CN211199137U - Circulating fluidized bed pulverized coal pyrolysis-gasification device - Google Patents
Circulating fluidized bed pulverized coal pyrolysis-gasification device Download PDFInfo
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- CN211199137U CN211199137U CN201921598335.2U CN201921598335U CN211199137U CN 211199137 U CN211199137 U CN 211199137U CN 201921598335 U CN201921598335 U CN 201921598335U CN 211199137 U CN211199137 U CN 211199137U
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Abstract
The utility model discloses a circulating fluidized bed fine coal pyrolysis-gasification equipment, include: a feeder; the fluidized bed pyrolysis furnace is connected with the feeding machine through a feeding inclined pipe; the fluidized bed gasification furnace is connected with the fluidized bed pyrolysis furnace through a pyrolysis inclined pipe; 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; and the fine powder settling/stripping device is arranged outside the fast bed gasification furnace and is connected with the fluidized bed pyrolysis furnace through a gasification inclined pipe.
Description
Technical Field
The utility model belongs to the coal gasification field relates to a circulating fluidized bed fine coal pyrolysis-gasification 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.
Patent CN102212399B discloses a pyrolysis and gasification combined method and device, which proposes 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 for gasification, and coal gas generated by the gasification furnace carries solid particles to enter a cyclone separator; the solid particles collected by the cyclone separator are sent above a dense-phase area of the pyrolysis furnace to provide heat for fuel pyrolysis. 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 cannot be ensured, and gasification strength is low.
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 by heat generation, the volatile matters are cooled and separated to obtain tar and pyrolysis coal gas, pyrolysis semicoke generated by coal pyrolysis is sent to a fluidized bed gasification furnace, gasification reaction is carried out by taking steam and O2 as gasification agents to prepare synthesis gas, the semicoke which is not completely gasified in the gasification furnace is sent to a circulating fluidized bed combustion furnace, air is blown in for conventional combustion, or O2/CO2 is blown in 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 utility model has the advantages that the pyrolysis gasification burning step through the coal utilizes the coproduction that has realized tar, pyrolysis coal gas and synthetic gas, but its burning, pyrolysis, gasified heat step utilization order is unreasonable, has the space of further improvement and optimization to the rational utilization of energy.
In summary, although the existing pyrolysis-gasification coupled staged utilization technology solves the disadvantages of the traditional gasification technology for preparing synthesis gas and pyrolysis oil to a certain extent, the carbon conversion rate and gasification intensity are low due to the adoption of fluidized bed technology and process condition limitations. Therefore, how to further improve the carbon conversion rate and gasification strength, reasonably utilize the heat gradient utilization of combustion, gasification and pyrolysis and realize the true quality-grading, high-efficiency and clean utilization of the pyrolysis-gasification integrated pulverized coal is the key for the development of the coal gasification technology.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a new circulating fluidized bed fine coal pyrolysis-gasification device to the problems that the carbon conversion rate and the gasification intensity are low, the fine coal utilization rate is lower and the low-order coal is difficult to utilize in the prior art.
The utility model provides a circulating fluidized bed fine coal pyrolysis-gasification equipment, include:
a feeder;
the fluidized bed pyrolysis furnace is connected with the feeding machine through a feeding inclined pipe;
the fluidized bed gasification furnace is connected with the fluidized bed pyrolysis furnace through a pyrolysis inclined pipe;
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;
the fine powder settling/stripping device is arranged outside the fast bed gasification furnace and is connected with the fluidized bed pyrolysis furnace through a gasification inclined pipe;
and the fast bed cyclone separator is connected with an upper outlet of the fast bed gasification furnace.
According to some embodiments of the present invention, the fluidized bed pyrolysis furnace comprises, from bottom to top, a dense phase zone and a olefinic phase zone.
According to the preferred embodiment of the utility model, the lower part of the side wall of the dense-phase area is respectively provided with a pulverized coal inlet and a gasification semicoke inlet, and the pulverized coal inlet is connected with the feeder through a feeding inclined pipe; the gasification semicoke inlet is connected with the fine powder settling/stripping device through a gasification inclined pipe; the middle part of the side wall of the dense-phase area is provided with a pyrolysis semicoke outlet which is connected with the fluidized bed gasification furnace through a pyrolysis inclined pipe.
According to the utility model discloses a preferred embodiment, be provided with fluidized bed pyrolysis oven cyclone in the alkene phase district for the gas that produces in the dense phase district is separated.
According to a preferred embodiment of the present invention, the fluidized bed pyrolysis furnace is provided with a pyrolysis fluidizing gas inlet at the bottom thereof for receiving pyrolysis fluidizing gas.
According to the utility model discloses a preferred embodiment the top of fluidized bed pyrolysis furnace is provided with pyrolysis gas export, and it links to each other with fluidized bed pyrolysis furnace cyclone's gas outlet for discharge through the pyrolysis gas of separation.
