阅读说明：本技术 一种器流床和生物质反应炉 (Fluidized bed and biomass reaction furnace ) 是由 王雄鹰 王冬阳 邹建球 钟铁军 黄燕丽 于 2021-08-30 设计创作，主要内容包括：本发明涉及一种器流床和生物质反应炉,器流床包括至少一组反应流化组件、流化室和补风排料组件,反应流化组件包括综合反应器和流化器,综合反应器一端有反应器进料口和反应器排气口,综合反应器另一端与流化器的一端固定并连通,流化器的轴线水平且可转动的安装于流化室内,流化器一端侧壁有排渣装置,流化器另一端侧壁有多个流化孔,补风排料组件固定于流化室内且在流化器下方,反应器排气口与流化室连通。有益效果是：综合反应器作为物料均质化预处理段,解决流化床需要均质化预处理、投资大、占地大、成本高的难题。流化器和流化室作为综合反应器二次反应阶段,解决了综合反应器烟气或燃气反应不充分,烟气含VOC高或燃气含焦油和酚的难题。(The invention relates to a fluidized bed and a biomass reaction furnace, wherein the fluidized bed comprises at least one group of reaction fluidization components, a fluidization chamber and an air supplementing and discharging component, each reaction fluidization component comprises a comprehensive reactor and a fluidizer, one end of the comprehensive reactor is provided with a reactor feeding port and a reactor discharging port, the other end of the comprehensive reactor is fixed and communicated with one end of the fluidizer, the axis of the fluidizer is horizontally and rotatably arranged in the fluidization chamber, the side wall of one end of the fluidizer is provided with a slag discharging device, the side wall of the other end of the fluidizer is provided with a plurality of fluidization holes, the air supplementing and discharging component is fixed in the fluidization chamber and below the fluidizer, and the reactor discharging port is communicated with the fluidization chamber. The beneficial effects are that: the comprehensive reactor is used as a material homogenizing pretreatment section, and the problems of homogenizing pretreatment, large investment, large occupied area and high cost of the fluidized bed are solved. The fluidizer and the fluidizing chamber are used as the secondary reaction stage of the comprehensive reactor, and the problems that the reaction of the flue gas or the fuel gas of the comprehensive reactor is insufficient, the VOC content of the flue gas is high or the tar and the phenol content of the fuel gas are solved.)

1. The fluidized bed is characterized by comprising a reaction fluidization assembly, a fluidization chamber (3) and an air supplementing discharge assembly, wherein the reaction fluidization assembly is at least one group, each group of the reaction fluidization assembly comprises an integrated reactor (1) and a fluidizer (2), one end of the integrated reactor (1) is provided with a reactor feeding hole (101) and a reactor exhaust hole (102), the other end part of the integrated reactor (1) is fixedly connected and communicated with one end part of the fluidizer (2), the axis of the fluidizer (2) is horizontally arranged and rotatably arranged in the fluidization chamber (3), one end side wall of the fluidizer (2) is provided with a slag discharge device (4), the other end side wall of the fluidizer (2) is provided with a plurality of fluidization holes (201), the air supplementing discharge assembly is fixed in the fluidization chamber (3) and is positioned below the fluidizer (2), the reactor outlet (102) communicates with the fluidizing chamber (3), and the upper part of the fluidizing chamber (3) has a fluidizing chamber outlet (301).

2. A fluidized bed according to claim 1, characterized in that the side walls of the integrated reactor (1) are provided with reactor insulation (103), and the reactor exhaust (102) is in communication with the aeration discharge assembly or the lower side wall of the fluidization chamber (3).

3. A fluidized bed according to claim 1, wherein the integrated reactor (1) is rotatably mounted in the fluidizing chamber (3), the side wall of the fluidizing chamber (3) is provided with a fluidizing chamber insulating layer (302), and the reactor inlet (101) is located outside the fluidizing chamber (3).

4. A fluidized bed according to claim 3, wherein each set of the reaction fluidizing components further comprises an auger (5), the reactor gas outlet (102) is located outside the fluidizing chamber (3) and communicates with the fluidizing chamber (3) at a position corresponding to one end of the integrated reactor (1), the auger (5) is installed at the bottom inside the fluidizing chamber (3) and extends from one end of the integrated reactor (1) to the air supplementing discharge component.

5. A fluidized bed according to claim 2 or 4, wherein each set of reaction fluidization components further comprises a crude gas induced draft fan (6) and an induced draft pipeline (13), the fluidization chamber (3) or the air supplement discharge component is communicated with the reactor exhaust port (102) through the induced draft pipeline (13), and the crude gas induced draft fan (6) is fixed in the induced draft pipeline (13).

6. A fluidized bed according to claim 5, wherein the integrated reactor (1) comprises a reactor cylinder, a reactor feed cylinder (7) and a reactor exhaust cylinder (8), one end of the reactor feed cylinder (7) is provided with the reactor feed port (101), the other end is communicated with one end of the reactor cylinder, the reactor feed cylinder (7) is fixed in the reactor exhaust cylinder (8), one end of the reactor exhaust cylinder (8) is provided with the reactor exhaust port (102), one end of the reactor cylinder is rotatably sleeved outside the other end of the reactor exhaust cylinder (8), and the other end of the reactor cylinder is fixedly connected and communicated with one end of the fluidized bed (2).

7. A flow bed according to claim 3, wherein the integrated reactor (1) comprises a reactor body and a reactor feed cylinder (7), the reactor feed cylinder (7) is fixedly arranged and has the reactor feed inlet (101) at one end, the reactor body is positioned in the fluidization chamber (3), and has one end rotatably sleeved outside the other end of the reactor feed cylinder (7) and communicated with the reactor feed cylinder (7), and the reactor gas outlet (102) is arranged on one side wall of the reactor body; still include auger (5), auger (5) install in bottom in fluidization chamber (3), and follow the one end of reactor barrel extends to the material subassembly is arranged in the tonifying wind.

8. A fluidized bed according to claim 7, wherein each set of the reactive fluidizing components further comprises a high temperature positive pressure blower (9), an air inlet of the high temperature positive pressure blower (9) is communicated with the fluidizing chamber (3), and an air outlet of the high temperature positive pressure blower (9) is communicated with the other end of the fluidizer (2).

9. An ebullated bed according to claim 1, wherein the air supply and discharge assembly comprises an air box (10) and a chain grate furnace (11), one end of the chain grate furnace (11) is fixed in the fluidization chamber (3) and is located below the slag discharge device (4), the other end of the chain grate furnace is communicated with the outside of the fluidization chamber (3), the air box (10) is fixed in the fluidization chamber (3) and is located below the fluidization holes (201), and the top wall of the air box (10) is an air distribution plate (1001).

10. A flow bed according to claim 9, wherein the air supplement and discharge assembly further comprises a steam conduit, the steam conduit communicating with the wind box (10).

11. A fluidized bed according to any one of claims 1-4 and 7-10, further comprising a cyclone (12), wherein the fluidizing chamber gas outlet (301) is in communication with a separator gas inlet of the cyclone (12), and wherein the solids outlet of the cyclone (12) is in communication with a lower portion of the fluidizing chamber (3).

12. A biomass reactor comprising a fluidized bed according to any one of claims 1 to 11.

13. The biomass reaction furnace according to claim 12, wherein the biomass reaction furnace is a boiler, a gasification furnace or a hot blast stove.

Technical Field

The invention relates to the field of environment-friendly equipment, in particular to a fluidized bed and a biomass reaction furnace.

Background

The fuel adaptability of the fluidized bed furnace is strong. The fluidized reaction efficiency of the combustion furnace, incinerator or boiler comprising the fluidized bed is high, and the carbon conversion rate is high. The fuel gas produced by the gasification furnace containing the fluidized bed does not contain tar and phenol harmful substances, and the fuel gas purification process is simplified. Fluidized bed furnaces have become the most popular combustion or gasification unit in the eye.

However, fluidized beds have several major drawbacks:

1. the fuel needs to be particle homogenized. The fluidized state is formed by passing a gas stream (e.g., air, steam, etc.) through the particulate material to suspend it, and a relatively homogeneous material is a prerequisite for forming the fluidized state. Therefore, the fluidized bed furnace is mostly fueled by pulverized coal. Biomass, particularly biomass solid waste (such as household garbage and industrial garbage) is widely applied due to the fact that the dual attributes of environmental protection and energy are increasingly encouraged by national environmental governance and recycling economy policies. However, the biomass is difficult to homogenize due to the complex and various physicochemical shapes, the investment cost is high, the treatment cost is high, the occupied area is large, and the application of the fluidized bed furnace in the field of biomass is limited.

2. The heat value of the fuel gas of the fluidized bed gasification furnace is low. The fluidized bed gasification furnace generally adopts air as a fluidizing agent (the fluidizing agent is also called as a suspending agent) and a gasifying agent, and is simple and economical. However, the air contains nearly eight nitrogen components, thereby diluting the fuel gas and ensuring that the calorific value of the fuel gas is generally lower than 1200 Kcal/cubic meter.

Disclosure of Invention

The invention aims to solve the technical problem of how to directly apply the heterogeneous material to the fluidized bed and avoid the reduction of the heat value of the fuel gas.

The technical scheme for solving the technical problems is as follows: the utility model provides a fluidized bed, includes reaction fluidization subassembly, fluidization chamber and air supplement row's material subassembly, the reaction fluidization subassembly is at least a set of, every group the reaction fluidization subassembly includes comprehensive reactor and fluidizer, the one end of synthesizing the reactor has reactor feed inlet and reactor gas vent, synthesize the reactor other end tip with the one end tip fixed connection and the intercommunication of fluidizer, the axis level of fluidizer set up and rotatable install in the fluidization chamber, the one end lateral wall of fluidizer has row sediment device, the other end lateral wall of fluidizer has a plurality of fluidization holes, air supplement row's material subassembly is fixed in the fluidization chamber just is located the below of fluidizer, the reactor gas vent with fluidization chamber intercommunication, the upper portion of fluidization chamber has fluidization chamber gas vent.

