CN211199136U - Device for fluidized catalytic gasification of pulverized coal - Google Patents
Device for fluidized catalytic gasification of pulverized coal Download PDFInfo
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- CN211199136U CN211199136U CN201921598334.8U CN201921598334U CN211199136U CN 211199136 U CN211199136 U CN 211199136U CN 201921598334 U CN201921598334 U CN 201921598334U CN 211199136 U CN211199136 U CN 211199136U
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Abstract
The utility model discloses a device of fine coal fluidization catalytic gasification, include: a feeder; the fast bed pyrolysis furnace is connected with the feeding machine through a feeding inclined pipe; the fluidized bed gasification furnace is connected with the fast bed pyrolysis furnace; the lower inlet of the fast bed gasification furnace is connected with the upper outlet of the fluidized bed gasification furnace; the upper inlet of the fluidized bed combustion chamber is connected with the lower outlet of the fluidized bed gasification furnace; a fine powder settling/stripping device connected with the fast bed pyrolysis furnace through a gasification inclined pipe.
Description
Technical Field
The utility model belongs to coal gasification field relates to a fine coal fluidization catalytic gasification's device.
Background
Coal, petroleum and natural gas are three major primary energy sources in the world, wherein coal accounts for about 79% of the world energy reserves, and coal is one of the main fuel resources for generating power, heat, coal tar processing and by-product asphalt. China is a country with coal as a main energy structure, and the coal cannot be changed for a long time in the future, and according to statistics, the coal reaches 63.7% in a primary energy consumption structure of China in 2015. 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. 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 preparing substitute natural gas from coal. The method is a key for realizing sustainable energy development in China and is an effective way for solving the global energy and environment problems.
China is the largest coal gasification technology application market in the world, and at present, various coal gasification technologies have been successfully applied in industrialization. The prior art widely belongs to an entrained flow gasification technology, and the carbon conversion rate is improved at the cost of high temperature and high pressure, so that the problems of high energy consumption, difficult gas purification, strict requirements on equipment and the like are caused. At the same time, the excessive operating temperatures of entrained flow slag gasification technology increase the investment, maintenance and operating costs of the entrained flow. Research reports of the American Electric Power Research Institute (EPRI) indicate that the existing industrial entrained-flow gasifier is not suitable for the gasification of high-ash and high-ash fusion-point coal, and the world needs an industrialized fluidized bed gasification technology. The fluidized bed technology has the nature of adapting to high ash melting point and high ash coal types no matter combustion or gasification, and the evidence proves that the circulating fluidized bed boiler successfully combusts coal gangue.
The natural gas is a high-quality fuel and an important chemical raw material, and has the advantages of safety, reliability, environmental protection and the like. With the rapid development of the economy of China and the acceleration of the urbanization pace, the demand for natural gas is increasing day by day. The natural gas yield of China is the amount which cannot meet the demand of natural gas, the contradiction between supply and demand is increasingly prominent, the supply gap can only be made up by relying on import, and the energy safety of China is greatly influenced. The existing coal-based natural gas technology can be divided into: two-step and one-step processes. The two-step coal-to-natural gas technology belongs to the more traditional technology, and is a method for converting coal into synthesis gas (CO + H2) and performing methanation to obtain SNG, which needs to undergo the following steps: gasification, shift cooling, purification, methane synthesis, and the like. The one-step coal-to-natural gas technology is characterized in that coal is used as a raw material to directly synthesize methane, and gasification, transformation and methanation reaction processes are realized in a gasification furnace through a catalyst to obtain the synthesis gas rich in methane. The two-step coal-to-natural gas technology needs to be realized in different reactors, so that the temperature and the pressure in each reaction process are not matched, the heat loss is high during the internal circulation of the system, and the energy conversion efficiency of the system is reduced. The one-step coal-based natural gas technology effectively solves the problems, realizes the coupling of material flow and heat, and has higher economical efficiency and feasibility, thereby becoming an important research direction in the field of coal-based natural gas.
