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    • 专利摘要:
    Process and system for the production of synthetic gas from pyrolysis biomass - A process and system for the production of synthetic gas from pyrolysis biomass are disclosed. The process comprises the following steps: 1) pre-treatment of biomass feedstock (1), 2) pyrolysis of biomass feedstock (1) by means of rapid biomass pyrolysis technology to obtain a gas of pyrolysis and carbon powder in a pyrolysis bed (5), 3) separating the pyrolysis gas, carbon powder and a heat carrier by a cyclone type separator (6), and 4) separating the carbon powder to from the cyclic heat transpotator through a solid-solid separator (7), with the carbon powder being collected by means of a coal dust loading funnel (8) and the solid heat carrier to be recycled in the pyrolysis bed (5) after being heated in a heated fluidized bed carrier (9-2); 5) supplying the generated pyrolysis gas to a condensation condensing reservoir (12) sprayed with the condensable portion of the condensed pyrolysis gas to produce the biofuel oil which is compacted by a high pressure oil pump 917) and then introduced into a gasification furnace (20) to be gasified, and 6) providing one part of the noncondensed pyrolysis gas with a combustion bed (9-1) for combustion with air, delivering the other part to the pyrolysis bed. (5) as an average fluidization. The raw material is directly dried using hot flue gas produced by the heated fluidized bed conveyor (9-2). The heat generated by combustion of the noncondensed pyrolysis gas produced by the pyrolysis bed (5) with air in the combustion bed (9-1) is supplied to the pyrolysis bed (5).
    公开号:BR112012024082B1
    申请号:R112012024082-0
    申请日:2011-03-23
    公开日:2018-08-07
    发明作者:Kan SONG；Manyi Jiang；Qin Sun；Shirong Zhang；Haiqing Zhang；Jinqiao Zhang
    申请人:Wuhan Kaidi Engineering Technology Research Institute Co., Ltd.；
    IPC主号:
    专利说明:

    (54) Title: PROCESS AND SYSTEM FOR THE PRODUCTION OF SYNTHETIC GAS FROM PYROLYSIS BIOMASS (51) Int.CI .: C10J 3/66; C10B 53/02; C10B 57/10; C10B 49/22; C01B 3/36 (30) Unionist Priority: 23/03/2010 CN 201010132481.3 (73) Holder (s): WUHAN KAIDI ENGINEERING TECHNOLOGY RESEARCH INSTITUTE CO., LTD (72) Inventor (s): SONG, KAN; JIANG, MANYI; SUN, QIN; ZHANG, SHIRONG; ZHANG, HAIQING; ZHANG, JINQIAO (85) National Phase Start Date: 24/09/2012
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    PROCESS AND SYSTEM FOR THE PRODUCTION OF SYNTHETIC GAS FROM BIOMASS BY PYROLYSIS
    FIELD OF THE INVENTION
    The invention relates to the production of synthetic gas, and more particularly to a method and system for the production of synthetic gas from biomass by pyrolysis. The method belongs to the field of synthetic gas or gas fuel technology using biomass. Synthetic gas is a mixed gas that contains CO, H2 and a variety of carbohydrates that contain carbon, hydrogen and oxygen. The synthetic gas produced by the method according to the invention can be used for gas turbines to generate power systems, fuel cells, synthetic oil, metallurgical and other systems.
    STATUS OF THE TECHNIQUE OF THE INVENTION
    With the decrease in reserves of traditional fossil fuels (coal, oil and natural gas) and the problems of pollution of the environment, caused by the use of fossil fuels, directly threaten human survival and its development, showing the importance of the development of renewable energies and that do not harm the environment have become a consensus of governments in all countries. Biomass, an organic matter generated by plants through photosynthesis, has large sources and large quantities available. It can be transformed into clean gas or liquid fuel for energy production, producing raw materials and chemicals. While this energy is clean, renewable, with zero carbon dioxide emissions and the potential to completely replace fossil fuels as a source of new energy, it has become a priority issue for all countries.
    There are many methods for transforming biomass into clean gas or liquid fuel, among which biomass gasification technology can adapt to a wide variety of species and has good expandability. Biomass gasification is a thermochemical process, that is, the biomass reacts with a gasification agent (such as air, oxygen, steam, carbon dioxide, etc.), under high temperature conditions to produce a mixed gas consisting of carbohydrates, containing carbon, hydrogen and oxygen. The gas mixture is called synthetic gas. The components of the synthetic gas are decided by the type of biomass used, the type of gasification agent, the reaction conditions, and the structure of a gasifier used there. The objective of gasification is, on the one hand, to minimize the consumption of materials and the gasification agent, as well as the tar content contained in the syngas, on the other hand, to maximize the efficiency of gasification and the efficiency of carbon conversion, as well as the content the
    2/16 active ingredient (CO H2), contained in synthetic gas. The objectives are decided by the type of gasifier used, the type of gasification agent, the size of the biomass particle, the pressure of the gasification and the temperature, the humidity and ash of the biomass, etc.
