CN115029160A - Device and method for increasing yield of oil gas through synergistic conversion of biomass and coal in circulating fluidized bed - Google Patents

Device and method for increasing yield of oil gas through synergistic conversion of biomass and coal in circulating fluidized bed Download PDF

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CN115029160A
CN115029160A CN202210576186.XA CN202210576186A CN115029160A CN 115029160 A CN115029160 A CN 115029160A CN 202210576186 A CN202210576186 A CN 202210576186A CN 115029160 A CN115029160 A CN 115029160A
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gas
outlet
solid
tank
oil
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CN115029160B (en
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黄勇
刘巧霞
刘丹
王武生
孔少亮
靳皎
贺文晋
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Shaanxi Yanchang Petroleum Group Co Ltd
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Shaanxi Yanchang Petroleum Group Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
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    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/30—Active carbon
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    • C01B32/318—Preparation characterised by the starting materials
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    • C01B32/354—After-treatment
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
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    • C01B32/354—After-treatment
    • C01B32/36—Reactivation or regeneration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
    • C10B49/20—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form
    • C10B49/22—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form according to the "fluidised bed" technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
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    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
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    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/62—Processes with separate withdrawal of the distillation products
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
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    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
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    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C10G2300/1014—Biomass of vegetal origin
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C10J2300/092—Wood, cellulose
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
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    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
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    • C10J2300/0959—Oxygen
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    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
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    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
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    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1615—Stripping
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract

The invention discloses a device and a method for increasing yield of oil gas by synergistic conversion of biomass and coal in a circulating fluidized bed. The feeding fluidization unit establishes circulating steady fluidization for the added solid particles in the system, so that continuous and stable feeding of the biomass and the coal is realized; the coupling reaction unit completes the rapid pressurization hydrogenation segmental pyrolysis reaction of the biomass and the coal, the online separation of gas and solid, the circulating return of solid particles and the high-efficiency gasification reaction of semicoke; the purification and recovery unit realizes collection of pyrolysis oil and fractional cyclic utilization of heavy oil and light oil by multi-stage washing and purification recovery of high-temperature oil gas and efficient separation and recovery of gas-liquid two phases; the separation and utilization unit realizes the separation and the recycling of the activated carbon and the pyrolysis water. The invention is suitable for different biomasses and coal types, and has the advantages of obvious synergistic efficiency, high energy conversion efficiency, high oil product yield, high synthetic gas content and large treatment scale.

Description

Device and method for increasing yield of oil gas through biomass and coal cooperative conversion in circulating fluidized bed
Technical Field
The invention belongs to the technical field of coal conversion, relates to a device for biomass and coal cooperative conversion, and particularly relates to a device and a method for increasing yield of oil gas by biomass and coal cooperative conversion in a circulating fluidized bed.
Background
The co-conversion technology of biomass and coal is always a key research point at home and abroad, free hydrogen and small-molecule free radicals generated by biomass pyrolysis are easy to combine with macromolecular free radicals generated by coal pyrolysis, the pyrolysis reaction of coal is promoted, the removal of sulfur and nitrogen in coal is facilitated, the yield of coal pyrolysis tar and the large-scale utilization of biomass are improved, and the method is an optional route with low cost, the yield of tar is improved, and the oil quality is improved.
Factors such as raw material type, reactor type and pyrolysis conditions influence the co-conversion process of biomass and coal, the reaction mechanism is not clear, and no unified conclusion is made on whether synergistic effect exists. The main reason for the difference in understanding of the reaction process of biomass and coal is the difference in the types of raw materials, the types of reactors and the operating conditions, which makes it difficult to obtain uniform and regular understanding. However, different reaction conditions interact with each other, and properties such as volatile components, semicoke and co-pyrolysis oil generated by the reaction are complex, so that product distribution and synergistic effect are influenced, and the interaction mechanism of key products is not deeply known. The action between the volatile components of the biomass and the coal is weakened at a slow temperature rise rate, and the co-pyrolysis synergistic effect is not obvious. The fluidized bed has the characteristics of high heating rate, full particle mixing, uniform bed layer temperature distribution, good heat and mass transfer effects and the like, so that the biomass and coal can quickly reach the optimal reaction temperature, the pyrolysis sections can overlap and influence each other, but the fluidized bed reactor has less related research or application in the coal pyrolysis reaction.
Based on the above, a novel biomass and coal grading high-efficiency conversion technology which is suitable for different biomass and coal types, has obvious synergistic efficiency, high energy conversion efficiency, high oil product yield, high synthesis gas content and large processing scale is urgently needed to be developed.
Disclosure of Invention
Aiming at the defects in the prior art, the invention aims to provide a device and a method for increasing the yield of oil gas by the synergistic conversion of biomass and coal in a circulating fluidized bed, which are suitable for different biomass and coal types, and have the advantages of obvious synergistic efficiency, high energy conversion efficiency, high oil product yield, high synthetic gas content and large treatment scale.
In order to achieve the purpose, the invention adopts the following technical scheme to realize the purpose:
a device for increasing yield of oil gas by synergistic conversion of biomass and coal in a circulating fluidized bed comprises a feeding fluidization unit, a coupling reaction unit, a purification and recovery unit and a separation and utilization unit;
the coupling reaction unit comprises a pyrolysis gasification system, a fluidized gas system, a gasifying agent system and a gas-solid dust removal system;
the purification and recovery unit comprises a grading washing system, a rectification system and a gas-liquid separation system;
the separation and utilization unit comprises an activated carbon adsorption system, an activated carbon recycling system and a purified water circulating system;
the pyrolysis gasification system comprises an integrated reactor connected with an outlet of a feeding fluidization unit, an outlet at the top of the integrated reactor is connected with an inlet at the upper part of a gas-solid separation circulator, and an outlet at the bottom of the integrated reactor is connected with an ash cooler;
the integrated reactor comprises a pyrolysis zone, a transition zone and a gasification zone;
the bottom outlet of the gas-solid separation circulator is connected to the lower inlet of the integrated reactor to form primary solid circulation, and the top outlet of the gas-solid separation circulator is connected to a gas-solid dust removal system to perform gas-solid separation;
the outlet of the gas-solid dust removal system is connected to the activated carbon adsorption system and the grading washing system, and the outlet of the grading washing system is connected to the gas-liquid separation system and the activated carbon adsorption system;
a gas outlet of the gas-liquid separation system is connected to a fluidized gas system and gas collecting equipment, and a liquid outlet of the gas-liquid separation system is connected to a rectification system;
the gas flow outlet of the rectification system is connected to the grading washing system for circulating washing and separation, and the liquid outlet of the rectification system is connected to an oil product tank for oil product collection;
the solid outlet of the active carbon adsorption system is connected to the active carbon recycling system, the liquid outlet of the active carbon adsorption system is connected to the purified water circulating system, and the gas outlet of the active carbon adsorption system is connected to the grading washing system;
the activated carbon recycling system comprises a solid dryer connected with a solid outlet of the activated carbon adsorption system, an outlet of the solid dryer is connected to a combustion heating furnace, and an outlet of the combustion heating furnace is respectively connected with the activated carbon adsorption system, the integrated reactor and the feeding fluidization unit;
the fluidized gas system comprises a synthetic gas buffer tank connected with the gas flow outlet end of the gas-liquid separation system, the outlet of the synthetic gas buffer tank is connected with a synthetic gas supercharger, one part of the gas flow outlet of the synthetic gas supercharger is connected with the inlet of a fluidized gas source, and the other part of the gas flow outlet of the synthetic gas supercharger is connected with a combustion heating furnace and is used for providing fuel for the combustion heating furnace; the outlet end of the fluidizing gas source is sequentially connected with a fluidizing gas mixer and a fluidizing gas preheater, and the outlet of the fluidizing gas preheater is connected to the inlet of the integrated reactor;
the gasification agent system comprises a gasification agent mixer connected with the outlet of the purified water circulation system, and the gas outlet of the gasification agent mixer is preheated by a gasification agent preheater and then connected to the inlet of the integrated reactor.
The invention also has the following technical characteristics:
preferably, the grading washing system is provided with internal circulation, and the grading washing system and the gas-solid dust removal system, the rectification system and the grading washing system, and the purified water circulation system and the activated carbon adsorption system are in associated circulation;
the pyrolysis gasification system, the gas-solid dust removal system, the gas sampling tank and the connecting pipeline are provided with heat tracing and heat insulating devices which enable the operating temperature to be higher than 450 ℃.
