carbonizing furnace is maintained at the level of 200-400°C, adjusting the proportion of pyrolytic gas and air, the rate of temperature rise carbonizing furnace regulate in the range of 5-20°C/min and the retention time of the original biomass materials in the furnace regulate in the range of 20-90 minutes the temperature of the carbonizing furnace is preferably maintained at 250°C±10°C, the rate of temperature rise in the carbonizing furnace is preferably maintained at 15°C/min and the retention time of the original biomass materials in an oven, preferably on the support is preferably equal to 50 minutes In the method of grinding powdered charcoal with getting the suspension applied atmospheric refining, and then add water and additives for grinding with obtaining coal suspension. The content of powdered charcoal in a charcoal suspension is 50-70 wt.%, preferably 60-65 wt.%. The process works: 1. The system startup process: 1) open the control valve V1 on the pipeline from a hopper 3 for the storage of biomass to carbonizing furnace 4 and the control valve V4 on the exhaust pipe N2 and hold closed control valve V2 in the layer 7 combustion and control valve V3 on the pipeline from the cyclone separator 5 to the compressor 8; 2) open the control valve V6 pipeline N1 for external fuel regulating valve V5 to the duct 6 to the layer of combustion, and the valve V8 to the pipeline from the layer 7 of combustion to a carbonizing furnace 4 and the control valve V9 to the pipeline from layer 7 to the combustion system 2 drying and keep closed control valve V7 on the pipeline from the layer 7 of combustion to the heat exchanger 9 for heating the recycled pyrolysis gas, thus ensuring the flow of hot flue gas resulting from combustion of fuel and air in the layer 7 of the combustion system 2 drying and carbonizing furnace to provide energy; and 3) after 20-40 minutes of work on the way from stage 1) stage 2) open control valves V2, V3 and V7, simultaneously closing the control valves V4, V6, V8 and V9, so that the system at the same time beginning to work normally. 2. The normal process of how the system works: Source material biomass is loaded into the drying system 2 input channel 1 supply of the source material biomass. The source material of the biomass is dried and dehydrated hot smoke in the system, and then transported to a hopper 3 for biomass storage, and source material biomass is served in a carbonizing furnace 4. Product carbonizing furnace 4 includes pyrolytic gas and charcoal containing CO, H2, CO2H2O, CH4and resin. Raw pyrolytic gas separated in the cyclone separator 5, and then the particles of charcoal in the raw pyrolysis gas is fed into the hopper 12 for storing charcoal and pyrolytic gas after pre-cleaning is loaded into the layer of combustion 7 and the compressor 8. In the layer of combustion 7 pyrolytic gas for combustion is subjected to combustion with air from the pipeline 6. Hot smoke generated during combustion, heats the circulating pyrolytic gas; setting the share of pyrolytic gas formed during combustion with air, the temperature carbonizer the Onna furnace 4 regulate at the level of 400-600°C, and the rate of temperature rise carbonizing furnace 4 regulate at the level of 5-20°C/min After introduction into the compressor 8 to increase the pressure of reusable pyrolytic gas is heated to a certain temperature in the heat exchanger 9 to heat the recycled pyrolysis gas, and then heated recycled pyrolysis gas enters the carbonizing furnace 4 to ensure that it is the energy required for carbonizing furnace, the hot flue gas after heat exchange is supplied to the system 2 drying for drying raw materials biomass. Charcoal is formed in the carbonizing furnace 4, fed into the hopper 12 for storing charcoal deposited after cooling to water-cooled screw conveyor 11. Charcoal is fed into the mill 13 to grind with the water from the water pipe 14 with getting suspension for grinding and the addition of the pipe 15 for supplements to grind with obtaining coal suspension. Received coal slurry is injected into the container 16 for the coal slurry, and then by means of a pump 17 high pressure coal suspension is served in the injection burner 19 of the furnace for gasification after raising the pressure of the coal slurry to the working pressure in the furnace for gasification 20. Oxygen from pipe 18 to oxygen also dostavljajut injection burner 19 of the furnace for gasification for the reaction of high-temperature gasification furnace 20 for gasification, as the temperature of the synthesis gas at the outlet of the furnace for gasification supported at the level of 1200-1600°C, adjusting the amount of oxygen and the amount of heat in the heat exchange with the water-cooled wall 21 (furnace for gasification), which is injected desalted and obeskislorozhennuju water. The gasification products are mainly CO and H2, a small amount of CO2and H2O and a small amount of CH4; desalted and obeskislorozhennaja water forms a high-pressure saturated steam after absorbing the heat of the water cooled wall 21 of the furnace for gasification, high-pressure saturated steam enters the downstream system through the pipeline 25 for saturated steam, and ash formed during gasification, remove the pipe 23 for the remainder of the ash. Example 1 As a source of biomass material used wood. Elemental composition and characteristics of dried wood are presented in table 1. /tr>
