CN117720952A - Biomass abnormal double-flow pressurizing gasification system and method - Google Patents
Biomass abnormal double-flow pressurizing gasification system and method Download PDFInfo
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- 238000002309 gasification Methods 0.000 title claims abstract description 159
- 239000002028 Biomass Substances 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 18
- 230000002159 abnormal effect Effects 0.000 title claims abstract description 10
- 238000000197 pyrolysis Methods 0.000 claims abstract description 89
- 230000005587 bubbling Effects 0.000 claims abstract description 81
- 238000006243 chemical reaction Methods 0.000 claims abstract description 28
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 19
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 18
- 239000000571 coke Substances 0.000 claims description 40
- 239000007789 gas Substances 0.000 claims description 27
- 238000005336 cracking Methods 0.000 claims description 26
- 238000001816 cooling Methods 0.000 claims description 21
- 239000000463 material Substances 0.000 claims description 21
- 238000002485 combustion reaction Methods 0.000 claims description 13
- 239000000446 fuel Substances 0.000 claims description 12
- 239000002245 particle Substances 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 10
- 239000002893 slag Substances 0.000 claims description 10
- 230000001502 supplementing effect Effects 0.000 claims description 10
- 238000007599 discharging Methods 0.000 claims description 9
- 239000002737 fuel gas Substances 0.000 claims description 8
- 230000001105 regulatory effect Effects 0.000 claims description 8
- 238000001035 drying Methods 0.000 claims description 6
- 239000007787 solid Substances 0.000 claims description 5
- 239000010419 fine particle Substances 0.000 claims description 4
- 239000012071 phase Substances 0.000 claims description 4
- 239000007790 solid phase Substances 0.000 claims description 3
- 238000005243 fluidization Methods 0.000 abstract description 14
- 238000005516 engineering process Methods 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000003860 storage Methods 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000004939 coking Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
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- 238000003763 carbonization Methods 0.000 description 1
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- 238000010438 heat treatment Methods 0.000 description 1
- 239000012770 industrial material Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
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- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention discloses a biomass abnormal state double-flow pressurizing gasification system and a method, which belong to the field of biological gasification, and comprise a spouted pyrolysis fluidized bed and a bubbling gasification fluidized bed; the spouted pyrolysis fluidized bed is connected with the bubbling gasification fluidized bed in series; the spouted pyrolysis fluidized bed and the bubbling gasification fluidized bed form a reaction device of the pressurizing gasification section. The biomass abnormal state double flow pressurizing gasification system and method disclosed by the invention adopt an abnormal state double flow technology, so that the safe operation of the gasification furnace under the pressure of more than 0.5Mpa can be realized; compared with the normal pressure technology, the gas production rate of the gasification furnace per unit volume can be greatly improved; the occupied area of equipment and the energy consumption of the pressure boosting of the synthesis gas are effectively reduced; the spouted pyrolysis fluidized bed and the bubbling gasification fluidized bed can independently adjust the fluidization state and the operation temperature, so that the gasification device has better load adjusting capability.
Description
Technical Field
The invention relates to the field of biological gasification, in particular to a biomass abnormal state double-flow supercharging gasification system and method.
Background
The biomass has obvious attribute of 0 carbon, and under the development trend of carbon neutralization, the economy of synthesizing chemical products by taking biomass as a raw material is more obvious; the country which is rich in biological resources has more potential and advantage in biomass resource utilization; the conventional fluidized bed gasification furnace can only operate under normal pressure or low pressure due to the limitation of easy coking property of biomass fuel at high temperature; the gasification furnace running at low pressure not only occupies large area, but also needs to boost the pressure of the synthesis gas to match with the chemical synthesis working section, which causes space and energy waste.
