CN107916141B - Biomass and low-rank coal gasification-flash pyrolysis staged utilization method - Google Patents

Biomass and low-rank coal gasification-flash pyrolysis staged utilization method Download PDF

Info

Publication number
CN107916141B
CN107916141B CN201610882933.7A CN201610882933A CN107916141B CN 107916141 B CN107916141 B CN 107916141B CN 201610882933 A CN201610882933 A CN 201610882933A CN 107916141 B CN107916141 B CN 107916141B
Authority
CN
China
Prior art keywords
pyrolysis
gasification
biomass
gas
furnace
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201610882933.7A
Other languages
Chinese (zh)
Other versions
CN107916141A (en
Inventor
霍威
钟思青
徐俊
屠功毅
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Original Assignee
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by China Petroleum and Chemical Corp, Sinopec Shanghai Research Institute of Petrochemical Technology filed Critical China Petroleum and Chemical Corp
Priority to CN201610882933.7A priority Critical patent/CN107916141B/en
Publication of CN107916141A publication Critical patent/CN107916141A/en
Application granted granted Critical
Publication of CN107916141B publication Critical patent/CN107916141B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • 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
    • 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
    • C10J3/62—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
    • 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
    • C10J2300/093—Coal
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention relates to a biomass and low-rank coal gasification-flash pyrolysis graded utilization method, which mainly solves the problems that the yield of tar is low, low-rank coal is difficult to utilize, excessive dependence on a heat carrier is caused and the like in the prior art. The invention mainly comprises the following steps by adopting the combination of technologies of gasification synthesis gas preparation and flash pyrolysis tar preparation: the mixture of the low-rank coal and the biomass enters a pyrolysis furnace through a feeding device, is heated by high-temperature circulating semicoke from a gasification furnace, is subjected to flash pyrolysis at high linear speed, and is separated out to obtain semicoke; volatile components are sent into a condenser for rapid condensation through a gas-solid separation device to obtain a tar product mainly containing biomass oil, and the semicoke is sent into a gasification furnace to react with a gasification agent to generate synthesis gas and high-temperature circulating semicoke; after the separation, the synthesis gas is purified and processed by the purification device to serve as chemical raw materials, and the high-temperature circulating semicoke is sent into the pyrolysis furnace to continue to provide heat for the raw materials for pyrolysis, so that the method can be used in the technical field of coal chemical industry.