Preferably, the feeding fluidization unit comprises a solid particle feeding system, a biomass feeding system and a coal powder feeding system;
the solid particle feeding system comprises a solid particle storage tank, an outlet of the solid particle storage tank is connected with an inlet of a solid particle pressurizing tank, an outlet of the solid particle pressurizing tank is connected with an inlet of a solid particle feeder, and an outlet of the solid particle feeder is connected with an inlet of the integrated reactor;
the biomass feeding system comprises a biomass storage tank, an outlet of the biomass storage tank is connected with an inlet of a biomass pressurizing tank, an outlet of the biomass pressurizing tank is connected with an inlet of a biomass feeder, and an outlet of the biomass feeder is connected with an inlet of an integrated reactor;
the pulverized coal feeding system comprises a pulverized coal storage tank, an outlet of the pulverized coal storage tank is connected with an inlet of a pulverized coal pressurizing tank, an outlet of the pulverized coal pressurizing tank is connected with an inlet of a pulverized coal feeder, and an outlet of the pulverized coal feeder is connected with an inlet of the integrated reactor.
Preferably, the gas-solid dust removal system comprises a primary gas-solid separator connected with a top outlet of the gas-solid separation circulator, and the top outlet of the primary gas-solid separator is connected to a lower inlet of the secondary gas-solid separator;
the bottom outlet of the primary gas-solid separator is respectively connected with a coarse particle collector and a primary material return controller, and the outlet of the primary material return controller is connected to the lower inlet of the gas-solid separation circulator;
the bottom outlet of the secondary gas-solid separator is connected with a fine ash particle collector;
and outlets at the bottoms of the coarse particle collector and the fine ash particle collector are connected to an activated carbon adsorption system.
Further, the staged washing system comprises a quenching washing tower and a flash separation tank which are connected with an outlet at the top of the secondary gas-solid separator, wherein an outlet of the flash separation tank is connected with a heavy oil collecting tank and a primary liquid-solid separator, and an outlet of the primary liquid-solid separator is connected with the heavy oil collecting tank and the activated carbon adsorption system;
the top outlet of the quenching washing tower is connected to the inlet of the secondary washing tower, and the bottom outlet of the quenching washing tower is connected to the heavy oil collecting tank;
the outlet of the heavy oil collecting tank is connected with the inlet of the middle part of the quenching washing tower and the inlet of the oil product intermediate tank;
the top outlet of the secondary washing tower is connected to a gas-liquid separation system, the bottom outlet of the secondary washing tower is connected to a light oil collecting tank, the middle outlet of the light oil collecting tank is connected to the middle inlet of the secondary washing tower, and the bottom outlet of the secondary washing tower is connected to an oil-water standing tank;
the outlet of the oil-water standing tank is connected to a separation utilization unit;
the primary gas-solid separator, the secondary gas-solid separator and the heavy oil collecting tank are all connected to a gas sampling tank;
the gas sampling tank is composed of an internal structure and an external cold hydrazine structure, wherein the internal structure comprises bottom washing absorption, middle condensation recovery and upper evaporation azeotropy, and the external cold hydrazine structure is used for obtaining full-fraction pyrolysis oil.
Further, the gas-liquid separation system comprises a gas-liquid reinforced condenser connected with a top outlet of the secondary washing tower, a top outlet of the gas-liquid reinforced condenser is connected to the adsorption filtration tank, a bottom outlet of the gas-liquid reinforced condenser is connected to the gas-liquid reinforced separator, a middle outlet of the gas-liquid reinforced separator is connected to an inlet of the oil-water standing tank, and a bottom outlet of the gas-liquid reinforced separator is connected to the rectification system;
a back-blowing supercharger and a back-blowing heater are arranged between the outlet of the adsorption filtration tank and the secondary gas-solid separator;
a synthetic gas buffer tank and a synthetic gas supercharger are respectively arranged between the outlet of the adsorption filtration tank and the fluidized gas source, the gas-solid separation circulator and the combustion heating furnace;
the adsorption filtration tank is provided with two or more than two adsorption filtration tanks in parallel.
Furthermore, the rectification system comprises a rectification tower connected with a bottom outlet of the gas-liquid intensified separator and an outlet of an oil product intermediate tank, wherein a bottom outlet of the rectification tower is connected to an oil product tank, a lower outlet of the rectification tower is connected with an inlet of a heavy oil storage tank, an outlet of the heavy oil storage tank is connected with an upper inlet of a quenching washing tower, an upper outlet of the rectification tower is connected with an inlet of a light oil storage tank, and an outlet of the light oil storage tank is connected with an upper inlet of a secondary washing tower.
Furthermore, the activated carbon adsorption system comprises a carbonization and activation device connected with outlets at the bottoms of the coarse particle collector, the fine ash particle collector and the primary liquid-solid separator, and an outlet pipeline of the carbonization and activation device is sequentially connected with a washing and separating device, a separating and drying device and an adsorption and separation tank; the top inlet of the adsorption separation tank is connected with the bottom outlet of the oil-water standing tank, the outlet of the adsorption separation tank is connected with a secondary liquid-solid separator and a purified water circulating system, and the outlet of the secondary liquid-solid separator is respectively connected with the purified water circulating system, an activated carbon recycling system and an oil product intermediate tank;
the purified water circulating system comprises a circulating regeneration purified water tank connected with outlets of the oil-water standing tank, the adsorption separation tank and the secondary liquid-solid separator, an outlet of the circulating regeneration purified water tank is connected to the purified water vapor generator, and an outlet of the purified water vapor generator is connected with an inlet of the gasifying agent system.
The invention also discloses a method for increasing the yield of oil gas by the synergistic conversion of biomass and coal in the circulating fluidized bed by adopting the device, which comprises the following steps:
the method comprises the following steps: fluidized temperature rise
1) Introducing a certain amount of inert gas into the integrated reactor and the gas-solid separation circulator for replacement purging, introducing a small amount of gas into a pressure measuring port of the system to ensure the smoothness of a pipeline, and establishing a gas fluidization system of the system;
2) the solid particles are fed in line through a solid particle storage tank, a solid particle pressurization tank and a solid particle feeder, and form circulating fluidization between the integrated reactor and the gas-solid separation circulator. Large particles are continuously abraded and are brought to a primary gas-solid separator and a secondary gas-solid separator for capture, and small particles form stable circulating fluidization in the system;
3) taking solid particles as a heat carrier, carrying a large amount of heat generated by combustion in a combustion heating furnace, performing high-rate circulating material return with a circulating rate of 50-200 between an integrated reactor and a gas-solid separation circulator, and performing fluidization temperature rise by a system at a temperature rise rate of 5-20 ℃/h to gradually rise the temperature to 400-1400 ℃;
step two: pyrolysis gasification
1) Coal powder and biomass enter a pyrolysis zone of the integrated reactor according to a certain mass ratio; the biomass, the coal powder and the solid particle heat carrier are fully mixed, and a rapid co-pyrolysis reaction is carried out at the pyrolysis temperature of 400-800 ℃, so that high-temperature oil gas and semicoke are generated, and high-rate circulation is carried out along with a large amount of inert solid particles;
2) the method comprises the following steps that high-temperature oil gas containing semicoke and solid particles enters a gas-solid separation circulator, 50-70% of the semicoke and the solid particles are captured and returned to a gasification zone of an integrated reactor, 10-20% of the semicoke enters a primary gas-solid separator, the semicoke is captured and returned to the gasification zone of the integrated reactor through a primary material returning controller, and the remaining 1-10% of the semicoke enters a secondary gas-solid separator for capture and reuse;
3) the semicoke and the gasifying agent from the gasifying agent preheater which are circularly returned enter a gasification zone of the integrated reactor, and are subjected to combustion or gasification reaction with the gasifying agent at the high temperature of 900-1400 ℃, so that high-temperature synthetic gas which contains solid particles and is rich in hydrogen and carbon monoxide is generated and enters a pyrolysis zone of the integrated reactor, when the carbon source of the gasification zone is insufficient, redundant coal powder is supplemented and enters the gasification zone, and sufficient reaction heat and atmosphere are generated and supplied for pyrolysis reaction;