Disclosure of Invention
To overcome the prior artThe technical problem to be solved by the invention is to provide a biomass abnormal state double flow pressurizing gasification system and method, which can realize safe operation of a gasification furnace under the pressure of more than 0.5Mpa by adopting an abnormal state double flow technology; compared with the normal pressure technology, the gas production rate of the gasification furnace per unit volume can be greatly improved; the occupied area of equipment and the energy consumption of the pressure boosting of the synthesis gas are effectively reduced; the spouted pyrolysis fluidized bed and the bubbling gasification fluidized bed can independently adjust the fluidization state and the operation temperature, so that the gasification device has better load adjusting capability; meanwhile, the control means of the storage quantity of the thermal cycle materials is provided, so that the fuel adaptability of the gasification furnace is greatly improved; the tar high-temperature pyrolysis device is arranged at the downstream of the gasification furnace, so that the content of tar and carbon residue in the synthesis gas can be reduced, and the quality of the fuel gas is further improved 。
To achieve the purpose, the invention adopts the following technical scheme:
the invention provides a biomass abnormal state double-flow pressurizing gasification system and a method, comprising a spouted pyrolysis fluidized bed and a bubbling gasification fluidized bed; the spouted pyrolysis fluidized bed is connected with the bubbling gasification fluidized bed in series; the spouted pyrolysis fluidized bed and the bubbling gasification fluidized bed form a reaction device of a pressurizing gasification section; drying and pyrolysis reaction are carried out in a spouted pyrolysis fluidized bed; the bubbling gasification fluidized bed is used for combustion and gasification reaction.
The invention further adopts the technical scheme that the spouted pyrolysis fluidized bed is connected with a biomass pressurizing feeding device, a hot ash returning device and a high-efficiency cyclone separation device; the bubbling gasification fluidized bed is connected with a coke returning device, a hot ash returning device, a high-efficiency cyclone separator, a circulating ash supplementing device and a gasification furnace slag cooling device.
The invention further adopts the technical scheme that a biomass pressurizing feeding device is arranged at one side of the spouted pyrolysis fluidized bed; the other side of the spouted pyrolysis fluidized bed is provided with a hot ash returning device; the top of the spouted pyrolysis fluidized bed is connected with a high-efficiency cyclone separation device; a hot ash returning device is arranged at the lower part of one side of the bubbling gasification fluidized bed; the upper part of one side of the bubbling gasification fluidized bed is provided with a circulating ash supplementing device; a coke returning device is arranged on the other side of the bubbling gasification fluidized bed; the top of the bubbling gasification fluidized bed is connected with a high-efficiency cyclone separator; the bottom of the bubbling gasification fluidized bed is connected with a gasification furnace slag cooling device.
The biomass pressurizing and feeding device is used for feeding biomass fuel in a normal pressure environment into a spouted pyrolysis fluidized bed in a pressurizing environment; coke generated by the pyrolysis of the spouted pyrolysis fluidized bed is ground in a dense phase section of the spouted pyrolysis fluidized bed, and is carried by pyrolysis gas to be sent into a high-efficiency cyclone separator for gas-solid separation after the coke is thinned, solid-phase products are sent into a bubbling gasification fluidized bed for combustion and gasification through a hot ash returning device, and generated hot ash is sent into the spouted pyrolysis fluidized bed through the hot ash returning device.
The further technical scheme of the invention is that hot fuel gas and fine particle ash generated by the bubbling gasification fluidized bed are sent into a high-efficiency cyclone separator, and more hot ash enters the spouted pyrolysis fluidized bed through a hot ash returning device; when the material in the bubbling gasification fluidized bed needs to be regulated, the material can be supplemented by the circulating ash supplementing device.
The further technical scheme of the invention is that the gasification furnace slag cooling device is used for carrying out slag discharging and hot slag cooling on the bubbling gasification fluidized bed under a pressurized state.
The invention further adopts the technical scheme that the high-efficiency cyclone separator is connected with the spouted pyrolysis fluidized bed, the bubbling gasification fluidized bed, the coke returning device and the tar cracking device; the synthesis gas separated by the high-efficiency cyclone separator enters a tar cracking device for reaction, and the separated coke and ash particles enter a bubbling gasification fluidized bed for reaction.
The further technical scheme of the invention is that the coke returning device is connected with the high-efficiency cyclone separator and the bubbling gasification fluidized bed; the ash-containing particles which are separated by the high-efficiency cyclone separator and mainly contain coke are sent into a bubbling gasification fluidized bed for gasification reaction through a coke returning device.
