CN112625755B - Circulating fluidized bed pulverized coal pyrolysis-gasification device and pulverized coal pyrolysis-gasification method - Google Patents
Circulating fluidized bed pulverized coal pyrolysis-gasification device and pulverized coal pyrolysis-gasification method Download PDFInfo
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- CN112625755B CN112625755B CN201910905164.1A CN201910905164A CN112625755B CN 112625755 B CN112625755 B CN 112625755B CN 201910905164 A CN201910905164 A CN 201910905164A CN 112625755 B CN112625755 B CN 112625755B
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- 238000002309 gasification Methods 0.000 title claims abstract description 182
- 239000003245 coal Substances 0.000 title claims abstract description 146
- 238000000034 method Methods 0.000 title claims abstract description 29
- 238000000197 pyrolysis Methods 0.000 claims abstract description 204
- 238000002485 combustion reaction Methods 0.000 claims abstract description 79
- 238000006243 chemical reaction Methods 0.000 claims abstract description 59
- 239000000843 powder Substances 0.000 claims abstract description 52
- 238000004062 sedimentation Methods 0.000 claims abstract description 45
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 37
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 35
- 239000003795 chemical substances by application Substances 0.000 claims description 32
- 230000015572 biosynthetic process Effects 0.000 claims description 29
- 238000003786 synthesis reaction Methods 0.000 claims description 29
- 239000007787 solid Substances 0.000 claims description 21
- 239000002994 raw material Substances 0.000 claims description 19
- 238000005243 fluidization Methods 0.000 claims description 18
- 238000000926 separation method Methods 0.000 claims description 8
- 239000003054 catalyst Substances 0.000 claims description 7
- 150000001336 alkenes Chemical class 0.000 claims description 6
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 6
- 239000007800 oxidant agent Substances 0.000 claims description 5
- 239000002817 coal dust Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 230000001590 oxidative effect Effects 0.000 claims description 4
- 239000002028 Biomass Substances 0.000 claims description 2
- 229910052783 alkali metal Inorganic materials 0.000 claims description 2
- 150000001340 alkali metals Chemical class 0.000 claims description 2
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims description 2
- 150000001342 alkaline earth metals Chemical class 0.000 claims description 2
- 229910052723 transition metal Inorganic materials 0.000 claims description 2
- 150000003624 transition metals Chemical class 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 92
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 35
- 239000002956 ash Substances 0.000 description 29
- 239000011269 tar Substances 0.000 description 19
- 238000005516 engineering process Methods 0.000 description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- 239000011261 inert gas Substances 0.000 description 11
- 239000003077 lignite Substances 0.000 description 11
- 239000000463 material Substances 0.000 description 8
- 238000011161 development Methods 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 239000010881 fly ash Substances 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 4
- 229910052700 potassium Inorganic materials 0.000 description 4
- 239000002893 slag Substances 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000011280 coal tar Substances 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 230000004927 fusion Effects 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 239000010426 asphalt Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007580 dry-mixing Methods 0.000 description 1
- 238000001983 electron spin resonance imaging Methods 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 238000010812 external standard method Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000011286 gas tar Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
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
-
- 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
-
- 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
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
-
- 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
- C10J3/723—Controlling or regulating the gasification process
-
- 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
- C10J3/725—Redox processes
-
- 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
- C10J2300/0969—Carbon dioxide
-
- 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
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0983—Additives
- C10J2300/0986—Catalysts
-
- 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
- C10J2300/12—Heating the gasifier
- C10J2300/1223—Heating the gasifier by burners
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention discloses a circulating fluidized bed pulverized coal pyrolysis-gasification device, which comprises: a feeder; the fluidized bed pyrolysis furnace is connected with the feeder through a feeding inclined pipe; the fluidized bed gasification furnace is connected with the fluidized bed pyrolysis furnace through a pyrolysis inclined tube; the lower inlet of the fast bed gasifier is connected with the upper outlet of the fluidized bed gasifier; the upper inlet of the fluidized bed combustion chamber is connected with the lower outlet of the fluidized bed gasifier; the fine powder sedimentation/stripping device is arranged outside the rapid bed gasifier and is connected with the fluidized bed pyrolysis furnace through a gasification inclined tube. The invention also discloses a method for pyrolyzing and gasifying pulverized coal by adopting the device. The invention has the characteristics of high carbon conversion rate, high gasification intensity, high pulverized coal utilization rate, wide adaptability of gasified coal, reasonable energy utilization, stable and efficient device operation.
Description
Technical Field
The invention belongs to the field of coal gasification, and relates to a circulating fluidized bed pulverized coal pyrolysis-gasification device and a method for carrying out pulverized coal pyrolysis-gasification by adopting the same.
Background
Coal, oil, and natural gas are three major primary energy sources in the world, wherein coal accounts for about 79% of the world's energy reserves, and coal is one of the main fuel resources for power, heat, char processing, and by-product asphalt. China is a country with coal as a main energy structure, and the coal is not changed in a long time in the future, so that the statistics shows that the coal reaches 63.7% in a primary energy consumption structure of China in 2015. Along with the increasing shortage of petroleum resources, the effective utilization of coal resources has become a strategy for sustainable development of energy sources 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 moisture and low coalification degree, and has low direct combustion efficiency, so that resources are wasted, the environment is polluted, and acid rain, PM2.5, SOx, NOx and other chamber gases are discharged. The coal gasification technology is a key technology for realizing clean, efficient and comprehensive utilization of coal, is an important way for coal conversion, and is also one of key technologies for synthesizing chemicals, combined cycle power generation and coal substitute natural gas. The method is a key for realizing the sustainable development of energy in China and an effective way for solving the energy and environment problems facing the world.
The largest coal gasification technology application market in the world is in China, and at present, various coal gasification technologies successfully realize industrialized application. The method belongs to entrained flow gasification technology widely at present, and improves the carbon conversion rate at the cost of high temperature and high pressure, so that the problems of high energy consumption, difficult gas purification, severe requirements on equipment and the like are brought. Meanwhile, the excessive operation temperature of the entrained flow slag gasification technology increases the investment, maintenance and operation cost of the entrained flow. Research reports of the American electric institute (EPRI) indicate that the existing industrial entrained flow gasifier is not suitable for gasifying high ash and high ash fusion point coal, and industrial fluidized bed gasification technology is needed in the world. The fluidized bed technology has the property of adapting to high ash fusion point and high ash coal types no matter burning or gasifying, and the fact that the circulating fluidized bed boiler has successfully burned coal gangue is obvious.