US patent 4077778 proposes a process for preparing methane by coal one-step method, which uses alkali metal carbonate or alkali metal hydroxide as catalyst, controls the reaction temperature in the furnace at about 700 ℃ by superheated steam, and reacts with coal powder under the action of catalyst to directly obtain methane-rich gas. The process needs to heat superheated steam to about 850 ℃, has high energy consumption and low carbon conversion rate, is difficult to maintain the reaction temperature under the condition of no external heat supply, and is still in the research and development stage.
Chinese patent CN102021037B proposes a method for producing methane by coal catalytic gasification in one step, which is to divide a gasification furnace into a synthesis gas generation section, a coal methanation section and a synthesis gas methanation section, so that the combustion, gasification, methanation and pyrolysis reactions are performed in stages. However, the gasification furnace needs to be provided with a plurality of layers of air distribution plates and overflow channels, the structure in the furnace is complex, the gasification efficiency and the methane yield are low, and the introduction of oxygen at the bottom of the fluidized bed is easy to melt and agglomerate ash slag to form large slag which blocks an outlet and a gas distributor of the gasification furnace, so that the operation stability of the device is affected and the technology is not provided with an industrialized device.
In summary, although the existing coal catalytic gasification technology solves the disadvantages of the traditional fixed bed and entrained flow gasification for preparing methane-rich synthesis gas to a certain extent, the existing coal catalytic gasification technology is in the research and development or amplification stage, and has not yet been applied industrially. Due to the limitations of fluidized bed technology and catalytic process conditions, carbon conversion and gasification intensity are low. Therefore, the key for the development of the coal gasification technology is how to effectively improve the carbon conversion rate and the gasification strength, effectively perform gradient utilization of heat of combustion, gasification and pyrolysis, reasonably couple reaction processes of combustion, gasification, pyrolysis, transformation, methanation and the like, and realize the true quality-based grading, high efficiency and clean utilization of the pyrolysis-gasification integrated pulverized coal.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a fine coal fluidization catalytic gasification device of fine coal pyrolysis, burning, gasification coupling to the problem that carbon conversion rate and gasification intensity are low, methane productivity are low, fine coal utilization ratio is lower and the low order coal is difficult to utilize that prior art exists.
The utility model provides a device of fine coal fluidization catalytic gasification, include:
a feeder;
the fast bed pyrolysis furnace is connected with the feeding machine through a feeding inclined pipe;
the fluidized bed gasification furnace is connected with the fast bed pyrolysis furnace;
the lower inlet of the fast bed gasification furnace is connected with the upper outlet of the fluidized bed gasification furnace;
the upper inlet of the fluidized bed combustion chamber is connected with the lower outlet of the fluidized bed gasification furnace;
a fine powder settling/stripping device connected with the fast bed pyrolysis furnace through a gasification inclined pipe;
a gas-solid rapid separator connected with the synthesis gas outlet of the fine powder settling/stripping device;
and the gas separation device is connected with the gas-solid rapid separator.
According to some embodiments of the present invention, the lower portion of the sidewall of the fast bed pyrolysis furnace is provided with a pulverized coal inlet and a gasified semicoke inlet, respectively, and the pulverized coal inlet is connected to the feeding machine through a feeding inclined tube; the gasification semicoke inlet is connected with the fine powder settling/stripping device through a gasification inclined pipe; the upper part of the fast bed pyrolysis furnace is provided with a pyrolysis product outlet which is connected with the fluidized bed gasification furnace.
According to the utility model discloses a preferred embodiment the bottom of fast bed pyrolysis oven is provided with pyrolysis fluidization gas entry for receive pyrolysis fluidization gas.
According to the preferred embodiment of the present invention, the fluidized-bed gasification furnace and the fast-bed pyrolysis furnace are arranged in parallel.