    The gasification oven used in the gasification process can be divided into three classes: fixed bed, fluidized bed, dragged flow bed. The fixed bed has a simple gasification structure, the convenience operation, the flexible operation mode, a higher carbon conversion rate, a wide range of load operation, which can be between 20% and 110%, remaining the fuel solid in bed for a long period of time. However, the temperature is not uniform and has a lower heat exchange efficiency, a low heating value of synthetic gas at the air outlet, and synthetic gas containing a large amount of tar. The fluidized bed is convenient for adding ash release material, the temperature is uniform and easier for adjustments. However, it is sensitive to the characteristics of the raw material. If the adhesion, thermal stability, moisture content or melting point of the ashes with the raw materials change, the operation will become abnormal. In addition, in order to ensure the normal fluidity of the gasification oven, it is necessary to keep the temperature lower, and the synthetic gas has a large amount of tar. Since a large amount of tar is produced in the fixed bed and in the fluidized bed, a tar cracking unit and purification equipment must be installed, which results in a complicated process. The entrained flow bed has a constant and high operating temperature, good amplification characteristics, and particularly suitable for large scale industrialization. The tar is completely cracked. However, the entrained flow bed has a strict particle size requirement of the raw materials. Based on current milling technology, there is no way to mill the biomass having too much cellulose to a size suitable for the entrained flow bed. Thus, the entrained flow bed cannot be used for biomass gasification. Today, tar breakage and pre-treatment of biomass before gasification are difficult problems for the development of biomass gasification.
    Chinese patent application No. 200510043836.0 describes a method and device for the gasification of low tar biomass. The method includes pyrolysis and gasification independently, with the biomass being transformed into synthetic gas containing low tar content. In the method, pyrolysis gas and coal experience incomplete combustion in the gasifier at around 1000 ° C, the tar being cracked under high temperature conditions. Although the tar content
    3/16 reduce a lot, a large amount of coal is consumed, which results in a low CO content produced in the subsequent reduction reaction and a high CO2 content in the synthetic gas. Second, due to a low temperature in the combustion reaction, the temperature in the subsequent reduction becomes lower, and the average temperature in the reduction zone is less than 700 ° C, and thus the effective synthetic gas yield ( CO H2) is significantly decreased (around 30%). Third, ash and carbon residues that did not react from the reduction reaction are directly discharged, resulting in a low rate of carbon conversion. Finally, the gasifier used in the method is in the form of a fixed bed, since the reduction reaction absorbs heat, the temperature difference between the top and the bottom (the top is about 1000 ° C and the bottom is about 500 ° C) the bed is huge, which is an inherent disadvantage of fixed bed.
    U.S. Patent No. 6,863,878 B2 describes a method and device for producing synthetic gas with carbon containing materials. The method includes carbonization (or pyrolysis) and gasification in independent forms. In the method, the carbonization temperature is controlled at less than 450 ° F, in order to reduce the tar content resulting from pyrolysis. However, during the carbonization phase, the solid products are not ground before being transported to the gasification reaction coils, which will affect the speed and degree of reaction of the gasification. Secondly, since the reaction and gasification take place in the reaction coil, a large amount of carrier gas is required, but the carrier gas will take out a large amount of heat during transport and thus the efficiency of the gasification it is low, the temperature is not uniform and the subsequent loss of waste from the heat recovery system is enormous. Third, it is not economical for newly produced synthetic gas to be used to provide heat for gasification and carbonization. Fourth, combustion products (mainly CO2 and H2O) are directly discharged if not fully utilized, resulting in low gasification efficiency. Finally, ash and carbon residues that have not reacted in the synthetic gas are also directly discharged, resulting in a low rate of carbon conversion.
    Chinese patent application No. 200810236639.4 discloses a method of producing synthetic gas from biomass by high temperature gasification. The method also adopts a combination of carbonization and high temperature gasification. However, the method has the following problems: first, the heat from the carbonization furnace is provided by direct combustion of the external fuel gas and oxygen; the high-quality external fuel gas introduced increases
    4/16 considerably the energy consumption of the system; secondly, the pyrolysis gas adopted in the powder feed system is complicated, when the high temperature pyrolysis gas is mixed with the low temperature carbon powder and fed into the gasification oven, the mixture can be easily condensed to form tar, causing blockage and influencing normal operation; and, finally, the high pressure _ produced in the carbonization furnace is fed into the normal pressure milling machine after being decompressed and cooled, so that it becomes powder and then the carbon powder is pressurized and fed to inside the pyrolysis gas gasification furnace. The whole process is complicated and high in energy consumption so that the project's viability is poor.
    From the aforementioned methods, conventional gasification, whether from biomass or from solids containing carbon materials, cannot produce synthetic gas with high efficiency and low cost. Although the independent pyrolysis and gasification technology can adapt to a variety of biomass and reduce the tar content of the synthetic gas, deficiencies such as the non-uniform temperature, the large investment in equipment for heat recovery, consumption high-efficiency material and low carbon conversion rate gasification limit the application of biomass gasification in industry. In particular, there is no effective method for gasification with biomass being applied to a entrained bed stream.
    SUMMARY OF THE INVENTION
    In view of the problems described above, it is an objective of the present invention to provide a method and a system for the production of synthetic gas from biomass by pyrolysis, which have high efficiency and low cost.
    The technical scheme of the invention is described as follows.