Patent CN102212399B discloses a pyrolysis gasification combined method and a device, which are used for providing that fuel is pyrolyzed in a low-speed bed pyrolysis furnace, semicoke is sent into a circulating fluidized bed gasification furnace through a material returning device to be gasified, and gas generated by the gasification furnace carries solid particles into a cyclone separator; the solid particles trapped by the cyclone separator are sent to the upper part of the dense-phase zone of the pyrolysis furnace to provide heat for the pyrolysis of the fuel. The device adopts a circulating fluidized bed as a gasification furnace, or the gasification furnace has large volume and high energy consumption; or high carbon conversion rate and low gasification strength cannot be ensured.
Patent CN102504842A discloses a three-fluidized bed solid heat carrier coal pyrolysis gasification combustion cascade utilization method. The method takes high-temperature circulating ash as a solid heat carrier, coal is mixed with the high-temperature circulating ash in a fluidized bed pyrolysis furnace, volatile matters are separated out through pyrolysis, tar and pyrolysis coal gas are obtained through cooling separation of the volatile matters, pyrolysis semicoke generated by coal pyrolysis is sent to a fluidized bed gasification furnace, steam and O2 are taken as gasification agents to carry out gasification reaction, synthesis gas is prepared, semicoke which is not completely gasified in the gasification furnace is sent to a circulating fluidized bed combustion furnace, air is blown for conventional combustion, or O2/CO2 is blown for oxygen-enriched combustion, the solid heat carrier circulating ash is heated, and high-temperature flue gas generated by combustion is used for producing gasification agent steam required by the gasification furnace. The invention has the advantages that the co-production of tar, pyrolysis gas and synthesis gas is realized through the cascade utilization of pyrolysis gasification combustion of coal, but the cascade utilization sequence of heat of combustion, pyrolysis and gasification is unreasonable, and further improvement and optimization space exists for reasonable utilization of energy.
In summary, the existing pyrolysis-gasification coupling classification utilization technology solves the defects of the traditional gasification to prepare the synthetic gas and the pyrolysis to prepare the oil to a certain extent, but has low carbon conversion rate and gasification strength due to the adoption of the fluidized bed technology and the limitation of process conditions. Therefore, how to further improve the carbon conversion rate and the gasification intensity, reasonably apply the heat cascade utilization of combustion, gasification and pyrolysis, and realize the quality-graded and efficient and clean utilization of the pyrolysis-gasification integrated pulverized coal in the true sense is the key of the development of the coal gasification technology.
Disclosure of Invention
The invention aims to provide a novel circulating fluidized bed pulverized coal pyrolysis-gasification device and a method for carrying out pulverized coal pyrolysis-gasification by adopting the same, aiming at the problems of low carbon conversion rate and gasification intensity, low pulverized coal utilization rate and difficult utilization of low-rank coal in the prior art. The invention has the characteristics of high carbon conversion rate, high gasification intensity, high pulverized coal utilization rate, wide adaptability of gasified coal, reasonable energy utilization, stable and efficient device operation.
According to an aspect of the present invention, there is provided a circulating fluidized bed pulverized coal pyrolysis-gasification apparatus comprising:
A feeder;
The fluidized bed pyrolysis furnace is connected with the feeder through a feeding inclined pipe;
The fluidized bed gasification furnace is connected with the fluidized bed pyrolysis furnace through a pyrolysis inclined tube;
the lower inlet of the fast bed gasifier is connected with the upper outlet of the fluidized bed gasifier;
the upper inlet of the fluidized bed combustion chamber is connected with the lower outlet of the fluidized bed gasifier;
The fine powder sedimentation/stripping device is arranged outside the rapid bed gasifier and is connected with the fluidized bed pyrolysis furnace through a gasification inclined tube.
According to some embodiments of the invention, the fluidized bed pyrolysis furnace comprises a dense phase zone and an olefin phase zone from bottom to top.
According to the preferred embodiment of the invention, the lower part of the side wall of the dense-phase zone is respectively provided with a pulverized coal inlet and a gasified semicoke inlet, and the pulverized coal inlet is connected with a feeder through a feeding inclined tube; the gasification semicoke inlet is connected with the fine powder sedimentation/stripping device through a gasification inclined tube; the middle part of the side wall of the dense-phase zone is provided with a pyrolysis semicoke outlet which is connected with the fluidized bed gasifier through a pyrolysis inclined tube.
According to a preferred embodiment of the invention, a cyclone separator of the fluidized bed pyrolysis furnace is arranged in the olefin phase zone for separating the gas generated in the dense phase zone.
According to a preferred embodiment of the present invention, a pyrolysis fluidization gas inlet is provided in the bottom of the fluidized bed pyrolysis furnace for receiving pyrolysis fluidization gas.
According to a preferred embodiment of the invention, a pyrolysis gas outlet is provided at the top of the fluidized bed pyrolysis furnace, which is connected to the gas outlet of the cyclone separator of the fluidized bed pyrolysis furnace for discharging separated pyrolysis gas.
According to a preferred embodiment of the present invention, the fluidized-bed gasification furnace is arranged in parallel with the fluidized-bed pyrolysis furnace.
According to some embodiments of the invention, a pyrolysis semicoke inlet is arranged at the lower part of the side wall of the fluidized bed gasification furnace and is connected with the fluidized bed pyrolysis furnace through a pyrolysis chute.
According to a preferred embodiment of the present invention, a gasifying agent inlet is provided at a lower portion of a side wall of the fluidized-bed gasification furnace, the gasifying agent inlet being for receiving gasifying agent.
According to a preferred embodiment of the present invention, the lower outlet of the fluidized-bed gasification furnace is connected to the upper inlet of the fluidized-bed combustion chamber.
According to some embodiments of the invention, a gas distribution plate is disposed below the interior of the fluidized bed combustion chamber; the bottom of the fluidized bed combustion chamber is provided with an ash discharge port which is connected with an ash tank.
According to a preferred embodiment of the present invention, the upper outlet of the fluidized bed gasification furnace is reduced in diameter and then connected to the lower inlet of the rapid bed gasification furnace.
According to a preferred embodiment of the invention, the apparatus further comprises a rapid bed cyclone connected to the upper outlet of the rapid bed gasifier.
According to a preferred embodiment of the present invention, the rapid bed gasifier is axially extended from the bottom center of the fine powder settling/stripper, and both are communicated through the rapid bed gasifier cyclone.
According to some embodiments of the invention, the fines settler/stripper comprises a stripping section, a fines settling section, and a fines settling/stripper cyclone; the lower part of the side wall of the fine powder sedimentation/stripping device is provided with a stripping gas inlet for receiving stripping gas; the lower part of the side wall of the fine powder sedimentation/stripping device is provided with a semicoke outlet which is connected with the fluidized bed pyrolysis furnace through a gasification inclined tube; the top of the fine powder sedimentation/stripping device is provided with a synthesis gas outlet which is connected with a gas outlet of the cyclone separator of the fine powder sedimentation/stripping device and is used for discharging the separated synthesis gas.