The invention further adopts the technical scheme that the hot ash returning device is connected with a spouted pyrolysis fluidized bed and a bubbling gasification fluidized bed; the hot ash returning device is positioned between the spouted pyrolysis fluidized bed and the bubbling gasification fluidized bed; and (3) feeding the hot ash particles generated by the bubbling gasification fluidized bed into the spouted pyrolysis fluidized bed through a hot ash returning device.
The further technical scheme of the invention is that the tar cracking device is connected with the high-temperature cyclone separator and the cracking furnace ash cooling device, and the cracked pressurized high-quality synthesis gas is sent to downstream equipment; the tar cracking device adopts a post-combustion mode, and the fine-particle coke generated by the high-temperature cyclone separator is gasified in the tar cracking device; the ash discharging and cooling device of the cracking furnace discharges ash and cools hot ash under the supercharging state of the tar cracking device.
The beneficial effects of the invention are as follows:
1. by adopting the heterogeneous double-flow technology, the gasification furnace can safely run under the pressure of more than 0.5 Mpa; compared with the normal pressure technology, the gas production rate of the gasification furnace per unit volume can be greatly improved; effectively reduces the occupied area of equipment and the energy consumption of the pressure boost of the synthesis gas.
2. The spouted pyrolysis fluidized bed and the bubbling gasification fluidized bed can independently adjust the fluidization state and the operation temperature, so that the gasification device has better load adjusting capability; meanwhile, the control means for the storage quantity of the thermal cycle materials is provided, and the fuel adaptability of the gasification furnace is greatly improved.
3. The tar high-temperature pyrolysis device is arranged at the downstream of the gasification furnace, so that the content of tar and carbon residue in the synthesis gas can be reduced, and the quality of the fuel gas is further improved.
Drawings
FIG. 1 is a diagram of a biomass heterogeneous dual-fluidized pressurized gasification system of the present invention.
In the figure:
spouted pyrolysis fluidized bed 01; bubbling gasification fluidized bed 02; a high-efficiency cyclone separator 03; a coke returning device 04; a hot ash returning device 05; a tar cracking device 06; a biomass pressurizing and feeding device 07; a circulating material replenishing device 08; a gasification furnace slag cooling device 09; the pyrolysis furnace ash cooling device 10.
Detailed Description
The invention is further described below in connection with the following detailed description. Wherein the drawings are for illustrative purposes only and are shown in schematic, non-physical, and not intended to be limiting of the present patent; for the purpose of better illustrating embodiments of the invention, certain elements of the drawings may be omitted, enlarged or reduced and do not represent the size of the actual product; it will be appreciated by those skilled in the art that certain well-known structures in the drawings and descriptions thereof may be omitted.
The same or similar reference numbers in the drawings of embodiments of the invention correspond to the same or similar components; in the description of the present invention, it should be understood that, if there is an azimuth or positional relationship indicated by terms such as "upper", "lower", "left", "right", etc., based on the azimuth or positional relationship shown in the drawings, it is only for convenience of describing the present invention and simplifying the description, but it is not indicated or implied that the apparatus or element referred to must have a specific azimuth, be constructed and operated in a specific azimuth, and thus terms describing the positional relationship in the drawings are merely illustrative and should not be construed as limitations of the present patent, and specific meanings of the terms described above may be understood by those skilled in the art according to specific circumstances.
The first embodiment is as follows:
the present invention relates to a bio-gasification system, and more particularly, to a biomass heterogeneous double-flow pressurized gasification system and method, a spouted pyrolysis fluidized bed 01 and a bubbling gasification fluidized bed 02; the spouted pyrolysis fluidized bed 01 is connected with the bubbling gasification fluidized bed 02 in series; the spouted pyrolysis fluidized bed 01 and the bubbling gasification fluidized bed 02 form a reaction device of a pressurizing gasification section; drying and pyrolysis reaction are carried out in the spouted pyrolysis fluidized bed 01; the bubbling gasification fluidized bed 02 performs combustion and gasification reactions.