    A method for producing synthetic gas from biomass by pyrolysis comprising the following steps;
    1) a pre-processing of a raw biomass material: crush the raw biomass material to have particle sizes of 1-6 mm and drying the raw material until the water content is 10-20 wt. %;
    2) pyrolysis of the crude biomass material using rapid biomass pyrolysis technology, and a product of a pyrolysis bed being a pyrolysis gas and a carbon powder;
    3) separating the pyrolysis gas from carbon powder, and a solid heat carrier through a cyclone separator;
    4) separate the carbon powder away from the heat carrier through a
    5/16 solid-solid separator, feeding the carbon powder to a carbon powder stock tray for collection, heating the solid heat carrier in a heating fluidized bed and transmitting the heat carrier to the solid to the bed from pyrolysis to the use of recycling; transmitting a residual heat smoke generated in the heated fluidized bed conveyor to dry the raw biomass material from step 1);
    5) transmit the pyrolysis gas to a condensed tank for the spray condensation, condensing a condensable part in the pyrolysis gas to generate biofuel oil, pressurizing the biofuel oil generated by a high pressure oil pump and then feeding the gasification furnace to be aerated; and
    6) feeding a part of non-condensable pyrolysis gas to the combustion bed, to make combustion with air, transmitting the other part of the non-condensing pyrolysis gas to the pyrolysis bed as a medium fluidity; control the relationship between the non-condensable air pyrolysis gas and the temperature of the fluidized bed warming carrier as in step 6), to make sure that the temperature of the pyrolysis bed is 400-600 ° C and resides in the gas phase in the pyrolysis bed being 0.5-5 s.
    Spray condensation adopts an external circular method, the biological fuel oil at the bottom of the condensation tank is pressurized and pumped by the oil pump, the biological fuel oil is returned to the condensation tank for spray condensation after it has been cooled by a biofuel from the oil heat exchanger, the condensable pyrolysis gas is condensed to produce the biofuel oil, part of the biofuel oil is fed into the biofuel oil tank the other part is pressurized by the circulation pump of oil and cooled until the heat exchanger biofuel into the oil circularly spray the pyrolysis gas.
    A gasification system for the production of synthetic gas from biomass by biomass pyrolysis comprises a pretreatment part material, a pyrolysis part, a condensation part, and a gasification part. The pyrolysis part includes a pyrolysis bed and a combustion bed; a condensation tank of the condensed part is connected to a non-condensable pyrolysis gas compressor, by means of a pipeline; an outlet of the non-condensable pyrolysis gas compressor is connected to the pyrolysis bed and the combustion bed respectively; a non-condensable pyrolysis gas is used as a combustion bed fuel, and a pyrolysis bed fluidity medium.
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    The condensing part adopts spray condensation in external circulation. The lower part of the condensation tank is connected with a circulating oil pump through a conduit, and the oil circulating pump is connected to the external oil heat biofuel exchanger, a part of the combustible biological oil is pressurized by circulating oil pump and cooled by the biological fuel oil heat exchanger, in order to circulate and spray the pyrolysis gas, just as a lower part of the condensation tank is connected with the biological fuel oil tank.
    The pyrolysis bed is connected with the cyclone separator and the solid-solid separator. The solid-solid separator is connected with the powdered carbon storage compartment and the carrier heating fluidized bed. The lower part of the carrier heating fluidized bed is provided with a conduit connected to the pyrolysis bed, in order to transmit the heated solid carrier to the pyrolysis bed for recycling use.
    The upper part of the heating transport fluidized bed is connected with a drying system for the biomass material, the pre-processing part through a residual heat and smoke pipeline, and an upper part of the combustion bed is connected with a air inlet conduit.
    The connection of an outlet pipeline from the biological fuel oil tank and a gasification oven is provided with the high pressure oil pump, and the biological fuel oil is pressurized and transported to the gasification oven for gasification.
    The advantages of the invention are summarized below:
    First, the invention adopts fast pyrolysis technology. Compared to the gasification method disclosed in Chinese patent application No. 200810236639.4, the invention can directly transform biomass into biofuel oil, which improves the energy density of the biomass volume and makes transportation and storage convenient; on the other hand, the high energy yield (60-80%) can be achieved at a temperature of 400-600 ° C, which reduces energy consumption and can also improve the carbon conversion rate of the entire system.
    Second, the invention also adopts the technology of heating the solid cyclic heat carrier as a source of heat for the pyrolysis bed by means of the heat generated by the combustion of the self-production of non-condensable pyrolysis gas. The heating technology of the pyrolysis bed of the invention has the following three aspects: 1) the heat necessary for the pyrolysis technique is provided by the internal part of the system, in order to achieve the thermal balance of the system and not to introduce
    7/16 external energy fundamentally; 2) the heat for heating the solid cyclic heat carrier is provided by direct combustion of the non-condensable pyrolysis gas and air. That is, the chemical energy of the pyrolysis gas is used, instead of pure oxygen, which greatly reduces the cost of the entire system, and increases the flexibility of using the pyrolysis bed; 3) the solid cyclic heated heat carrier is transported directly to the pyrolysis bed for contact with the raw material, which not only increases the heating efficiency of the pyrolysis bed but also improves the yield of the quick pyrolysis oil reaction .
    Third, the invention uses the residual smoke heat generated by the combustion of the non-condensable pyrolysis gas to dry the raw material, which improves the energy efficiency of the entire system.