According to a preferred embodiment of the invention, a pyrolysis semicoke return valve is arranged on the pyrolysis chute, which is a non-mechanical return valve, preferably a U valve, a J valve, an L valve or an M valve. And introducing loosening gas into the pyrolysis semicoke valve, and controlling the circulation amount of the pyrolysis semicoke by adjusting the air quantity of the loosening gas, or the bed density of the fluidized bed gasification furnace, or the material level of the fluidized bed pyrolysis furnace.
According to a preferred embodiment of the invention, a gasification carbocoal return valve is arranged on the gasification inclined tube, which is a non-mechanical return valve, preferably a U valve, a J valve, an L valve or an M valve. And introducing loosening gas into the gasification semicoke valve, and controlling the circulation amount of gasification semicoke, or the material level of the fine powder sedimentation/stripper, or the temperature of the fluidized bed pyrolysis furnace by adjusting the air quantity of the loosening gas.
According to another aspect of the present invention, there is provided a pulverized coal pyrolysis-gasification method using the above apparatus, comprising the steps of:
(a) The pulverized coal raw material is sent into a fluidized bed pyrolysis furnace by a feeder, and is mixed with high-temperature gasified semicoke in the fluidized bed pyrolysis furnace to be heated, and the pulverized coal undergoes pyrolysis reaction to generate pyrolysis semicoke and pyrolysis gas;
(b) The pyrolysis semicoke enters a fluidized bed gasifier through a pyrolysis inclined tube, contacts with gasifying agents, and performs gasification reaction in the fluidized bed gasifier and a fast bed gasifier to generate synthesis gas and carbon-containing gasification semicoke;
(c) The synthesis gas enters a fine powder sedimentation/stripping device to separate high-temperature gasification semicoke, and the high-temperature gasification semicoke enters a fluidized bed pyrolysis furnace through a gasification inclined tube;
(d) The carbon-containing gasified semicoke downwards enters a fluidized bed combustion chamber from a fluidized bed gasifier to undergo a combustion reaction to produce ash and high-temperature gas; the high-temperature gas upwards enters the fluidized bed gasifier to be used as a gasifying agent.
According to some embodiments of the invention, the pulverized coal feedstock comprises pulverized coal and at least one of a catalyst and biomass; preferably, the catalyst comprises at least one of alkali metal, alkaline earth metal and transition metal.
According to a preferred embodiment of the invention, the catalyst is supported on the pulverized coal in a manner of an impregnation method, a dry mixing method or an ion exchange method, and the catalyst loading amount is 0.1-30% of the mass of the pulverized coal.
According to some embodiments of the invention, the pulverized coal raw material is fed into a dense-phase zone of the fluidized bed pyrolysis furnace by a feeder, and is mixed with high-temperature gasified semicoke in the dense-phase zone to be heated, and the pulverized coal undergoes pyrolysis reaction to generate pyrolysis semicoke and pyrolysis gas; the pyrolysis semicoke enters a fluidized bed gasifier through a pyrolysis inclined tube; the pyrolysis gas entrains fine coal dust, the pyrolysis gas upwards enters an olefin phase region and is subjected to gas-solid separation through a cyclone separator of the fluidized bed pyrolysis furnace, solids (fine coal dust) return to a dense phase region, and gas leaves the fluidized bed pyrolysis furnace.
According to a preferred embodiment of the present invention, the pyrolysis pressure of the fluidized bed pyrolysis furnace is 0-6.5MPa, and the pyrolysis temperature is 400-800 ℃; and/or the pulverized coal average density of the dense-phase zone of the fluidized bed pyrolysis furnace is 200-550kg/m 3, and the superficial linear velocity is 0.1-1.0m/s.
According to a preferred embodiment of the present invention, the pyrolysis fluidization gas is introduced into the fluidized bed pyrolysis furnace through a pyrolysis fluidization gas inlet at the bottom of the furnace; the pyrolysis fluidization gas includes at least one of steam, CO 2, CO, hydrogen, and an inert gas.
According to some embodiments of the invention, the pyrolysis semicoke enters the lower part of the fluidized bed gasifier through the pyrolysis inclined tube, contacts with gasifying agent, and performs gasification reaction in the fluidized bed gasifier and the fast bed gasifier to generate synthesis gas and carbon-containing gasification semicoke.
According to the preferred embodiment of the invention, the loosening gas is introduced into the pyrolysis semicoke valve, and the circulation amount of the pyrolysis semicoke, the bed density of the fluidized bed gasification furnace or the material level of the fluidized bed pyrolysis furnace is controlled by adjusting the air quantity of the loosening gas.
According to a preferred embodiment of the invention, the loosening gas comprises at least one of water vapor, CO 2, CO, air, oxygen, and an inert gas.
According to a preferred embodiment of the present invention, the gasifying agent is a high-temperature gas from a fluidized bed combustion chamber or a gasifying agent from outside introduced through a gasifying agent inlet; the gasifying agent comprises water vapor and/or CO 2.
According to the preferred embodiment of the invention, the gasification pressure of the fluidized bed gasifier is 0-6.5MPa, the gasification temperature is 700-1200 ℃, the average density of pulverized coal is 200-450kg/m 3, and the average superficial linear velocity is 0.2-1.2m/s.
According to the preferred embodiment of the invention, the gasification pressure of the rapid bed gasifier is 0-6.5MPa, the gasification temperature is 700-1200 ℃, the average density of pulverized coal is 50-150kg/m 3, and the average superficial linear velocity is 1.0-3.0m/s.
According to some embodiments of the invention, the synthesis gas exiting the rapid bed gasifier is entrained with unvaporized semicoke fines, which first enter the rapid bed cyclone for primary gas-solid separation, the solids fall into the stripping section of the fines settler/stripper, and the gas enters the settling section of the fines settler/stripper.
According to a preferred embodiment of the invention, the gas coming out of the fast bed cyclone enters the settling section of the fines settling/stripper and the fines settling/stripper cyclone, further separating out solids, which fall into the stripping section of the fines settling/stripper, and the gas leaves the fines settling/stripper.
According to the preferred embodiment of the invention, the stripping gas is introduced into the stripping section of the fine powder sedimentation/stripping device through the stripping gas inlet, the solid in the stripping section is stripped, fly ash carried in the solid is removed, and the high-temperature gasified semicoke is obtained, and enters the fluidized bed pyrolysis furnace through the gasification inclined tube.