Description

Biomass and low-rank coal gasification-flash pyrolysis staged utilization method
Technical Field
The invention belongs to the technical field of pyrolysis, gasification and staged utilization of biomass and coal, and particularly relates to a method for realizing co-production of synthesis gas and tar by staged utilization of biomass and low-rank coal gasification and flash pyrolysis.
Background
China is a country which takes coal as a main energy structure and cannot change for a long time in the future, and according to statistics, coal reaches 66% in the primary energy consumption structure of China. With the increasing shortage of petroleum resources, the effective utilization of coal resources has become a strategy for sustainable development of energy in China. The reserve of low-rank coal in China accounts for more than 55% of the total amount of coal resources, but the low-rank coal has high water content, low coalification degree and low direct combustion efficiency, thereby not only wasting resources, but also polluting the environment and causing the emission of acid rain, PM2.5, SOx, NOx and other greenhouse gases. Therefore, coal conversion techniques aimed at reducing pollution have received great attention. Among the coal utilization technologies, coal gasification is a basic technology for coal energy conversion and is also the most important process in the development of coal chemical industry. The realization of the efficient and clean utilization of coal is the key for realizing the sustainable development of energy in China and is an effective way for solving the global energy and environment problems.
The biomass mainly comprises carbohydrates formed by fixing solar energy through plant photosynthesis, has the characteristics of wide distribution, huge reserves, environmental friendliness, zero emission of greenhouse gases and the like, and is the only renewable resource capable of being converted into gas, liquid and solid fuels simultaneously. Compared with coal, the structure of the biomass gasification furnace is loose, the content of elements such as hydrogen and oxygen is high, hydrogen-rich gas or rich tar can be generated by pyrolysis, and the gasification reaction activity of biomass is also high. According to the report, a certain synergistic effect exists in the process of co-gasification or co-pyrolysis of biomass and coal, so that the co-pyrolysis or co-gasification of the biomass and the coal not only overcomes the problems in the process of separate gasification or pyrolysis of the biomass and the coal, but also improves the efficiency of gasification or pyrolysis, and is an economic and environment-friendly energy utilization mode.
The synthesis gas prepared by gasifying coal or biomass can further synthesize various chemical products (such as methanol, ethylene, propylene and the like), and is the technology with the most development situation in the thermochemical conversion technology. In addition, the biomass is subjected to flash pyrolysis, so that a large amount of biomass oil can be obtained, the dual effects of reducing the pollution to the environment and improving the utilization of resources can be achieved, and researches show that the biomass oil is an excellent liquid fuel and a chemical product raw material, so that the biomass oil preparation technology also receives wide attention.
In a traditional process for preparing synthesis gas by gasifying biomass or coal, air-steam, air-carbon dioxide and the like are generally adopted as gasification media and are subjected to gasification reaction with raw materials under a high-temperature condition, so that the synthesis gas is obtained, continuous production can be guaranteed, and the treatment efficiency is high. However, the generated gas contains more tar, and generally needs subsequent equipment to treat the tar, a reforming synthesizer and other problems, so that the operation is complicated and the flow is complex. The traditional biomass flash pyrolysis oil production is generally that the biomass is pyrolyzed under the condition of complete oxygen deficiency or limited oxygen supply, the pyrolysis product takes condensable gas as the main component, and finally the condensable gas is condensed into the biomass oil, the oil production process is simple, the yield of liquid products is high, and a matched heat source is required in the process to supply heat required by the pyrolysis of the raw materials. In the prior art, heated sand particles and other substances are generally used as heat carriers to supply heat required by pyrolysis of raw materials. However, the addition of the heat carrier not only increases the raw material cost, but also brings many difficulties to the subsequent separation treatment, so that the operation of the whole process flow becomes complicated, and the problems of abrasion to equipment, high power consumption and the like exist.
In order to solve the difficulties in the traditional process, the Chinese invention patent CN102504842A provides a pyrolysis-gasification-combustion three fluidized bed device, which aims to realize the co-production of synthesis gas and tar, but the pyrolysis device of the process adopts a bubbling bed reactor, the residence time distribution of medium and low rank coal in the reactor is wide, the residence time is longer, the selectivity of the target product tar is reduced, and the generation of high-quality tar is not facilitated. The university of Tokyo (Chemical Engineering Journal,164(2010) 221-229; Chemical Engineering Science,66(2011)4212-4220) of Japan proposes a gasification pyrolysis graded utilization process, realizes the precise control of pyrolysis time, simultaneously realizes the separation of pyrolysis gas-solid products in front of a gasification furnace, avoids the inhibiting effect of volatile components on the gasification of the semicoke to prepare synthesis gas, but the process adopts quartz sand as a heat-carrying substance, which causes the serious abrasion of equipment.