4) when the temperature of the gasification zone of the integrated reactor is too high or the overall circulating material level is too high, the circulating material level height can be judged through the pressure difference of gas-solid separation circulating gas. Solid particles in the reactor can be discharged through the ash cooler by opening the online discharging device, so that when a large amount of solid particles enter the primary gas-solid separator, the temperature of the integrated reactor and the height of a circulating material level are balanced, a large amount of high-temperature sensible heat is recovered, and medium-pressure steam is further byproduct and enters the gasifying agent mixer as a gasifying agent;
step three: purification and recovery
1) Spraying a cooling medium into the high-temperature oil gas from the secondary gas-solid separator, wherein the cooling medium can be self-produced heavy oil or light oil, and enabling solid particles in the oil gas to enter a flash separation tank; the high-temperature oil gas without solid particles sequentially enters a quenching washing tower and a secondary washing tower for circular washing, and the recovered pyrolysis oil is separated into oil and water in an oil-water standing tank and an adsorption separation tank; fractionating in the rectifying tower to obtain heavy oil and light oil as cooling medium for the quenching washing tower and the secondary washing tower;
2) the oil gas washed by the secondary washing tower enters a gas-liquid separation system, passes through a gas-liquid reinforced condenser, a gas-liquid reinforced separator and an adsorption filtration tank, and the residual light oil component, pyrolysis water and synthesis gas are recovered in a grading manner;
3) part of the generated synthesis gas passes through a back-blowing heater and a back-blowing supercharger and is respectively used as back-blowing gas of a secondary gas-solid separator and conveying gas of a solid particle feeder, a biomass feeder and a coal powder feeder; the other part of the gas passes through a synthesis gas buffer tank and a synthesis gas compressor and respectively enters a combustion heating furnace, a gas-solid separation circulator and a fluidized gas source;
step four: separate utilization of
1) The semicoke from the coarse particle collector, the fine ash particle collector and the primary liquid-solid separator sequentially passes through a carbonization activation device and a washing separation device, and is subjected to directional extraction, raffinate template guiding and chemical activation to prepare activated carbon, the activated carbon is subjected to a biological reaction with pyrolysis water in an adsorption separation tank to adsorb and remove the pyrolysis water, and the removal rate is over 95 percent;
2) after pyrolysis water and pyrolysis oil are removed from saturated activated carbon through a secondary liquid-solid separator, the saturated activated carbon sequentially enters a solid dryer and a combustion heating furnace, solid ash rich in alkali/alkaline earth metal generated by reaction enters an integrated reactor as a pyrolysis catalyst, and the conversion rate of coal, the co-pyrolysis synergistic effect and the co-pyrolysis oil yield are improved;
3) the removed pyrolysis water is converted into medium-pressure steam with the pressure of 2.5-6 MPa and the temperature of 350-450 ℃ through a circulating regeneration purification water tank and a purified water steam generator, and the medium-pressure steam is used as a gasifying agent and enters a gasifying agent mixer for recycling, so that the input of outsourcing steam is greatly reduced.
The solid particles are one or a combination of more of quartz sand, semicoke, biomass semicoke, petroleum coke, waste tire powder, waste catalysts, waste activated carbon and other carbon-containing materials, the particle size range is 10-500 mu m, the solid particles are added or discharged on line, and the reaction temperature and the bed material level are controlled;
the biomass type is one or a combination of more of straw, walnut shells, sawdust, rice hulls and branches, and is suitable for biomass with the particle size range of 10-500 mu m, the water content of less than 50% and 10-60% of volatile components;
the particle size of the pulverized coal is 10-500 mu m, and the pulverized coal is suitable for medium-low-rank coal with the water content of less than 35%, the volatile component of 10-40% and the ash melting point of 1500 ℃;
the feeding rate of the biomass and the coal is 10-10000 kg/h, the mixing ratio of the biomass and the coal can be different according to the reaction temperature, the product yield and the product property, and the mixing ratio range is as follows: 10%, 90% -80%, 20%;
the feeding proportion of the solid particles to the mixture of the biomass and the coal dust in the integrated reactor is as follows: 50: 1-200: 1;
the heating heat source of the integrated reactor and the carbonization activation device is provided by a combustion heating furnace, and the fuel is self-produced synthetic gas or one or more of dry gas, associated gas, natural gas, diesel oil, heavy oil and pyrolysis oil;
the gasification agent is divided into an upper path, a middle path and a lower path and enters a gasification zone of the integrated reactor, the type of the gasification agent is oxygen or air or steam, the temperature of the gasification agent is 100-300 ℃, and the pressure is 0.001-8.0 MPa; the proportion of the gasification agents in the upper path, the middle path and the lower path is 5-20%: 20-50%: 30-75%.
Compared with the prior art, the invention has the following technical effects:
according to the pyrolysis and gasification integrated reactor of the circulating fluidized bed, biomass and coal are quickly pressurized, hydrogenated and converted into high-quality pyrolysis oil and synthesis gas in a segmented mode, hydrogen-rich elements, alkali metals/alkaline earth metals and free radical molecules in the coal are cooperatively utilized to carry out hydrogenation and catalytic reaction, the reaction cooperative efficiency, the carbon conversion rate and the energy conversion rate are remarkably improved, and the pyrolysis and gasification integrated reactor has the characteristics of high oil-gas yield, high synthesis gas components, high synthesis gas heat value, obvious pyrolysis oil lightening and the like, and realizes the quality-based conversion of coal resources and the resource utilization of biomass energy;
the process does not produce semicoke, except that the synthesis gas generated by gasification reaction provides heat and active atmosphere for pyrolysis reaction, the process of in-situ chemical activation of the residual semicoke is innovatively adopted to prepare the activated carbon with porous distribution and high specific surface area, the activated carbon is applied to adsorption and separation of pyrolysis water, the activated carbon is used as a pyrolysis catalyst for recycling after combustion, alkali metal/alkaline earth metal elements in ash damage the bonding coking reaction of coal, volatile components in the coal are released in a heating mode, and the yield of pyrolysis oil and the effective gas content of the synthesis gas are improved;
the process of the invention separates, purifies and recovers the cooled and recovered pyrolysis water step by step, and the pyrolysis water is converted into steam and then used as a gasifying agent to participate in gasification reaction, thereby achieving the dual purposes of reducing the steam consumption at the front end and recycling the pyrolysis water at the tail end; meanwhile, the self-produced synthesis gas is used as the fluidizing gas of the reactor, the fuel gas of the combustion heating furnace and the back blowing gas of the secondary gas-solid separator, and the active components such as hydrogen, carbon monoxide and the like in the synthesis gas are efficiently recycled for pyrolysis and gasification reaction, so that the yield of pyrolysis oil and the effective gas content of the synthesis gas are improved, the energy consumption of the device is greatly reduced, and the energy conversion efficiency is remarkable;
the process can continuously treat different types of biomass and coal, has the advantages of wide raw material adaptability, high conversion efficiency, high pyrolysis oil yield, high content of effective gas of synthesis gas and easy large-scale popularization and application, and is a green, efficient and economic processing and conversion method of biomass resources and coal.
Drawings
FIG. 1 is a schematic overall flow diagram of the present invention;
the meaning of each reference number in the figures is: 1-a solid particle storage tank; 2-solid particle pressurization tank; 3-a solid particle feeder; 4-a biomass storage tank; 5-biomass pressurized tank; 6-biomass feeder; 7-a pulverized coal storage tank; 8-a pulverized coal pressurizing tank; 9-pulverized coal feeder; 10-a fluidizing gas source; 11-a fluidized gas mixer; 12-a fluidizing gas preheater; 13-a gasifying agent mixer; 14-gasifying agent preheater; 15-ash cooler; 16-an integrated reactor; 17-gas-solid separation circulator; 18-primary gas-solid separator; 19-primary return controller; 20-a coarse particle collector; 21-secondary gas-solid separator; 22-fine ash particle collector; 23-a flash separation tank; 24-a primary liquid-solid separator; 25-quench wash tower; 26-heavy oil collection tank; 27-a secondary wash column; 28-a light oil collection tank; 29-oil water standing tank; 30-an adsorption separation tank; 31-secondary liquid-solid separator; 32-a gas-liquid intensified condenser; 33-gas-liquid intensified separator; 34-a rectifying tower; 35-oil product intermediate tank; 36-a light oil storage tank; 37-heavy oil storage tank; 38-oil tank; 39-adsorption filtration tank; 40-a back-blowing heater; 41-back-blowing booster; 42-a gas sampling tank; 43-carbonization activation device; 44-a washing separation device; 45-a separation and drying device; 46-a cyclic regeneration purified water tank; 47-purified water steam generator; 48-solid dryer; 49-combustion furnace; 50-a syngas surge tank; 51-syngas booster.
Detailed Description
The present invention will be explained in further detail with reference to examples.