The invention has the beneficial effects that: the reactor-fluid bed is mainly formed by coupling a horizontal counter-current rotary comprehensive reactor, a fluidizer and a fluidizing chamber. The comprehensive reactor is used as a material homogenizing pretreatment section, and the problems of homogenizing pretreatment, large investment, large occupied area and high cost of the fluidized bed are solved. The fluidizer and the fluidizing chamber are used as the secondary reaction stage of the comprehensive reactor, and the problems that the reaction of the flue gas or the fuel gas of the comprehensive reactor is insufficient, the VOC (volatile organic compounds) in the flue gas is high or the tar and the phenol in the fuel gas are contained are solved.

The non-homogenized material is directly fed into the comprehensive reactor from the feed inlet of the reactor, the comprehensive reactor is in a positive pressure or negative pressure state by blowing or exhausting air to the outside, pyrolysis gasification reaction is generated under positive pressure or negative pressure in the comprehensive reactor, and the crude fuel gas generated by the pyrolysis gasification is introduced into the fluidization chamber through the exhaust port of the reactor. The material in the comprehensive reactor is pyrolyzed and gasified to form powdery carbon slag, the carbon slag which has already reached the ignition temperature and has fine granularity is screened by the fluidization holes under the action of centrifugal force generated by the rotation of the fluidizer along with the rotation of the fluidizer and the comprehensive reactor, and then is thrown into the fluidizing chamber to react with oxidant or gasifying agent violently to form ascending gas flame, and the ascending gas flame is introduced or injected into coarse fuel gas with certain pressure in the fluidizing chamber, upward fluidization power is provided for the fluidizing chamber at the moment, and a certain amount of water vapor generated by drying biomass in the coarse fuel gas is added to be used as the gasifying agent, so that the air supplement amount (suspending agent and gasifying agent) can be reduced, the mixing of ineffective nitrogen into the fuel gas is reduced, and the quality, particularly the heat value of the fuel gas is obviously improved. In an oxidizing atmosphere state, namely, the oxygen in the fluidizing chamber is sufficient, the carbon and the crude fuel gas are burnt out at high temperature in the fluidizing chamber, and VOC in the flue gas discharged by the fluidizing chamber is removed; under the reducing atmosphere state, namely the fluidization chamber is in an anoxic state, the high temperature in the fluidization chamber further cracks and gasifies carbon and crude fuel gas, and tar and phenolic substances in the fuel gas discharged by the fluidization chamber are removed. Wherein, the substances which can not be pyrolyzed in the comprehensive reactor can be discharged from the slag discharge device periodically and discharged out of the fluidization chamber through the air supplementing and discharging component. When the oxidant or gasifying agent such as oxygen, water vapor and the like in the crude fuel gas is insufficient, the air supplementing and discharging component supplements air and/or water vapor to the fluidizing chamber.

The fluidized bed of the invention has the following advantages:

1. the fluidized bed does not need to carry out homogenization pretreatment on biomass materials, and has strong fuel adaptability and low production cost.

2. The VOC content in the flue gas discharged by the biomass boiler and the hot blast stove adopting the fluidized bed is extremely low, and the flue gas purification cost is reduced.

3. The fuel gas produced by the biomass gasification furnace adopting the fluidized bed of the device does not contain tar and phenolic harmful substances, thereby greatly simplifying the fuel gas purification process and reducing the cost.

4. The heat utilization rate of the fluidized bed furnace is high, so that the biomass energy conversion rate is high.

5. The integration level of the fluidized bed furnace is high, complex homogenization treatment equipment is not needed, pipeline connection of multiple devices or material transportation among the multiple devices is not needed, the occupied area is small, and the investment is low.

6. The reaction fluidizing components are at least one group, and the biomass treatment capacity can be increased and the treatment scale can be enlarged by increasing the number of the reaction fluidizing components.

On the basis of the technical scheme, the invention can be further improved as follows.

Furthermore, the side wall of the comprehensive reactor is provided with a reactor insulating layer, and the reactor exhaust port is communicated with the air supplementing and discharging assembly or the side wall of the lower part of the fluidization chamber.

The beneficial effect of adopting the further scheme is that: when the exhaust port of the reactor is communicated to the air supplementing and discharging component, the coarse fuel gas of the comprehensive reactor enters the fluidizing chamber for air supplementing by means of the air pressure of the air supplementing and discharging component, and the coarse fuel gas realizes secondary reaction. When the exhaust port of the reactor is communicated with the side wall of the fluidizing chamber, the crude fuel gas enters the fluidizing chamber for secondary reaction.

Furthermore, the comprehensive reactor can be rotatably arranged in the fluidizing chamber, the side wall of the fluidizing chamber is provided with a fluidizing chamber insulating layer, and the reactor feed inlet is positioned outside the fluidizing chamber.

The beneficial effect of adopting the further scheme is that: the high temperature in the fluidizing chamber provides heat energy for the comprehensive reactor, and the heat energy is fully utilized.

Further, every group the reaction fluidization subassembly still includes the auger, the reactor gas vent is located the outside of fluidization chamber, and with the fluidization chamber corresponds the position department intercommunication of comprehensive reactor one end, the auger install in bottom in the fluidization chamber, and follow the one end of comprehensive reactor extends to mend wind and arrange the material subassembly.

The beneficial effect of adopting the further scheme is that: the gas outlet of the reactor is directly communicated with the fluidizing chamber, the coarse fuel gas provides heat energy for the inside of the fluidizing chamber, however, the coarse fuel gas contains particles such as dust, carbon powder and the like, the particles can be deposited at the bottom of the fluidizing chamber, and the packing auger delivers the particles accumulated at the bottom of the fluidizing chamber to the air supplementing and discharging assembly and discharges the particles. And because the temperature near the fluidizer is higher, carbon powder in the particles is conveyed to the lower part of the fluidizer and then is burnt at high temperature, and heat energy is further provided for the fluidizing chamber.

Further, every group the reaction fluidization subassembly still includes coarse fuel gas draught fan and induced air pipeline, the fluidization chamber or mend the wind and arrange the material subassembly with the reactor gas vent passes through induced air pipeline intercommunication, induced air pipeline internal fixation has the coarse fuel gas draught fan.

The beneficial effect of adopting the further scheme is that: the crude gas draught fan conveys the crude gas from the exhaust port of the reactor to the fluidization chamber through a draught pipeline for secondary oxidation or gasification reaction to remove VOC or tar and phenols; water vapor in the crude fuel gas is used as a gasifying agent to participate in the gasification reaction of carbon and tar in the fluidizing chamber; meanwhile, the comprehensive reactor is in a negative pressure state, so that negative pressure pyrolysis gasification is realized, and the capacity is improved.

Further, synthesize the reactor and include reactor barrel, reactor feed cylinder and reactor aiutage, the one end of reactor feed cylinder has the reactor feed inlet, the other end with the one end intercommunication of reactor barrel, reactor feed cylinder is fixed in the reactor aiutage, the one end of reactor aiutage has the reactor gas vent, the rotatable cover of one end of reactor barrel is in the outside of reactor aiutage other end, the other end of reactor barrel with the one end fixed connection and the intercommunication of fluidization ware.

The beneficial effect of adopting the further scheme is that: the reactor feeding barrel and the reactor exhaust barrel which are fixedly arranged realize feeding and exhausting at the same end of the integrated reactor, particularly, materials are fed into the reactor feeding barrel, space between the reactor feeding barrel and the reactor exhaust barrel is used for exhausting, the materials and gas in the reactor barrel flow reversely, heat transfer is fast, and reaction efficiency is high.

Further, the comprehensive reactor comprises a reactor cylinder body and a reactor feeding cylinder, the reactor feeding cylinder is fixedly arranged, one end of the reactor feeding cylinder is provided with the reactor feeding hole, the reactor cylinder body is positioned in the fluidization chamber, one end of the reactor cylinder body is rotatably sleeved outside the other end of the reactor feeding cylinder and is communicated with the reactor feeding cylinder, and one end side wall of the reactor cylinder body is provided with the reactor exhaust port; still include the auger, the auger install in the bottom in the fluidization chamber, and follow the one end of reactor barrel extends to mend wind and arrange the material subassembly.

The beneficial effect of adopting the further scheme is that: the material gets into the reactor barrel from reactor feed cylinder, and the thick gas that the pyrolysis gasification produced directly discharges in the fluidization chamber from the reactor gas vent on the lateral wall of reactor barrel one end, simple structure, and thick gas provides heat energy for fluidization chamber and reactor barrel.

Further, every group the reaction fluidization subassembly still includes high temperature malleation air-blower, the air inlet of high temperature malleation air-blower with fluidization chamber intercommunication, the gas outlet of high temperature malleation air-blower with the other end intercommunication of fluidizer.

The beneficial effect of adopting the further scheme is that: the high-temperature positive pressure blower introduces high-temperature hot gas of the fluidization chamber into the fluidizer, on one hand, reaction temperature and a gasifying agent of the fluidizer and the comprehensive reactor are provided, pyrolysis gasification reaction is carried out to generate crude fuel gas, on the other hand, positive pressure is formed in the comprehensive reactor communicated with the fluidizer, and the crude fuel gas is extruded to be discharged from an exhaust port of the reactor.