The second embodiment is as follows:
the first embodiment is further described with reference to fig. 1, in which the spouted pyrolysis fluidized bed 01 is connected to a biomass pressurizing and feeding device 07, a hot ash returning device 05, and a high-efficiency cyclone 03; the bubbling gasification fluidized bed 02 is connected with a coke returning device 04, a hot ash returning device 05, a high-efficiency cyclone separator 03, a circulating ash supplementing device 08 and a gasification furnace slag cooling device 09.
And a third specific embodiment:
next, referring to fig. 1, a description will be given of the present embodiment, in which a biomass pressurizing feeder 07 is provided on one side of a spouted pyrolysis fluidized bed 01; the other side of the spouted pyrolysis fluidized bed 01 is provided with a hot ash returning device 05; the top of the spouted pyrolysis fluidized bed 01 is connected with a high-efficiency cyclone separation device 03; a hot ash returning device 05 is arranged at the lower part of one side of the bubbling gasification fluidized bed 02; the upper part of one side of the bubbling gasification fluidized bed 02 is provided with a circulating ash supplementing device 08; a coke returning device 04 is arranged on the other side of the bubbling gasification fluidized bed 02; the top of the bubbling gasification fluidized bed 02 is connected with a high-efficiency cyclone separator 03; the bottom of the bubbling gasification fluidized bed 02 is connected with a gasification furnace slag cooling device 09.
The working principle of the first, second and third embodiments and the beneficial effects thereof are as follows: the spouted pyrolysis fluidized bed 01 is a reaction device for drying and pyrolyzing biomass fuel, adopts water vapor and oxygen as fluidizing mediums, and sprays the water vapor and the oxygen into a material concentrated phase area through a central tube at the bottom of a cone, and a heat source required by drying and pyrolyzing mainly comes from circulating hot materials, and a part of the water vapor and the oxygen are combusted from the fuel; the flow of the hot material can be regulated by a hot material returning device, and the combustion share is regulated by controlling the flow of oxygen; the pyrolysis temperature is controlled between 500 ℃ and 700 ℃ in two regulation modes, and meanwhile, high-speed jet flows enter a fluidization medium in a bed to promote hot materials to surge vigorously, so that good viscosity breaking and heat transfer effects are provided for biomass fuel, and the coking of biomass under the condition of pressurization is effectively prevented; the spouted pyrolysis fluidized bed 01 has a local strong disturbance effect, and can rapidly grind the pyrolyzed coke.
Through the structure of the serial heterogeneous double fluidized bed and the high-temperature cracking furnace, pyrolysis, gasification and tar cracking of biomass fuel are respectively carried out, so that the problems of easy coking and high tar content in produced gas during biomass pressurization gasification are solved, the biomass can produce high-heating-value synthetic gas under the condition of pressurization, and reliable guarantee is provided for preparation of biomass-based low-carbonization industrial materials under the condition of pressurization.
By adopting the heterogeneous double-flow technology, the gasification furnace can safely run under the pressure of more than 0.5 Mpa; compared with the normal pressure technology, the gas production rate of the gasification furnace per unit volume can be greatly improved; the occupied area of equipment and the energy consumption of the pressure boosting of the synthesis gas are effectively reduced; the spouted pyrolysis fluidized bed and the bubbling gasification fluidized bed can independently adjust the fluidization state and the operation temperature, so that the gasification device has better load adjusting capability; meanwhile, the control means of the storage quantity of the thermal cycle materials is provided, so that the fuel adaptability of the gasification furnace is greatly improved; the tar high-temperature pyrolysis device is arranged at the downstream of the gasification furnace, so that the content of tar and carbon residue in the synthesis gas can be reduced, and the quality of the fuel gas is further improved.
The specific embodiment IV is as follows:
next, referring to fig. 1, the first embodiment will be further described, in which a biomass pressurizing and feeding device 07 feeds biomass fuel in a normal pressure environment into a spouted pyrolysis fluidized bed 01 in a pressurizing environment; coke generated by the pyrolysis of the spouted pyrolysis fluidized bed 01 is ground in a dense phase section of the spouted pyrolysis fluidized bed 01, and after the coke is thinned, the coke is carried by pyrolysis gas and is sent into a high-efficiency cyclone separator 03 for gas-solid separation, a solid phase product is sent into a bubbling gasification fluidized bed 02 through a hot ash returning device 05 for combustion and gasification, and generated thermal ash is sent into the spouted pyrolysis fluidized bed 01 through the hot ash returning device 05.