As shown in FIG. 1, the embodiment provides a device for increasing oil gas yield by the synergistic conversion of biomass and coal in a circulating fluidized bed, which comprises a feeding fluidization unit, a coupling reaction unit, a purification and recovery unit and a separation and utilization unit;
the coupling reaction unit comprises a pyrolysis gasification system, a fluidized gas system, a gasifying agent system and a gas-solid dust removal system;
the purification and recovery unit comprises a grading washing system, a rectification system and a gas-liquid separation system;
the separation and utilization unit comprises an activated carbon adsorption system, an activated carbon recycling system and a purified water circulating system;
the pyrolysis gasification system comprises an integrated reactor 16 connected with an outlet of the feeding fluidization unit, an outlet at the top of the integrated reactor 16 is connected with an inlet at the upper part of a gas-solid separation circulator 17, and an outlet at the bottom of the integrated reactor 16 is connected with an ash cooler 15;
the integrated reactor 16 includes a pyrolysis zone, a transition zone, and a gasification zone; the pressure of the pyrolysis zone is 0.001-8.0 MPa, the temperature of the pyrolysis zone is 400-800 ℃, the gas velocity of the pyrolysis zone is 5-20 m/s, and the retention time is 1-10 s;
the pressure of the gasification zone is 0.001-8.0 MPa, the temperature is 900-1400 ℃, the gas velocity of the gasification zone is 0.1-2.0 m/s, and the solid circulation rate is 50-200 times;
the bottom outlet of the gas-solid separation circulator 17 is connected to the lower inlet of the integrated reactor 16 to form primary solid circulation, and the top outlet of the gas-solid separation circulator 17 is connected to a gas-solid dedusting system to perform gas-solid separation;
the outlet of the gas-solid dust removal system is connected to the activated carbon adsorption system and the grading washing system, and the outlet of the grading washing system is connected to the gas-liquid separation system and the activated carbon adsorption system;
a gas outlet of the gas-liquid separation system is connected to the fluidized gas system and the gas collecting device, and a liquid outlet of the gas-liquid separation system is connected to the rectification system;
the gas flow outlet of the rectification system is connected to the grading washing system for circulating washing and separation, and the liquid outlet of the rectification system is connected to an oil product tank 38 for oil product collection;
a solid outlet of the activated carbon adsorption system is connected to the activated carbon recycling system, a liquid outlet of the activated carbon adsorption system is connected to the purified water circulating system, and a gas outlet of the activated carbon adsorption system is connected to the grading washing system;
the activated carbon recycling system comprises a solid dryer 48 connected with a solid outlet of the activated carbon adsorption system, an outlet of the solid dryer 48 is connected to a combustion heating furnace 49, and an outlet of the combustion heating furnace 49 is respectively connected with the activated carbon adsorption system, the integrated reactor 16 and the feeding fluidization unit;
the fluidization gas system comprises a synthesis gas buffer tank 50 connected with the gas flow outlet end of the gas-liquid separation system, the outlet of the synthesis gas buffer tank 50 is connected with a synthesis gas supercharger 51, one part of the gas flow outlet of the synthesis gas supercharger 51 is connected with the inlet of the fluidization gas source 10, and the other part of the gas flow outlet of the synthesis gas supercharger 51 is connected with the combustion heating furnace 49 and used for providing fuel for the combustion heating furnace 49; the outlet end of the fluidization gas source 10 is sequentially connected with a fluidization gas mixer 11 and a fluidization gas preheater 12, and the outlet of the fluidization gas preheater 12 is connected to the inlet of an integrated reactor 16;
the gasifying agent system comprises a gasifying agent mixer 13 connected with the outlet of the purified water circulating system, and the gas outlet of the gasifying agent mixer 13 is preheated by a gasifying agent preheater 14 and then connected to the inlet of an integrated reactor 16.
The gasification agent enters a gasification zone of the integrated reactor in three ways of upper, middle and lower, the type of the gasification agent is oxygen, air or steam, the temperature of the gasification agent is 100-400 ℃, and the pressure is 0.001-8.0 MPa; the proportion relation of gasification agents of an upper path, a middle path and a lower path is as follows: 5-20%: 20-50%: 30-75%; 4-12 gasification agent nozzles uniformly distributed in an annular manner are arranged on each path, the nozzles are inclined downwards by 10-60 ℃, the gas velocity of the nozzles is 5-100 m/s, and the oxygen concentration in the gasification agent at the nozzles is 10-70%;
the grading washing system is provided with internal circulation, and the correlation circulation is arranged between the grading washing system and the gas-solid dust removal system, between the rectification system and the grading washing system, and between the purified water circulation system and the activated carbon adsorption system;
the pyrolysis gasification system, the gas-solid dust removal system, the gas sampling tank 42 and the connecting pipeline are provided with a heat tracing and heat insulating device which ensures that the operating temperature is more than 450 ℃, the heat tracing and heat insulating device ensures that the outlet of the integrated reactor 16 reaches the inlet of the quenching washing tower 25, and the temperatures of the gas-solid separation circulator 17, the primary gas-solid separator 18, the primary material returning controller 19, the coarse particle collector 20, the secondary gas-solid separator 21, the fine ash particle collector 22, the gas sampling tank 42 and the connecting pipeline are more than 450 ℃.
The yield of the co-pyrolysis oil is 15-30%, and the carbon conversion rate is>97% of the effective gas component of the syngas>75% of heat value of the synthesis gas>2200kcal/Nm 3 (ii) a The specific surface area of the activated carbon is 1400-2800 m 2 G, ash content<0.1 percent and the specific capacitance is more than or equal to 120-280F/g. Compared with coal tar, the content of sulfur in the co-pyrolysis oil is reduced by more than 50%, H/C is improved by 5-20%, the content of aliphatic hydrocarbon and aromatic hydrocarbon is increased by 10-20%, and the quality of an oil product is improved. Semicoke is not generated in the reaction process, and no pyrolysis water and polluting smoke are discharged.
The feeding fluidization unit comprises a solid particle feeding system, a biomass feeding system and a coal powder feeding system;
the solid particle feeding system comprises a solid particle storage tank 1, an outlet of the solid particle storage tank 1 is connected with an inlet of a solid particle pressurizing tank 2, an outlet of the solid particle pressurizing tank 2 is connected with an inlet of a solid particle feeder 3, and an outlet of the solid particle feeder 3 is connected with an inlet of an integrated reactor 16;
the biomass feeding system comprises a biomass storage tank 4, an outlet of the biomass storage tank 4 is connected with an inlet of a biomass pressurizing tank 5, an outlet of the biomass pressurizing tank 5 is connected with an inlet of a biomass feeder 6, and an outlet of the biomass feeder 6 is connected with an inlet of an integrated reactor 16;
the coal powder feeding system comprises a coal powder storage tank 7, an outlet of the coal powder storage tank 7 is connected with an inlet of a coal powder pressurizing tank 8, an outlet of the coal powder pressurizing tank 8 is connected with an inlet of a coal powder feeder 9, and an outlet of the coal powder feeder 9 is connected with an inlet of an integrated reactor 16.
The solid particle feeder 3, the biomass feeder 6 and the pulverized coal feeder 9 comprise a pressurized rotary feeder and a pressurized fluidized feeder;
the pressurized rotary feeder comprises a sealing rotating shaft, a spiral cylinder, a coupler, a variable frequency vibrator, a dynamic shaft seal, a shaft cooling device, a feeder, a balance pipeline, a loose pipeline, a conveying pipeline and the like;
the pressurized fluidized feeder comprises an inner cylinder, an outer cylinder, a downcomer, a loosening device, a gas distributor, a metal sintering device, a sewage discharger, a loosening pipeline, a conveying pipeline, a discharge pipeline and the like.
The solid particles are one or a combination of more of quartz sand, semicoke, biomass semicoke, petroleum coke, waste tire powder, waste catalysts, waste activated carbon and other carbon-containing materials, the particle size range is 10-500 mu m, and the reaction temperature and the bed material level are controlled by adding or discharging the solid particles on line.