Although the existing pyrolysis-gasification grading utilization technology solves the defects of the traditional gasification for preparing synthesis gas and pyrolysis for preparing oil to a certain extent, the yield of tar is obviously reduced due to the limitation of the process flow, or the problems of overlarge energy consumption, equipment damage and the like occur due to the additional addition of a heat carrier. Therefore, how to further improve the tar yield, reasonably use or simplify the heat carrier and realize the synthesis gas-tar co-production in the real sense becomes the development key of the pyrolysis-gasification graded utilization technology.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a gasification-pyrolysis grading utilization method suitable for high-efficiency utilization of biomass and low-rank coal, so that the dependence on a heat carrier in the prior art is simplified, the yield of tar is greatly improved, and the co-production of synthesis gas and tar is realized.
In order to solve the technical problem, the invention provides a technical scheme of a biomass and low-rank coal gasification-flash pyrolysis graded utilization method, which comprises the following steps:
a biomass and low-rank coal gasification-flash pyrolysis graded utilization method is characterized in that a mixture of biomass and coal of a raw material A enters a pyrolysis furnace 1 through feeding equipment and is mixed with high-temperature circulating semicoke particles from a gasification furnace 4, the raw material is rapidly heated by heat carried by the high-temperature circulating semicoke particles, rapid pyrolysis is realized under an inert atmosphere B, and volatile components are separated out to generate pyrolysis semicoke particles; the volatile components and the semicoke particles generated by pyrolysis are separated by the first gas-solid separation equipment 2, wherein the gas is sent into the condenser 3 for rapid condensation, and high-quality tar mainly comprising the biomass oil C is generated, and the pyrolysis semicoke particles are sent into the gasification furnace 4 after being separated and are subjected to gasification reaction with the gasification agent D, so that a large amount of synthesis gas and high-temperature circulating semicoke particles are formed. And (3) separating the synthesis gas E generated by gasification and the high-temperature circulating semicoke particles through a second gas-solid separation device 5, wherein the high-temperature circulating semicoke particles are separated and then enter the pyrolysis furnace 1, and the synthesis gas E is separated and then sent to a gas purification device 6 for purification and processing to be used as a chemical raw material.
The raw material coal is a mixture of biomass and coal, wherein the raw material coal is low-rank low-grade coal, and the raw material biomass is garden waste of herbaceous or woody plants.
The particle size of the mixture of the raw material coal and the biomass is smaller than 1mm, so that complete release of volatile components in the flash pyrolysis process is facilitated.
The mass ratio of the raw material coal to the biomass is 2-4: 10.
The temperature of the pyrolysis furnace 1 is 500-650 ℃, and the pressure is normal pressure.
The inert atmosphere B is selected from one of nitrogen or argon.
The pyrolysis furnace 1 adopts a flash pyrolysis technology, the linear speed in the furnace is 20-30m/s, and the residence time of particles in the furnace is 0.60-1 s.
Preferably, the pyrolysis furnace 1 employs flash pyrolysis technology, with a linear velocity in the furnace of 25-28m/s and a residence time of the particles in the furnace of 0.7-0.8 s.
In the biomass and low-rank coal gasification-flash pyrolysis staged utilization method, volatile matters enter a condenser 3 to be rapidly condensed into liquid after passing through a first gas-solid separation device 2. In order to prevent the condensable gas from being converted into the non-condensable gas through secondary pyrolysis, the condenser adopts a spray type condenser.
The temperature of the gasification furnace 4 is 700-850 ℃, and the pressure is 4MPa-6.5 MPa.
The gasification agent in the gasification furnace 4 is a mixture of oxygen and water vapor, wherein the oxygen accounts for 15-20% of the total amount. .
Brief description of the invention
The gasification and flash pyrolysis are coupled into a whole, the flash pyrolysis is carried out in the pyrolysis furnace, the gasification reaction of the pyrolysis semicoke particles is carried out in the gasification furnace, and the high-temperature circulating semicoke particles after gasification are used as a heat carrier and circularly enter the pyrolysis furnace to be used as a heat source of the flash pyrolysis, so that the energy consumption of the whole circulating system is reduced, and the cost of the heat carrier added in the traditional process is saved. The raw material of the circulating system adopts the mixture of the low-rank coal and the biomass, and the reasonable proportion of the low-rank coal and the biomass ensures the synergistic effect of the coal and the biomass in the pyrolysis and gasification processes, so that the carbon conversion rate is improved (up to 98 percent), and the current situation that the low-rank coal is difficult to utilize is also solved.