According to the utility model discloses a preferred embodiment, fluidized bed gasifier and fluidized bed pyrolysis oven are arranged side by side.
According to some embodiments of the utility model, the lateral wall lower part of fluidized bed gasifier is provided with the pyrolysis semicoke entry, and it links to each other with the fluidized bed pyrolysis furnace through the pyrolysis pipe chute.
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 utility model discloses a preferred embodiment, the fast bed gasifier is stretched into wherein along the axial from fine powder settlement/stripper bottom center, and both communicate through fast bed gasifier cyclone.
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 fluidized 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 utility model discloses a preferred embodiment be provided with pyrolysis semicoke return valve on the pyrolysis pipe chute, it is non-mechanical return valve, preferably U valve, J valve, L valve or M valve to let in the pyrolysis semicoke valve and loosen the gas, control the circulation volume of pyrolysis semicoke through adjusting the amount of wind of pine gas, or the bed density of fluidized bed gasifier, or the material level of fluidized bed pyrolysis furnace.
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 the gasification semicoke is interior to be let in the pine and move gas, controls the circulation volume of gasification semicoke through adjusting the amount of wind of pine and moves gas, or the material level of fine powder subsides/stripper, or the temperature of fluidized bed pyrolysis furnace.
The technical scheme of the utility model carry out the pyrolysis of fine coal raw materials at the pyrolysis oven, obtain pyrolysis gas (containing the coal tar) and gasification raw materials-pyrolysis semicoke, obtain gasification raw materials through the pyrolysis, enlarged the accommodation of coal kind. And carrying out gasification reaction of the pyrolysis semicoke particles in the gasification furnace to generate synthesis gas. And most of the high-temperature gasified semicoke particles which are not gasified are used as heat carriers and circularly enter the pyrolysis furnace to be used as a heat source for pyrolysis, so that the energy consumption is reduced, and the cost of the heat carriers added in the traditional process is saved. A small part of gasified semicoke particles which are not gasified enter the combustion chamber to be subjected to combustion reaction with oxygen, and semicoke is converted into ash, so that 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 rejection in the gasification reaction and to provide the necessary gasification agent for the gasification reaction. The utility model discloses the farine subsides/stripper has been exclusively established, and its purpose is in order to get rid of the flying dust smugglied secretly in the high temperature gasification semicoke that gets into the pyrolysis furnace to reduce the flying dust smugglied secretly in the pyrolysis gas, avoid the flying dust to the jam of relevant equipment, reduce the degree of difficulty of liquid-solid separation.
The utility model discloses be in the same place pyrolysis and gasification, gasification and combustion coupling, can produce synthetic gas and coal tar, realize the branch matter hierarchical utilization of low order coal. The pulverized coal can be directly gasified or catalytically gasified, and the high-efficiency, clean and reasonable comprehensive utilization of the coal is realized.
Drawings
FIG. 1 is a schematic diagram of the circulating fluidized bed pyrolysis-gasification device of the present invention:
in the figure 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 fluidized bed pyrolysis furnace cyclone separator, 6 is a pyrolysis semicoke return valve, 7 is a fluidized bed combustion chamber, 8 is a fluidized bed gasification furnace, 9 is a fine powder sedimentation/stripping device, 10 is a stripping zone, 11 is a fine powder sedimentation zone, 12 is a fine powder sedimentation/stripping device cyclone separator, 13 is a fast bed gasification furnace, 14 is a fast bed gasification furnace cyclone separator, 15 is a gas distribution plate, 16 is an ash discharge port, 17 is an ash tank, 18 is a gasification semicoke return valve, 19 is a feed inclined pipe, 20 is a pyrolysis inclined pipe, 21 is a gasification inclined pipe, A is a pulverized coal raw material, B is pyrolysis fluidizing gas, C is an oxidant, D is a gasification agent, E is a stripping gas, F, G, H, I is a loose gas, K is a pyrolysis gas, and L is ash.
Detailed Description
The present invention will be further illustrated by the following examples, but is not limited to the examples.