Further, mend wind and arrange the material subassembly and include bellows and chain row stove, the one end of chain row stove is fixed in the fluidization chamber and be located arrange sediment device below, the other end with the outdoor intercommunication of fluidization chamber, bellows are fixed in the fluidization chamber and be located a plurality of fluidization hole below, the roof of bellows is the air distribution plate.

The beneficial effect of adopting the further scheme is that: the materials which are discharged by the slag discharging device and cannot be pyrolyzed or coarse slag fall onto the chain grate furnace, the combustible materials are further combusted in the chain grate furnace to provide heat for the fluidizing chamber, the air box blows upwards, jet flow is formed through the small air holes in the air distribution plate, and partial power is provided for fluidization in the fluidizing chamber.

Further, the air supplementing and discharging assembly further comprises a steam pipeline, and the steam pipeline is communicated with the air box.

The beneficial effect of adopting the further scheme is that: the steam pipeline is used for supplementing steam into the fluidizing chamber. When the water content of the materials in the comprehensive reactor is low, a steam pipeline can be opened and steam is supplemented into the fluidizing chamber, and the steam, the air and the crude fuel gas are jointly used as fluidizing agents, so that the fluidizing reaction in the fluidizing chamber is facilitated. Meanwhile, steam in the fluidizing chamber is blown in by a high-temperature positive pressure blower or pumped into the comprehensive reactor by a crude gas draught fan, and the steam is favorable for pyrolysis gasification reaction in the comprehensive reactor.

The fluidized bed further comprises a cyclone separator, wherein the air outlet of the fluidizing chamber is communicated with the air inlet of the cyclone separator, and the solid outlet of the cyclone separator is communicated with the lower part of the fluidizing chamber.

The beneficial effect of adopting the further scheme is that: the cyclone separator separates large-particle carbon ash in flue gas or fuel gas at the exhaust port of the fluidization chamber, and the carbon ash flows back into the fluidization chamber for reaction again, so that the carbon conversion rate is improved.

The invention also provides a biomass reaction furnace which comprises the reactor flow bed. A biomass reactor refers to a device comprising the reactor flow bed of the present invention, and also equipped with other necessary processing equipment.

Further, the biomass reaction furnace is a boiler, a gasification furnace or a hot blast stove.

Among them, boilers are generally used for producing steam; gasifiers are commonly used to produce fuel gas; hot blast stoves are commonly used for producing high temperature air, which may be used in the field of spray granulation of ceramics, for example. Of course, the biomass reactor of the present invention may also include other devices that contain a reactor flow bed.

Drawings

FIG. 1 is a block diagram of a first embodiment of a fluid bed of the present invention;

FIG. 2 is a view from the B-B direction of the fluidizer of FIG. 1;

FIG. 3 is a block diagram of a second embodiment of the fluid bed of the present invention;

FIG. 4 is a block diagram of a third embodiment of the fluid bed of the present invention;

FIG. 5 is a boiler using an embodiment of the present invention with a fluidized bed;

FIG. 6 is a boiler using an embodiment two fluid bed according to the present invention;

FIG. 7 is a boiler using an embodiment three-fluid bed according to the present invention;

FIG. 8 is a gasification furnace of the present invention using a fluidized bed of the second embodiment;

FIG. 9 is a schematic view of the arrangement of at least two sets of reaction fluidization assemblies.

In the drawings, the components represented by the respective reference numerals are listed below:

1. a comprehensive reactor; 101. a reactor feed inlet; 102. a reactor vent; 103. a reactor insulation layer; 2. a fluidizer; 201. a fluidization aperture; 3. a fluidizing chamber; 301. a fluidizing chamber exhaust port; 302. a fluidization chamber insulating layer; 4. a slag discharge device; 401. a slag discharge door; 5. a packing auger; 6. a crude gas induced draft fan; 7. a reactor feed cylinder; 8. a reactor exhaust funnel; 9. a high temperature positive pressure blower; 10. an air box; 1001. a wind distribution plate; 11. a chain grate furnace; 12. a cyclone separator; 13. an air inducing duct; 14. pushing the material barrel; 15. a hydraulic station; 16. a bellows blower; 17. a material returning device; 18. a drive motor; 19. a superheater; 20. a coal economizer; 21. an air preheater; 22. a dust remover; 23. a chimney; 24. a spray tower; 25. an air storage tank.

Detailed Description

The principles and features of this invention are described below in conjunction with examples which are set forth to illustrate, but are not to be construed to limit the scope of the invention.

As shown in fig. 1-4, the invention provides a fluidized bed, comprising at least one group of reaction fluidizing components, a fluidizing chamber 3 and an air supplement discharge component, wherein each group of reaction fluidizing components comprises an integrated reactor 1 and a fluidizer 2, one end of the integrated reactor 1 is provided with a reactor feed inlet 101 and a reactor discharge outlet 102, the other end of the integrated reactor 1 is fixedly connected and communicated with one end of the fluidizer 2, the axis of the fluidizer 2 is horizontally arranged and rotatably arranged in the fluidizing chamber 3, one end side wall of the fluidizer 2 is provided with a slag discharge device 4, the other end side wall of the fluidizer 2 is provided with a plurality of fluidizing holes 201, the air supplement discharge component is fixed in the fluidizing chamber 3 and positioned below the fluidizer 2, and the reactor discharge outlet 102 is communicated with the fluidizing chamber 3, the upper part of the fluidizing chamber 3 has a fluidizing chamber exhaust 301.

The reactor-flow bed is mainly formed by coupling a horizontal counter-current rotary comprehensive reactor 1, a fluidizer 2 and a fluidizing chamber 3. The comprehensive reactor 1 is used as a material homogenizing pretreatment section, and the problems of homogenizing pretreatment, large investment, large occupied area and high cost of a fluidized bed are solved. The fluidizer 2 and the fluidizing chamber are used as the secondary reaction stage of the comprehensive reactor 1, and the problems that the reaction of the flue gas or the fuel gas of the comprehensive reactor 1 is insufficient, the VOC (volatile organic compounds) content of the flue gas is high or the tar and the phenol content of the fuel gas are solved.

The materials which are not homogenized and pretreated are directly put into the comprehensive reactor 1 from the reactor feeding hole 101, the comprehensive reactor 1 is in a positive pressure or negative pressure state by blowing air or exhausting air to the outside, pyrolysis gasification reaction is carried out under the positive pressure or negative pressure in the comprehensive reactor 1, the crude fuel gas generated by the pyrolysis gasification is led into the fluidizing chamber 3 by the reactor exhaust port 102, and meanwhile, the high-temperature gas in the fluidizing chamber 3 enters the comprehensive reactor 1 from the fluidizing hole 201. The material in the comprehensive reactor 1 is pyrolyzed and gasified to form powdery carbon slag, the powdery carbon slag which reaches the ignition temperature and has fine granularity is screened by the fluidization holes 201 under the action of centrifugal force generated by the rotation of the fluidizer 2 and the comprehensive reactor 1, and then is thrown into the fluidization chamber 3 to react with oxidant or gasifying agent violently to form gas-lifting flame, and the gas-lifting flame is introduced or injected into the coarse fuel gas with certain pressure in the fluidization chamber 3, upward fluidization power is provided for the fluidization chamber 3 at this time, and a certain amount of water vapor generated by drying biomass in the coarse fuel gas is added as the gasifying agent, so that the air supplement amount (suspending agent and gasifying agent) can be reduced, the mixing of ineffective nitrogen gas is reduced, and the quality of the fuel gas, particularly the heat value, is obviously improved. In an oxidizing atmosphere state, namely, sufficient oxygen exists in the fluidizing chamber 3, carbon and crude fuel gas are burnt out at high temperature in the fluidizing chamber 3, and VOC in flue gas discharged from the fluidizing chamber 3 is removed; under the reducing atmosphere state, namely the fluidization chamber 3 is in an oxygen-deficient state, the high temperature in the fluidization chamber 3 further cracks and gasifies carbon and crude fuel gas, and tar and phenolic substances in the fuel gas discharged by the fluidization chamber 3 are removed. Wherein, the substances which can not be pyrolyzed in the integrated reactor 1 can be discharged from the slag discharge device 4 periodically and discharged out of the fluidization chamber 3 through the air supplement discharge assembly. When the oxidant or gasifying agent such as oxygen, water vapor and the like in the crude fuel gas is insufficient, the air supplementing and discharging component supplements air and/or water vapor to the fluidizing chamber 3.

The fluidized bed of the invention has the following advantages:

1. the fluidized bed does not need to carry out homogenization pretreatment on biomass materials, and has strong fuel adaptability and low production cost.

2. The VOC content in the flue gas discharged by the biomass boiler and the hot blast stove adopting the fluidized bed is extremely low, and the flue gas purification cost is reduced.

3. The fuel gas produced by the biomass gasification furnace adopting the fluidized bed of the device does not contain tar and phenolic harmful substances, and the cost of the fuel gas purification process is greatly simplified.

4. The heat utilization rate of the fluidized bed furnace is high, so that the biomass energy conversion rate is high.

5. The integration level of the fluidized bed furnace is high, complex homogenization treatment equipment is not needed, pipeline connection of multiple devices or material transportation among the multiple devices is not needed, the occupied area is small, and the investment is low.

6. The reaction fluidizing components are at least one group, and the biomass treatment capacity can be increased and the treatment scale can be enlarged by increasing the number of the reaction fluidizing components.

The plurality of fluidizing holes 201 on the other end side wall of the fluidizer 2 are preferably uniformly distributed by the plurality of fluidizing holes 201, but may be non-uniformly distributed by the plurality of fluidizing holes 201.

Wherein, the other end of the integrated reactor 1 is open and fixedly connected and communicated with one end of the fluidizer 2 by welding or flange connection, and the axes of the integrated reactor 1 and the fluidizer 2 are horizontally arranged. The integrated reactor 1 is internally fixed with a plurality of guide plates and lifting blades for pushing materials from one end to the other end of the integrated reactor 1 in the rotation process, and the structures and the arrangement modes of the guide plates and the lifting blades can be realized by adopting the prior art. For example, a plurality of material guide plates and material raising plates are arranged in a spiral direction on the inner wall of the integrated reactor 1.

Wherein, to the row's sediment device 4 of the one end lateral wall of fluidizer 2, specifically do, as shown in fig. 2, arrange sediment device 4 including row's sediment door 401, the one end lateral wall of fluidizer 2 has the carbon sediment discharge port, arrange sediment door 401 set up in the inboard of fluidizer 2, arrange sediment door 401 one side with the carbon sediment discharge port is followed 2 circumference of fluidizer arbitrary one side is articulated, arrange sediment door 401 rotatable to with the inner wall butt of fluidizer 2 blocks the carbon sediment discharge port, or rotatable to letting out the carbon sediment discharge port makes the inside and outside intercommunication of fluidizer 2. Optionally, the slag discharging door 401 is a plate-shaped structure without holes, or the slag discharging door 401 has a plurality of slag discharging holes.

The forward or reverse rotation of the fluidizer 2 can be controlled, so that when the slag discharge door 401 rotates to be right below the fluidizer 2 along with the fluidizer 2, a carbon slag discharge port is opened or not. When the slag discharge door 401 blocks the carbon slag discharge port, a small amount of carbon slag is discharged from the slag discharge port, and the carbon slag is combusted in the high-temperature environment of the fluidizing chamber 3 to provide heat energy for fluidization. When the slag discharge door 401 opens the carbon slag discharge port, carbon slag accumulated in the fluidizer 2 can be discharged.

In the pyrolysis state, the fluidizer 2 rotates to the positions shown as 1-1 to 1-4 in fig. 2 in sequence, the fluidizer 2 rotates along the direction from one side of the slag discharge door 401 to the other side, at the position 1-3 in fig. 2, the slag discharge door 401 abuts against the inner wall of the fluidizer 2 to close the carbon slag discharge port, carbon slag can be directly discharged through the slag discharge port on the slag discharge door 401 in the pyrolysis and fluidization processes, and is thrown in the fluidization chamber 3 under the action of centrifugal force to realize fluidization.

If a large amount of inorganic matter materials which cannot be pyrolyzed are accumulated in the fluidizer 2, the fluidizer 2 is inverted, and in the discharge state, the fluidizer 2 is sequentially rotated to positions 2-1 to 2-4 in fig. 2, and when the fluidizer 2 is rotated to a position where the carbon slag discharge port is directed downward, as shown in 2-3 in fig. 2, the slag discharge door 401 is opened, and the materials which cannot be pyrolyzed are discharged from the carbon slag discharge port. The fluidizer 2 can discharge materials without stopping, and has high production efficiency. And a large number of experiments prove that the materials cannot fall out of the fluidizer 2 at the positions 1-1, 1-2, 1-4, 2-1, 2-2 and 2-4 shown in the figure 2.

Part of the pyrolysis gas can be discharged from the slag discharge port during the rotation of the fluidizer 2 and combusted in the fluidizing chamber 3 to provide heat energy for the fluidization in the fluidizing chamber 3.

Wherein, the working principle and the beneficial effects of the comprehensive reactor 1 are as follows: when the integrated reactor 1 rotates forward, that is, sequentially rotates to the positions shown in fig. 1-1 to 1-4 of fig. 2, the fluidizer 2 rotates in a direction from one side of the slag discharge door 401 to the other side, and the integrated reactor 1 is fixedly connected to the fluidizer 2 so that the rotation directions are the same. Under the action of the material guide plate and the material raising plate in the integrated reactor 1, the materials roll to the other end of the integrated reactor 1 and move from the feeding end with lower temperature to the end of the fluidizer with higher temperature. The materials pass through in sequence: drying the materials in a section within 100-200 ℃, and evaporating water; pyrolyzing the material in a 200-400 ℃ section in an anoxic state, and volatilizing volatile matters; mainly carrying out gasification reaction in a 400-600 ℃ section, further degrading macromolecular organic matters to form solid carbon, and forming carbon slag together with the solid inorganic matters. In the process, the solid material and the carbon slag are mutually rubbed and extruded in a rolling state, so that the particle size is reduced, the reaction surface area is increased, and the pyrolysis gasification reaction is favorably carried out. Since the feeding and the exhaust are at the same end in the integrated reactor 1, as shown in fig. 1, 3 and 4, the material moves from right to left, the gas flow moves from left to right, and the material and the gas flow move in opposite directions and form a counter-current state. The gas flow is obtained by mixing high-temperature gas sucked from the fluidizing chamber 3, fuel gas generated by the pyrolysis gasification reaction of the materials and steam generated by drying the materials, and is named as crude fuel gas because the gas flow contains a large amount of steam, dust, tar and phenolic harmful substances. The comprehensive reactor 1 changes the biomass material from non-homogenized solid matter into relatively homogenized gaseous coarse fuel gas and powdered carbon slag, and has the precondition of further fluidization reaction.

In order to utilize the heat in the fluidizing chamber 3 as usual in the prior art, it is only conceivable to pass the integrated reactor 1, which requires thermal energy, through the fluidizing chamber 3. However, this arrangement is only based on the side wall of the integrated reactor 1 for heat transfer, and is of external heating type, and the heat transfer efficiency is low, and the reaction rate in the integrated reactor 1 is only related to the side wall conductivity and surface area of the integrated reactor 1, and cannot be adjusted during operation. The utilization rate of heat energy in the fluidization chamber 3 is limited, only positive pressure pyrolysis or dry distillation can be realized, the treatment capacity of solid waste is limited, and the fluidized bed can only be used for small-scale experiments and cannot reach the economic scale of industrial production. And the substances which can not be pyrolyzed can not be discharged outside, and the substances which can not be pyrolyzed need to be picked out in advance, namely the substances need to be pretreated.

The comprehensive reactor 1 of the invention takes internal heat as main part and external heat as auxiliary part. The internal heating specifically means: a crude gas draught fan 6 is adopted to pump out crude gas, so that negative pressure is formed in the comprehensive reactor 1, and heat of the fluidization chamber 3 is directly introduced into the comprehensive reactor 1 through a fluidization hole 201 and/or a slag discharge hole on a slag discharge door 401; or hot air in the fluidizing chamber 3 is blown into the fluidizer 2 and the integrated reactor 1 by a high-temperature positive pressure blower 9. The invention utilizes the airflow of the fluidization chamber 3 to directly heat the interior of the comprehensive reactor 1, fully utilizes the heat in the fluidization chamber 3, realizes the adjustable reaction rate in the comprehensive reactor 1 by controlling the flow of the fan, greatly improves the treatment capacity of solid wastes, and can lead the comprehensive reactor 1 to reach the industrial production scale. The external heating means: by virtue of the heat-retaining effect of the fluidizing chamber 3, the high temperature in the fluidizing chamber 3 is thermally conducted to the side wall of the fluidizer 2 disposed in the fluidizing chamber 3 or to both the fluidizer 2 disposed in the fluidizing chamber 3 and the integrated reactor 1.

One end of the comprehensive reactor 1 is rotatably arranged on the side wall of the fluidization chamber 3 through a bearing, the comprehensive reactor 1 and the fluidization device 2 are fixedly connected and synchronously rotate, a reactor transmission gear is fixed on the outer side of the end part of the comprehensive reactor 1, and the output end of the transmission motor 18 is in transmission connection with the reactor transmission gear and drives the comprehensive reactor 1 to rotate.

The fluidization device 2 is a horizontal rotary roller, one end of the fluidization device is open and is fixedly connected and communicated with the other end of the comprehensive reactor 1 in a sealing mode, fluidization holes 201 are uniformly distributed on the wall, close to the other end, of the roller, the aperture of each fluidization hole 201 is 1-50 mm, the aperture of each fluidization hole 201 is preferably 5-20 mm, and the wall of the open section of the roller is provided with the slag discharge device 4. The fluidizer 2 is transversely arranged at the middle lower part in the fluidizing chamber 3, the other end of the fluidizer 2 is rotatably arranged on the side wall of the fluidizing chamber 3 through a bearing, and the fluidizer 2 rotates positively and negatively along with the integrated reactor 1. Due to the high temperature at the fluidizer 2, a high temperature resistant material is preferably used for the fluidizer 2.

Wherein, the theory of operation and the beneficial effect of fluidization ware 2 lie in:

1. screening: the biomass material is degraded and ground through the physicochemical action (the physicochemical action refers to the physical change of the material thinning through rolling, extruding and grinding and the chemical change of the pyrolysis and gasification reaction) of the comprehensive reactor 1, the obtained granular carbon slag is screened, the granules smaller than the fluidization holes 201 are discharged through the fluidization holes 201, and the materials which can not pass through the fluidization holes 201 are continuously remained in the comprehensive reactor 1 for further thermal degradation and grinding until the materials can be discharged through the fluidization holes 201.

2. Deslagging: when the fluidizer 2 is reversed, coarse slag which cannot be discharged from the fluidizing holes 201 within a certain period of time can be discharged to the grate furnace 11 through the slag discharging device 4 on the side wall, and the space in the integrated reactor 1 is released. This has the advantage that the biomass fuel, which is not homogenized, is utilized in a balanced and thorough manner under the selective sifting action of the fluidizer 2.

3. Fluidization: under the action of centrifugal force generated by the rotation of the fluidizer 2, carbon powder which has already reached the ignition temperature and has fine granularity is thrown into the fluidizing chamber 3 to react with oxidant or gasifying agent violently to form ascending gas flame, and at the moment, a small amount of blast of the wind box 10 is assisted, so that the fluidizing state in the fluidizing chamber 3 can be maintained, and the initial fluidizing speed is reduced remarkably. When the fluidized bed is applied to a boiler or an incinerator, the oxygen in the fluidizing chamber 3 is sufficient, the fluidizing air quantity can be controlled, the VOC (volatile organic compound) emission of flue gas is reduced, and the investment cost and the operation cost of a flue gas treatment system are reduced; the fluidized bed is applied to a gasification furnace, and because the fluidizer 2 rotates and throws materials to realize fluidization, compared with the existing fluidized bed, the fluidizing agent (air) can be reduced, so that invalid nitrogen mixed into fuel gas is reduced, and the quality, particularly the heat value, of the fuel gas is obviously improved.

Wherein, the fluidization chamber 3 adopts heat-insulating refractory material as a wall, and a vertical empty barrel well is formed at the position of the fluidization device 2. The biomass material is subjected to a first physicochemical reaction in the integrated reactor 1 to become crude fuel gas injected through the air distribution plate 1001 of the air box 10 and carbon powder sprayed through the fluidizer 2, gaseous crude fuel gas with temperature and powdered carbon powder which reaches the ignition temperature earlier enter the high-temperature (> 850 ℃) fluidizing chamber 3, and rapidly and fully react with an oxidant (oxygen) or a gasifying agent (oxygen and steam) in a suspension fluidizing state, so that the fluidizing chamber 3 provides a secondary reaction space for the biomass material in a high-temperature state, and the biomass material is thoroughly degraded. When the fluidized bed is applied to a boiler or an incinerator, the fluidizing chamber 3 serves as a secondary combustion chamber to fully burn off combustible substances in the flue gas, and the VOC (volatile organic compounds) of the flue gas is extremely low; when the fluidized bed is applied to a gasification furnace, the fluidizing chamber 3 is used as a high-temperature decoking chamber and is fully degraded to change macromolecular organic matters in flue gas into micromolecular organic matters with carbon number less than five, liquid substances (tar) are not generated in the flue gas at normal temperature, and tar and phenolic harmful substances are not contained in the fuel gas.

Wherein, the reactor exhaust port 102 is communicated with the fluidization chamber 3, which may be specifically: 1. the reactor exhaust port 102 is positioned outside the fluidizing chamber 3 and is communicated with the air supplementing and discharging assembly through an air guide pipeline 13; 2. the reactor outlet 102 is located outside the fluidizing chamber 3 and the reactor outlet 102 communicates with the side wall of the fluidizing chamber 3 through an air draft duct 13; 3. the reactor cylinder of the integrated reactor 1 is located in the fluidizing chamber 3, the side wall of the reactor cylinder is provided with a reactor exhaust port 102, and the reactor cylinder is directly communicated with the inner cavity of the fluidizing chamber 3 through the reactor exhaust port 102.

Wherein, when there are at least two groups of reaction fluidizing components, as shown in fig. 9, the reaction fluidizing components of at least two groups are arranged laterally at intervals. The at least two groups of reaction fluidizing components are preferably arranged on the same horizontal plane, but may be offset from each other, and in order to ensure the fluidizing effect, the fluidizer 2 of each group of reaction fluidizing components is preferably arranged at the lower part of the fluidizing chamber 3. The integrated reactors 1 of the at least two sets of reactive fluidization assemblies are both directed towards the same side of the fluidization chamber 3, for example as shown in fig. 9, with both integrated reactors 1 directed towards the right side of the fluidization chamber 3; alternatively, the integrated reactor 1 of at least one set of reaction fluidizing components faces one side of the fluidizing chamber 3, and the integrated reactors 1 of at least one other set of reaction fluidizing components faces the other side of the fluidizing chamber 3, for example, when the reaction fluidizing components are two sets, one integrated reactor 1 faces the right side of the fluidizing chamber 3, and the other one faces the left side of the fluidizing chamber 3. As shown in fig. 9, the air supplement discharge assembly is one and is positioned below all the fluidizers 2; or the air supplementing and discharging assemblies and the reaction fluidizing assemblies are the same in number and are correspondingly arranged below the corresponding fluidizers 2.

On the basis of the above scheme, as shown in fig. 1, one of the installation modes of the integrated reactor 1 is as follows: the side wall of the integrated reactor 1 is provided with a reactor insulating layer 103, and the reactor exhaust port 102 is communicated with the air supplementing and discharging assembly or the side wall of the lower part of the fluidization chamber 3.

Specifically, as shown in FIG. 1, the integrated reactor 1 is installed outside the fluidizing chamber 3 and has a reactor insulation layer 103.

Specifically, the reactor exhaust port 102 is communicated with the air box 10 of the air supplementing and discharging assembly through an air guide pipeline 13, the coarse fuel gas enters the fluidizing chamber 3 through air pressure of the air supplementing and discharging assembly by means of jet flow, and the secondary reaction is realized by the coarse fuel gas. When the reactor exhaust port 102 of the integrated reactor 1 is communicated with the side wall of the fluidizing chamber, the crude fuel gas directly enters the fluidizing chamber for secondary reaction.

Preferably, the air-guiding duct 13 is provided with a duct insulation layer, so as to ensure that the crude fuel gas having a certain temperature and pressure is fed into the air box 10 through this duct.

On the basis of the above scheme, optionally, a fluidizer guide plate spirally mounted along the inner wall is fixed on the inner wall of the fluidizer 2. When the integrated reactor 1 and the fluidizer 2 are synchronously and positively conveyed, the material flows from one end of the fluidizer 2 to the other end under the action of the material guide plate of the fluidizer. When the comprehensive reactor 1 and the fluidizer 2 are synchronously conveyed reversely, the material flows from the other end of the fluidizer 2 to one end thereof under the action of the material guide plate of the fluidizer, so that the material which cannot be pyrolyzed or discharged from the fluidizing holes 201 can be discharged from the slag discharging device 4 positioned on the side wall of one end of the fluidizer 2.

On the basis of the above scheme, as shown in fig. 3 and 4, another installation mode of the integrated reactor 1 is as follows: the integrated reactor 1 is rotatably arranged in the fluidizing chamber 3, the side wall of the fluidizing chamber 3 is provided with a fluidizing chamber insulating layer 302, and the reactor feed inlet 101 is positioned outside the fluidizing chamber 3.

The high temperature in the fluidizing chamber 3 provides heat energy for the integrated reactor 1, making full use of the heat.

Specifically, the fluidizing chamber 3 includes a vertical section and a horizontal section which are communicated with each other, as shown in fig. 3 and 4, the fluidizing chamber 3 is L-shaped, the integrated reactor 1 is disposed in the horizontal section, and the fluidizer 2 is disposed at the lower portion of the vertical section. When the number of the reaction fluidization components is at least two, the number of the horizontal sections is one, and all the integrated reactors 1 are positioned in one horizontal section; or the number of horizontal segments and reaction fluidization components is the same, and the integrated reactor 1 is positioned in the corresponding horizontal segment.

As shown in fig. 3 and 4, the reactor exhaust port 102 is communicated with the fluidizing chamber 3 at a position corresponding to one end of the integrated reactor 1 through an induced draft duct 13, preferably, the induced draft duct 13 has a duct insulating layer; or the reactor exhaust port 102 is communicated with the wind box 10 of the air supplementing discharge assembly through the induced draft pipeline 13.

On the basis of another kind of mounting means of synthesizing reactor 1, every group the reaction fluidization subassembly still includes auger 5, reactor gas vent 102 is located the outside of fluidization chamber 3, and with fluidization chamber 3 corresponds the position department intercommunication of synthesizing reactor 1 one end, auger 5 install in bottom in the fluidization chamber 3, and follow one end of synthesizing reactor 1 extends to the material subassembly is arranged in the tonifying wind.

Auger 5 install in bottom in the fluidization chamber 3, and follow one end of synthesizing reactor 1 extends to the material subassembly is arranged in the tonifying wind, specifically is: the packing auger 5 is positioned at the bottom of the horizontal section of the L-shaped fluidization chamber 3, the feeding end of the packing auger 5 is correspondingly arranged below one end of the comprehensive reactor 1, and the discharging end of the packing auger 5 is positioned above the air supplementing and discharging assembly. In one specific embodiment, the discharge end of the auger 5 is arranged above the chain grate 11 in the air supplementing and discharging assembly.

The gas outlet 102 of the reactor is directly communicated with the fluidizing chamber 3, the coarse fuel gas provides heat energy for the interior of the fluidizing chamber 3, however, the coarse fuel gas contains particles such as dust, carbon powder and the like, the particles can be deposited at the bottom of the fluidizing chamber 3, and the packing auger 5 sends the particles accumulated at the bottom of the fluidizing chamber 3 to the air supplementing and discharging assembly and discharges the particles. And because the temperature near the fluidizer 2 is higher, carbon powder in the particles is conveyed to the lower part of the fluidizer 2 and then is burnt at high temperature, and heat energy is further provided for the fluidizing chamber 3.

On the basis of any scheme, as shown in fig. 1 and 3, each group of reaction fluidization components further comprises a crude gas induced draft fan 6 and an induced draft pipeline 13, the fluidization chamber 3 or the air supplementing discharge component is communicated with the reactor exhaust port 102 through the induced draft pipeline 13, and the crude gas induced draft fan 6 is fixed in the induced draft pipeline 13.

The fluidization chamber 3 or the air supplementing discharge assembly is communicated with the reactor exhaust port 102 through an air guide pipeline 13, specifically: the fluidization chamber 3 is in communication with the reactor outlet 102 via an air-inducing duct 13; alternatively, the wind box 10 in the air supplement discharge assembly is communicated with the reactor exhaust port 102 through an induced draft pipeline 13.

The crude gas draught fan 6 pumps the material drying and pyrolysis gasification mixed gas (i.e. crude gas) from the exhaust port 102 of the reactor to the fluidization chamber 3 through the air draft pipeline, so as to carry out secondary oxidation or gasification reaction, remove VOC or tar and phenols, and make the air pressure in the inner cavity of the comprehensive reactor 1 slightly lower than the air pressure in the fluidization chamber 3, the high-temperature gas in the fluidization chamber 3 enters the inner cavity of the comprehensive reactor 1 from the fluidization hole 201 and flows to the feed end, and the temperature is continuously reduced under the heat absorption action of the material which is continuously reversed, so that the stable high-low temperature difference is formed from the other end to one end (feed end) in the inner cavity of the comprehensive reactor 1, and heat energy is provided for a series of comprehensive reactions of the material in the comprehensive reactor 1. Meanwhile, the crude gas is sent into the induced draft pipeline 13 and provides conveying power, the crude gas with the temperature contains a certain amount of air and water vapor, and the crude gas enters the fluidizing chamber 3 to serve as a gasifying agent to participate in the gasification reaction of carbon and tar in the fluidizing chamber, so that the cost for producing the water vapor is saved, and the heat loss of the fluidizing chamber 3 is reduced.

In the prior art, because the comprehensive reactor 1 is in a horizontal rotating state, corresponding structural design is lacked, negative pressure is difficult to realize in the comprehensive reactor 1, and the heat value of fuel gas is generally considered to be reduced by negative pressure pyrolysis. However, compare in traditional scheme that relies on the interior malleation of comprehensive reactor 1 to discharge pyrolysis gas, comprehensive reactor 1 in this scheme adopts negative pressure pyrolysis gasification technology for the handling capacity increases, and the pyrolysis gas that produces in the unit interval increases, and heat supply capacity is greater than the malleation pyrolysis far away on the contrary.

On the basis of the above scheme, as shown in fig. 1 and fig. 3, one of the feed exhausts of the integrated reactor 1 has the structure: synthesize reactor 1 and include reactor barrel, reactor feed cylinder 7 and reactor aiutage 8, the one end of reactor feed cylinder 7 has reactor feed inlet 101, the other end with the one end intercommunication of reactor barrel, reactor feed cylinder 7 is fixed in the reactor aiutage 8, the one end of reactor aiutage 8 has reactor air vent 102, the rotatable cover of one end of reactor barrel is in the outside of the 8 other ends of reactor aiutage, the other end of reactor barrel with the one end fixed connection and the intercommunication of fluidizer 2.

Wherein, the reactor feed cylinder 7 and the reactor exhaust cylinder 8 can be coaxially arranged or eccentrically arranged.

Specifically, pyrolysis gas at the exhaust port 102 of the reactor is extracted through the crude gas draught fan 6, the double cylinders of the reactor feed cylinder 7 and the reactor exhaust cylinder 8 are sleeved, the reactor feed cylinder 7 is fed inside, pyrolysis gas is discharged from an interlayer between the reactor feed cylinder 7 and the reactor exhaust cylinder 8, negative pressure is formed in the reactor cylinder, and pyrolysis gasification is achieved. Compared with the positive pressure pyrolysis, the method greatly improves the material heat conversion capacity of unit integrated reactor 1 volume, and can provide enough high temperature and enough heat for fluidization.

The reactor feeding device is characterized in that the reactor feeding hole 101 is formed in the upper wall of one end of the reactor feeding cylinder 7, a funnel-shaped feeding hopper is fixed on the reactor feeding hole 101, a material pushing cylinder 14 is arranged on the inner side of the end portion of one end of the reactor feeding cylinder 7 in a sliding mode, the material pushing cylinder 14 is driven by a hydraulic oil cylinder and moves in the reactor feeding cylinder 7 in a reciprocating mode, and the hydraulic station 15 supplies oil to the hydraulic oil cylinder.

The raw biomass material which is not subjected to homogenization pretreatment is input into a feed hopper through a grab bucket, a forklift, a conveyor belt and the like, the material falls into a reactor feed inlet 101 through the feed hopper, the material is pushed to one end of a reactor barrel along a reactor feed cylinder 7 through a material pushing cylinder 14, one end of the reactor feed cylinder 7 close to the reactor barrel is always kept with a section of material plug, the reactor feed cylinder 7 is sealed by the material plug, no pyrolysis gas overflows from the reactor feed inlet 101, and the material pressed into the reactor feed cylinder 7 at the back extrudes the material plug at the front end to fall into the reactor barrel. The feeding structure of the reactor feeding barrel 7 can receive hard materials with the diameter smaller than that of the reactor feeding barrel 7 and flexible materials with any physical and chemical properties to complete feeding, and meanwhile, pyrolysis gas can be taken from a reactor exhaust port 102 at the feeding end of the reactor in a state that a reactor feeding port 101 is sealed, so that the materials and the pyrolysis gas flow reversely in the rotary comprehensive reactor 1.

On the basis of the above scheme, as shown in fig. 4, another structure of the feed exhaust of the integrated reactor 1 is: the comprehensive reactor 1 comprises a reactor cylinder body and a reactor feeding cylinder 7, the reactor feeding cylinder 7 is fixedly arranged, one end of the reactor feeding cylinder is provided with the reactor feeding hole 101, the reactor cylinder body is positioned in the fluidization chamber 3, one end of the reactor cylinder body is rotatably sleeved outside the other end of the reactor feeding cylinder 7 and is communicated with the reactor feeding cylinder 7, and one end side wall of the reactor cylinder body is provided with the reactor exhaust port 102; still include auger 5, auger 5 install in bottom in the fluidization chamber 3, and follow the one end of reactor barrel extends to the material subassembly is arranged in the tonifying wind.

The material gets into the reactor barrel from reactor feed cylinder 7, and the thick gas that the pyrolysis gasification back produced directly discharges in fluidization chamber 3 from the reactor gas vent on the lateral wall of reactor barrel one end, simple structure, and thick gas provides heat energy for fluidization chamber 3 and reactor barrel.

This scheme is the same with the feeding structure of aforementioned scheme, specifically does: the reactor feeding device is characterized in that the reactor feeding hole 101 is formed in the upper wall of one end of the reactor feeding cylinder 7, a funnel-shaped feeding hopper is fixed on the reactor feeding hole 101, a material pushing cylinder 14 is arranged on the inner side of the end portion of one end of the reactor feeding cylinder 7 in a sliding mode, the material pushing cylinder 14 is driven by a hydraulic oil cylinder and moves in the reactor feeding cylinder 7 in a reciprocating mode, and the hydraulic station 15 supplies oil to the hydraulic oil cylinder.

On the basis of any one scheme, each group of reaction fluidization components further comprise a high-temperature positive-pressure blower 9, an air inlet of the high-temperature positive-pressure blower 9 is communicated with the fluidization chamber 3, and an air outlet of the high-temperature positive-pressure blower 9 is communicated with the other end of the fluidizer 2.

The air outlet of the high-temperature positive pressure air blower 9 is communicated with the other end of the fluidizer 2 through an air outlet pipeline, and the air outlet pipeline is coaxially arranged with the fluidizer 2 and is connected with the fluidizer 2 through a bearing. The fluidizer 2 is sleeved outside the end part of the air outlet pipeline and can rotate relative to the air outlet pipeline.

The high-temperature positive pressure blower 9 introduces the high-temperature hot gas in the fluidizing chamber 3 into the fluidizing device 2, on one hand, provides the reaction temperature and the gasifying agent of the fluidizing device 2 and the comprehensive reactor 1, generates pyrolysis gasification reaction to generate crude fuel gas, on the other hand, forms positive pressure in the comprehensive reactor 1 communicated with the fluidizing device 2, extrudes the crude fuel gas, and discharges the crude fuel gas from the reactor exhaust port 102.

On the basis of any one of the above schemes, the air supplementing and discharging assembly comprises an air box 10 and a chain grate furnace 11, one end of the chain grate furnace 11 is fixed in the fluidization chamber 3 and is positioned below the slag discharging device 4, the other end of the chain grate furnace is communicated with the outside of the fluidization chamber 3, the air box 10 is fixed in the fluidization chamber 3 and is positioned below the fluidization holes 201 in a plurality, and the top wall of the air box 10 is an air distribution plate 1001.

Wherein, the air distribution plate 1001 can adopt the air distribution plate structure in the current fluidized bed to realize, has evenly distributed's wind hole on the air distribution plate 1001, makes the air current even in the fluidization chamber 3, realizes good fluidization operating mode.

Wherein, the wind box 10 is used for supplying wind, and the chain grate furnace 11 is used for discharging. Of course, the grate furnace 11 for discharging can also be used with other types of high-temperature-resistant conveying devices, such as grate bars, auger devices, etc.

The materials or coarse slag which are discharged by the slag discharging device 4 and cannot be pyrolyzed fall on the chain grate furnace 11, the chain grate furnace 11 and the air box 10 are arranged side by side and are positioned at one side of the feeding end of the fluidizer 2, and the functions of igniting carbon slag, supporting combustion and discharging coarse slag are achieved. The combustible materials are further combusted in the chain grate furnace 11 to provide heat for the fluidization chamber 3, the air box 10 blows upwards, jet flow is formed through small air holes in the air distribution plate, and partial power is provided for fluidization in the fluidization chamber 3.

Further, a wind box fan 16 is provided outside the fluidizing chamber 3, and the wind box fan 16 communicates with the wind box 10 and blows air into the wind box 10. Specifically, when the amount of an oxidizing agent or a gasifying agent such as oxygen and steam blown into the fluidizing chamber 3 through the air guide duct 13 is insufficient, the wind box fan 16 can supply air into the fluidizing chamber 3, which is advantageous for controlling the fluidizing reaction.

When the air supplement discharge assembly is one, the bellows fan 16 is one. When the number of the air supplementing and discharging assemblies is the same as that of the reaction fluidization assemblies, one air box fan 16 is respectively communicated with at least two air boxes 10, or the number of the air box fans 16 is the same as that of the air boxes 10, and the air box fans are correspondingly connected and communicated one by one.

On the basis of any scheme, the air supplementing and discharging assembly further comprises a steam pipeline, and the steam pipeline is communicated with the air box 10.

The steam line is used to feed steam into the fluidizing chamber 3. When the water content of the materials in the comprehensive reactor 1 is low, a steam pipeline can be opened and steam is supplemented into the fluidizing chamber 3, and the steam, the air and the crude fuel gas are jointly used as fluidizing agents, so that the fluidizing reaction in the fluidizing chamber 3 is facilitated. Meanwhile, steam in the fluidizing chamber 3 is blown in by a high-temperature positive pressure blower or is pumped into the comprehensive reactor 1 by a crude gas draught fan, and the steam is favorable for pyrolysis gasification reaction in the comprehensive reactor 1.

When the air supplementing and discharging assemblies are one, the steam pipelines are one. When the number of the air supplementing and discharging assemblies is the same as that of the reaction fluidization assemblies, one steam pipeline is communicated with at least two air boxes 10, or the number of the steam pipelines is the same as that of the air boxes 10, and the steam pipelines are correspondingly connected and communicated one by one.

When the fluidized bed of the present invention is used in a boiler, steam generated by the boiler may be introduced into the steam line.

On the basis of any scheme, the fluidized bed reactor further comprises a cyclone separator 12, wherein the fluidization chamber exhaust port 301 is communicated with a separator inlet of the cyclone separator 12, and a solid outlet of the cyclone separator 12 is communicated with the lower part of the fluidization chamber 3.

Further, the fluidized bed reactor also comprises a material returning device 17, wherein a solid outlet at the lower end of the cyclone separator 12 is connected with an inlet of the material returning device 17, and an outlet of the material returning device 17 is communicated with the lower part of the fluidizing chamber 3.

The cyclone separator 12 separates large particle carbon ash in flue gas or fuel gas at the air outlet 301 of the fluidization chamber, and the carbon ash flows back into the fluidization chamber 3 for reaction again, so that the carbon conversion rate is improved.

The device flow bed of the present invention includes, but is not limited to, the following three specific embodiments:

the first implementation mode comprises the following steps: as shown in figure 1, the reactor fluid bed comprises at least one group of reaction fluidizing components, a fluidizing chamber 3 and an air supplementing discharge component, each group of reaction fluidizing components comprises an integrated reactor 1 and a fluidizer 2, one end of the integrated reactor 1 has a reactor inlet 101 and a reactor outlet 102, the other end part of the integrated reactor 1 is fixedly connected and communicated with one end part of the fluidizer 2, the axis of the fluidizer 2 is horizontally arranged and can be rotatably arranged in the fluidizing chamber 3, one end side wall of the fluidizer 2 is provided with a slag discharging device 4, the other end of the side wall of the fluidizer 2 is provided with a plurality of fluidization holes 201, the air supplementing discharge assembly is fixed in the fluidization chamber 3 and is positioned below the fluidizer 2, the reactor outlet 102 communicates with the fluidizing chamber 3, and the upper part of the fluidizing chamber 3 has a fluidizing chamber outlet 301.

The side wall of the integrated reactor 1 is provided with a reactor insulating layer 103, and the reactor exhaust port 102 is communicated with the lower side wall of the air supplementing and discharging assembly or the fluidizing chamber 3.

The integrated reactor 1 is installed outside the fluidizing chamber 3 and has a reactor insulation 103.

The reactor exhaust port 102 is communicated with the wind box 10 of the air supplementing discharge assembly through an induced draft pipeline 13. The crude fuel gas of the comprehensive reactor 1 is supplied with air into the fluidizing chamber 3 through the air supply and discharge assembly. Alternatively, as shown in FIG. 1, the reactor outlet 102 communicates with the lower side wall of the fluidizing chamber 3 through an air introduction duct 13.

Each group of reaction fluidization component also comprises a crude gas induced draft fan 6, and the crude gas induced draft fan 6 is fixed in the induced draft pipeline 13.

Synthesize reactor 1 and include reactor barrel, reactor feed cylinder 7 and reactor aiutage 8, the one end of reactor feed cylinder 7 has reactor feed inlet 101, the other end with the one end intercommunication of reactor barrel, reactor feed cylinder 7 is fixed in the reactor aiutage 8, the one end of reactor aiutage 8 has reactor air vent 102, the rotatable cover of one end of reactor barrel is in the outside of the 8 other ends of reactor aiutage, the other end of reactor barrel with the one end fixed connection and the intercommunication of fluidizer 2.

The reactor feeding device is characterized in that the reactor feeding hole 101 is formed in the upper wall of one end of the reactor feeding cylinder 7, a funnel-shaped feeding hopper is fixed on the reactor feeding hole 101, a material pushing cylinder 14 is arranged on the inner side of the end portion of one end of the reactor feeding cylinder 7 in a sliding mode, the material pushing cylinder 14 is driven by a hydraulic oil cylinder and moves in the reactor feeding cylinder 7 in a reciprocating mode, and the hydraulic station 15 supplies oil to the hydraulic oil cylinder.

Make up wind and arrange material subassembly and include bellows 10 and chain row stove 11, the one end of chain row stove 11 is fixed in the fluidization chamber 3 and be located arrange sediment device 4 below, the other end with the outer intercommunication of fluidization chamber 3, bellows 10 is fixed in the fluidization chamber 3 and be located a plurality ofly fluidization hole 201 below, the roof of bellows 10 is air distribution plate 1001.

A wind box fan 16 is arranged outside the fluidization chamber 3, and the wind box fan 16 is communicated with the wind box 10 and can blow wind into the wind box 10.

The air supplementing and discharging assembly further comprises a steam pipeline, and the steam pipeline is communicated with the air box 10.

The fluidized bed reactor further comprises a cyclone separator 12, wherein the fluidization chamber exhaust port 301 is communicated with a separator inlet of the cyclone separator 12, and a solid outlet of the cyclone separator 12 is communicated with the lower part of the fluidization chamber 3.

The fluidized bed reactor further comprises a material returning device 17, a solid outlet at the lower end of the cyclone separator 12 is connected with an inlet of the material returning device 17, and an outlet of the material returning device 17 is communicated with the lower part of the fluidizing chamber 3.

The second embodiment: as shown in figure 3, the reactor fluid bed comprises at least one group of reaction fluidizing components, a fluidizing chamber 3 and an air supplementing discharge component, each group of reaction fluidizing components comprises an integrated reactor 1 and a fluidizer 2, one end of the integrated reactor 1 has a reactor inlet 101 and a reactor outlet 102, the other end part of the integrated reactor 1 is fixedly connected and communicated with one end part of the fluidizer 2, the axis of the fluidizer 2 is horizontally arranged and can be rotatably arranged in the fluidizing chamber 3, one end side wall of the fluidizer 2 is provided with a slag discharging device 4, the other end of the side wall of the fluidizer 2 is provided with a plurality of fluidization holes 201, the air supplementing discharge assembly is fixed in the fluidization chamber 3 and is positioned below the fluidizer 2, the reactor outlet 102 communicates with the fluidizing chamber 3, and the upper part of the fluidizing chamber 3 has a fluidizing chamber outlet 301.

The integrated reactor 1 is rotatably arranged in the fluidizing chamber 3, the side wall of the fluidizing chamber 3 is provided with a fluidizing chamber insulating layer 302, and the reactor feed inlet 101 is positioned outside the fluidizing chamber 3.

The fluidization chamber 3 is L-shaped, the integrated reactor 1 is arranged in the horizontal section, and the fluidization device 2 is positioned at the lower part of the vertical section. The reactor outlet 102 communicates with the fluidizing chamber 3 at the end near the integrated reactor 1 via the draught line 13.

Every group the reaction fluidization subassembly still includes auger 5, reactor gas vent 102 is located the outside of fluidization chamber 3, and with fluidization chamber 3 corresponds the position department intercommunication of 1 one end of comprehensive reactor, auger 5 install in bottom in fluidization chamber 3, and follow the one end of comprehensive reactor 1 extends to the material subassembly is arranged in the tonifying qi wind.

Every group the reaction fluidization subassembly still includes coarse fuel gas draught fan 6 and induced air pipeline 13, reactor gas vent 102 with fluidization chamber 3 passes through induced air pipeline 13 intercommunication, induced air pipeline 13 internal fixation has coarse fuel gas draught fan 6.

Synthesize reactor 1 and include reactor barrel, reactor feed cylinder 7 and reactor aiutage 8, the one end of reactor feed cylinder 7 has reactor feed inlet 101, the other end with the one end intercommunication of reactor barrel, reactor feed cylinder 7 is fixed in the reactor aiutage 8, the one end of reactor aiutage 8 has reactor air vent 102, the rotatable cover of one end of reactor barrel is in the outside of the 8 other ends of reactor aiutage, the other end of reactor barrel with the one end fixed connection and the intercommunication of fluidizer 2.

The reactor feeding device is characterized in that the reactor feeding hole 101 is formed in the upper wall of one end of the reactor feeding cylinder 7, a funnel-shaped feeding hopper is fixed on the reactor feeding hole 101, a material pushing cylinder 14 is arranged on the inner side of the end portion of one end of the reactor feeding cylinder 7 in a sliding mode, the material pushing cylinder 14 is driven by a hydraulic oil cylinder and moves in the reactor feeding cylinder 7 in a reciprocating mode, and the hydraulic station 15 supplies oil to the hydraulic oil cylinder.

Make up wind and arrange material subassembly and include bellows 10 and chain row stove 11, the one end of chain row stove 11 is fixed in the fluidization chamber 3 and be located arrange sediment device 4 below, the other end with the outer intercommunication of fluidization chamber 3, bellows 10 is fixed in the fluidization chamber 3 and be located a plurality ofly fluidization hole 201 below, the roof of bellows 10 is air distribution plate 1001.

A wind box fan 16 is arranged outside the fluidization chamber 3, and the wind box fan 16 is communicated with the wind box 10 and can blow wind into the wind box 10. Specifically, when the amount of an oxidizing agent or a gasifying agent such as oxygen and steam blown into the fluidizing chamber 3 through the air guide duct 13 is insufficient, the wind box fan 16 can supply air into the fluidizing chamber 3, which is advantageous for controlling the fluidizing reaction.

The air supplementing and discharging assembly further comprises a steam pipeline, and the steam pipeline is communicated with the air box 10.

The fluidized bed reactor further comprises a cyclone separator 12, wherein the fluidization chamber exhaust port 301 is communicated with a separator inlet of the cyclone separator 12, and a solid outlet of the cyclone separator 12 is communicated with the lower part of the fluidization chamber 3.

The fluidized bed reactor further comprises a material returning device 17, a solid outlet at the lower end of the cyclone separator 12 is connected with an inlet of the material returning device 17, and an outlet of the material returning device 17 is communicated with the lower part of the fluidizing chamber 3.

The third embodiment is as follows: as shown in figure 4, the reactor fluid bed comprises at least one group of reaction fluidizing components, a fluidizing chamber 3 and an air supplementing discharge component, each group of reaction fluidizing components comprises an integrated reactor 1 and a fluidizer 2, one end of the integrated reactor 1 has a reactor inlet 101 and a reactor outlet 102, the other end part of the integrated reactor 1 is fixedly connected and communicated with one end part of the fluidizer 2, the axis of the fluidizer 2 is horizontally arranged and can be rotatably arranged in the fluidizing chamber 3, one end side wall of the fluidizer 2 is provided with a slag discharging device 4, the other end of the side wall of the fluidizer 2 is provided with a plurality of fluidization holes 201, the air supplementing discharge assembly is fixed in the fluidization chamber 3 and is positioned below the fluidizer 2, the reactor outlet 102 communicates with the fluidizing chamber 3, and the upper part of the fluidizing chamber 3 has a fluidizing chamber outlet 301.

The integrated reactor 1 is rotatably arranged in the fluidizing chamber 3, the side wall of the fluidizing chamber 3 is provided with a fluidizing chamber insulating layer 302, and the reactor feed inlet 101 is positioned outside the fluidizing chamber 3.

The fluidization chamber 3 is L-shaped, the integrated reactor 1 is arranged in the horizontal section, and the fluidization device 2 is positioned at the lower part of the vertical section.

Every group the reaction fluidization subassembly still includes auger 5, reactor gas vent 102 is located the outside of fluidization chamber 3, and with fluidization chamber 3 corresponds the position department intercommunication of 1 one end of comprehensive reactor, auger 5 install in bottom in fluidization chamber 3, and follow the one end of comprehensive reactor 1 extends to the material subassembly is arranged in the tonifying qi wind.

The comprehensive reactor 1 comprises a reactor cylinder body and a reactor feeding cylinder 7, the reactor feeding cylinder 7 is fixedly arranged, one end of the reactor feeding cylinder is provided with the reactor feeding hole 101, the reactor cylinder body is positioned in the fluidization chamber 3, one end of the reactor cylinder body is rotatably sleeved outside the other end of the reactor feeding cylinder 7 and is communicated with the reactor feeding cylinder 7, and one end side wall of the reactor cylinder body is provided with the reactor exhaust port 102; still include auger 5, auger 5 install in bottom in the fluidization chamber 3, and follow the one end of reactor barrel extends to the material subassembly is arranged in the tonifying wind.

The reactor feeding device is characterized in that the reactor feeding hole 101 is formed in the upper wall of one end of the reactor feeding cylinder 7, a funnel-shaped feeding hopper is fixed on the reactor feeding hole 101, a material pushing cylinder 14 is arranged on the inner side of the end portion of one end of the reactor feeding cylinder 7 in a sliding mode, the material pushing cylinder 14 is driven by a hydraulic oil cylinder and moves in the reactor feeding cylinder 7 in a reciprocating mode, and the hydraulic station 15 supplies oil to the hydraulic oil cylinder.

Every group the reaction fluidization subassembly still includes high temperature malleation air-blower 9, high temperature malleation air-blower 9 the air inlet with fluidization chamber 3 intercommunication, high temperature malleation air-blower 9 the gas outlet with the other end intercommunication of fluidizer 2.

Make up wind and arrange material subassembly and include bellows 10 and chain row stove 11, the one end of chain row stove 11 is fixed in the fluidization chamber 3 and be located arrange sediment device 4 below, the other end with the outer intercommunication of fluidization chamber 3, bellows 10 is fixed in the fluidization chamber 3 and be located a plurality ofly fluidization hole 201 below, the roof of bellows 10 is air distribution plate 1001.

A wind box fan 16 is arranged outside the fluidization chamber 3, and the wind box fan 16 is communicated with the wind box 10 and can blow wind into the wind box 10. Specifically, when the amount of an oxidizing agent or a gasifying agent such as oxygen and steam blown into the fluidizing chamber 3 through the air guide duct 13 is insufficient, the wind box fan 16 can supply air into the fluidizing chamber 3, which is advantageous for controlling the fluidizing reaction.

The air supplementing and discharging assembly further comprises a steam pipeline, and the steam pipeline is communicated with the air box 10.

The fluidized bed reactor further comprises a cyclone separator 12, wherein the fluidization chamber exhaust port 301 is communicated with a separator inlet of the cyclone separator 12, and a solid outlet of the cyclone separator 12 is communicated with the lower part of the fluidization chamber 3.

The fluidized bed reactor further comprises a material returning device 17, a solid outlet at the lower end of the cyclone separator 12 is connected with an inlet of the material returning device 17, and an outlet of the material returning device 17 is communicated with the lower part of the fluidizing chamber 3.

The invention also provides a biomass reaction furnace which comprises the reactor flow bed.

A biomass reactor refers to a device comprising the reactor flow bed of the present invention, and also equipped with other necessary processing equipment.

Further, the biomass reaction furnace is a boiler, a gasification furnace or a hot blast stove.

Among them, boilers are generally used for producing steam; gasifiers are commonly used to produce fuel gas; hot blast stoves are commonly used for producing high temperature air, which may be used in the field of spray granulation of ceramics, for example. Of course, the biomass reactor of the present invention may also include other devices that contain a reactor flow bed.

Specifically, as shown in fig. 5-7, the boiler of the present invention includes the fluidized bed.

The boiler also comprises a superheater 19, an economizer 20, an air preheater 21, a dust remover 22 and a chimney 23, wherein a flue gas outlet of the cyclone separator 12 in the fluidized bed is communicated with a boiler flue, and the superheater 19, the economizer 20 and the air preheater 21 are sequentially arranged in the boiler flue along the flue gas flowing direction. The exhaust port of the boiler flue is communicated with the inlet of a dust remover 22, and the flue gas is dedusted by the dust remover. The outlet of the dust remover is communicated to a chimney 23 through a boiler fan, and the flue gas is discharged from the chimney 23.

The boiler of the present invention may employ any of the above-described forms of fluidized beds, and as shown in fig. 5 to 7, three specific embodiments are shown, each of which is a boiler employing three fluidized beds according to the first to third embodiments.

Specifically, as shown in fig. 8, the gasification furnace of the present invention includes the fluidized bed.

The gasification furnace further comprises a superheater 19, an economizer 20, an air preheater 21, a dust remover 22, a spray tower 24 and an air storage tank 25. The flue gas outlet of the cyclone separator 12 in the fluidized bed is communicated with a gasification furnace flue, an air preheater 21, a superheater 19 and an economizer 20 are sequentially arranged in the gasification furnace flue along the flue gas flowing direction, the exhaust port of the gasification furnace flue is communicated with the inlet of a dust remover 22, and flue gas is dedusted by the dust remover 22. After the flue gas at the outlet of the dust remover 22 is desulfurized and dedusted by the spray tower 24, the clean flue gas is conveyed to the gas storage tank 25 by the gasifier fan for storage. The flue gas of the gas storage tank 25 contains combustible gas and can be used for combustion in a generator set to generate heat.

The gasification furnace of the present invention may employ any of the above-described forms of the entrained flow bed, and as shown in fig. 8, a specific embodiment is a gasification furnace employing the second embodiment of the entrained flow bed.

In the description of the present invention, it should be noted that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc., indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention.

Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.

In the present invention, unless otherwise expressly stated or limited, the first feature "on" or "under" the second feature may be directly contacting the first and second features or indirectly contacting the first and second features through an intermediate. Also, a first feature "on," "over," and "above" a second feature may be directly or diagonally above the second feature, or may simply indicate that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature may be directly under or obliquely under the first feature, or may simply mean that the first feature is at a lesser elevation than the second feature.

In the description herein, references to the description of the term "one embodiment," "some embodiments," "an example," "a specific example," or "some examples," etc., mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.

In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.

The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.