By adopting the technical scheme of the invention, the synthesis gas and tar are coproduced in the real sense under the arrangement of gasification of the mixture of the low-rank coal and the biomass and grading utilization of flash pyrolysis and the processes of high linear speed of the pyrolysis furnace, short retention of particles and quick cooling of product gas. The yield of tar in the product can reach 46 percent, and the effective gas H in the gas product2+CH4The content of CO is 67%, the carbon conversion rate is 98%, and the method has the characteristics of high gasification strength, high energy utilization rate, low pollution and the like, reduces the production cost to a great extent, and has a good application prospect.
Drawings
Fig. 1 is a schematic diagram of the staged utilization of biomass and low-rank coal gasification-flash pyrolysis provided by the invention.
In the figure, 1-pyrolysis furnace; 2-a first gas-solid separation device; 3-a condenser; 4-gasification furnace; 5-a second gas-solid separation device; 6-gas purification device. A-raw materials; b-inert atmosphere; c-biomass oil; d-a gasifying agent; e-synthesis gas.
Detailed Description
The features of the invention will be described in more detail below with reference to the accompanying drawings and examples.
[ example 1 ]
The mixture of biomass and lignite with the ratio of 10:2 is fed into a pyrolysis furnace 1 through feeding equipment, and is mixed with high-temperature circulating semicoke particles which come from a gasification furnace 4 and are separated by second gas-solid separation equipment 5, so that the mixture of raw material biomass and low-order low-grade coal (particle size)<1mm) is rapidly heated by the heat carried by the high-temperature circulating semicoke, and the pyrolysis gas and the pyrolysis semicoke are generated through the thermolysis volatile reaction under the nitrogen atmosphere. And separating the pyrolysis gas and the pyrolysis semicoke through a first gas-solid separation device 2, wherein the pyrolysis gas is sent into a condenser 3 for rapid condensation, the operation temperature of the pyrolysis furnace is controlled to be 500 ℃, and the linear speed is 30 m/s. Therefore, most pyrolysis gas is condensable gas, high-quality tar mainly comprising biomass oil is obtained after rapid condensation, and the tar yield is as high as 44%. And the pyrolysis semicoke is separated and then sent into a gasification furnace 4 to be subjected to gasification reaction with a gasification agent (oxygen and water vapor) to form a large amount of synthesis gas and high-temperature circulating semicoke. The operation temperature of the gasification furnace is controlled by adjusting the oxygen content in the gasification agent, and when the oxygen content is controlled to be about 15%, the operation temperature of the gasification furnace is 700 ℃. The synthesis gas and the high-temperature circulating semi-coke generated by gasification are separated by a second gas-solid separation device 5, wherein the synthesis gas is separated and then sent to a gas purification device 6 for purification and processing. When the operating pressure of the gasification furnace is 4.0MPa,its synthesis gas effective component H2CO and CH4The contents are 42.3%, 18.9% and 5.1% respectively. And the high-temperature circulating semicoke is separated by the second gas-solid separation equipment 5 and then is sent into the pyrolysis furnace 1 to continuously carry out pyrolysis reaction with the mixture of the raw material biomass and the coal, and the carbon conversion rate of the whole circulating reaction system reaches 96% due to the synergistic effect of the coal and the biomass in the pyrolysis and gasification reactions.
[ example 2 ]
The mixture of biomass and lignite with the ratio of 10:2 is fed into a pyrolysis furnace 1 through feeding equipment, and is mixed with high-temperature circulating semicoke particles which come from a gasification furnace 4 and are separated by second gas-solid separation equipment 5, so that the mixture of raw material biomass and low-order low-grade coal (particle size)<1mm) is rapidly heated by the heat carried by the high-temperature circulating semicoke, and the pyrolysis gas and the pyrolysis semicoke are generated through the thermolysis volatile reaction under the nitrogen atmosphere. And separating the pyrolysis gas and the pyrolysis semicoke through a first gas-solid separation device 2, wherein the pyrolysis gas is sent into a condenser 3 for rapid condensation, the operation temperature of the pyrolysis furnace is controlled to be 650 ℃, and the linear speed is 30 m/s. Therefore, most pyrolysis gas is condensable gas, high-quality tar mainly comprising biomass oil is obtained after rapid condensation, and the tar yield reaches 41%. And the pyrolysis semicoke is separated and then sent into a gasification furnace 4 to be subjected to gasification reaction with a gasification agent (oxygen and water vapor) to form a large amount of synthesis gas and high-temperature circulating semicoke. The operation temperature of the gasification furnace is controlled by adjusting the oxygen content in the gasification agent, and when the oxygen content is controlled to be about 20 percent, the operation temperature of the gasification furnace is 850 ℃. The synthesis gas and the high-temperature circulating semi-coke generated by gasification are separated by a second gas-solid separation device 5, wherein the synthesis gas is separated and then sent to a gas purification device 6 for purification and processing. When the operating pressure of the gasification furnace is 4.0MPa, the effective component H of the synthesis gas2CO and CH4The contents are 39.9%, 20.1% and 6.3% respectively. The high-temperature circulating semicoke is separated by the second gas-solid separation equipment 5 and then is sent into the pyrolysis furnace 1 to be continuously subjected to pyrolysis reaction with the mixture of the raw material biomass and the coal, and the carbon conversion rate of the whole circulating reaction system reaches 98 percent due to the synergistic effect of the coal and the biomass in the pyrolysis reaction and the gasification reaction。