    Fourthly, the invention does not adopt the pre-treatment process of the raw material, at the entrance of the gasification oven. The raw material is introduced directly into the gasification oven after being pressurized by the high pressure oil pump. The process is simple and efficient. Compared to the method disclosed in the gasification of Chinese patent application No. 200810236639.4 for inlet feed, the method of the invention avoids the technical problem of pneumatic powder transportation and tar block during the feeding of dry carbon powder, as well as reducing the energy consumption of the raw material intake device and increasing the stability, reliability and viability of the system.
    Fifth, the invention adopts an external vapor condensation cycle. The biofuel oil heat exchanger is placed outside the condensation tank, which is convenient for cleaning and maintenance and also prevents interruption for maintenance.
    Sixth, the invention adopts pressurizing and transporting oil pump technology. Compared with the gasification method disclosed in Chinese patent application No. 200810236639.4, the method of the invention avoids the technical problem of pneumatic powder transport and tar block during the feeding of dry carbon powder, and also increases stability , system reliability and feasibility.
    Seventhly, with the technology of rapid pyrolysis, the biofuel oil generated almost contains no coal slag, which saves the work of high ash melting point in the process of making synthesis gas from biomass. The slag tracking system for the gasification furnace is also not necessary, which prevents corrosion of alkali metals and ash accumulation, and also increases the stability, reliability and viability of the system.
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    In short, the invention aims to realize the simplicity, efficiency, energy conservation, economy and high viability of the project. On the other hand, the invention improves gasification efficiency, decreases the amount of effective synthetic gas and improves the energy conversion rate of the system.
    BRIEF DESCRIPTION OF THE DRAWINGS
    FIG.1 is a schematic diagram of a method and a system for producing synthetic gas from biomass by pyrolysis according to an embodiment of the invention.
    DETAILED DESCRIPTION OF THE CORPORATIONS
    The preferred examples, the method and the arrangement of the frame system according to the invention are described with the accompanying drawing.
    As shown in FIG. 1, a gasification system for the production of synthetic gas from biomass comprises a pre-treatment part, a pyrolysis part, a condensation part and a gasification part. Specifically, the gasification system comprises: a raw biomass material 1, a grinding system 2, a drying system 3 a biomass stock tray 4, a pyrolysis bed 5, a cyclone 6 separator, a solid separator -solid 7, a stock for carbon powder 8, a combustion bed 9-1, a heated fluidized bed conveyor 9-2, an air inlet conduit 10 for the combustion bed, a residual heat smoke conduit 11, a residual smoke outlet from the drying system 11a, a condensation tank 12, an oil circulation pump 13, an oil fuel heat exchanger 14, a non-condensable pyrolysis gas compressor 15, a biofuel oil reservoir 16, a high pressure oil pump 17, a gasification furnace burner 18, an oxygen conduit 19 which leads to the gasification furnace burner, a gasification furnace 20, cooling water of the water from the gas oven fication 21, a synthetic gas conduit 22, a coal spout conduit 23, a desalinated and deoxidized water conduit 24, a conduit for saturated water vapor 25, an external conduit for fuel N1, an air conduit N2 that conducts to the combustion bed and an emptying conduit N3.
    The pyrolysis part comprises the pyrolysis bed 5, the combustion bed 9-1, the heated fluidized bed conveyor 9-2. The pyrolysis bed 5 is connected with the cyclone type separator 6 and the solid-solid separator 7. The solid-solid separator 7 is connected with the carbon powder stock box 8 and the heated fluid bed conveyor 9-2. The lower part of the heated fluidized bed conveyor 9-2 is provided with a conduit connected to the pyrolysis bed 5 in order to transmit the heated solid carrier to the pyrolysis bed 5 for recycling use.
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    The upper part of the heated fluid bed conveyor 9-2 is connected with the drying system 3 of the biomass material of the pre-processing part through the residual heat from the smoke from the conduit 11. The upper part of the combustion bed 9-1 is connected to an air inlet conduit 10.
    The condensation tank 12 is connected to the non-condensable pyrolysis gas compressor 15 via a conduit. The outlet of the non-condensable pyrolysis gas compressor 15 is connected, respectively, with the pyrolysis bed 5 and the combustion bed 9-1. Non-condensable pyrolysis gas is used as the fuel for the 9-1 combustion bed and the pyrolysis bed 5 flow medium.
    The condensation of the spray adopts an external method of circulation. The lower part of the condensation tank 12 is connected with the oil circulation pump 13 through a conduit. Circulation pump oil 13 is connected with the external biofuel oil heat exchanger 14. Part of the biofuel oil is pressurized by the oil circulation pump 13 and cooled by the oil biofuel heat exchanger 14, to circulate and spray the pyrolysis gas. The lower part of the condensation tank 12 is connected with the biofuel oil tank 16.
    The conduit connecting the outlet of the biofuel oil tank 16 and the gasification oven 20 is supplied with the high pressure oil pump 17. The biofuel oil is pressurized and transported to the gasification oven 20 for gasification.