The biomass is one or a combination of more of straw, walnut shells, sawdust, rice hulls, branches, livestock waste, urban household garbage and the like, and the biomass has a particle size range of 10-500 mu m, a water content of less than 50% and a volatile component of 10-60%; the particle size of the pulverized coal is 10-500 mu m, and the pulverized coal is suitable for medium-low-rank coal with the water content of less than 35%, the volatile component of 10-40% and the ash melting point of 1500 ℃; the feeding rate of the biomass and the pulverized coal is 10-10000 kg/h; the blending ratio of the biomass and the coal can be different according to the reaction temperature, the product yield and the product property, and the blending ratio range is as follows: 10 percent, 90 percent to 80 percent, 20 percent; the ratio of solid particles to the mixture of biomass and coal dust in the integrated reactor 16 is: 50: 1-200: 1;
the gas-solid dust removal system comprises a primary gas-solid separator 18 connected with an outlet at the top of the gas-solid separation circulator 17, and an outlet at the top of the primary gas-solid separator 18 is connected to an inlet at the lower part of a secondary gas-solid separator 21;
the bottom outlet of the primary gas-solid separator 18 is respectively connected with a coarse particle collector 20 and a primary material returning controller 19, and the outlet of the primary material returning controller 19 is connected with the lower inlet of the gas-solid separation circulator 17;
the outlet at the bottom of the secondary gas-solid separator 21 is connected with a fine ash particle collector 22;
the bottom outlets of the coarse particle collector 20 and the fine ash particle collector 22 are both connected to an activated carbon adsorption system.
The gas-solid separation circulator 17, the primary gas-solid separator 18 and the secondary gas-solid separator 21 collect particles with the proportion of 50-70%, 10-20% and 1-10% in sequence, and the particle diameters of the particles are 100-500 microns, 30-200 microns and 25-120 microns in sequence. The filter element in the secondary gas-solid separator 21 is composed of a double-layer structure of a large-aperture support matrix layer and a small-aperture membrane filter layer, the working temperature is 1000 ℃, the working pressure is 8.0MPa, the aperture of the filter element is 20-150 mu m, the porosity is 30-45%, and the filtering precision is 1-30 mu m.
The grading washing system comprises a quenching washing tower 25 and a flash separation tank 23 which are connected with the outlet at the top of the secondary gas-solid separator 21, the outlet of the flash separation tank 23 is connected with a heavy oil collecting tank 26 and a primary liquid-solid separator 24, and the outlet of the primary liquid-solid separator 24 is connected with the heavy oil collecting tank 26 and an activated carbon adsorption system;
the top outlet of the quench scrubber 25 is connected to the inlet of a secondary scrubber 27, and the bottom outlet is connected to a heavy oil collection tank 26;
the outlet of the heavy oil collecting tank 26 is connected with the inlet of the middle part of the quenching washing tower 25 and the inlet of the oil product intermediate tank 35;
the top outlet of the secondary washing tower 27 is connected to a gas-liquid separation system, the bottom outlet is connected to a light oil collection tank 28, the middle outlet of the light oil collection tank 28 is connected to the middle inlet of the secondary washing tower 27, and the bottom outlet is connected to an oil-water standing tank 29;
the outlet of the oil-water standing tank 29 is connected to a separation utilization unit;
the primary gas-solid separator 18, the secondary gas-solid separator 21 and the heavy oil collection tank 26 are all connected to the gas sampling tank 42;
the gas sampling tank 42 is composed of an internal structure and an external cold hydrazine structure, wherein the internal structure comprises bottom washing absorption, middle condensation recovery and upper evaporation azeotropy, and pyrolysis oil of full fraction is obtained; the solvent for bottom washing and absorption is one or a combination of more of acetone, dichloromethane, petroleum ether, ammonia water or washing oil, the oil gas temperature is 200-600 ℃, and the solvent amount is as follows: the oil gas amount is 2-10: 1; the middle part of the oil gas is provided with a condensing coil pipe for circulating a washing solvent, and the temperature of the oil gas is 10-200 ℃; the temperature of oil gas in the upper evaporation section is 10-100 ℃, and the azeotropic solvent is usedIs one or more of benzene and toluene, and the solvent amount is as follows: the oil amount is 0.5-5: 1; the temperature of the external cold hydrazine is 0 to (30) DEG C, and the cooling medium is one or the combination of more of glycol, ethanol and water; the density of the obtained full-fraction pyrolysis oil is 1.00-1.10 g/cm 3 The solid content is 0-0.5%, and the water content is 0-0.5%.
The gas-liquid separation system comprises a gas-liquid intensified condenser 32 connected with the top outlet of the secondary washing tower 27, the top outlet of the gas-liquid intensified condenser 32 is connected to an adsorption filtering tank 39, the bottom outlet of the gas-liquid intensified condenser is connected to a gas-liquid intensified separator 33, the middle outlet of the gas-liquid intensified separator 33 is connected to the inlet of the oil-water standing tank 29, and the bottom outlet of the gas-liquid intensified separator 33 is connected to a rectification system;
a back-blowing supercharger 41 and a back-blowing heater 40 are arranged between the outlet of the adsorption filtration tank 39 and the secondary gas-solid separator 21; the back-blowing gas medium is self-produced synthesis gas, and the back-blowing gas pressure is 2-6 times of the system pressure.
A synthetic gas buffer tank 50 and a synthetic gas supercharger 51 are respectively arranged between the outlet of the adsorption filtration tank 39 and the fluidized gas source 10, the gas-solid separation circulator 17 and the combustion heating furnace 49;
the adsorption filtration tank 39 is provided in parallel with two or more.
The rectification system comprises a rectification tower 34 connected with the bottom outlet of the gas-liquid intensified separator 33 and the outlet of an oil product intermediate tank 35, the bottom outlet of the rectification tower 34 is connected to an oil product tank 38, the lower outlet of the rectification tower 34 is connected with the inlet of a heavy oil storage tank 37, the outlet of the heavy oil storage tank 37 is connected with the upper inlet of the quenching washing tower 25, the upper outlet of the rectification tower 34 is connected with the inlet of a light oil storage tank 36, and the outlet of the light oil storage tank 36 is connected with the upper inlet of a secondary washing tower 27.
A settling cover, a spray head, a filter screen, a herringbone baffle plate, an anti-mixing cover and other structures, a remote transmission and on-line double-measurement liquid level meter and an anti-blocking blowing line are arranged in the quenching washing tower 25 from top to bottom, and distillate oil at 200-350 ℃ is utilized for cyclic washing; the height-diameter ratio is 5-20, the operating gas speed is 0.1-3.0 m/s, the process gas temperature is 200-350 ℃, the pressure is 0.001-8.0 MPa, and the dust content is 0-1%.
A wire mesh demister, a gas-liquid intensified separator, a horizontal tower plate, a herringbone baffle and other structures are arranged in the secondary washing tower 27 from top to bottom, and a remote transmission and online double-measurement liquid level meter is arranged, so that the secondary washing tower is circularly washed by using component oil at the temperature of 50-200 ℃; the height-diameter ratio is 3-15, the operating gas speed is 0.2-4.0 m/s, the process gas temperature is 100-250 ℃, the pressure is 0.001-8.0 MPa, and the dust content is 0-0.5%.
The activated carbon adsorption system comprises a carbonization and activation device 43 connected with outlets at the bottoms of the coarse particle collector 20, the fine ash particle collector 22 and the primary liquid-solid separator 24, an outlet pipeline of the carbonization and activation device 43 is sequentially connected with a washing and separating device 44, a separating and drying device 45 to the adsorption and separation tank 30, an inlet at the top of the adsorption and separation tank 30 is connected with an outlet at the bottom of the oil-water standing tank 29, an outlet of the adsorption and separation tank 30 is connected with a secondary liquid-solid separator 31 and a purified water circulating system, and an outlet of the secondary liquid-solid separator 31 is respectively connected with the purified water circulating system, the activated carbon recycling system and the oil product intermediate tank 35;
the carbonization and activation device is provided with a mixing tank, a distillation tank, a carbonization tank and an activation tank, the washing and separation device is provided with a reactor, a washer and a separator, and the separation and drying device is provided with a drying tank, a purification tank and a middle tank which are sequentially connected;
the heating source of the integrated reactor 16 and the carbonization activation device 43 is provided by a combustion heating furnace 49, and the fuel is one or more of self-produced synthesis gas or dry gas, associated gas, natural gas and combustible fuel such as diesel oil, heavy oil, pyrolysis oil and the like.
The purified water circulating system comprises a circulating regeneration purified water tank 46 connected with the outlets of the oil-water standing tank 29, the adsorption separation tank 30 and the secondary liquid-solid separator 31, the outlet of the circulating regeneration purified water tank 46 is connected to a purified water vapor generator 47, and the outlet of the purified water vapor generator 47 is connected with the inlet of the gasifying agent system.