[ example 3 ]
The mixture of biomass and lignite with the ratio of 10:2 is fed into a pyrolysis furnace 1 through feeding equipment, and is mixed with high-temperature circulating semicoke particles which come from a gasification furnace 4 and are separated by second gas-solid separation equipment 5, so that the mixture of raw material biomass and low-order low-grade coal (particle size)<1mm) is rapidly heated by the heat carried by the high-temperature circulating semicoke, and the pyrolysis gas and the pyrolysis semicoke are generated through the thermolysis volatile reaction under the nitrogen atmosphere. And separating the pyrolysis gas and the pyrolysis semicoke through a first gas-solid separation device 2, wherein the pyrolysis gas is sent into a condenser 3 for rapid condensation, the operation temperature of the pyrolysis furnace is controlled to be 500 ℃, and the linear speed is 30 m/s. Therefore, most pyrolysis gas is condensable gas, high-quality tar mainly comprising biomass oil is obtained after rapid condensation, and the tar yield reaches 44%. And the pyrolysis semicoke is separated and then sent into a gasification furnace 4 to be subjected to gasification reaction with a gasification agent (oxygen and water vapor) to form a large amount of synthesis gas and high-temperature circulating semicoke. The operation temperature of the gasification furnace is controlled by adjusting the oxygen content in the gasification agent, and when the oxygen content is controlled to be 15%, the operation temperature of the gasification furnace is 700 ℃. The synthesis gas and the high-temperature circulating semi-coke generated by gasification are separated by a second gas-solid separation device 5, wherein the synthesis gas is separated and then sent to a gas purification device 6 for purification and processing. When the operating pressure of the gasification furnace is 6.5MPa, the effective component H of the synthesis gas2CO and CH4The contents are respectively 37.5%, 20.9% and 8.3%. And the high-temperature circulating semicoke is separated by the second gas-solid separation equipment 5 and then is sent into the pyrolysis furnace 1 to continuously carry out pyrolysis reaction with the mixture of the raw material biomass and the coal, and the carbon conversion rate of the whole circulating reaction system reaches 96% due to the synergistic effect of the coal and the biomass in the pyrolysis and gasification reactions.
[ example 4 ]
The mixture of biomass and lignite with the ratio of 10:4 is fed into the pyrolysis furnace 1 through feeding equipment, and is mixed with high-temperature circulating semicoke particles which come from the gasification furnace 4 and are separated by the second gas-solid separation equipment 5, and the mixture (particle size) of raw material biomass and low-order low-grade coal is obtained<1mm) is rapidly heated by the heat carried by the high-temperature circulating semicokeAnd carrying out thermal decomposition volatile component removal reaction under the nitrogen atmosphere to generate pyrolysis gas and pyrolysis semicoke. And separating the pyrolysis gas and the pyrolysis semicoke through a first gas-solid separation device 2, wherein the pyrolysis gas is sent into a condenser 3 for rapid condensation, the operation temperature of the pyrolysis furnace is controlled to be 500 ℃, and the linear speed is 30 m/s. Therefore, most pyrolysis gas is condensable gas, high-quality tar mainly comprising biomass oil is obtained after rapid condensation, and the tar yield is as high as 37%. And the pyrolysis semicoke is separated and then sent into a gasification furnace 4 to be subjected to gasification reaction with a gasification agent (oxygen and water vapor) to form a large amount of synthesis gas and high-temperature circulating semicoke. The operation temperature of the gasification furnace is controlled by adjusting the oxygen content in the gasification agent, and when the oxygen content is controlled to be about 15%, the operation temperature of the gasification furnace is 700 ℃. The synthesis gas and the high-temperature circulating semi-coke generated by gasification are separated by a second gas-solid separation device 5, wherein the synthesis gas is separated and then sent to a gas purification device 6 for purification and processing. When the operating pressure of the gasification furnace is 4.0MPa, the effective component H of the synthesis gas2CO and CH4The contents are respectively 40.9%, 19.8% and 5.2%. And the high-temperature circulating semicoke is separated by the second gas-solid separation equipment 5 and then is sent into the pyrolysis furnace 1 to continuously carry out pyrolysis reaction with the mixture of the raw material biomass and the coal, and the carbon conversion rate of the whole circulating reaction system reaches 95% due to the synergistic effect of the coal and the biomass in the pyrolysis and gasification reactions.
[ example 5 ]