According to the preferred embodiment of the invention, the gasification semicoke valve is filled with the loose air, and the circulation amount of gasification semicoke, or the material level of the fine powder sedimentation/stripping device, or the temperature of the fluidized bed pyrolysis furnace is controlled by adjusting the air quantity of the loose air.
According to a preferred embodiment of the invention, the loosening gas comprises at least one of water vapor, CO 2, CO, air, oxygen, and an inert gas.
According to a preferred embodiment of the present invention, the stripping gas comprises at least one of steam, CO 2, CO and inert gas.
According to a preferred embodiment of the present invention, the pressure of the fine powder settling/stripper is 0-6.5MPa, the temperature is 700-1200 ℃, the average density of pulverized coal is 350-550kg/m 3, and the average superficial linear velocity is 0.1-0.5m/s.
According to some embodiments of the invention, the carbonaceous gasification semicoke enters the fluidized bed combustion chamber downwards from the fluidized bed gasification furnace, contacts with an oxidant, and undergoes a combustion reaction to produce ash and high-temperature gas; the high-temperature gas upwards enters a fluidized bed gasifier to be used as a gasifying agent and provides heat for gasification reaction; ash is discharged to an ash tank through an ash discharge port, and is further discharged.
According to a preferred embodiment of the invention, the oxidizing agent comprises air and/or oxygen.
According to a preferred embodiment of the invention, the combustion pressure of the fluidized bed combustion chamber is 0-6.5MPa, the combustion temperature is 800-1500 ℃, the average density of pulverized coal is 300-450kg/m 3, and the average superficial linear velocity is 0.2-0.6m/s.
According to the technical scheme, the pulverized coal raw material is pyrolyzed in the pyrolysis furnace to obtain pyrolysis gas (comprising coal tar) and gasification raw material-pyrolysis semicoke, and the gasification raw material is obtained through pyrolysis, so that the application range of coal types is enlarged. And (3) carrying out gasification reaction of pyrolysis semicoke particles in a gasification furnace to generate synthesis gas. Most of unvaporized high-temperature gasified semicoke particles are used as a heat carrier and circularly enter a pyrolysis furnace to be used as a heat source for pyrolysis, so that the energy consumption is reduced, and the cost of the heat carrier added in the traditional process is saved. And a small part of gasified semicoke particles which are not gasified enter a combustion chamber to perform combustion reaction with oxygen, so that semicoke is converted into ash, and the carbon conversion rate and the utilization rate of carbon residue are improved. The heat generated by the combustion reaction is used to provide heat consumption and heat loss in the gasification reaction and to provide the necessary gasifying agent for the gasification reaction. The invention is specially provided with a fine powder sedimentation/stripping device, and aims to remove fly ash carried in high-temperature gasified semicoke entering a pyrolysis furnace, thereby reducing the fly ash carried in pyrolysis gas, avoiding the blockage of the fly ash to related equipment and reducing the difficulty of liquid-solid separation.
According to the invention, pyrolysis and gasification, gasification and combustion are coupled together, so that synthesis gas and coal tar can be produced, and the quality-grading and grading utilization of low-rank coal can be realized. Can be used for direct gasification of pulverized coal or catalytic gasification of pulverized coal, and realizes high-efficiency, clean and reasonable comprehensive utilization of coal.
Compared with the prior art, the gasification outlet carbon conversion rate in the reactor is increased to 98%, the methane content in the synthesis gas is increased to 15%, and the yield of tar is increased by 10%.
Drawings
FIG. 1 is a schematic view of a circulating fluidized bed pyrolysis-gasification apparatus of the present invention:
In fig. 1,1 is a feeder; 2 is a fluidized bed pyrolysis furnace; 3 is a dense phase zone of the fluidized bed pyrolysis furnace; 4 is a dilute phase zone of the fluidized bed pyrolysis furnace; 5 is a cyclone separator of the fluidized bed pyrolysis furnace; 6 is a pyrolysis semicoke material returning valve; 7 is a fluidized bed combustion chamber; 8, a fluidized bed gasifier; 9 is a fine powder sedimentation/stripper; 10 is a stripping section; 11 is a fine powder sedimentation section; 12 is a fines settler/stripper cyclone; 13 is a rapid bed gasifier; 14 is a rapid bed gasifier cyclone; 15 is a gas distribution plate; 16 is ash discharge port; 17 is an ash pot; 18 is a gasification carbocoal return valve; 19 is a feeding inclined tube; 20 is a pyrolysis chute; 21 is a gasification inclined tube. A is pulverized coal raw material; b is pyrolysis fluidization gas; c is an oxidant; d is a gasifying agent; e is stripping gas; F. g, H, I is a loosening gas; k is pyrolysis gas; l is ash.
Detailed Description
The present invention is further illustrated by, but not limited to, the following examples.
In the following examples, the evaluation and test methods involved are as follows:
The carbon conversion rate is calculated based on carbon residue in ash, and the specific formula is as follows:
cc= (1-C ash/Craw) ×100%, where CC is carbon conversion, C ash is carbon content in ash, C raw is carbon content in pulverized coal feedstock;
Measuring the gas component by an on-line gas chromatograph external standard method to measure the methane content in the synthesis gas;
the tar yield is calculated through the mass balance of gas, liquid and solid products, and the specific formula is as follows:
Y tar＝(Mraw-Mgas-Mash)/Mraw x 100%, where Y tar is tar yield, M raw is pulverized coal feed mass flow, M gas is product gas mass flow, and M ash is ash mass flow.