The method for increasing the yield of oil gas by the synergistic conversion of the circulating fluidized bed biomass and the coal comprises the following steps:
the method comprises the following steps: fluidized temperature rise
1) Introducing a certain amount of inert gas into the integrated reactor 16 and the gas-solid separation circulator 17 for replacement purging, introducing a small amount of gas into a pressure measuring port of the system to ensure the smoothness of a pipeline, and establishing a gas fluidization system of the system;
2) the solid particles are fed in line through a solid particle storage tank 1, a solid particle pressurizing tank 2 and a solid particle feeder 3, and form circulating fluidization between an integrated reactor 16 and a gas-solid separation circulator 17. Large particles are continuously abraded and are brought to the primary gas-solid separator 18 and the secondary gas-solid separator 21 for collection, and small particles form stable circulating fluidization in the system;
3) taking solid particles as a heat carrier, carrying a large amount of heat generated by combustion in a combustion heating furnace 49, performing high-rate circulating material return (circulation rate is 50-200) between an integrated reactor 16 and a gas-solid separation circulator 17, and performing fluidization temperature rise by a system at a temperature rise rate of 5-20 ℃/h to gradually rise the temperature to 400-1400 ℃;
step two: pyrolysis gasification
1) The coal powder and the biomass enter a pyrolysis zone of the integrated reactor 16 according to a certain mass ratio; the biomass, the coal powder and the solid particle heat carrier are fully mixed (the ratio of the solid particles to the mixture of the biomass and the coal powder is 50: 1-200: 1), and the mixture is subjected to fast co-pyrolysis reaction at the pyrolysis temperature of 400-800 ℃ to generate high-temperature oil gas and semicoke, and high-rate circulation is carried out along with a large amount of inert solid particles;
2) the high-temperature oil gas containing the semicoke and the solid particles enters a gas-solid separation circulator 17, 50-70% of the semicoke and the solid particles are captured and returned to a gasification area of an integrated reactor 16, 10-20% of the semicoke enters a primary gas-solid separator 18, the semicoke is captured and returned to the gasification area of the integrated reactor 16 through a primary material returning controller 19, and the remaining 1-10% of the semicoke enters a secondary gas-solid separator 21 for capture and reuse;
3) the semicoke and the gasifying agent from the gasifying agent preheater 14 which are circularly returned enter a gasification area of the integrated reactor 16, and are subjected to combustion or gasification reaction with the gasifying agent at the high temperature of 900-1400 ℃, so that high-temperature synthesis gas which contains solid particles and is rich in hydrogen and carbon monoxide is generated and enters a pyrolysis area of the integrated reactor 16, when the carbon source of the gasification area is insufficient, redundant coal powder is supplemented and enters the gasification area, and sufficient reaction heat and atmosphere are generated to supply the pyrolysis reaction;
4) when the temperature of a gasification zone of the integrated reactor 16 is too high (> 1300-1400 ℃) or the overall circulating material level is too high, the circulating material level height can be judged through the pressure difference (within the range of 10-50KPa) of the gas-solid separation circulating gas 17. Solid particles in the reactor can be discharged through the ash cooler 15 by opening the online discharging device, so that when a large amount of solid particles enter the primary gas-solid separator 18, the temperature of the integrated reactor 16 and the height of the circulating material level are balanced, a large amount of high-temperature sensible heat is recovered, medium-pressure steam is further byproduct and enters the gasifying agent mixer 13 as a gasifying agent;
step three: purification and recovery
1) Spraying high-temperature oil gas from the secondary gas-solid separator 21 into a cooling medium, wherein the cooling medium can be self-produced heavy oil (350 ℃) or light oil (350 ℃), and enabling solid particles in the oil gas to enter a flash separation tank 23; the high-temperature oil gas without solid particles sequentially enters a quenching washing tower 25 and a secondary washing tower 27 for circular washing, and the recovered pyrolysis oil is separated into oil and water in an oil-water standing tank 29 and an adsorption separation tank 30; fractionating in the rectifying tower 34 to obtain heavy oil (350 ℃) and light oil (350 ℃) which are used as cooling media of the quenching washing tower 25 and the secondary washing tower 27;
2) the oil gas washed by the secondary washing tower 27 enters a gas-liquid separation system, passes through a gas-liquid enhanced condenser 32, a gas-liquid enhanced separator 33 and an adsorption filtration tank 39, and the residual light oil components, pyrolysis water and synthesis gas are recycled in a grading manner;
3) part of the generated synthesis gas passes through a back-blowing heater 40 and a back-blowing supercharger 41 and is respectively used as back-blowing gas (intermittent gas feeding, the back-blowing pressure is 2-6 times of the system pressure) of the secondary gas-solid separator 21 and conveying gas (the conveying pressure is 1.2-2 times of the system pressure) of the solid particle feeder 3, the biomass feeder 6 and the coal powder feeder 9; the other part of the gas passes through a synthetic gas buffer tank 50 and a synthetic gas compressor 51 and respectively enters a combustion heating furnace 49, a gas-solid separation circulator 17 and a fluidizing gas source 10, and the pressure is 1.2-2 times of the system pressure;
step four: separate utilization of
1) The semicoke from the coarse particle collector 20, the fine ash particle collector 22 and the primary liquid-solid separator 24 sequentially passes through a carbonization-activation device 43 and a washing-separation device 44, and is subjected to directional extraction, raffinate template guiding and chemical activation to prepare activated carbon;
the specific surface area of the prepared activated carbon is 1400-2800 m 2 G, ash content<0.1 percent, and the specific capacitance is more than or equal to 120-280F/g;
the activated carbon and the pyrolysis water are subjected to a biological reaction in the adsorption separation tank 30, the pyrolysis water is adsorbed and removed, and the removal rate reaches more than 95%;
2) after pyrolysis water and pyrolysis oil are removed from the saturated activated carbon through the secondary liquid-solid separator 31, the saturated activated carbon sequentially enters a solid dryer 48 and a combustion heating furnace 49, solid ash rich in alkali/alkaline earth metal generated by reaction enters the integrated reactor 16 as a pyrolysis catalyst, and the conversion rate of coal, the co-pyrolysis synergistic effect and the co-pyrolysis oil yield are improved;
3) the removed pyrolysis water is converted into medium-pressure steam with the pressure of 2.5-6 MPa and the temperature of 350-450 ℃ through a circulating regeneration purification water tank 46 and a purified water steam generator 47, and the medium-pressure steam is used as a gasifying agent and enters a gasifying agent mixer 13 for recycling, so that the input of outsourced steam is greatly reduced.
It should be noted that the above embodiments are not all embodiments of the present invention, and those skilled in the art can make various changes, substitutions and alterations without departing from the spirit of the present invention.

Claims (10)

1. A device for increasing yield of oil gas by the synergistic conversion of biomass and coal in a circulating fluidized bed is characterized by comprising a feeding fluidization unit, a coupling reaction unit, a purification and recovery unit and a separation and utilization unit;
the coupling reaction unit comprises a pyrolysis gasification system, a fluidized gas system, a gasifying agent system and a gas-solid dust removal system;
the purification and recovery unit comprises a grading washing system, a rectification system and a gas-liquid separation system;
the separation and utilization unit comprises an activated carbon adsorption system, an activated carbon recycling system and a purified water circulating system;
the pyrolysis gasification system comprises an integrated reactor (16) connected with an outlet of a feeding fluidization unit, an outlet at the top of the integrated reactor (16) is connected with an inlet at the upper part of a gas-solid separation circulator (17), and an outlet at the bottom of the integrated reactor (16) is connected with an ash cooler (15);
the integrated reactor (16) comprises a pyrolysis zone, a transition zone and a gasification zone;
the bottom outlet of the gas-solid separation circulator (17) is connected to the lower inlet of the integrated reactor (16) to form primary solid circulation, and the top outlet of the gas-solid separation circulator (17) is connected to a gas-solid dedusting system to perform gas-solid separation;
the outlet of the gas-solid dust removal system is connected to the activated carbon adsorption system and the grading washing system, and the outlet of the grading washing system is connected to the gas-liquid separation system and the activated carbon adsorption system;
a gas outlet of the gas-liquid separation system is connected to the fluidized gas system and the gas collecting equipment, and a liquid outlet of the gas-liquid separation system is connected to the rectification system;
the gas flow outlet of the rectification system is connected to a grading washing system for circulating washing and separation, and the liquid outlet of the rectification system is connected to an oil product tank (38) for oil product collection;
a solid outlet of the activated carbon adsorption system is connected to the activated carbon recycling system, a liquid outlet of the activated carbon adsorption system is connected to the purified water circulating system, and a gas outlet of the activated carbon adsorption system is connected to the grading washing system;
the activated carbon recycling system comprises a solid dryer (48) connected with a solid outlet of the activated carbon adsorption system, an outlet of the solid dryer (48) is connected to a combustion heating furnace (49), and an outlet of the combustion heating furnace (49) is respectively connected with the activated carbon adsorption system, the integrated reactor (16) and a feeding fluidization unit;
the fluidized gas system comprises a synthesis gas buffer tank (50) connected with the gas flow outlet end of the gas-liquid separation system, the outlet of the synthesis gas buffer tank (50) is connected with a synthesis gas booster (51), one part of the gas flow outlet of the synthesis gas booster (51) is connected with the inlet of a fluidized gas source (10), and the other part of the gas flow outlet of the synthesis gas booster is connected with a combustion heating furnace (49) and used for providing fuel for the combustion heating furnace (49); the outlet end of the fluidization gas source (10) is sequentially connected with a fluidization gas mixer (11) and a fluidization gas preheater (12), and the outlet of the fluidization gas preheater (12) is connected to the inlet of the integrated reactor (16);
the gasification agent system comprises a gasification agent mixer (13) connected with the outlet of the purified water circulation system, and the gas outlet of the gasification agent mixer (13) is preheated by a gasification agent preheater (14) and then connected to the inlet of the integrated reactor (16).