    A method for producing synthetic gas from biomass by pyrolysis comprises steps as follows:
    1) pre-treatment of the raw biomass material: crush the raw biomass material until obtaining particle sizes of 1-6 mm and drying the raw material until the water content is 10-20 wt. %;
    2) the pyrolysis of the raw biomass material using the rapid biomass pyrolysis technology, ensuring that the temperature of the pyrolysis bed is between 400-600 ° C, by adjusting the proportion of the non-condensable pyrolysis gas to the air and controlling the temperature of the heated fluidized bed carrier, the residence time of the gas phase in the pyrolysis bed being 0.5-5 s and the product of the pyrolysis bed being pyrolysis gas and carbon powder;
    3) separating the pyrolysis gas from carbon powder and the solid heat carrier through the cyclone separator;
    4) separate the carbon powder away from the solid heat carrier through the solid-solid separator, feeding the carbon powder to the carbon powder stock tray for collection, heating the solid heat carrier in the
    10/16 heating pump fluidized bed and then transporting the heat carrier to the solid pyrolysis bed for recycled use;
    5) transport the generated pyrolysis gas to the condensation tank for the spray condensation, condensing the condensable part of the pyrolysis gas to generate the biofuel oil, pressurize the biofuel oil generated by the high pressure oil pump and, in then the feed to the gasification oven to be aerated; and
    6) feeding part of the non-condensable pyrolysis gas to the combustion bed to burn with air, transmitting the other part of the non-condensing pyrolysis gas to the pyrolysis bed as the average fluidization.
    The spray condensation adopts an external circulation method. The biofuel oil at the bottom of the condensation reservoir is pressurized and pumped by the oil pump and the biofuel oil is returned to the condensation tank for the spray condensation after it has been cooled by the external biofuel oil heat exchanger. . A portion of the condensable pyrolysis gas is condensed to produce the biofuel oil. A part of the biofuel oil is fed into the biofuel oil tank and the other part is pressurized by the oil circulation pump and cooled by the biofuel oil heat exchanger to circulate the pyrolysis gas circularly.
    The smoke from the residual heat generated in the heating conveyor fluidized bed in step 2) is used to dry the raw biomass material in step
    1) for the pre-processing of biomass raw material.
    Work process:
    1. System initialization process:
    1) opening the control valve V3 in the emptying conduit N3, keeping the control valve V2 leading to the condensation tank 12 and the control valve V9 in the conduit between the reservoir 12 and the non-condensable condensing gas compressor by pyrolysis closed;
    2) opening the control valve V1 in the external fuel conduit N1 and the control valve V7 in the air conduits N2 leading to the combustion bed, keeping the control valve V8 in the conduit between the non-condensable pyrolysis gas compressor 15 and from the pyrolysis bed 5, closed in order to feed the heat smoke generated by the combustion of fuel and combustion air in bed 9-1 to the heated conveyor of the fluidized bed 9-2 to heat the solid heat conveyor;
    within that system is then transported to the stock tray of
    11/16 biomass 4 for storage. It can also be transported to the pyrolysis bed 5 by a feeder. Opening the control valve V5 in the residual heat smoke conduit between the heating fluidized bed the conveyor 92, the pyrolysis bed 5 and the V6 control valve in the conduit between the biomass stock tray 4 and the pyrolysis bed 5, to partially feed residual heat smoke the drying system 3 to dry the crude biomass material, partially feed residual heat smoke to the pyrolysis bed 5 as a fluidization medium, separating solids from the mixed pyrolysis gas generated by the reaction in the pyrolysis bed 5 through cyclone separator 6 and then discharging out of the system through conduit N3; and
    Opening control valve V2 after implementing steps 1), 2) and 3) for 10-20 minutes, the cooling of the pyrolysis gas, by spraying the condensation reservoir 12, collects the biofuel oil; after running for 15-30 min, opening the V9 valve control, closing the control valve V1, V5 and V7, opening the control valves V4 and V8 at the same time, the system starts to run normally under the circumstances.
    2. Normal system operation process:
    The raw biomass material is fed to the drying system 3, through the grinding system 2. The raw biomass material is dried and dehydrated by the heat smoke from the system and is then transported to the biomass stock tray 4 for storage. . It can also be transported to the pyrolysis bed 5 by a feeder. Opening the control valve V5 in the residual heat smoke conduit, between the heated fluid bed conveyor 9-2, the pyrolysis bed 5 and the control valve V6 in the conduit between the biomass stock tray 4 and the bed of pyrolysis 5 feeds partially residual heat smoke to the drying system 3 to dry the crude biomass material, feeding partially residual heat smoke to the pyrolysis bed 5 as a fluidization medium, separating solids from the mixed pyrolysis gas generated by the reaction in the pyrolysis bed 5 through cyclone 6 separator and then discharging out of the system through conduit N3; and
    The product of the pyrolysis bed 5 includes the pyrolysis gas and the coal powder containing CO, H2, CO2, H2O, CH4, and tar. The coarse pyrolysis gas is separated by the cyclone-type separator 6, and then the solid heat carrier and the carbon powder particles in the pyrolysis gas fall into the solid-solid separator 7, through the ash discharge port.
    The first separated pyrolysis gas is supplied to the condensation reservoir 12 to be sprayed round by the biofuel oil. O
    12/16 non-condensable pyrolysis gas is pressurized in the non-condensable pyrolysis gas compressor 15 and then respectively, fed to the combustion bed 9-1 and the pyrolysis bed 5. The condensable pyrolysis gas is condensed to produce the oil biofuel. Part of the biofuel oil generated can be used for cyclic spraying. The rest is generated in biofuel oil and supplied to the biofuel oil reservoir 16.