[ Example 1]
The reaction flow is as follows: the pulverized coal raw material is sent into a dense-phase zone (3) by a feeder (1), and is mixed with high-temperature gasified semicoke to be heated, pyrolysis reaction occurs, the pyrolysis gas carrying fine pulverized coal is returned to the dense-phase zone (3) after being subjected to gas-solid separation, and the pyrolysis semicoke enters the lower part of a fluidized bed gasifier (8) after the circulation quantity is controlled by a pyrolysis semicoke return valve (6). The pyrolysis semicoke is contacted with a gasifying agent D, gasification reaction is carried out in a fluidized bed gasification furnace (8) and a rapid bed gasification furnace (13) to generate synthesis gas, the gasification semicoke which is not gasified is separated by a cyclone separator (14) of the rapid bed gasification furnace and then enters a settling section (11) at the upper part of a fine powder settling/stripping device (9), and the gasification semicoke which is not gasified falls into a stripping section (10) at the lower part of the fine powder settling/stripping device (9). The carbon-containing gasified semicoke falls into a fluidized bed combustion chamber (7) from the bottom of a fluidized bed gasifier (8), contacts and mixes with an oxidant C, and generates a combustion reaction to convert the carbon-containing semicoke into ash. The high-temperature gas generated by combustion enters the fluidized bed gasifier (8) upwards to be used as gasifying agent and provides heat for the gasifying medium. The synthesis gas coming out of the top of the cyclone separator (14) of the rapid bed gasification furnace is separated from the gasification device and enters a subsequent separation and purification device after the fine powder is recovered by the fine powder sedimentation section (11) and the fine powder sedimentation/stripping cyclone separator (12), and the fine powder recovered by the fine powder sedimentation/stripping cyclone separator (12) falls into the stripping section (10) through a material leg. The stripping section (10) adopts stripping gas E to strip unreacted carbon-containing semicoke and ash slag, fly ash carried in the unreacted carbon-containing semicoke and ash slag is reduced, the stripped carbon-containing semicoke and ash slag compound enters a gasification inclined tube (21), and enters the lower part of a dense-phase zone (3) of the fluidized bed pyrolysis furnace (2) after the circulation quantity is controlled by a gasification semicoke return valve (18) to be mixed with fresh pulverized coal, and the newly-fed pulverized coal is heated for pyrolysis.
In the reaction flow, pulverized coal raw materials are lignite, the pyrolysis pressure of a fluidized bed pyrolysis furnace (2) is 0MPa, the pyrolysis temperature is 400 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 200kg/m 3, and the line speed of an empty tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 1.0m/s; the gasification pressure of the fluidized bed gasifier (8) is 0MPa, the gasification temperature is 700 ℃, the average density of pulverized coal is 200kg/m 3, and the average empty tower linear speed in the fluidized bed gasifier (8) is 1.2m/s; the gasification pressure of the rapid bed gasifier (13) is 0MPa, the gasification temperature is 700 ℃, the average density of pulverized coal is 50kg/m 3, the average empty tower linear speed in the rapid bed gasifier (13) is 3.0m/s, the combustion pressure of the fluidized bed combustion chamber (7) is 0MPa, the combustion temperature is 800 ℃, the average density of pulverized coal is 300kg/m 3, and the average empty tower linear speed in the fluidized bed combustion chamber (7) is 0.6m/s; the pressure of the fine powder sedimentation/stripping device (9) is 0MPa, the temperature is 700 ℃, the average density of pulverized coal is 350kg/m 3, and the average empty tower linear speed in the fine powder sedimentation/stripping device (9) is 0.5m/s. The pyrolysis fluidization gas B adopts inert gas; the gasifying agent D adopts water vapor. Through the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 95%, the methane content in the synthesis gas is improved to 9.2%, and the tar yield is 8.1%. The detailed results are shown in Table 1.
[ Example 2]
The reaction scheme was the same as in example 1. In the reaction flow, pulverized coal raw materials adopt lignite, the pyrolysis pressure of a fluidized bed pyrolysis furnace (2) is 6.5MPa, the pyrolysis temperature is 400 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 200kg/m 3, and the linear speed of an empty tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 1.0m/s; the gasification pressure of the fluidized bed gasifier (8) is 0MPa, the gasification temperature is 700 ℃, the average density of pulverized coal is 200kg/m 3, and the average empty tower linear speed in the fluidized bed gasifier (8) is 1.2m/s; the gasification pressure of the rapid bed gasifier (13) is 0MPa, the gasification temperature is 700 ℃, and the average density of pulverized coal is 50kg/m 3; the average empty tower linear velocity in the fast bed gasifier (13) is 3.0m/s, the combustion pressure in the fluidized bed combustion chamber (7) is 0MPa, the combustion temperature is 800 ℃, the average density of pulverized coal is 300kg/m 3, and the average empty tower linear velocity in the fluidized bed combustion chamber (7) is 0.6m/s; the pressure of the fine powder sedimentation/stripping device (9) is 0MPa, the temperature is 700 ℃, the average density of pulverized coal is 350kg/m 3, and the average empty tower linear speed in the fine powder sedimentation/stripping device (9) is 0.5m/s. The pyrolysis fluidization gas B adopts inert gas; the gasifying agent D adopts water vapor. Through the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 95%, the methane content in the synthesis gas is improved to 9.6%, and the tar yield is 7.5%. The detailed results are shown in Table 1.
[ Example 3]
The reaction scheme was the same as in example 1. In the reaction flow, pulverized coal raw materials adopt lignite, the pyrolysis pressure of a fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 800 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 200kg/m 3, and the line speed of an empty tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 1.0m/s; the gasification pressure of the fluidized bed gasifier (8) is 0, the gasification temperature is 1200 ℃, the average density of pulverized coal is 200kg/m 3, and the average empty tower linear speed in the fluidized bed gasifier (8) is 1.2m/s; the gasification pressure of the rapid bed gasifier (13) is 0, the gasification temperature is 1200 ℃, and the average density of pulverized coal is 50kg/m 3; the average linear velocity of the empty tower in the fast bed gasifier (13) is 3.0m/s, the combustion pressure of the fluidized bed combustion chamber (7) is 0, the combustion temperature is 1500 ℃, the average density of pulverized coal is 300kg/m 3, and the average linear velocity of the empty tower in the fluidized bed combustion chamber (7) is 0.6m/s; the pressure of the fine powder sedimentation/stripping device (9) is 0, the temperature is 1200 ℃, the average density of pulverized coal is 350kg/m 3, and the average empty tower linear speed in the fine powder sedimentation/stripping device (9) is 0.5m/s. The pyrolysis fluidization gas B adopts inert gas; the gasifying agent D adopts water vapor. By the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 98%, the methane content in the synthesis gas is improved to 11.6%, and the tar yield is 5.7%. The detailed results are shown in Table 1.
[ Example 4]
The reaction scheme was the same as in example 1. In the reaction flow, pulverized coal raw materials adopt lignite, the pyrolysis pressure of a fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 800 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 200kg/m 3, and the line speed of an empty tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 1.0m/s; the gasification pressure of the fluidized bed gasifier (8) is 6.5MPa, the gasification temperature is 1200 ℃, the average density of pulverized coal is 200kg/m 3, and the average empty tower linear velocity in the fluidized bed gasifier (8) is 1.2m/s; the gasification pressure of the rapid bed gasifier (13) is 6.5MPa, the gasification temperature is 1200 ℃, and the average density of pulverized coal is 50kg/m 3; the average air tower linear speed in the fast bed gasifier (13) is 3.0m/s, the combustion pressure of the fluidized bed combustion chamber (7) is 6.5MPa, the combustion temperature is 1500 ℃, the average density of pulverized coal is 300kg/m 3, and the average air tower linear speed in the fluidized bed combustion chamber (7) is 0.6m/s; the pressure of the fine powder sedimentation/stripping device (9) is 6.5MPa, the temperature is 1200 ℃, the average density of pulverized coal is 350kg/m 3, and the average empty tower linear velocity in the fine powder sedimentation/stripping device (9) is 0.5m/s. The pyrolysis fluidization gas B adopts inert gas; the gasifying agent D adopts water vapor. By the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 98%, the methane content in the synthesis gas is improved to 12.9%, and the tar yield is 5.1%. The detailed results are shown in Table 1.