2. The device for increasing the yield of oil and gas through the synergistic conversion of biomass and coal in the circulating fluidized bed according to claim 1, wherein the staged washing system is provided with internal circulation, and the staged washing system and the gas-solid dust removal system, the rectification system and the staged washing system, and the purified water circulation system and the activated carbon adsorption system are in associated circulation;
the pyrolysis gasification system, the gas-solid dust removal system, the gas sampling tank (42) and the connecting pipeline are provided with a heat tracing and heat insulating device which ensures that the operation temperature is more than 450 ℃.
3. The device for increasing the yield of oil and gas through the cooperative conversion of biomass and coal in the circulating fluidized bed according to claim 1, wherein the feeding fluidization unit comprises a solid particle feeding system, a biomass feeding system and a coal dust feeding system;
the solid particle feeding system comprises a solid particle storage tank (1), wherein an outlet of the solid particle storage tank (1) is connected with an inlet of a solid particle pressurizing tank (2), an outlet of the solid particle pressurizing tank (2) is connected with an inlet of a solid particle feeder (3), and an outlet of the solid particle feeder (3) is connected with an inlet of an integrated reactor (16);
the biomass feeding system comprises a biomass storage tank (4), an outlet of the biomass storage tank (4) is connected with an inlet of a biomass pressurizing tank (5), an outlet of the biomass pressurizing tank (5) is connected with an inlet of a biomass feeder (6), and an outlet of the biomass feeder (6) is connected with an inlet of an integrated reactor (16);
buggy charge-in system include buggy storage tank (7), the exit linkage buggy pressurized tank (8) of buggy storage tank (7) enter the mouth, buggy pressurized tank (8) exit linkage buggy feeder (9) entry, the exit linkage integration reactor (16) entry of buggy feeder (9).
4. The device for the synergistic conversion of biomass and coal into oil and gas for the stimulation of oil and gas of claim 1, wherein the gas-solid dust removal system comprises a primary gas-solid separator (18) connected with a top outlet of a gas-solid separation circulator (17), and a top outlet of the primary gas-solid separator (18) is connected with a lower inlet of a secondary gas-solid separator (21);
the bottom outlet of the primary gas-solid separator (18) is respectively connected with a coarse particle collector (20) and a primary material returning controller (19), and the outlet of the primary material returning controller (19) is connected to the lower inlet of the gas-solid separation circulator (17);
the bottom outlet of the secondary gas-solid separator (21) is connected with a fine ash particle collector (22);
the bottom outlets of the coarse particle collector (20) and the fine ash particle collector (22) are connected to an activated carbon adsorption system.
5. The device for the synergistic conversion of biomass and coal into oil and gas for the stimulation of oil and gas of the circulating fluidized bed as claimed in claim 4, wherein the staged washing system comprises a quenching washing tower (25) and a flash separation tank (23) which are connected with the top outlet of the secondary gas-solid separator (21), the outlet of the flash separation tank (23) is connected with a heavy oil collecting tank (26) and a primary liquid-solid separator (24), and the outlet of the primary liquid-solid separator (24) is connected with the heavy oil collecting tank (26) and an activated carbon adsorption system;
the top outlet of the quenching washing tower (25) is connected to the inlet of the secondary washing tower (27), and the bottom outlet is connected to the heavy oil collecting tank (26);
the outlet of the heavy oil collecting tank (26) is connected with the inlet in the middle of the quenching washing tower (25) and the inlet of the oil product intermediate tank (35);
the top outlet of the secondary washing tower (27) is connected to a gas-liquid separation system, the bottom outlet of the secondary washing tower is connected to a light oil collecting tank (28), the middle outlet of the light oil collecting tank (28) is connected to the middle inlet of the secondary washing tower (27), and the bottom outlet of the secondary washing tower is connected to an oil-water standing tank (29);
the outlet of the oil-water standing tank (29) is connected to a separation utilization unit;
the primary gas-solid separator (18), the secondary gas-solid separator (21) and the heavy oil collecting tank (26) are all connected to a gas sampling tank (42);
the gas sampling tank (42) is composed of an internal structure and an external cold hydrazine structure, wherein the internal structure comprises bottom washing absorption, middle condensation recovery and upper evaporation azeotropy, and the external cold hydrazine structure is adopted to obtain full fraction pyrolysis oil.
6. The device for increasing the yield of oil and gas through the synergistic conversion of the circulating fluidized bed biomass and the coal as claimed in claim 5, wherein the gas-liquid separation system comprises a gas-liquid enhanced condenser (32) connected with the top outlet of the secondary washing tower (27), the top outlet of the gas-liquid enhanced condenser (32) is connected to the adsorption filtration tank (39), the bottom outlet of the gas-liquid enhanced condenser is connected to the gas-liquid enhanced separator (33), the middle outlet of the gas-liquid enhanced separator (33) is connected to the inlet of the oil-water standing tank (29), and the bottom outlet of the gas-liquid enhanced separator (33) is connected to the rectification system;
a back-blowing supercharger (41) and a back-blowing heater (40) are arranged between the outlet of the adsorption filtration tank (39) and the secondary gas-solid separator (21);
the outlet of the adsorption filtration tank (39) is respectively connected with a fluidized gas source (10), a gas-solid separation circulator (17) and a combustion heating furnace (49), and a synthetic gas buffer tank (50) and a synthetic gas supercharger (51) are arranged on the outlet pipeline of the adsorption filtration tank (39);
the adsorption filtration tank (39) is provided with two or more than two in parallel.
7. The device for increasing the yield of oil and gas by the synergistic conversion of the circulating fluidized bed biomass and coal as claimed in claim 6, wherein the rectification system comprises a rectification tower (34) connected with a bottom outlet of the gas-liquid enhanced separator (33) and an outlet of an oil intermediate tank (35), the bottom outlet of the rectification tower (34) is connected to an oil tank (38), a lower outlet of the rectification tower (34) is connected to an inlet of a heavy oil storage tank (37), an outlet of the heavy oil storage tank (37) is connected to an upper inlet of the quenching washing tower (25), an upper outlet of the rectification tower (34) is connected to an inlet of a light oil storage tank (36), and an outlet of the light oil storage tank (36) is connected to an upper inlet of the secondary washing tower (27).
8. The device for increasing the yield of oil and gas through the cooperative conversion of the biomass and the coal in the circulating fluidized bed according to claim 6, wherein the activated carbon adsorption system comprises a carbonization and activation device (43) connected with outlets at the bottoms of the coarse particle collector (20), the fine ash particle collector (22) and the primary liquid-solid separator (24), and an outlet pipeline of the carbonization and activation device (43) is sequentially connected with a washing and separation device (44) and a separation and drying device (45) to the adsorption and separation tank (30); the top inlet of the adsorption separation tank (30) is connected with the bottom outlet of the oil-water standing tank (29), the outlet of the adsorption separation tank (30) is connected with a secondary liquid-solid separator (31) and a purified water circulating system, and the outlet of the secondary liquid-solid separator (31) is respectively connected with the purified water circulating system, an activated carbon recycling system and an oil product intermediate tank (35);
the purified water circulating system comprises a circulating regeneration purified water tank (46) connected with outlets of an oil-water standing tank (29), an adsorption separation tank (30) and a secondary liquid-solid separator (31), an outlet of the circulating regeneration purified water tank (46) is connected to a purified water vapor generator (47), and an outlet of the purified water vapor generator (47) is connected with an inlet of a gasifying agent system.