Fifth embodiment:
next, referring to fig. 1, this embodiment will be further described, in which hot gas and fine ash produced by the bubbling gasification fluidized bed 02 are sent into the high-efficiency cyclone 03, and more hot ash is sent into the spouted pyrolysis fluidized bed 01 through the hot ash returning device 05; when the material in the bubbling gasification fluidized bed 02 needs to be regulated, the material can be supplemented by the circulating ash supplementing device 08.
The bubbling gasification fluidized bed 02 is a reaction device for burning and gasifying biomass coke, steam and oxygen are adopted as fluidization mediums, and the fluidization mediums uniformly enter the lower part of a hearth through an air distribution device positioned at the bottom of the fluidized bed, so that coke particles form a stable bubbling fluidization state, and uniform burning and gasification are maintained.
The heat required for gasification comes from the combustion exotherm of a portion of the char, and by controlling the proportion of oxygen in the fluidizing medium, the reaction temperature of the bed can be controlled. The temperature of the bed layer is between 800 and 1000 ℃ during normal operation; the bubbling fluidized bed has higher heat transfer and mass transfer characteristics, can effectively avoid local concentrated overheating, and is beneficial to safely carrying out gasification reaction on coke.
The circulating material supplementing device 08 can send materials with certain granularity into the bubbling gasification fluidized bed 02 to supplement the circulating bed materials, and the bubbling gasification fluidized bed 02 is maintained in a better fluidization operation state.
Specific embodiment six:
next, this embodiment will be further described with reference to fig. 1, in which a slag-discharging cooling device 09 of a gasification furnace performs slag-discharging and hot slag-cooling of a bubbling gasification fluidized bed 02 in a pressurized state.
Seventh embodiment:
next, referring to fig. 1, a description will be given of the first embodiment, in which the high-efficiency cyclone 03 is connected to the spouted pyrolysis fluidized bed 01, the bubbling gasification fluidized bed 02, the coke returning device 04, and the tar cracking device 06; the synthesis gas separated by the high-efficiency cyclone separator 03 enters a tar cracking device 06 for reaction, and the separated coke and ash particles enter a bubbling gasification fluidized bed 02 for reaction.
The high-efficiency cyclone separator 03 is a device for carrying out gas-solid separation on the synthesis gas containing coke and ash, the high-efficiency cyclone separator 03 is a key component for maintaining the stable operation of the gasification device, and the separator needs to have higher gas-solid separation efficiency according to the requirement of a system.
Eighth embodiment:
next, referring to fig. 1, a first embodiment will be further described, in which a coke returning device 04 is connected to a high-efficiency cyclone 03 and a bubbling gasification fluidized bed 02; the ash-containing particles which are separated by the high-efficiency cyclone separator 03 and mainly contain coke are sent into the bubbling gasification fluidized bed 02 for gasification reaction through the coke returning device 04.
The coke returning device 04 adopts a micro-fluidized bed structure, and the fluidizing medium is water vapor or CO2, so that the self-balancing flow of the materials is realized.
Detailed description nine:
next, referring to fig. 1, a description will be given of the first embodiment, in which a hot ash returning device 05 is connected to a spouted pyrolysis fluidized bed 01 and a bubbling gasification fluidized bed 02; the hot ash returning device 05 is positioned between the spouted pyrolysis fluidized bed 01 and the bubbling gasification fluidized bed 02; the hot ash particles generated by the bubbling gasification fluidized bed 02 are fed into the spouted pyrolysis fluidized bed 01 through the hot ash returning device 05.
The hot ash returning device 05 has a hot ash flow regulating function, and is regulated according to the pyrolysis requirement of the spouted bed so as to cope with the parameter fluctuation in operation; the flow regulating function is realized by changing different fluidization air volumes, and meanwhile, a microfluidization bed structure and a zoned fluidization design scheme are adopted; the fluidization medium is water vapor or CO2, the fluidization air quantity has a larger adjusting range, and the adjustment of the material returning flow quantity is realized.