[ Example 5]
The reaction scheme was the same as in example 1. In the reaction flow, pulverized coal raw materials adopt lignite, the pyrolysis pressure of a fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 800 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 550kg/m 3, and the line speed of an empty tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 0.1m/s; the gasification pressure of the fluidized bed gasifier (8) is 6.5MPa, the gasification temperature is 1200 ℃, the average density of pulverized coal is 450kg/m 3, and the average empty tower linear velocity in the fluidized bed gasifier (8) is 0.2m/s; the gasification pressure of the rapid bed gasifier (13) is 6.5MPa, the gasification temperature is 1200 ℃, and the average density of pulverized coal is 150kg/m 3; the average air tower linear speed in the fast bed gasifier (13) is 1.0m/s, the combustion pressure of the fluidized bed combustion chamber (7) is 6.5MPa, the combustion temperature is 1500 ℃, the average density of pulverized coal is 500kg/m 3, and the average air tower linear speed in the fluidized bed combustion chamber (7) is 0.2m/s; the pressure of the fine powder sedimentation/stripping device (9) is 6.5MPa, the temperature is 1200 ℃, the average density of pulverized coal is 550kg/m 3, and the average empty tower linear speed in the fine powder sedimentation/stripping device (9) is 0.1m/s. The pyrolysis fluidization gas B adopts inert gas; the gasifying agent D adopts water vapor. By the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 98%, the methane content in the synthesis gas is improved to 13.4%, and the tar yield is 5.0%. The detailed results are shown in Table 1.
[ Example 6]
The reaction scheme was the same as in example 1. In the reaction flow, pulverized coal raw materials adopt lignite, the pyrolysis pressure of a fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 600 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 550kg/m 3, and the line speed of an empty tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 0.1m/s; the gasification pressure of the fluidized bed gasifier (8) is 6.5MPa, the gasification temperature is 900 ℃, the average density of pulverized coal is 450kg/m 3, and the average empty tower linear velocity in the fluidized bed gasifier (8) is 0.2m/s; the gasification pressure of the rapid bed gasifier (13) is 6.5MPa, the gasification temperature is 900 ℃, and the average density of pulverized coal is 150kg/m 3; the average air tower linear speed in the fast bed gasifier (13) is 1.0m/s, the combustion pressure of the fluidized bed combustion chamber (7) is 6.5MPa, the combustion temperature is 1100 ℃, the average density of pulverized coal is 500kg/m 3, and the average air tower linear speed in the fluidized bed combustion chamber (7) is 0.2m/s; the pressure of the fine powder sedimentation/stripping device (9) is 6.5MPa, the temperature is 900 ℃, the average density of pulverized coal is 550kg/m 3, and the average empty tower linear speed in the fine powder sedimentation/stripping device (9) is 0.1m/s. The pyrolysis fluidization gas B adopts inert gas; the gasifying agent D adopts water vapor. By the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 97%, the methane content in the synthesis gas is improved to 13.9%, and the tar yield is 9.8%. The detailed results are shown in Table 1.
[ Example 7]
The reaction scheme was the same as in example 1. In the reaction flow, pulverized coal raw materials adopt lignite+5% K 2CO3, the pyrolysis pressure of a fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 600 ℃, the average density of pulverized coal in a dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 550kg/m 3, and the linear velocity of an empty tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 0.1m/s; the gasification pressure of the fluidized bed gasifier (8) is 6.5MPa, the gasification temperature is 900 ℃, the average density of pulverized coal is 450kg/m 3, and the average empty tower linear velocity in the fluidized bed gasifier (8) is 0.2m/s; the gasification pressure of the rapid bed gasifier (13) is 6.5MPa, the gasification temperature is 900 ℃, and the average density of pulverized coal is 150kg/m 3; the average air tower linear speed in the fast bed gasifier (13) is 1.0m/s, the combustion pressure of the fluidized bed combustion chamber (7) is 6.5MPa, the combustion temperature is 1100 ℃, the average density of pulverized coal is 500kg/m 3, and the average air tower linear speed in the fluidized bed combustion chamber (7) is 0.2m/s; the pressure of the fine powder sedimentation/stripping device (9) is 6.5MPa, the temperature is 900 ℃, the average density of pulverized coal is 550kg/m 3, and the average empty tower linear speed in the fine powder sedimentation/stripping device (9) is 0.1m/s. The pyrolysis fluidization gas B adopts inert gas; the gasifying agent D adopts water vapor. By the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 99%, the methane content in the synthesis gas is improved to 14.6%, and the tar yield is 8.8%. The detailed results are shown in Table 1.
[ Example 8]
The reaction scheme was the same as in example 1. In the reaction flow, lignite+5% K 2CO3 is adopted as raw materials, the pyrolysis pressure of a fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 600 ℃, the average density of pulverized coal in a dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 550kg/m 3, and the linear velocity of an empty tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 0.1m/s; the gasification pressure of the fluidized bed gasifier (8) is 6.5MPa, the gasification temperature is 900 ℃, the average density of pulverized coal is 450kg/m 3, and the average empty tower linear velocity in the fluidized bed gasifier (8) is 0.2m/s; the gasification pressure of the rapid bed gasifier (13) is 6.5MPa, the gasification temperature is 900 ℃, and the average density of pulverized coal is 150kg/m 3; the average air tower linear speed in the fast bed gasifier (13) is 1.0m/s, the combustion pressure of the fluidized bed combustion chamber (7) is 6.5MPa, the combustion temperature is 1100 ℃, the average density of pulverized coal is 500kg/m 3, and the average air tower linear speed in the fluidized bed combustion chamber (7) is 0.2m/s; the pressure of the fine powder sedimentation/stripping device (9) is 6.5MPa, the temperature is 900 ℃, the average density of pulverized coal is 550kg/m 3, and the average empty tower linear speed in the fine powder sedimentation/stripping device (9) is 0.1m/s. The pyrolysis fluidization gas B adopts hydrogen; the gasifying agent D adopts water vapor. By the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 99%, the methane content in the synthesis gas is improved to 14.8%, and the tar yield is 8.1%. The detailed results are shown in Table 1.