The mixture of biomass and lignite with the ratio of 10:2 is fed into a pyrolysis furnace 1 through feeding equipment, and is mixed with high-temperature circulating semicoke particles which come from a gasification furnace 4 and are separated by second gas-solid separation equipment 5, so that the mixture of raw material biomass and low-order low-grade coal (particle size)<1mm) is rapidly heated by the heat carried by the high-temperature circulating semicoke, and the pyrolysis gas and the pyrolysis semicoke are generated through the thermolysis volatile reaction under the nitrogen atmosphere. And separating the pyrolysis gas and the pyrolysis semicoke through a first gas-solid separation device 2, wherein the pyrolysis gas is sent into a condenser 3 for rapid condensation, the operation temperature of the pyrolysis furnace is controlled to be 500 ℃, and the linear speed is 25 m/s. Therefore, most of pyrolysis gas is condensable gas, and the high biomass oil mainly obtained by rapid condensationThe tar yield of the quality tar is as high as 46%. And the pyrolysis semicoke is separated and then sent into a gasification furnace 4 to be subjected to gasification reaction with a gasification agent (oxygen and water vapor) to form a large amount of synthesis gas and high-temperature circulating semicoke. The operation temperature of the gasification furnace is controlled by adjusting the oxygen content in the gasification agent, and when the oxygen content is controlled to be about 15%, the operation temperature of the gasification furnace is 700 ℃. The synthesis gas and the high-temperature circulating semi-coke generated by gasification are separated by a second gas-solid separation device 5, wherein the synthesis gas is separated and then sent to a gas purification device 6 for purification and processing. When the operating pressure of the gasification furnace is 4.0MPa, the effective component H of the synthesis gas2CO and CH4The contents are 41.6%, 18.7% and 5.1%, respectively. And the high-temperature circulating semicoke is separated by the second gas-solid separation equipment 5 and then is sent into the pyrolysis furnace 1 to continuously carry out pyrolysis reaction with the mixture of the raw material biomass and the coal, and the carbon conversion rate of the whole circulating reaction system reaches 96% due to the synergistic effect of the coal and the biomass in the pyrolysis and gasification reactions.
[ COMPARATIVE EXAMPLE 1 ]
The mixture with the ratio of biomass to lignite of 10:2 is fed into a pyrolysis furnace 1 through feeding equipment, and is mixed with high-temperature circulating semicoke particles which come from a gasification furnace 4 and are separated by second gas-solid separation equipment 5, the mixture (with the average particle size of 3mm) of raw material biomass and low-order low-grade coal is rapidly heated by heat carried by the high-temperature circulating semicoke, and is subjected to pyrolysis volatilization reaction under the nitrogen atmosphere to generate pyrolysis gas and pyrolysis semicoke. And separating the pyrolysis gas and the pyrolysis semicoke through a first gas-solid separation device 2, wherein the pyrolysis gas is sent into a condenser 3 for rapid condensation, the operation temperature of the pyrolysis furnace is controlled to be 500 ℃, and the linear speed is 30 m/s. Therefore, most pyrolysis gas is condensable gas, high-quality tar mainly comprising biomass oil is obtained after rapid condensation, and the tar yield is as high as 29%. And the pyrolysis semicoke is separated and then sent into a gasification furnace 4 to be subjected to gasification reaction with a gasification agent (oxygen and water vapor) to form a large amount of synthesis gas and high-temperature circulating semicoke. The operation temperature of the gasification furnace is controlled by adjusting the oxygen content in the gasification agent, and when the oxygen content is controlled to be about 15%, the operation temperature of the gasification furnace is 700 ℃. Synthesis gas produced by gasification and high temperature cycle halfThe coke is separated by a second gas-solid separation device 5, wherein the synthesis gas is separated and then sent to a gas purification device 6 for purification and processing. When the operating pressure of the gasification furnace is 4.0MPa, the effective component H of the synthesis gas2CO and CH4The contents are 42.3%, 18.9% and 5.1% respectively. And the high-temperature circulating semicoke is separated by the second gas-solid separation equipment 5 and then is sent into the pyrolysis furnace 1 to continuously carry out pyrolysis reaction with the mixture of the raw material biomass and the coal, and the carbon conversion rate of the whole circulating reaction system reaches 90 percent due to the synergistic effect of the coal and the biomass in the pyrolysis and gasification reactions.
[ COMPARATIVE EXAMPLE 2 ]
Adopts a traditional Lurgi furnace pressurization fixed bed gasification device, the raw material adopts brown coal with the grain diameter of 5-30mm, the operation pressure is 3.0MPa, the gasification temperature is 850 ℃, and the linear speed is high<1.5m/s, CO + H in the exit gas component2The content was 61.0%, the methane content was 8.3%, and gasification yielded a certain amount of tar product, but the yield was only 11%, and the carbon conversion was only 90%.
[ COMPARATIVE EXAMPLE 3 ]
Adopts a pyrolysis gasification combined device proposed by the institute of engineering thermal physics of Chinese academy of sciences, and adopts particle size as raw material<1mm of straw, the gasification temperature is 900 ℃, the gasification pressure is 4.0MPa, the pyrolysis temperature is 850 ℃, and the linear speed is<10m/s, CO + H in the exit gas component2The content was 58.4%, the methane content was 7.0%, and the carbon conversion was 95%, but the tar yield was only 20%.
Figure BDA0001127391450000081