    After the solid heat carrier and the carbon powder in the solid-solid separator 7 are separated, the heat descends to the heated carrier bed of the fluidized bed 9-2 and the carbon powder is supplied to the powdered carbon stock pin. 8.
    In combustion bed 9-1, the non-condensable pyrolysis gas for combustion is subjected to combustion reaction with air from conduit 10. The heat smoke generated by combustion is supplied to the heated conveyor in the fluidized bed 9-2 for heat the cyclic solid heat carrier. The temperature of the pyrolysis bed 5 is controlled as 400-600 ° C by adjusting the proportion of the non-condensable pyrolysis gas generated by combustion with air. The residence time of the gas phase in the pyrolysis bed 5 is controlled to be 0.5-5 s. The residual smoke heat that passes through the conveyor from the heated fluidized bed 9-2 and is fed to the drying system 3 for drying.
    The pressure of the biofuel oil in the biofuel oil reservoir 16 is first set to equal the working pressure of the gasification oven 20 by the high pressure pump 17 and then the supply to the gasification burner furnace 18 Oxygen in conduit 19 is also supplied to the gasification burner oven 18 to generate the high temperature gasification reaction gasification 20. The temperature of the synthetic gas 22 at the outlet of the gasification oven is controlled at 1200-1600 ° C, adjusting the amount of oxygen and the amount of heat exchange of the cooling water of the wall 21 of the gasification oven with the desalinated and deoxidized water. The gasification product mainly refers to CO, H2 and also comprises a small amount of CO2, H2O and CH4 traces. The desalinated and deoxidized water is cooled by the cooling water of the wall 21 of the gasification oven, to generate an intermediate saturated water vapor pressure, which is supplied to the tracking system through conduit 25. The rest generated by the gasification of the coal is discharged through conduit 23.
    Example 1
    Take wood as a raw material for biomass. The elemental composition and characteristic data of the dry wood are listed in table 1.
    Table 1 elementary composition and characteristic data of dry wood
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    Items Symbol unity Value Carbon D a r % (Kg / Kg) 39.43 Hydrogen H ar % (Kg / Kg) 5.21 Oxygen Oar % (Kg / Kg) 38.36 Nitrogen Λ / air % (Kg / Kg) 0.15 Sulfur S a r % (Kg / Kg) 0.21 Chlorine With air % (Kg / Kg) 0.00 GreyAir % (Kg / Kg) 5.00 Moisture M ar % (Kg / Kg) 11.64 Melting point of FT ° C 1436 Grey Low value of LHV MJ / Kg 14.75 heat
    The main operating conditions are as follows;
    1) the diameter of the material grains at the outlet of the grinding system 2 is 6 mm;
    2) the water content of the material at the exit of the drying system 3 is 15 wt. %;
    3) the pressure of the pyrolysis bed 5 is normal pressure and the temperature is controlled at 400 ° C;
    4) the dwell time of the gas in the pyrolysis bed phase 5 is 5 s; and
    5) the pressure of the gasification oven 20 is controlled to be at 4.0 Mpa (A) and the temperature is at 1400 ° C.
    In accordance with the conditions established above, the main data, the performance parameters of the system and the process of carrying out the invention are explained in detail, with the attached drawings:
    1) the quality of the yield of the biomass raw material feeding the pyrolysis bed 5 is 55%;
    2) the dry matter content of CO and H2 in the synthetic gas outlet through conduit 22 is 76%;
    3) the carbon conversion rate of the system is 99.9% and the effective oxygen consumption of the synthetic gas is 0.33 mol / mol.
    Example 2
    Take wood in example 1 as a raw material for biomass (table 1).
    The main operating conditions are as follows:
    1) the diameter of the material grains at the outlet of the grinding system 2 is 5 mm;
    2) the water content of the material at the exit of the drying system 3 is 20 wt. %;
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    3) the pressure of the pyrolysis bed 5 is of normal pressure and the temperature is controlled at 500 ° C;
    4) the residence time of the gas in the pyrolysis bed phase 5 is 3 s;
    5) the pressure of the gasification oven 20 is controlled to be 4.0 MPa (A) and the temperature is controlled at 1400 0 C.
    According to the conditions set out above, the main data and performance parameters of the system in its process of implementing the invention are explained in detail with the attached drawings:
    1) the quality of the biological fuel yield of the biomass raw material supplied to the pyrolysis bed 5 is 60%;
    2) the dry matter content of CO and H2 in the outlet of the synthetic gas through the conduit is 80%; and
    3) the carbon conversion rate of the system is 99.9% and the effective oxygen consumption of the synthetic gas is 0.31 mol / mol.
    Example 3
    Take the wood from Example 1 as a raw material for biomass (Table 1).
    The main operating conditions are as follows:
    1) the diameter of the material grains at the outlet of the grinding system 2 is 4 mm;
    2) the water content of the material at the exit of the drying system 3 is 10 wt. %;
    3) the pressure of the pyrolysis bed 5 is of normal pressure and the temperature is controlled at 600 ° C;
    4) the dwell time of the gas in the pyrolysis bed phase 5 is 2 s; and
    5) the pressure of the gasification oven 20 is controlled to be 4 Mpa (A) and the temperature is controlled at 1400 ° C.