According to some embodiments of the present invention, the upper portion of the sidewall of the fluidized-bed gasification furnace is provided with a pyrolysis product inlet, which is connected to the fast-bed pyrolysis furnace.
According to the preferred embodiment of the present invention, a gasification agent inlet is provided at a lower portion of the sidewall of the fluidized-bed gasification furnace, and the gasification agent inlet is used for receiving a gasification 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 present invention, a gas distribution plate is disposed below an interior of the fluidized bed combustor; and an ash residue discharge port is arranged at the bottom of the fluidized bed combustion chamber and is connected with an ash residue tank.
According to the preferred embodiment of the present invention, the upper outlet of the fluidized bed gasification furnace is connected to the lower inlet of the fast bed gasification furnace after reducing the diameter.
According to the preferred embodiment of the present invention, the fast bed gasifier comprises, from bottom to top, a fast bed gasification/pyrolysis zone, a fast bed steam shift zone and a fast bed methanation zone; preferably, a steam inlet is arranged on the side wall of the fast bed steam shift zone, and a synthesis gas return port is arranged on the side wall of the fast bed methanation zone.
According to some embodiments of the invention, the fines settling/stripper comprises a stripping section, a fines settling section and a fines settling/stripper cyclone; a stripping gas inlet is formed in the lower part of the side wall of the fine powder settling/stripping device and used for receiving stripping gas; a semicoke outlet is arranged at the lower part of the side wall of the fine powder settling/stripping device and is connected with the fast bed pyrolysis furnace through a gasification inclined pipe; the top of the fine powder settling/stripping device is provided with a synthesis gas outlet which is connected with a gas outlet of the cyclone separator of the fine powder settling/stripping device and used for discharging the separated synthesis gas.
According to the preferred embodiment of the present invention, a fast bed cyclone is provided inside the fine powder settling/stripping apparatus, and is connected to the upper outlet of the fast bed gasification furnace.
According to the utility model discloses a preferred embodiment, gas-solid quick separation ware is provided with synthesis gas entry, flying dust export and the gas-solid quick separation ware gas outlet, the synthesis gas entry with the synthetic gas export of fine powder settlement/stripper links to each other, gas-solid quick separation ware gas outlet links to each other with gas separation device.
According to the utility model discloses a preferred embodiment, gas separation device is provided with gas inlet, circulation gas export and synthesis gas export, gas inlet with gas-solid quick separation ware gas outlet links to each other, circulation gas export with the synthesis gas returning charge mouth in fast bed methanation district links to each other.
According to some embodiments of the invention, the apparatus further comprises a catalyst system comprising a catalyst recovery device and a catalyst loading device; the upstream of the catalyst recovery device is connected with the ash tank, and the downstream of the catalyst recovery device is connected with the catalyst loading device; the upstream of the catalyst loading device is connected with the catalyst recovery device, and the downstream of the catalyst loading device is connected with the feeder.
According to the utility model discloses a preferred embodiment, catalyst recovery unit is provided with entry, ash outlet and catalyst export, the entry links to each other with the ash can, the catalyst export with catalyst loading device links to each other.
According to the utility model discloses a preferred embodiment, catalyst loading device is provided with first catalyst entry, second catalyst entry, carrier entry and catalyst export, first catalyst entry with catalyst recovery unit's catalyst export, second catalyst entry is used for replenishing the catalyst, the carrier entry is used for adding the carrier, the catalyst export with the batcher links to each other.
According to the utility model discloses a preferred embodiment be provided with gasification semicoke return valve on the gasification pipe chute, it is non-mechanical return valve, preferably U valve, J valve, L valve or M valve to inject the pine gas in the gasification semicoke return valve, control the circulation volume of gasification semicoke through adjusting the amount of wind of pine gas, or the material level of fine powder subsides/stripper, or the temperature of fast bed pyrolysis furnace.