Have established the following primary operating conditions: 1) the water content of the material at the exit of the system 2 drying was 15 wt.%; 2) the pressure in the carbonizing furnace 4 was atmospheric pressure, and the temperature in the carbonizing furnace 4 was maintained at a level of 200°C; 3) the rate of growth temperature in the carbonizing furnace 4 was maintained at 20°C/min; 4) the retention time of the original biomass materials in an oven maintained at 90 min; 5) high-temperature charcoal was cooled to 60°C for water-cooled screw conveyor 11; and 6) the pressure in the furnace 20 for gasification was maintained at a level of 4.0 MPa (A), and the temperature in the furnace 20 for gasification was maintained at a level of 1400°C. According to the specified conditions in the implementation illustrated in the accompanying drawings system master data and system performance parameters were as follows: 1) the mass yield of charcoal from the original biomass materials introduced into the carbonizing furnace 4 was 75%; 2) in the synthesis gas, the output on line 22 to synthesis gas, the content of CO and H2was 78%; 3) the degree of the envelopes is these carbon in the gasification system was 99.9%, the and the consumption of oxygen available synthesis gas was 0.33 mol/mol. Example 2 As the source material of the biomass (table 1) used the wood from example 1. Have established the following primary operating conditions: 1) the water content of the material at the exit of the system 2 drying was 10 wt.%; 2) the pressure in the carbonizing furnace 4 was atmospheric pressure, and the temperature in the carbonizing furnace 4 was maintained at a level of 300°C; 3) the rate of temperature rise in the carbonizing furnace 4 was maintained at 10°C/min; 4) the retention time of the original biomass materials in an oven maintained at 80 min; 5) high-temperature charcoal was cooled to 60°C for water-cooled screw conveyor 11; and 6) the pressure in the furnace 20 for gasification was maintained at a level of 4.0 MPa (A), and the temperature in the furnace 20 for gasification was maintained at a level of 1400°C. According to the specified conditions in the implementation illustrated in the accompanying drawings system master data and system performance parameters were as follows: 1) the mass yield of charcoal from the original biomass materials introduced into the carbonizing furnace 4 was 80%; 2) in the synthesis gas, the output on line 22 to synthesis gas, the content of CO and H2was 82%; 3) frame the conversion of carbon in the gasification system was 99.9%, the and the consumption of oxygen available synthesis gas was 0.32 mol/mol. Example 3 As the source material of the biomass (table 1) used the wood from example 1. Have established the following primary operating conditions: 1) the water content of the material at the exit of the system 2 drying was 20 wt.%; 2) the pressure in the carbonizing furnace 4 was atmospheric pressure, and the temperature in the carbonizing furnace 4 was maintained at 400°C; 3) the rate of temperature rise in the carbonizing furnace 4 was maintained at 5°C/min; 4) the retention time of the original biomass materials in the furnace was maintained at a level of 30 min; 5) high-temperature charcoal was cooled to 60°C for water-cooled screw conveyor 11; and 6) the pressure in the furnace 20 for gasification was maintained at a level of 4.0 MPa (A), and the temperature in the furnace 20 for gasification was maintained at a level of 1400°C. According to the specified conditions in the implementation illustrated in the attached drawings system master data and system performance parameters were as follows: 1) the mass yield of charcoal from the original biomass materials introduced into the carbonizing furnace 4 was 70%; 2) in the synthesis gas, the output on line 22 to synthesis gas, the content of CO and H2was 75%; 3) extent the ü conversion of carbon in the gasification system was 99.9%, the and the consumption of oxygen available synthesis gas was 0.34 mol/mol. Example 4 As the source material of the biomass (table 1) used the wood from example 1. Have established the following primary operating conditions: 1) the water content of the material at the exit of the drying system 2 was 12 wt.