Claims (5)

1. The biomass and low-rank coal gasification-flash pyrolysis graded utilization method is characterized in that a mixture of biomass and coal as a raw material (A) enters a pyrolysis furnace (1) through feeding equipment and is mixed with high-temperature circulating semicoke particles from a gasification furnace (4), the raw material is rapidly heated by heat carried by the high-temperature circulating semicoke particles, rapid pyrolysis is realized under inert atmosphere (B), and volatile components are separated out to generate pyrolysis semicoke particles; volatile components and semi-coke particles generated by pyrolysis are separated through a first gas-solid separation device (2), wherein gas is sent into a condenser (3) for rapid condensation, high-quality tar mainly comprising biomass oil (C) is generated, and the pyrolysis semi-coke particles are sent into a gasification furnace (4) after being separated and are subjected to gasification reaction with a gasification agent (D), so that a large amount of synthesis gas and high-temperature circulation semi-coke particles are formed; and (2) separating the synthesis gas (E) and the high-temperature circulating semicoke particles generated by gasification through a second gas-solid separation device (5), wherein the high-temperature circulating semicoke particles are separated and then enter a pyrolysis furnace (1), the synthesis gas (E) is separated and then sent to a gas purification device (6) for purification and processing to be used as a chemical raw material, the mass ratio of the raw material coal to the biomass is 2:10, the raw material coal is low-rank inferior coal, the raw material biomass is garden waste of herbs or woody plants, the temperature of the pyrolysis furnace (1) is 500-.
2. The biomass and low-rank coal gasification-flash pyrolysis staged utilization method according to claim 1, wherein: the volatile matter enters a condenser (3) to be rapidly condensed into liquid after passing through a first gas-solid separation device (2); the condenser adopts a spray condenser.
3. The biomass and low-rank coal gasification-flash pyrolysis staged utilization method according to claim 1, wherein: the temperature of the gasification furnace (4) is 700 ℃ and 850 ℃, and the pressure is 4MPa-6.5 MPa.
4. The biomass and low-rank coal gasification-flash pyrolysis staged utilization method according to claim 1, wherein: the gasification agent in the gasification furnace (4) is a mixture of oxygen and water vapor, wherein the oxygen accounts for 15-20% of the total amount.
5. The biomass and low-rank coal gasification-flash pyrolysis staged utilization method according to claim 1, wherein: the particle size of the mixture of the raw material coal and the biomass is less than 1 mm.
CN201610882933.7A 2016-10-10 2016-10-10 Biomass and low-rank coal gasification-flash pyrolysis staged utilization method Active CN107916141B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610882933.7A CN107916141B (en) 2016-10-10 2016-10-10 Biomass and low-rank coal gasification-flash pyrolysis staged utilization method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610882933.7A CN107916141B (en) 2016-10-10 2016-10-10 Biomass and low-rank coal gasification-flash pyrolysis staged utilization method