[ Example 9]
The reaction scheme was the same as in example 1. In the reaction flow, lignite+5% K 2CO3 is adopted as raw materials, the pyrolysis pressure of a fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 600 ℃, the average density of pulverized coal in a dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 550kg/m 3, and the linear velocity of an empty tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 0.1m/s; the gasification pressure of the fluidized bed gasifier (8) is 6.5MPa, the gasification temperature is 900 ℃, the average density of pulverized coal is 450kg/m 3, and the average empty tower linear velocity in the fluidized bed gasifier (8) is 0.2m/s; the gasification pressure of the rapid bed gasifier (13) is 6.5MPa, the gasification temperature is 900 ℃, and the average density of pulverized coal is 150kg/m 3; the average air tower linear speed in the fast bed gasifier (13) is 1.0m/s, the combustion pressure of the fluidized bed combustion chamber (7) is 6.5MPa, the combustion temperature is 1100 ℃, the average density of pulverized coal is 500kg/m 3, and the average air tower linear speed in the fluidized bed combustion chamber (7) is 0.2m/s; the pressure of the fine powder sedimentation/stripping device (9) is 6.5MPa, the temperature is 900 ℃, the average density of pulverized coal is 550kg/m 3, and the average empty tower linear speed in the fine powder sedimentation/stripping device (9) is 0.1m/s. The pyrolysis fluidization gas B adopts inert atmosphere; the gasifying agent D adopts CO 2. By the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 99%, the methane content in the synthesis gas is improved to 14.7%, and the tar yield is 8.8%. The detailed results are shown in Table 1.
[ Comparative example 1]
The reaction scheme was the same as in example 1. In the reaction flow, lignite+5% K 2CO3 is adopted as raw materials, the pyrolysis pressure of a fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 600 ℃, the average density of pulverized coal in a dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 550kg/m 3, and the linear velocity of an empty tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 0.1m/s; the gasification pressure of the fluidized bed gasifier (8) is 6.5MPa, the gasification temperature is 900 ℃, the average density of pulverized coal is 450kg/m 3, and the average empty tower linear velocity in the fluidized bed gasifier (8) is 0.2m/s; the gasification pressure of the rapid bed gasifier (13) is 6.5MPa, the gasification temperature is 900 ℃, and the average density of pulverized coal is 150kg/m 3; the average air tower linear speed in the fast bed gasifier (13) is 1.0m/s, the combustion pressure of the fluidized bed combustion chamber (7) is 6.5MPa, the combustion temperature is 1100 ℃, the average density of pulverized coal is 500kg/m 3, and the average air tower linear speed in the fluidized bed combustion chamber (7) is 0.2m/s; the fines settler/stripper (9) is not provided and is replaced by a cyclone only. The pyrolysis fluidization gas B adopts inert atmosphere; the gasifying agent D adopts water vapor. By the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 90%, the methane content in the synthesis gas is 13.5%, and the tar yield is 8.0%. The detailed results are shown in Table 1.
[ Comparative example 2]
The conventional lurgi furnace pressurized fixed bed gasification device (see Wang Peng, development and application of lurgi coal gasification technology [ J ]. Clean coal technology, 2009,15 (5): 48-51) is adopted in the prior art, anthracite with the grain diameter of 5-30mm is adopted as the raw material, the gasification temperature is 850 ℃, the linear velocity is less than 0.3m/s, the methane content in the outlet gas component is 4.7%, the yield of tar products is only 2% but not, the carbon conversion rate is far lower than 90%, and the results are shown in table 1 in detail.
[ Comparative example 3]
Adopts a new group PDU gasification reaction device (see Bi Jicheng, development and development of the technology of catalyzing gasification (one-step method) coal-based natural gas [ C ]. The fourth coal-based synthetic natural gas technical economy seminar in the prior art,
2013, Ullo-wood), brown coal is adopted as a raw material, 10% of potassium carbonate is added as a catalyst, the linear velocity is less than 10m/s, the operating temperature is 800 ℃, the methane content in the gasified outlet gas component is 14%, the carbon conversion rate is 90%, no tar product is generated, and the result is shown in table 1 in detail.
TABLE 1
Any numerical value recited in this disclosure includes all values incremented by one unit from the lowest value to the highest value if there is only a two unit interval between any lowest value and any highest value. For example, if the amount of a component, or a process variable such as temperature, pressure, time, etc., is stated to be 50-90, it is meant in this specification that values such as 51-89, 52-88 … …, and 69-71, and 70-71 are specifically recited. For non-integer values, 0.1, 0.01, 0.001 or 0.0001 units may be considered as appropriate. This is only a few examples of the specific designations. In a similar manner, all possible combinations of values between the lowest value and the highest value enumerated are to be considered to be disclosed.
It should be noted that the above-described embodiments are only for explaining the present invention and do not constitute any limitation of the present invention. The invention has been described with reference to exemplary embodiments, but it is understood that the words which have been used are words of description and illustration, rather than words of limitation. Modifications may be made to the invention as defined in the appended claims, and the invention may be modified without departing from the scope and spirit of the invention. Although the invention is described herein with reference to particular means, materials and embodiments, the invention is not intended to be limited to the particulars disclosed herein, as the invention extends to all other means and applications which perform the same function.
Claims (16)
1. A circulating fluidized bed pulverized coal pyrolysis-gasification apparatus comprising:
A feeder;
The fluidized bed pyrolysis furnace is connected with the feeder through a feeding inclined pipe;
The fluidized bed gasification furnace is connected with the fluidized bed pyrolysis furnace through a pyrolysis inclined tube;
the lower inlet of the fast bed gasifier is connected with the upper outlet of the fluidized bed gasifier;
the upper inlet of the fluidized bed combustion chamber is connected with the lower outlet of the fluidized bed gasifier;
A fine powder settling/stripping device which is arranged outside the rapid bed gasifier and is connected with the fluidized bed pyrolysis furnace through a gasification inclined tube;
The fine powder sedimentation/stripping device comprises a stripping section, a fine powder sedimentation section and a fine powder sedimentation/stripping device cyclone separator; the lower part of the side wall of the fine powder sedimentation/stripping device is provided with a stripping gas inlet for receiving stripping gas; the lower part of the side wall of the fine powder sedimentation/stripping device is provided with a semicoke outlet which is connected with the fluidized bed pyrolysis furnace through a gasification inclined tube; the top of the fine powder sedimentation/stripping device is provided with a synthesis gas outlet which is connected with a gas outlet of the cyclone separator of the fine powder sedimentation/stripping device and is used for discharging synthesis gas;
The fluidized bed pyrolysis furnace comprises a dense phase zone and an olefin phase zone;
The lower part of the side wall of the dense-phase zone is respectively provided with a pulverized coal inlet and a gasification semicoke inlet, and the pulverized coal inlet is connected with a feeder through a feeding inclined tube; the gasification semicoke inlet is connected with the fine powder sedimentation/stripping device through a gasification inclined tube; the side wall of the dense-phase zone is provided with a pyrolysis semicoke outlet which is connected with the fluidized bed gasifier through a pyrolysis inclined tube;
A cyclone separator of the fluidized bed pyrolysis furnace is arranged in the olefin phase region;
The lower part of the side wall of the fluidized bed gasification furnace is provided with a pyrolysis semicoke inlet which is connected with the fluidized bed pyrolysis furnace through a pyrolysis inclined tube.