Drawings
FIG. 1 is a schematic diagram of the device for fluidized catalytic gasification of pulverized coal of the present invention:
in fig. 1, 1 is a feeder; 2 is a feeding inclined tube; 3 is a fast bed pyrolysis furnace; 4 is a fluidized bed combustion chamber; 5 is a fluidized bed gasification furnace; 6 is a fast bed gasification furnace; 7 is a fast bed gasification/cracking zone; 8 is a fast bed steam shift zone; 9 is a fast bed methanation region; 10 is a fine powder settling/stripping device; 11 is a cyclone separator of a fast bed gasification furnace; 12 is a stripping section; 13 is a fine powder settling section; 14 is a fine powder settling/stripping cyclone separator; 15 is a gas distribution plate; 16 is a clinker outlet; 17 is a slag tank; 18 is a gasification inclined tube; 19 is a gasification semicoke return valve; 20 is a gas-solid rapid separator; 21 is a gas separation device; 22 is a catalyst recovery device; 23 is a pulverized coal catalyst loading device; a is a pulverized coal raw material; b is pyrolysis fluidization gas; c is an oxidant; d is a gasifying agent; e is water vapor; f is stripping gas; G. h is loosening air; i is fly ash; j is methane-rich syngas; k is ash; m is a carrier; n is a catalyst and/or biomass.
Detailed Description
The present invention will be further illustrated by the following examples, but is not limited to the examples.
The utility model discloses a device work flow as follows: the raw materials are sent into a fast bed pyrolysis furnace (3) by a feeder (1), and are mixed with high-temperature gasification semicoke/ash slag from a gasification furnace to be heated, so that pyrolysis reaction is carried out, and pyrolysis gas and pyrolysis semicoke enter a fluidized bed gasification furnace (5). Wherein, the pyrolysis semicoke is contacted with a gasifying agent D, and gasification reaction and tar cracking reaction are carried out in a fluidized bed gasification furnace (5) and a fast bed gasification furnace (6) to generate synthesis gas. While the fast bed gasification furnace (6) generates gasification reaction, the water vapor E is introduced into the fast bed water vapor shift zone (8) to generate water vapor shift reaction to adjust H2The ratio of/CO is that the circulating synthesis gas is introduced into the fast bed methanation region (9) to perform methanation reaction to improve the yield of methane in the product. The synthesis gas separated from the synthesis gas with the semi-coke fine powder enters a subsequent gas-solid rapid separator (20) to remove fly ash I, and partial synthesis gas in the synthesis gas is used as circulating gas to circulate to a rapid bed methanation region (9) for further methanation reaction, so that the yield of methane is improved. Fines recovered from the fines settling/stripper cyclone (14) fall through the dipleg into the stripping section (12). The stripping section (12) adopts stripping gas F to strip unreacted carbon-containing semicoke and ash, the carbon-containing semicoke and ash compounds after stripping enter the fast bed pyrolysis furnace (3) to be mixed with fresh pulverized coal after controlling the circulation quantity, and the fresh pulverized coal is heated to carry out pyrolysis. The carbon-containing gasified semicoke and ash fall into a fluidized bed combustion chamber (4) from the bottom of the fluidized bed gasification furnace (5) to be contacted and mixed with an oxidant C for combustion reaction, and the ash is discharged out of the device periodically or continuously. High-temperature gas generated by combustion enters the fluidized bed gasification furnace (5) upwards to be used as a gasification agent and provides heat for a gasification medium. After the ash containing the catalyst and discharged from the ash tank (17) is subjected to heat exchange,the catalyst enters a catalyst recovery device (22) to be recovered and then is discharged, and the recovered catalyst enters a catalyst loading device (23) to be recycled.
It should be noted that the above-mentioned embodiments are only used for explaining the present invention, and do not constitute any limitation to the present invention. The present invention has been described with reference to exemplary embodiments, but the words which have been used herein are words of description and illustration, rather than words of limitation. Modifications may be made to the invention as specified within the scope of the claims and modifications may be made without departing from the scope and spirit of the invention.