Detailed description ten:
in the following description of the present embodiment with reference to fig. 1, a first embodiment is further described, in which a tar cracker 06 is connected to a high-temperature cyclone 03 and a pyrolysis furnace ash cooling device 10, and the cracked pressurized high-quality synthesis gas is sent to downstream equipment; the tar cracking device 06 adopts a post combustion mode, and the fine-particle coke generated by the high-temperature cyclone separator 03 is gasified in the tar cracking device 06; the pyrolysis furnace ash cooling device 10 performs ash discharge and hot ash cooling in a pressurized state for the tar pyrolysis device 06.
The tar cracking device 06 is a device for cracking gaseous tar in the fuel gas, and the tar cracking device 06 adopts a post-combustion mode to raise the temperature of the fuel gas; through structural design, longer residence time is provided, so that tar can be effectively decomposed; cracking tar components in gasification products in a high-temperature environment by moderately combusting combustible components in the synthesis gas; at the same time, the fine-grained coke produced by the upstream equipment also undergoes gasification reaction in the tar cracking device 06, thereby improving the carbon conversion rate.
Working principle: spouted pyrolysis fluidized bed 01, bubbling gasification fluidized bed 02; the spouted pyrolysis fluidized bed 01 is connected with the bubbling gasification fluidized bed 02 in series; the spouted pyrolysis fluidized bed 01 and the bubbling gasification fluidized bed 02 form a reaction device of a pressurizing gasification section; drying and pyrolysis reaction are carried out in the spouted pyrolysis fluidized bed 01; the bubbling gasification fluidized bed 02 is subjected to combustion and gasification reaction, and the gasification furnace can safely run under the pressure of more than 0.5Mpa by adopting a heterogeneous double-flow technology; compared with the normal pressure technology, the gas production rate of the gasification furnace per unit volume can be greatly improved; the occupied area of equipment and the energy consumption of the pressure boosting of the synthesis gas are effectively reduced; the spouted pyrolysis fluidized bed and the bubbling gasification fluidized bed can independently adjust the fluidization state and the operation temperature, so that the gasification device has better load adjusting capability; meanwhile, the control means of the storage quantity of the thermal cycle materials is provided, so that the fuel adaptability of the gasification furnace is greatly improved; the tar high-temperature pyrolysis device is arranged at the downstream of the gasification furnace, so that the content of tar and carbon residue in the synthesis gas can be reduced, and the quality of the fuel gas is further improved 。
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted for elements thereof without departing from the spirit and scope of the invention. The invention is not to be limited by the specific embodiments disclosed herein, and other embodiments are within the scope of the invention as defined by the claims of the present application.
Claims (10)
1. A biomass abnormal state double-flow pressurizing gasification system and a method are characterized by comprising a spouted pyrolysis fluidized bed (01) and a bubbling gasification fluidized bed (02);
the spouted pyrolysis fluidized bed (01) is connected in series with the bubbling gasification fluidized bed (02);
the spouted pyrolysis fluidized bed (01) and the bubbling gasification fluidized bed (02) form a reaction device of a pressurizing gasification section;
drying and pyrolysis reaction are carried out in a spouted pyrolysis fluidized bed (01);
the bubbling gasification fluidized bed (02) is used for combustion and gasification reaction.
2. The biomass heterogeneous double-fluidized pressurized gasification system and method according to claim 1, wherein:
the spouted pyrolysis fluidized bed (01) is connected with a biomass pressurizing feeding device (07), a hot ash returning device (05) and a high-efficiency cyclone separation device (03);
the bubbling gasification fluidized bed (02) is connected with a coke returning device (04), a hot ash returning device (05), a high-efficiency cyclone separator (03), a circulating ash supplementing device (08) and a gasification furnace slag discharging and cooling device (09).