2. The apparatus of claim 1, wherein a pyrolysis fluidization gas inlet is provided at a bottom of the fluidized bed pyrolysis furnace for receiving pyrolysis fluidization gas; and/or a pyrolysis gas outlet is arranged at the top of the fluidized bed pyrolysis furnace and is connected with a gas outlet of a cyclone separator of the fluidized bed pyrolysis furnace for discharging pyrolysis gas.
3. The apparatus of claim 1, wherein a lower portion of a sidewall of the fluidized-bed gasification furnace is provided with a gasification agent inlet for receiving gasification agent.
4. A device according to any one of claims 1-3, characterized in that the bottom of the fluidized bed combustion chamber is provided with an ash discharge opening, which is connected to an ash tank.
5. A plant according to any one of claims 1-3, characterized in that the plant further comprises a rapid bed cyclone connected to the upper outlet of the rapid bed gasifier.
6. A pulverized coal pyrolysis-gasification method employing the apparatus of any one of claims 1-5, comprising the steps of:
(a) The pulverized coal raw material is sent into a fluidized bed pyrolysis furnace by a feeder, and is mixed with high-temperature gasified semicoke in the fluidized bed pyrolysis furnace to be heated, and the pulverized coal undergoes pyrolysis reaction to generate pyrolysis semicoke and pyrolysis gas;
(b) The pyrolysis semicoke enters a fluidized bed gasifier through a pyrolysis inclined tube, contacts with gasifying agents, and performs gasification reaction in the fluidized bed gasifier and a fast bed gasifier to generate synthesis gas and carbon-containing gasification semicoke;
(c) The synthesis gas enters a fine powder sedimentation/stripping device to separate high-temperature gasification semicoke, and the high-temperature gasification semicoke enters a fluidized bed pyrolysis furnace through a gasification inclined tube;
(d) The carbon-containing gasified semicoke downwards enters a fluidized bed combustion chamber from a fluidized bed gasifier to undergo a combustion reaction to produce ash and high-temperature gas; the high-temperature gas upwards enters the fluidized bed gasifier to be used as a gasifying agent.
7. The method of claim 6, wherein the pulverized coal feedstock comprises pulverized coal and at least one of a catalyst and biomass.
8. The method of claim 7, wherein the catalyst comprises at least one of an alkali metal, an alkaline earth metal, and a transition metal.
9. The method of any one of claims 6-8, wherein the pulverized coal feedstock is fed by a feeder into a dense phase zone of the fluidized bed pyrolysis furnace, is heated in the dense phase zone in combination with the high temperature gasification carbocoal, and undergoes a pyrolysis reaction to produce pyrolysis carbocoal and pyrolysis gas; the pyrolysis semicoke enters a fluidized bed gasifier through a pyrolysis inclined tube; the pyrolysis gas entrains fine coal dust, the fine coal dust upwards enters an olefin phase region and is subjected to gas-solid separation through a cyclone separator of the fluidized bed pyrolysis furnace, the solid returns to a dense phase region, and the gas leaves the fluidized bed pyrolysis furnace.
10. The method according to any one of claims 6 to 8, wherein the fluidized bed pyrolysis furnace has a pyrolysis pressure of 0 to 6.5MPa and a pyrolysis temperature of 400 to 800 ℃; and/or the pulverized coal average density of the dense-phase zone of the fluidized bed pyrolysis furnace is 200-550kg/m 3, and the superficial linear velocity is 0.1-1.0m/s.
11. The method according to any one of claims 6 to 8, wherein the fluidized bed gasifier has a gasification pressure of 0 to 6.5MPa, a gasification temperature of 700 to 1200 ℃, an average density of pulverized coal of 200 to 450 kg/m 3, and an average superficial linear velocity of 0.2 to 1.2 m/s; and/or the gasification pressure of the rapid bed gasifier is 0-6.5MPa, the gasification temperature is 700-1200 ℃, the average density of pulverized coal is 50-150 kg/m 3, and the average empty tower linear velocity is 1.0-3.0 m/s.
12. A method according to any one of claims 6 to 8, wherein the synthesis gas exiting the rapid bed gasifier is entrained with unvaporised semicoke fines, which are first passed to a rapid bed cyclone for gas-solid separation, the solids falling into the stripping section of the fines settler/stripper and the gas entering the settling section of the fines settler/stripper.
13. A method according to any one of claims 6-8, characterized in that the gas coming out of the fast bed cyclone enters the settling section of the fines settling/stripper and the fines settling/stripper cyclone, the solids are further separated off, the solids fall into the stripping section of the fines settling/stripper, and the gas leaves the fines settling/stripper.
14. The method according to any one of claims 6 to 8, wherein a stripping gas is introduced into the stripping section of the fines sedimentation/stripper, and the solids of the stripping section are stripped to obtain a high temperature gasified semicoke, which enters the fluidized bed pyrolysis furnace via a gasification chute.
15. The method of any one of claims 6-8, wherein the carbonaceous gasification carbocoal is passed downwardly from the fluidized bed gasifier into a fluidized bed combustion chamber for contact with an oxidant for combustion reaction to produce ash and high temperature gas; the high-temperature gas upwards enters a fluidized bed gasifier to be used as a gasifying agent; ash is discharged.
16. The method according to any one of claims 6 to 8, wherein the fine powder settling/stripper has a pressure of 0 to 6.5MPa, a temperature of 700 to 1200 ℃, an average density of pulverized coal of 350 to 550 kg/m 3, and an average superficial linear velocity of 0.1 to 0.5m/s; and/or the combustion pressure of the fluidized bed combustion chamber is 0-6.5MPa, the combustion temperature is 800-1500 ℃, the average density of pulverized coal is 300-450 kg/m 3, and the average empty tower linear velocity is 0.2-0.6 m/s.
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