    According to the conditions established above, the main data and performance parameters of the system in the process of implementing the invention are explained in detail with the attached drawing:
    1) the quality of the biological fuel yield of the biomass raw material supplied to the pyrolysis bed 5 is 65%;
    2) the dry matter content of CO and H2 in the outlet of the synthetic gas through the conduit is 82%; and
    3) the carbon conversion rate of the system is 99.9% and the effective oxygen consumption of the synthetic gas is 0.31 mol / mol.
    Example 4
    Take the wood from Example 1 as a raw material for biomass (Table 1).
    The main operating conditions are as follows:
    1) the diameter of the material grains at the outlet of the grinding system 2 is 3 mm;
    15/16
    2) the water content of the material at the exit of the drying system 3 is 13 wt. %;
    3) the pressure of the pyrolysis bed 5 is normal pressure and the temperature is controlled
    450 ° G.
    4) the time the gas remains in the pyrolysis bed phase is 1 s; and
    5) the pressure of the gasification oven 20 is controlled to be 4.0 MPa (A) and the temperature is controlled at 1400 ° C.
    In accordance with the conditions established above, the main data and performance parameters of the system in the process of implementing the invention are explained in detail with the attached drawing:
    1) the quality of the biological fuel yield of the biomass raw material supplied to the pyrolysis bed 5 is 66%;
    2) the dry matter content of CO and H2 in the outlet of the synthetic gas through the conduit is 84%; and
    3) the carbon conversion rate of the system is 99.9% and the effective oxygen consumption of the synthetic gas is 0.3 mol / mol.
    Example 5
    Take the wood from Example 1 as a raw material for biomass (Table 1).
    The main operating conditions are as follows:
    1) diameter of the material grains at the outlet of the grinding system 2 is 2 mm;
    2) the water content of the material at the outlet. Of drying system 3 is 16 wt. %;
    3) the pressure of the pyrolysis bed 5 is normal pressure and the temperature is controlled
    550 ° C;
    4) the residence time of the gas in the pyrolysis bed phase 5 is 1.5 s, and
    5) the pressure of the gasification oven 20 is controlled to be 4.0 MPa (A) and the temperature is controlled at 1400 ° C.
    In accordance with the conditions established above, the main data and performance parameters of the system in the process of implementing the invention are explained in detail with the attached drawing:
    1) the quality of the biological fuel yield of the biomass raw material supplied to that of the pyrolysis bed 5 is 70%;
    2) the dry matter content of CO and H2 in the outlet of the synthetic gas through the conduit is 86%; and
    3) the carbon conversion rate of the system is 99.9% and the effective oxygen consumption of the synthetic gas is 0.3 mol / mol.
    Example 6
    Take the wood from Example 1 as a raw material for biomass (Table 1).
    The main operating conditions are as follows:
    16/16
    1) the diameter of the material grains at the outlet of the grinding system 2 is 1 mm;
    2) the water content of the material at the exit of the drying system 3 is 18 wt. %;
    3) the pressure of the pyrolysis bed 5 is normal pressure and temperature is controlled at 520 0 C;
    4) the gas residence time in the pyrolysis bed 5 phase is 0.5 s, and
    5) the pressure of the gasification oven 20 is controlled to be 4.0 MPa (A) and the temperature is controlled at 1400 0 C.
    According to the conditions established above, the main data and performance parameters of the system in the process of implementing the invention are explained in detail with the attached drawing;
    1) the quality of the biological fuel yield of the biomass raw material supplied to the pyrolysis bed 5 is 75%;
    2) the dry matter content of CO and H2 in the outlet of the synthetic gas through conduit 22 is 90%; and
    3) the carbon conversion rate of the system is 99.9% and the effective oxygen consumption of the synthetic gas is 0.285 mol / mol.
    1/3
    权利要求:
    Claims (6)
    [1]
    1. Process for the production of synthetic gas from biomass by pyrolysis, characterized by comprising:
    1) pre-processing of a biomass raw material;
    [2]
    2) the pyrolysis of the biomass raw material uses the technology of rapid biomass pyrolysis, a product of a pyrolysis bed, being a pyrolysis gas and a carbon powder;
    [3]
    3) separation of the pyrolysis gas, carbon powder and a solid heat carrier using a cyclone separator;
    [4]
    4) the separation of the carbon powder away from the cyclic heat carrier, through a solid-solid separator, feeding the carbon powder to a carbon powder stock tray for collection, the heated carrier being in a fluidized bed of heating and transporting the solid heat carrier to the pyrolysis bed for recycled use;
    [5]
    5) the transport of the generated pyrolysis gas to a condensation reservoir for its pulverized condensation, condensing a condensable part of the pyrolysis gas, to generate the biofuel oil, pressurizing the biofuel oil generated by a high pressure oil pump and feeding a gasification oven to be gasified; and
    [6]
    6) feeding part of the non-condensable pyrolysis gas to a combustion bed to make combustion with air, transmitting the other part of the non-condensing pyrolysis gas to the pyrolysis bed, as a medium fluidization.