%; 2) the pressure in the carbonizing furnace 4 was atmospheric pressure, and the temperature in the carbonizing furnace 4 was maintained at 250°C; 3) the rate of temperature rise in the carbonizing furnace 4 was maintained at 15°C/min; 4) the retention time of the original biomass materials in an oven maintained at 40 min; 5) high-temperature charcoal was cooled to 60°C for water-cooled screw conveyor 11; and 6) the pressure in the furnace 20 for gasification was maintained at a level of 4.0 MPa (A), and the temperature in the furnace 20 for gasification was maintained at a level of 1400°C. According to the specified conditions in the implementation illustrated in the attached drawings system master data and system performance parameters were as follows: 1) the mass yield of charcoal from the original biomass materials introduced into the carbonizing furnace 4 was 82%; 2) in the synthesis gas, the output on line 22 to synthesis gas, the content of CO and H2was 84%; 3) frame the conversion of carbon in the gasification system was 99.9%, the and the consumption of oxygen available synthesis gas was 0.31 mol/mol. Example 5 As the source material of the biomass (table 1) used the wood from example 1. Have established the following primary operating conditions: 1) the water content of the material at the exit of the drying system 2 was 16 wt.%; 2) the pressure in the carbonizing furnace 4 was atmospheric pressure, and the temperature in the carbonizing furnace 4 was maintained at a level of 220°C; 3) the rate of temperature rise in the carbonizing furnace 4 was maintained at 12°C/min; 4) the retention time of the original biomass materials in an oven maintained at 50 min; 5) high-temperature charcoal was cooled to 60°C for water-cooled screw conveyor 11; and 6) the pressure in the furnace 20 for gasification was maintained at a level of 4.0 MPa (A), and the temperature in the furnace 20 for gasification was maintained at a level of 1400°C. According to the specified conditions in the implementation illustrated in the attached drawings system master data and system performance parameters were as follows: 1) the mass yield of charcoal from the original biomass materials introduced into the carbonizing furnace 4, 85%; 2) in the synthesis gas, the output on line 22 to synthesis gas, the content of CO and H2was 86%; 3) frame the conversion of carbon in the gasification system was 99.9%, the and the consumption of oxygen available synthesis gas was 0.3 mol/mol. Example 6 As the source material of the biomass (table 1) used the wood from example 1. Have established the following primary operating conditions: 1) the water content of the material at the exit of the drying system 2 was 18 wt.%; 2) the pressure in the carbonizing furnace 4 was atmospheric pressure, and the temperature in the carbonizing furnace 4 was maintained at a level of 320°C; 3) the rate of temperature rise in the carbonizing furnace 4 was maintained at a level of 18°C/min; 4) the retention time of the original biomass materials in the furnace was maintained at a level of 70 min; 5) high-temperature charcoal was cooled to 60°C for water-cooled screw conveyor 11; and 6) the pressure in the furnace 20 for gasification was maintained at a level of 4.0 MPa (A), and the temperature in the furnace 20 for gasification was maintained at a level of 1400°C. According to the specified conditions in the implementation illustrated in the attached drawings system master data and system performance parameters were as follows: 1) the mass yield of charcoal from the original biomass materials introduced into the carbonizing furnace 4, was 78%; 2) in the synthesis gas, the output on line 22 to synthesis gas, the content of CO and H2was 81%; 3) frame the conversion of carbon in the gasification system was 99.9%, the and the consumption of oxygen available synthesis gas was 0.32 mol/mol. 1. Method for production of synthesis gas from biomass carbonization, comprising the following stages: 2. The method according to claim 1, where in the method of grinding powdered charcoal to obtain a suspension uses atmospheric grinding and mill add water and additive. 3. The method according to claim 1 or 2, where the content of powdered charcoal in a charcoal suspension is 50-70 wt.%. 4. The method according to claim 1 or 2, where the temperature in the carbonizing furnace is maintained at 250°C±10°C, the rate of temperature rise in the carbonizing furnace is maintained at 15°C/min and the retention time of the original biomass materials in an oven maintained at 50 minutes 5. The method according to claim 1 or 2, where the content of powdered charcoal in a charcoal suspension is 60-65 wt.%. 6. System Ghazi the paths to produce synthesis gas from biomass by pyrolysis using the method according to any one of claims 1 to 6, including 7. The gasification system according to claim 6, where water-cooled screw conveyor (11) is in the pipeline from the output of coal from the carbonizing furnace (4) to the hopper (12) for storing charcoal and water-cooled screw conveyor (11) is used for cooling of the charcoal on the yield of charcoal from the carbonizing furnace to 60-280°C, and then cooled charcoal in the hopper (12) for storing charcoal. 8. The gasification system according to claim 6 or 7, where the mill (13), capacity (16) for the coal slurry and pump (17) high on the means for the coal slurry are consistently on the pipeline from the outlet of the hopper (12) for storing charcoal to the furnace (20) for gasification. 9. The gasification system according to claim 6 or 7, where the input pipe for gas supply in the layer (7) of combustion connected with the duct (6)and the air used to support combustion of the gas.
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