The utility model discloses the work flow of device is as follows: the pulverized coal raw material is sent into a dense-phase zone (3) by a feeder (1), is mixed with high-temperature gasification semi-coke and is heated to generate pyrolysis reaction, fine coal powder recovered after gas-solid separation of pyrolysis gas carrying fine coal powder returns to the dense-phase zone (3), and pyrolysis semi-coke enters the lower part of a fluidized bed gasification furnace (8) after the circulation quantity of the pyrolysis semi-coke is controlled by a pyrolysis semi-coke return valve (6). The pyrolysis semicoke is contacted with a gasifying agent D, gasification reaction is carried out on the fluidized bed gasification furnace (8) and the fast bed gasification furnace (13) to generate synthesis gas, the gasified semicoke which is not gasified is separated by the cyclone separator (14) of the fast bed gasification furnace and then enters the settling section (11) at the upper part of the fine powder settling/stripping device (9), and the gasified semicoke which is not gasified falls into the stripping section (10) at the lower part of the fine powder settling/stripping device (9). The carbon-containing gasification semicoke falls into a fluidized bed combustion chamber (7) from the bottom of the fluidized bed gasification furnace (8) and is contacted and mixed with an oxidant C to generate combustion reaction to convert the carbon-containing semicoke into ash. High-temperature gas generated by combustion enters a fluidized bed gasification furnace (8) upwards to be used as a gasification agent and provides heat for a gasification medium. The synthesis gas coming out of the top of the cyclone separator (14) of the fast bed gasification furnace is separated from the gasification device and enters a subsequent separation and purification device after being recovered by a fine powder settling section (11) and a fine powder settling/stripping cyclone separator (12), and the fine powder recovered by the fine powder settling/stripping cyclone separator (12) falls into a stripping section (10) through a dipleg. The stripping section (10) adopts stripping gas E to strip unreacted carbon-containing semicoke and ash, fly ash carried in the unreacted carbon-containing semicoke and ash is reduced, the stripped carbon-containing semicoke and ash compound enters a gasification inclined pipe (21), the circulating amount of the carbon-containing semicoke and ash compound is controlled by a gasification semicoke return valve (18), and then the carbon-containing semicoke and ash compound enters the lower part of a dense-phase area (3) of the fluidized bed pyrolysis furnace (2) to be mixed with fresh pulverized coal, and the newly-fed pulverized coal is heated for pyrolysis.
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. A circulating fluidized bed pulverized coal pyrolysis-gasification apparatus, comprising:
a feeder;
the fluidized bed pyrolysis furnace is connected with the feeding machine through a feeding inclined pipe;
the fluidized bed gasification furnace is connected with the fluidized bed pyrolysis furnace through a pyrolysis inclined pipe;
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;
the fine powder settling/stripping device is arranged outside the fast bed gasification furnace and is connected with the fluidized bed pyrolysis furnace through a gasification inclined pipe;
and the fast bed cyclone separator is connected with an upper outlet of the fast bed gasification furnace.
2. The apparatus of claim 1, wherein the fluidized bed pyrolysis furnace comprises a dense phase zone and an olefinic phase zone.
3. The device according to claim 2, characterized in that 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 the feeder through a feeding inclined pipe; the gasification semicoke inlet is connected with the fine powder settling/stripping device through a gasification inclined pipe; the side wall of the dense-phase area is provided with a pyrolysis semicoke outlet which is connected with the fluidized bed gasification furnace through a pyrolysis inclined pipe.
4. The apparatus of claim 2, wherein a fluidized bed pyrolysis furnace cyclone is disposed within the olefinic phase region.
5. The apparatus of claim 2, wherein a pyrolysis fluidization gas inlet is provided at a bottom of the fluidized bed pyrolysis furnace for receiving pyrolysis fluidization gas.
6. The apparatus according to claim 1, wherein a pyrolysis gas outlet is provided at the top of the fluidized bed pyrolysis furnace, which is connected to a gas outlet of a cyclone of the fluidized bed pyrolysis furnace, for discharging pyrolysis gas.
7. The apparatus according to claim 1, wherein a pyrolysis semicoke inlet is formed at a lower portion of a sidewall of the fluidized-bed gasification furnace, and the pyrolysis semicoke inlet is connected with the fluidized-bed pyrolysis furnace through a pyrolysis inclined tube; 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.
8. 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.
9. The apparatus of claim 1, wherein the fines settler/stripper comprises a stripping section, a fines settler section, and a fines settler/stripper cyclone.
10. The apparatus according to claim 9, 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 arranged at the lower part of the side wall of the fine powder settling/stripping device and is connected with the fluidized 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 synthesis gas.
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| CN201921598335.2U CN211199137U (en) | 2019-09-24 | 2019-09-24 | Circulating fluidized bed pulverized coal pyrolysis-gasification device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112625755A (en) * | 2019-09-24 | 2021-04-09 | 中国石油化工股份有限公司 | Circulating fluidized bed pulverized coal pyrolysis-gasification device and pulverized coal pyrolysis-gasification method |
| CN114106885A (en) * | 2021-11-23 | 2022-03-01 | 新奥科技发展有限公司 | Gasification furnace system and semicoke distribution control method thereof |
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2019
- 2019-09-24 CN CN201921598335.2U patent/CN211199137U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112625755A (en) * | 2019-09-24 | 2021-04-09 | 中国石油化工股份有限公司 | Circulating fluidized bed pulverized coal pyrolysis-gasification device and pulverized coal pyrolysis-gasification method |
| CN114106885A (en) * | 2021-11-23 | 2022-03-01 | 新奥科技发展有限公司 | Gasification furnace system and semicoke distribution control method thereof |
| CN114106885B (en) * | 2021-11-23 | 2022-07-26 | 新奥科技发展有限公司 | Gasification furnace system and semicoke distribution control method thereof |
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