9. A method for increasing oil and gas yield by using circulating fluidized bed biomass and coal for the cooperative conversion of the biomass and the coal in the device of any one of claims 1 to 8, which comprises the following steps:
the method comprises the following steps: fluidized temperature rise
1) Introducing a certain amount of inert gas into the integrated reactor (16) and the gas-solid separation circulator (17) for replacement purging, introducing a small amount of gas into a pressure measuring port of the system to ensure the smoothness of a pipeline, and establishing a gas fluidization system of the system;
2) the solid particles are fed in line through a solid particle storage tank (1), a solid particle pressurization tank (2) and a solid particle feeder (3), and the solid particles form circulating fluidization between an integrated reactor (16) and a gas-solid separation circulator (17). Large particles are continuously abraded and are brought to a primary gas-solid separator (18) and a secondary gas-solid separator (21) for capture, and small particles form stable circulating fluidization in the system;
3) taking solid particles as a heat carrier, carrying a large amount of heat generated by combustion in a combustion heating furnace (49), performing high-rate circulating material returning with the circulating rate of 50-200 between an integrated reactor (16) and a gas-solid separation circulator (17), and performing fluidization temperature rise by the system at the temperature rise rate of 5-20 ℃/h to gradually rise the temperature to 400-1400 ℃;
step two: pyrolysis gasification
1) Coal powder and biomass enter a pyrolysis zone of the integrated reactor (16) according to a certain mass ratio; the biomass, the coal powder and the solid particle heat carrier are fully mixed, and a rapid co-pyrolysis reaction is carried out at the pyrolysis temperature of 400-800 ℃, so that high-temperature oil gas and semicoke are generated, and high-rate circulation is carried out along with a large amount of inert solid particles;
2) high-temperature oil gas containing semicoke and solid particles enters a gas-solid separation circulator (17), 50-70% of semicoke and solid particles are captured and returned to a gasification zone of an integrated reactor (16), 10-20% of semicoke enters a primary gas-solid separator (18), the semicoke is captured and returned to the gasification zone of the integrated reactor (16) through a primary material returning controller (19), and the remaining 1-10% of semicoke enters a secondary gas-solid separator (21) for capture and reuse;
3) the semicoke and the gasifying agent from the gasifying agent preheater (14) which are circularly returned enter a gasification area of the integrated reactor (16), and are subjected to combustion or gasification reaction with the gasifying agent at the high temperature of 900-1400 ℃, so that high-temperature synthesis gas which contains solid particles and is rich in hydrogen and carbon monoxide is generated and enters a pyrolysis area of the integrated reactor (16), when the carbon source of the gasification area is insufficient, redundant coal powder is supplemented and enters the gasification area, and sufficient reaction heat and atmosphere are generated to supply the pyrolysis reaction;
4) when the temperature of the gasification zone of the integrated reactor (16) is overhigh or the whole circulating material level is overhigh, the circulating material level height can be judged through the pressure difference of the gas-solid separation circulating gas (17). Solid particles in the reactor can be discharged through the ash cooler (15) by opening the online discharging device, so that when a large amount of solid particles enter the primary gas-solid separator (18), the temperature of the integrated reactor (16) and the height of the circulating material level are balanced, a large amount of high-temperature sensible heat is recovered, medium-pressure steam is further byproduct, and the medium-pressure steam enters the gasifying agent mixer (13) as a gasifying agent;
step three: purification and recovery
1) Spraying high-temperature oil gas from the secondary gas-solid separator (21) into a cooling medium, wherein the cooling medium can be self-produced heavy oil or light oil, and enabling solid particles in the oil gas to enter a flash separation tank (23); the high-temperature oil gas without solid particles sequentially enters a quenching washing tower (25) and a secondary washing tower (27) for circular washing, and the recovered pyrolysis oil is subjected to oil-water separation in an oil-water standing tank (29) and an adsorption separation tank (30); heavy oil and light oil obtained by fractionation in the rectifying tower (34) are used as cooling media of the quenching washing tower (25) and the secondary washing tower (27);
2) the oil gas washed by the secondary washing tower (27) enters a gas-liquid separation system, passes through a gas-liquid reinforced condenser (32), a gas-liquid reinforced separator (33) and an adsorption filter tank (39), and the residual light oil components, pyrolysis water and synthesis gas are recycled in a grading manner;
3) part of the generated synthesis gas passes through a back-blowing heater (40) and a back-blowing supercharger (41) and is respectively used as back-blowing gas of a secondary gas-solid separator (21) and conveying gas of a solid particle feeder (3), a biomass feeder (6) and a coal powder feeder (9); the other part of the gas passes through a synthesis gas buffer tank (50) and a synthesis gas compressor (51) and respectively enters a combustion heating furnace (49), a gas-solid separation circulator (17) and a fluidizing gas source (10);
step four: separate utilization of
1) Semi-coke from a coarse particle collector (20), a fine ash particle collector (22) and a primary liquid-solid separator (24) sequentially passes through a carbonization and activation device (43) and a washing and separation device (44), active carbon is prepared by directional extraction, raffinate template guiding and chemical activation, the active carbon and pyrolysis water physically react in an adsorption and separation tank (30), the pyrolysis water is adsorbed and removed, and the removal rate reaches more than 95%;
2) after pyrolysis water and pyrolysis oil are removed from saturated activated carbon through a secondary liquid-solid separator (31), the saturated activated carbon sequentially enters a solid dryer (48) and a combustion heating furnace (49) to react to generate solid ash rich in alkali/alkaline earth metal, and the solid ash is used as a pyrolysis catalyst and enters an integrated reactor (16), so that the conversion rate of coal, the co-pyrolysis synergistic effect and the co-pyrolysis oil yield are improved;
3) the removed pyrolysis water is converted into medium-pressure steam with the pressure of 2.5-6 MPa and the temperature of 350-450 ℃ through a circulating regeneration purification water tank (46) and a purified water steam generator (47), and the medium-pressure steam is used as a gasifying agent and enters a gasifying agent mixer (13) for recycling, so that the input of outsourcing steam is greatly reduced.
10. The method for increasing the yield of oil and gas through the synergistic conversion of the circulating fluidized bed biomass and coal as claimed in claim 9, wherein the solid particles are one or a combination of more of quartz sand, semicoke, biomass coke, petroleum coke, waste tire powder, waste catalysts, waste activated carbon and other carbon-containing materials, the particle size range is 10-500 μm, and the reaction temperature and the bed material level are controlled by adding or discharging the solid particles on line;
the biomass type is one or a combination of more of straw, walnut shells, sawdust, rice hulls and branches, and is suitable for biomass with the particle size range of 10-500 mu m, the water content of less than 50% and the volatile component of 10-60%;
the particle size of the pulverized coal is 10-500 mu m, and the pulverized coal is suitable for medium-low-rank coal with the water content of less than 35%, the volatile component of 10-40% and the ash melting point of 1500 ℃;
the feeding rate of the biomass and the coal is 10-10000 kg/h, the mixing ratio of the biomass and the coal can be different according to the reaction temperature, the product yield and the product property, and the mixing ratio range is as follows: 10 percent, 90 percent to 80 percent, 20 percent;
the feeding proportion of the solid particles to the mixture of the biomass and the coal dust is as follows: 50: 1-200: 1;
the heating heat source of the integrated reactor (16) and the carbonization activation device (43) is provided by a combustion heating furnace (49), and the fuel is self-produced synthesis gas or one or more of dry gas, associated gas, natural gas, diesel oil, heavy oil and pyrolysis oil;
the gasification agent is divided into an upper path, a middle path and a lower path and enters a gasification zone of the integrated reactor (16), the type of the gasification agent is oxygen, air or steam, the temperature of the gasification agent is 100-300 ℃, and the pressure is 0.001-8.0 MPa; the proportion of the gasification agents in the upper path, the middle path and the lower path is 5-20%: 20-50%: 30-75%.
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CN110819384A (en) * 2019-11-26 2020-02-21 陕西延长石油（集团）有限责任公司 Fluidized bed heavy oil cracking and gasification grading conversion device and method
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