Claims (10)
1. An apparatus for fluidized catalytic gasification of pulverized coal, comprising:
a feeder;
the fast bed pyrolysis furnace is connected with the feeding machine through a feeding inclined pipe;
the fluidized bed gasification furnace is connected with the fast bed pyrolysis furnace;
the lower inlet of the fast bed gasification furnace is connected with the upper outlet of the fluidized bed gasification furnace;
the upper inlet of the fluidized bed combustion chamber is connected with the lower outlet of the fluidized bed gasification furnace;
a fine powder settling/stripping device connected with the fast bed pyrolysis furnace through a gasification inclined pipe;
a gas-solid rapid separator connected with the synthesis gas outlet of the fine powder settling/stripping device;
and the gas separation device is connected with the gas-solid rapid separator.
2. The device of claim 1, wherein a pulverized coal inlet and a gasified semicoke inlet are respectively arranged at the lower part of the side wall of the fast bed pyrolysis furnace, and the pulverized coal inlet is connected with the feeding machine through a feeding inclined pipe; the gasification semicoke inlet is connected with the fine powder settling/stripping device through a gasification inclined pipe; the upper part of the fast bed pyrolysis furnace is provided with an outlet which is connected with the fluidized bed gasification furnace.
3. The apparatus of claim 2, wherein a pyrolysis fluidization gas inlet is provided at a bottom of the fast bed pyrolysis furnace for receiving pyrolysis fluidization gas.
4. The apparatus of claim 1, wherein a pyrolysis product inlet is provided at an upper portion of a sidewall of the fluidized-bed gasification furnace, and is connected to an outlet of the fast-bed pyrolysis furnace; and a gasification agent inlet is arranged at the lower part of the side wall of the fluidized bed gasification furnace and is used for receiving a gasification agent.
5. The apparatus of claim 1, wherein the bottom of the fluidized bed combustion chamber is provided with an ash discharge port, the ash discharge port being connected to an ash tank.
6. The apparatus of claim 1, wherein the fast bed gasifier comprises, from bottom to top, a fast bed gasification/cracking zone, a fast bed steam shift zone, and a fast bed methanation zone; the side wall of the fast bed steam conversion zone is provided with a steam inlet, and the side wall of the fast bed methanation zone is provided with a synthetic gas return port.
7. The apparatus of claim 1, wherein the fines settler/stripper comprises a stripping section, a fines settler section, and a fines settler/stripper cyclone.
8. The apparatus according to claim 1, wherein the fines settler/stripper is provided with a stripping gas inlet at a lower portion of the side wall for receiving stripping gas; a semicoke outlet is formed in the lower part of the side wall of the fine powder settling/stripping device and is connected with the fast bed pyrolysis furnace through a gasification inclined pipe; the top of the fine powder settling/stripping device is provided with a synthesis gas outlet which is connected with a gas outlet of a cyclone separator of the fine powder settling/stripping device and used for discharging synthesis gas; and/or a fast bed cyclone separator is arranged in the fine powder settling/stripping device and is connected with the upper outlet of the fast bed gasification furnace.
9. The apparatus of claim 1, further comprising a catalyst system comprising a catalyst recovery device and a catalyst loading device.
10. The apparatus of claim 9, wherein the catalyst recovery unit is connected upstream to a ash tank and downstream to the catalyst loading unit; the upstream of the catalyst loading device is connected with the catalyst recovery device, and the downstream of the catalyst loading device is connected with the feeder.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201921598334.8U CN211199136U (en) | 2019-09-24 | 2019-09-24 | Device for fluidized catalytic gasification of pulverized coal |
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| CN201921598334.8U CN211199136U (en) | 2019-09-24 | 2019-09-24 | Device for fluidized catalytic gasification of pulverized coal |
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| CN211199136U true CN211199136U (en) | 2020-08-07 |
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