    2. Process according to claim 1, characterized by comprising the sprayed condensation, adopting an external circular method, the biological fuel oil at the bottom of the condensation reservoir is pressurized and pumped by the high pressure oil pump, and then the fuel oil biological is returned to the condensation reservoir for the sprayed condensation, after having been cooled by an external biofuel oil heat exchanger, the condensable pyrolysis gas is condensed to produce the biofuel oil, a part of the biofuel oil being supplied to the biofuel oil reservoir, and the other part being pressurized by an oil circulation pump and cooled by the biofuel oil heat exchanger circularly to spray the pyrolysis gas.
    3. Process according to claims 1 or 2, characterized by the residual heat smoke generated in the heating fluidized bed conveyor in step 4) to be used to dry the biomass raw material in step 1) for the pre-treatment of the raw material of biomass.
    2/3
    4. Process according to claims 1 or 2, characterized by the relationship between the non-condensable pyrolysis gas and the temperature of the heated fluidized bed conveyor in step 6) are controlled to ensure that the temperature of the pyrolysis bed is 400-600 ° C and the residence time of the gas phase in the pyrolysis bed is 0.5-5 s.
    5. Process according to claims 1 or 2, characterized by the pre-processing of biomass raw material in step 1) consisting of: crushing the biomass raw material, to have particle size of 1-6 mm, and the drying of the raw material until the water content is 10-20 wt. %.
    6. Gasification system for the production of synthetic gas from biomass by pyrolysis, characterized in that it uses the method of any of claims 1-5, characterized by a pre-processing part of biomass raw material, _a pyrolysis part , a condensation part and a gasification part; wherein the pyrolysis part comprises the pyrolysis bed (5) and a combustion bed (9-1); the condensation tank (12) of the condensation part is connected to a non-condensable pyrolysis gas compressor (15) through a conduit, an outlet of the non-condensable pyrolysis gas compressor (15) is connected with the pyrolysis bed ( 5) and the combustion bed (9-1); and the non-condensable pyrolysis gas is used as a bed combustion fuel (9-1) and a pyrolysis bed fluidization medium (5).
    7. Gasification system according to claim 6, characterized in that the condensation part adopts a sprayed condensation in external circulation, a lower part of the condensation reservoir (12) is connected with an oil circulation pump (13) through a conduit, the oil circulation pump (13) is related to an external biofuel oil heat exchanger (14), a part of the biofuel oil is pressurized by the oil circulation pump (13) and cooled by the fuel oil heat exchanger biological (14), in order to spray the pyrolysis gas circularly, and a lower part of the condensation tank (12) is connected to a reservoir of biological fuel oil (16).
    8. Gasification system according to claim 6 or 7, characterized in that the pyrolysis bed (5) is connected with the cyclone type separator (6) and the solid-solid separator (7), the solid-solid separator (7) is connected with the carbon powder stock tray (8) and the heated fluid bed conveyor (9-2), a lower part of the heated fluid bed conveyor (9-2) being provided by a conduit connected to the pyrolysis bed (5) , in order to transmit the heated solid carrier to the pyrolysis bed (5) for recycled use.
    3/3
    9. Gasification system according to claim 8, characterized in that an upper part of the heated fluidized bed conveyor (9-2) is connected with a drying system (3) of the pre-processing biomass raw material through a heat pipeline waste and smoke (11), and an upper part of the bed
    5 combustion (9-1) be connected with an air inlet duct (10).
    10. Gasification system according to claim 7, characterized in that a conduit is connected to an outlet of the biological fuel oil reservoir (16) and the gasification oven (20) is supplied with the high pressure oil pump (17); the biofuel oil is pressurized and transported to the gasification oven (20)
    10 for gasification.
    affi
    1/1
    类似技术:
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    同族专利:
    公开号 | 公开日
    JP5753253B2|2015-07-22|
    JP2013522421A|2013-06-13|
    AU2011232187B2|2014-07-31|
    AU2011232187A1|2012-11-08|
    EP2551331B1|2017-11-29|
    US9249358B2|2016-02-02|
    WO2011116689A1|2011-09-29|
    CA2798918A1|2011-09-29|
    EP2551331A1|2013-01-30|
    KR101445205B1|2014-09-29|
    ZA201207071B|2013-05-29|
    MY155965A|2015-12-31|
    SG184143A1|2012-10-30|
    EP2551331A4|2013-10-30|
    MX2012011002A|2013-02-27|
    US20160108319A1|2016-04-21|
    KR20130001284A|2013-01-03|
    AP4066A|2017-03-14|
    BR112012024082A2|2016-08-30|
    US9902907B2|2018-02-27|
    US20130019529A1|2013-01-24|
    AP2012006507A0|2011-10-31|
    CN101818080B|2013-03-13|
    CN101818080A|2010-09-01|
    RU2012144796A|2014-04-27|
    CA2798918C|2018-12-04|
    RU2519441C1|2014-06-10|
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    法律状态:
    2018-07-10| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2018-08-07| B16A| Patent or certificate of addition of invention granted|
    优先权:
    申请号 | 申请日 | 专利标题
    CN2010101324813A|CN101818080B|2010-03-23|2010-03-23|Process and system for manufacturing synthesis gas from biomass by pyrolysis|
    CN201010132481.3|2010-03-23|
    PCT/CN2011/072061|WO2011116689A1|2010-03-23|2011-03-23|Process and system for producing synthesis gas from biomass by pyrolysis|
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