3. The biomass heterogeneous double-fluidized pressurized gasification system and method according to claim 2, wherein:
a biomass pressurizing feeding device (07) is arranged at one side of the spouted pyrolysis fluidized bed (01);
the other side of the spouted pyrolysis fluidized bed (01) is provided with a hot ash returning device (05);
the top of the spouted pyrolysis fluidized bed (01) is connected with a high-efficiency cyclone separation device (03);
a hot ash returning device (05) is arranged at the lower part of one side of the bubbling gasification fluidized bed (02);
the upper part of one side of the bubbling gasification fluidized bed (02) is provided with a circulating ash supplementing device (08);
a coke returning device (04) is arranged on the other side of the bubbling gasification fluidized bed (02);
the top of the bubbling gasification fluidized bed (02) is connected with a high-efficiency cyclone separator (03);
the bottom of the bubbling gasification fluidized bed (02) is connected with a gasification furnace slag cooling device (09).
4. The biomass heterogeneous double-fluidized pressurized gasification system and method according to claim 2, wherein:
the biomass pressurizing feeding device (07) feeds biomass fuel in a normal pressure environment into a spouted pyrolysis fluidized bed (01) in a pressurizing environment;
coke generated by pyrolysis of the spouted pyrolysis fluidized bed (01) is ground in a dense phase section of the spouted pyrolysis fluidized bed (01), and after the coke is thinned, the coke is carried by pyrolysis gas and is sent into a high-efficiency cyclone separator (03) for gas-solid separation, a solid-phase product is sent into a bubbling gasification fluidized bed (02) through a hot ash returning device (05) for combustion and gasification, and generated thermal ash is sent into the spouted pyrolysis fluidized bed (01) through the hot ash returning device (05).
5. The biomass heterogeneous double-fluidized pressurized gasification system and method according to claim 2, wherein:
hot fuel gas and fine ash generated by the bubbling gasification fluidized bed (02) are sent into a high-efficiency cyclone separator (03), and more hot ash enters a spouted pyrolysis fluidized bed (01) through a hot ash returning device (05);
when the materials in the bubbling gasification fluidized bed (02) need to be regulated, the materials can be supplemented by a circulating ash supplementing device (08).
6. The biomass heterogeneous double-fluidized pressurized gasification system and method according to claim 2, wherein:
the gasification furnace slag-discharging cooling device (09) performs slag-discharging and hot slag-cooling on the bubbling gasification fluidized bed (02) under a pressurized state.
7. The biomass heterogeneous double-fluidized pressurized gasification system and method according to claim 2, wherein:
the high-efficiency cyclone separator (03) is connected with the spouted pyrolysis fluidized bed (01), the bubbling gasification fluidized bed (02), the coke returning device (04) and the tar cracking device (06);
the synthesis gas separated by the high-efficiency cyclone separator (03) enters a tar cracking device (06) for reaction, and the separated coke and ash particles enter a bubbling gasification fluidized bed (02) for reaction.
8. The biomass heterogeneous double-fluidized pressurized gasification system and method according to claim 2, wherein:
the coke returning device (04) is connected with the high-efficiency cyclone separator (03) and the bubbling gasification fluidized bed (02);
the ash-containing particles which are separated by the high-efficiency cyclone separator (03) and mainly contain coke are sent into the bubbling gasification fluidized bed (02) for gasification reaction through the coke returning device (04).
9. The biomass heterogeneous double-fluidized pressurized gasification system and method according to claim 2, wherein:
the hot ash returning device (05) is connected with the spouted pyrolysis fluidized bed (01) and the bubbling gasification fluidized bed (02);
the hot ash returning device (05) is positioned between the spouted pyrolysis fluidized bed (01) and the bubbling gasification fluidized bed (02);
and feeding the hot ash particles generated by the bubbling gasification fluidized bed (02) into the spouted pyrolysis fluidized bed (01) through a hot ash returning device (05).
10. The biomass heterogeneous double-fluidized pressurized gasification system and method according to claim 2, wherein:
the tar cracking device (06) is connected with the high-temperature cyclone separator (03) and the ash discharging and cooling device (10) of the cracking furnace, and the cracked pressurized high-quality synthesis gas is sent to downstream equipment;
the tar cracking device (06) adopts a post-combustion mode, and the fine-particle coke generated by the high-temperature cyclone separator (03) is gasified in the tar cracking device (06);
the ash discharging and cooling device (10) of the pyrolysis furnace discharges ash and cools hot ash under the supercharging state of the tar pyrolysis device (06).
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