Publications (2)

Publication Number Publication Date
CN107916141A CN107916141A (en) 2018-04-17
CN107916141B true CN107916141B (en) 2020-12-29

Family

ID=61891806

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610882933.7A Active CN107916141B (en) 2016-10-10 2016-10-10 Biomass and low-rank coal gasification-flash pyrolysis staged utilization method

Country Status (1)

Country Link
CN (1) CN107916141B (en)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110819390B (en) * 2018-08-13 2021-03-12 中国石油化工股份有限公司 Method and system for low-rank coal fractional conversion
CN110857391A (en) * 2018-08-24 2020-03-03 李大鹏 Self-adaptive three-cycle pressurized carbon-containing material step conversion system and method
CN114752720B (en) * 2022-05-18 2022-11-04 北京高创智信冶金科技有限公司 Hydrogen-rich thermal reduction blowing gas, preparation method thereof and application thereof in blast furnace iron making

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5423891A (en) * 1993-05-06 1995-06-13 Taylor; Robert A. Method for direct gasification of solid waste materials
CN101921627A (en) * 2010-07-30 2010-12-22 陕西华祥能源科技集团有限公司 Air-oil co-production device and method adopting fluidized bed pulverized coal gasification and solid heat carrier pyrolysis coupling
CN102504842A (en) * 2011-11-09 2012-06-20 浙江大学 Three-fluidized-bed solid heat carrier coal pyrolysis, gasification and combustion cascade utilization method
CN102703098A (en) * 2012-05-29 2012-10-03 东南大学 Device and method for preparing biological oil from biomass

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5423891A (en) * 1993-05-06 1995-06-13 Taylor; Robert A. Method for direct gasification of solid waste materials
CN101921627A (en) * 2010-07-30 2010-12-22 陕西华祥能源科技集团有限公司 Air-oil co-production device and method adopting fluidized bed pulverized coal gasification and solid heat carrier pyrolysis coupling
CN102504842A (en) * 2011-11-09 2012-06-20 浙江大学 Three-fluidized-bed solid heat carrier coal pyrolysis, gasification and combustion cascade utilization method
CN102703098A (en) * 2012-05-29 2012-10-03 东南大学 Device and method for preparing biological oil from biomass

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
生物质与煤共热解技术的研究进展;浙江大学宁波理工学院;《生物质与煤共热解技术的研究进展》;宁波节能;20110831(第4期);第19-21、24页 *

Also Published As

Publication number Publication date
CN107916141A (en) 2018-04-17

Similar Documents

Publication Publication Date Title
CA2736006C (en) Method and equipment for multistage liquefying of carbonaceous solid fuel
US9249064B2 (en) Storage of intermittent renewable energy as fuel using carbon containing feedstock
CN104789245B (en) A kind of pyrolysis gasifying device and technique
CN102977927A (en) Apparatus for preparing synthesis gas based on dual fluidized bed biomass gasification and preparation method thereof
Nguyen-Thi et al. Recent advances in hydrogen production from biomass waste with a focus on pyrolysis and gasification
CN100584928C (en) Technology of preparing synthetic gas using non agglomerating or weak agglomerating coal fluidized destructive distillation
CN102849676B (en) High-temperature water vapor pyrolysis-cracking-gasification device and method for solid fuel
CN109652103B (en) Down bed-fixed bed pyrolysis-gasification integrated method and device
MX2014012990A (en) Gas-steam efficient cogeneration process and system based on biomass gasification and methanation.
Park et al. Current developments in thermochemical conversion of biomass to fuels and chemicals
AU2009321965B2 (en) High temperature gasifying process with biomass and system thereof
CN103305285A (en) Device and method for preparing low-tar high-heat-value combustible gas by three-section-type gasification of biomass
CN1277740C (en) Process of catalyzing and gasifying fresh substance by solid thermophore for preparing hydrogen-rich gas
AU2009321964A1 (en) High temperature gasifying process with biomass and system thereof
CN107916141B (en) Biomass and low-rank coal gasification-flash pyrolysis staged utilization method
CN101538473A (en) Incoherence or weak caking coal deep processing method
CN108531220A (en) A kind of system and method for biomass microwave pyrolysis high yield gas
AU2009321963B2 (en) High temperature gasifying process with biomass and system thereof
CN111763526A (en) Process method for preparing biomass gas by pyrolyzing organic solid wastes
CN100441663C (en) Fluidization hydrogenation liquefaction method for coal
CN109652147B (en) Circulating fluidized bed pyrolysis-gasification device and method
Wang et al. Flash pyrolysis of biomass particles in fluidized bed for bio-oil production
CN108913172B (en) System and method for preparing oil by pyrolyzing seaweed
CN104046372A (en) Method for preparing bio-oil and synthesis gas from biomass
CN203065402U (en) Pulverized coal destructive distillation device

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant