CN207987121U - A kind of biomass gasification device - Google Patents

A kind of biomass gasification device Download PDF

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Publication number
CN207987121U
CN207987121U CN201721395300.XU CN201721395300U CN207987121U CN 207987121 U CN207987121 U CN 207987121U CN 201721395300 U CN201721395300 U CN 201721395300U CN 207987121 U CN207987121 U CN 207987121U
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China
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heat carrier
gasification
import
area
connect
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CN201721395300.XU
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卢艺
盖希坤
杨瑞芹
邸婧
吕成学
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Zhejiang Lover Health Science and Technology Development Co Ltd
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Zhejiang Lover Health Science and Technology Development Co Ltd
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Abstract

The utility model is related to a kind of biomass gasification devices, including gasification reactor, semicoke and heat carrier separator, fluid bed heat carrier heating device, heat carrier classification piece-rate system and the first synthesis gas collector.Biomass gasification process is divided into pyrolytic gasification and char Gasification Liang Ge workshop sections by the device, and pyrolytic gasification process uses " W " type gasification reactor, has the remarkable advantage that equipment volume is small, the reaction was complete, tar is free of in synthesis gas.

Description

A kind of biomass gasification device
Technical field
The utility model belongs to Biomass Energy Utilization field, and in particular to a kind of biomass gasification device.
Background technology
Energy problem has important strategic importance in world economy.The fossil fuels such as coal, oil and natural gas It is used for a long time, causes serious environmental pollution and greenhouse effects.In addition, fossil fuel is non-renewable energy resources, in the long term Liquid fuel shortage will be the big problem for perplexing human development.
Biomass liquefying technology includes indirect reformer method and direct liquefaction method, compares Direct liquefaction technology, and biomass is indirect Liquefaction technology has two big advantages:First, the liquid fuel of production is entirely free of sulphur, any standard requirement can be met;Second is that can be with It is needed according to national strategy and the market demand flexibly carries out Chemical Manufacture, such as methanol-fueled CLC, F- T synthesis.Therefore, biomass Indirect liquefaction technology is following most one of development potentiality technology, and wherein gasification technology is basis and the key of indirect liquefaction.
Gasification of biomass by whether using gasifying agent can be divided into using gasifying agent and do not use two kinds of gasifying agent.Use gasification Agent gasification can be divided into air gasification, oxygen gasified, steam gasification, carbon dioxide gasification and mixing gasifying etc..The study found that making It is a chemical reaction system for complicated multicomponent polymorphic type, including oxidation reaction, reduction with the gasification reaction process of gasifying agent Reaction and the cracking etc. of solid matter.Since gasification reaction is generally an endothermic reaction, it is necessary to provide enough heat ability It maintains reaction to carry out, therefore, gasifying agent is selected to generally comprise air or oxygen.Make gasifying agent using air, due in air Containing a large amount of nitrogen, cause flow rate in product low, later separation is of high cost.There was only pyrolysis gas without gasifying agent gasification Change one kind, it is the gasification reaction carried out in the case of complete anaerobic, has product calorific value height, reaction process simply excellent Point, but how to provide external heat source becomes critical issue, therefore, gasification reactor and reaction process are designed to for weight Point.In addition, the development of limitation biomass gasification technology and industrialized major obstacle are the elimination problems of by-product tar at present.It is burnt The presence of oil is easy to cause the damage of the blocking of gasification system, corrosion and equipment, causes the inactivation of downstream heat carrier and serious Environmental pollution etc..
Utility model content
The purpose of this utility model is that in view of the deficiencies of the prior art, a kind of biomass gasification device is provided, it will be biological Matter gasification is divided into pyrolytic gasification and char Gasification Liang Ge workshop sections, and pyrolytic gasification process uses " W " type gasification reactor, tool There is the remarkable advantage that equipment volume is small, the reaction was complete, tar is free of in synthesis gas.
Technical solution provided by the utility model is:
A kind of biomass gasification device, including gasification reactor, semicoke and heat carrier separator, the heating of fluid bed heat carrier Device, heat carrier classification piece-rate system and the first synthesis gas collector;
The gasification reactor includes pyrolytic gasification reaction zone, is arranged in the reforming reaction area of pyrolytic gasification reaction zone side And gas filtration area;Material inlet and the first heat carrier import are equipped at the top of the pyrolytic gasification reaction zone;The pyrolysis gas Change reaction zone to detach by partition board with reforming reaction area, and the pyrolytic gasification reaction zone is connected to be formed with reforming reaction area bottom Connected region, returning charge valve are set to the connected region lower end;The returning charge valve, semicoke and heat carrier separator, the first material returning device with Fluid bed heat carrier heating device import is sequentially connected;
It is respectively equipped with product gas outlet and the second heat carrier import at the top of the reforming reaction area;The gas filtration area It is arranged between reforming reaction area and product gas outlet, top is equipped with third heat carrier import, and lower part is equipped with regulating valve;It is described First heat carrier import, the second heat carrier import and the import of third heat carrier are connect with heat carrier classification piece-rate system respectively, institute Product gas outlet is stated to connect with the first synthesis gas collector;The fluid bed heat carrier heating device outlet and heat carrier classification point Import connection from system.
In above-mentioned technical proposal, biomass starting material and vapor are entered by material inlet, heat carrier by the first heat carrier into Mouth enters, and realizes mixing heating in pyrolytic gasification reaction zone and reacts, the gas-phase product of pyrolytic gasification reaction zone generation enters weight In whole reaction zone, is contacted with the heat carrier in reforming reaction area and continue to react.Gas-phase product after reforming reaction continue into Enter gas filtration area and synthesis gas is further obtained by the reaction, while gas filtration area also plays the work of dust in filtering gas-phase product With.
By the heat carrier reacted and the semicoke not reacted completely by returning in pyrolytic gasification reaction zone and reforming reaction area Material valve enters the separation that semicoke realizes semicoke and heat carrier with heat carrier separator.Heat carrier after separation passes through the first material returning device Into fluid bed heat carrier heating device, enters heat carrier later and be classified piece-rate system, gas mistake is respectively enterd according to different-grain diameter Filter area, pyrolytic gasification reaction zone, reforming reaction area or outer row.
Preferably, the heat carrier classification piece-rate system is composed in series by three-stage cyclone separator, upper level cyclonic separation The outlet of device is connect with next stage cyclone inlet;The ash bucket of the first order cyclone separator and gas filtration area top Third heat carrier import connection, the ash bucket of the second level cyclone separator carries with the first heat carrier import and the second heat respectively Body import connects, row outside the ash bucket of the third-stage cyclone separator and outlet respectively.
It is classified piece-rate system by heat carrier, can will press grain diameter by the heat carrier of fluid bed heat carrier heating device It is divided into 3 sections and puts into different workshop sections respectively, respectively:The heat that lower grain size is more than 0.5mm is detached by first order cyclone separator Carrier respectively enters gas filtration area and bubbling fluidized bed char Gasification reactor, and 0.1- is isolated by second level cyclone separator The heat carrier of 0.5mm respectively enters pyrolytic gasification reaction zone, reforming reaction area and bubbling fluidized bed char Gasification reactor, by Third-stage cyclone separator isolates the then outer row of the heat carrier less than 0.1mm.
Preferably, the biomass gasification device further includes that bubbling fluidized bed char Gasification reactor and the second synthesis gas are received Storage;The semicoke is exported with the semicoke of heat carrier separator and is connect with bubbling fluidized bed char Gasification reactor, the bubbling Fluidized bed semicoke gasification reactor is connect by the second material returning device with fluid bed heat carrier heating device import;The bubbling fluidized bed The syngas outlet of char Gasification reactor is connect with the second synthesis gas collector;The first order cyclone separator and the second level The ash bucket of cyclone separator is also connect with bubbling fluidized bed char Gasification reactor respectively.Due to being provided with bubbling fluidized bed semicoke Gasification reactor so that biomass gasification process is divided into pyrolytic gasification and char Gasification Liang Ge workshop sections, improves synthesis gas yield.
Preferably, the wall surface that the gas filtration area is contacted with reforming reaction area and product gas outlet uses sieve;Institute The aperture for stating sieve is less than the grain size of heat carrier in gas filtration area.
Preferably, reactiveness is moving bed in the gas filtration area, and heat carrier falling speed is by adjusting regulating valve To control.
Preferably, if being equipped with dry material mixed plate in the pyrolytic gasification reaction zone;The shape of the material mixed plate is Triangular prism is arranged in parallel and is layered Heterogeneous Permutation between each other, and the number of plies of the material mixed plate is 2-30 layers.Material mixed plate Contact area between SOLID ORGANIC matter particle and heat carrier can be increased, the reaction was complete for promotion.Further preferably 8~10 layers.
Preferably, if being equipped with dry material mixed plate in the reforming reaction area;The shape of the material mixed plate is Mitsubishi Column is arranged in parallel and is layered Heterogeneous Permutation between each other, and the number of plies of the material mixed plate is 2-30 layers.Material mixed plate can Increase contact area between gas-phase product and heat carrier, the reaction was complete for promotion.Further preferably 2~4 layers.
Preferably, the cross section of the material mixed plate is isosceles triangle, ranging from 45-90 ° of apex angle.
Preferably, the heat carrier is Al2O3
Preferably, the reaction temperature of the pyrolytic gasification reaction zone is 800-1050 DEG C, and heat carrier is returned by being gravitationally fallen to Expect that valve, returning charge valve there should be self-sealing function.
Preferably, the reaction temperature of the fluid bed heat carrier heating device is 850-1100 DEG C;The bubbling fluidized bed half The reaction temperature of coke gasification reactor is 800-1100 DEG C.
Preferably, the first heat carrier import is vertically arranged at the top of pyrolytic gasification reaction zone;The material inlet packet Two are included, is obliquely installed respectively at the top of pyrolytic gasification reaction zone.
Preferably, two material inlets are symmetricly set at the top of pyrolytic gasification reaction zone, and material inlet and first The angle of heat carrier import is 15-75 °.
Preferably, the second heat carrier import and third heat carrier inlet parallel are vertically arranged at reforming reaction area top Portion.
Preferably, the reforming reaction area includes two, is symmetricly set on pyrolytic gasification reaction zone both sides.
Preferably, steam gasification device is equipped in the fluid bed heat carrier heating device.The setting can effectively utilize The heat generated by the biomass semicoke not reacted completely, for the vapor that gasifies, vapor is then as the raw material of gasification reaction It comes into operation.
Compared with the existing technology, the beneficial effects of the utility model are embodied in:
(1) biomass gasification process is divided into pyrolytic gasification and half by biomass gasification device provided by the utility model Coke gasification Liang Ge workshop sections improve the utilization rate of raw material and the yield of synthesis gas.
(2) biomass gasification device provided by the utility model uses " W " type gasification reactor, has equipment volume It is small, the reaction was complete, in synthesis gas be free of tar remarkable advantage.
Description of the drawings
Fig. 1 is the structural schematic diagram of biomass gasification device in embodiment;
Fig. 2 is the structural schematic diagram of gasification reactor in embodiment.
Wherein, 1, gasification reactor;101, pyrolytic gasification reaction zone;102, reforming reaction area;103, gas filtration area; 104, partition board;105, material mixed plate;106, sieve;107, product gas outlet;108, connected region;109, material inlet; 110, the first heat carrier import;111, the second heat carrier import;112, third heat carrier import;113, returning charge valve;114, it adjusts Valve;2, semicoke and heat carrier separator;3, fluid bed heat carrier heating device;4, the first synthesis gas collector;5, the first material returning device; 6, the first cyclone separator;7, the second cyclone separator;8, third cyclone separator;9, steam gasification device;10, bubbling fluidization Bed char Gasification reactor;11, the second material returning device;12, the second synthesis gas collector.
Specific implementation mode
With reference to specific embodiment, the utility model is described in further detail.
Embodiment
As shown in Figure 1, biomass gasification device includes gasification reactor 1, semicoke and heat carrier separator 2, fluid bed heat Carrier heating device 3, heat carrier classification piece-rate system, the first synthesis gas collector 4, bubbling fluidized bed char Gasification reactor 10 with And the second synthesis gas collector 12.
As shown in Fig. 2, gasification reactor 1 includes pyrolytic gasification reaction zone 101, setting in 101 liang of pyrolytic gasification reaction zone The reforming reaction area 102 and gas filtration area 103 of side.
Can be vertical cuboid in the global shape actual production of pyrolytic gasification reaction zone 101, top is set there are two object Expect import 109 and the first heat carrier import 110, and bottom opening.It is anti-that first heat carrier import 110 is vertically arranged at pyrolytic gasification Answer the top of area 101, and two material inlets 109 are then respectively symmetrically inclined at 101 top of pyrolytic gasification reaction zone, material into Mouth 109 and the angle of the first heat carrier import 110 are 40 °.
Since the reforming reaction area 102 of 101 both sides of pyrolytic gasification reaction zone is arranged symmetrically, the weight of side is only introduced herein Whole reaction zone 102.The reforming reaction area 102 of pyrolytic gasification reaction zone 101 and both sides is arranged in reactor.Pyrolytic gasification is anti- Area 101 is answered to be detached by partition board 104 with reforming reaction area 102, and the reforming reaction area of pyrolytic gasification reaction zone 101 and both sides 102 bottoms are connected to form connected region 108, and returning charge valve 113 is set to 108 lower end of connected region, and returning charge valve 113 has self sealss work( Energy.
102 top of reforming reaction area is respectively equipped with product gas outlet 107 and the second heat carrier import 111, and gas produces Object outlet 107 is connect with the first synthesis gas collector 4.And gas filtration area 103 is then arranged in reforming reaction area 102 and gas production Between object outlet 107, top is equipped with third heat carrier import 112, and lower part is equipped with regulating valve 114, is reacted in gas filtration area 103 State is moving bed, and heat carrier falling speed is controlled by adjusting regulating valve 114.Gas filtration area 103 and reforming reaction area 102 and the wall surface that contacts of product gas outlet 107 use sieve 106, the aperture of sieve 106 to be less than heat in gas filtration area 103 The grain size of carrier.In addition, the second heat carrier import 111 and 112 parallel connection of third heat carrier import are vertically arranged at reforming reaction area 102 tops.
If in addition, being equipped with dry material mixed plate 105 in pyrolytic gasification reaction zone 101 and reforming reaction area 102, material is mixed The shape of plywood 105 is triangular prism, and both ends are individually fixed in the two side of pyrolytic gasification reaction zone 101 and reforming reaction area 102 Face.The cross section of material mixed plate 105 is isosceles triangle, and corner angle is 90 °, is arranged in parallel between each other and is layered dislocation It arranges, the number of plies of the material mixed plate 105 in pyrolytic gasification reaction zone 101 is 10 layers, the material mixing in reforming reaction area 102 The number of plies of plate 105 is 3 layers.
Heat carrier classification piece-rate system is composed in series by three-stage cyclone separator, and the outlet of upper level cyclone separator is under Primary cyclone import connects.The ash bucket of first order cyclone separator 6 is warm with the third at 103 top of gas filtration area respectively Carrier import 112 and bubbling fluidized bed char Gasification reactor 10 connect, and the ash bucket of second level cyclone separator 7 is respectively with first Heat carrier import 110, the second heat carrier import 111 and bubbling fluidized bed char Gasification reactor 10 connect, third level whirlwind Row outside the ash bucket of separator 8 and outlet respectively.
Semicoke is connect with the import of heat carrier separator 2 with the returning charge valve 113 of gasification reactor 1, semicoke and heat carrier point Heating medium outlet from device 2 is connect by the first material returning device with the import of fluid bed heat carrier heating device 3.In addition, semicoke and heat The semicoke outlet of carrier separator 2 is connect with bubbling fluidized bed char Gasification reactor 10, the reaction of bubbling fluidized bed char Gasification Device 10 is connect by the second material returning device 11 with 3 import of fluid bed heat carrier heating device.Bubbling fluidized bed char Gasification reactor 10 Syngas outlet connect with the second synthesis gas collector 12.The ash of first order cyclone separator 6 and second level cyclone separator 7 Bucket is also connect with bubbling fluidized bed char Gasification reactor 10 respectively.Due to being provided with bubbling fluidized bed char Gasification reactor 10 so that biomass gasification process is divided into pyrolytic gasification and char Gasification Liang Ge workshop sections, improves synthesis gas yield.
The outlet of fluid bed heat carrier heating device 3 is connect with the import of first order cyclone separator 6, the heating of fluid bed heat carrier 3 top of device is additionally provided with steam gasification device 9, for removing gasified water using the heat generated by the biomass semicoke not reacted completely Steam.
The course of work is as follows:
Biomass and vapor are passed into material inlet 109, and heat carrier Al2O3It is passed into the first heat carrier import 110, It enters in pyrolytic gasification reaction zone 101, reactiveness is fluid bed, and reaction temperature is 800-1050 DEG C, in material mixed plate Quickly mixing heating is realized by mutually colliding, and start vigorous reaction on 105.
Due to " W " type structure setting of pyrolytic gasification reaction zone 101 and reforming reaction area 102 so that pyrolytic gasification reacts The gas-phase product that area 101 generates can enter in reforming reaction area 102 from 101 bottom of pyrolytic gasification reaction zone, with reforming reaction area Heat carrier contact in 102 continues reforming reaction, and the heat carrier in reforming reaction area 102 is by the second heat carrier import 111 It is passed through.And if equally to also promote contact of the gas-phase product with heat carrier anti-for the dry material mixed plate 105 in reforming reaction area 102 It answers.
Gas-phase product after reaction enters gas filtration area 103 and further reacts, and first is entered after obtained synthesis gas Synthesis gas collector 4, filtering heat carrier are passed through by third heat carrier import 112, and play dust in filtering gas-phase product Effect.
The semicoke for passing through the heat carrier of reaction in pyrolytic gasification reaction zone 101 and reforming reaction area 102 and not reacting completely, Enter the separation of semicoke and heat carrier separator 2 realization semicoke and heat carrier by returning charge valve 113.
Heat carrier after separation enters fluid bed heat carrier heating device 3, reaction temperature 850- by the first material returning device 5 1100 DEG C, enters heat carrier later and be classified piece-rate system, put into different workshop sections respectively according to different-grain diameter, respectively:By first Lower heat carrier of the grain size more than 0.5mm of grade cyclone separator 6 separation respectively enters gas filtration area 103 and bubbling fluidized bed semicoke Gasification reactor 10, the heat carrier that 0.1-0.5mm is isolated by second level cyclone separator 7 respectively enter pyrolytic gasification reaction zone 101, reforming reaction area 102 and bubbling fluidized bed char Gasification reactor 10, are isolated by third-stage cyclone separator 8 and are less than The heat carrier of 0.1mm is then outer to be arranged.
And the semicoke after detaching then enters bubbling fluidized bed char Gasification reactor 10, with entrance bubbling fluidized bed semicoke gas Heat carrier, vapor and the oxygen changed in reactor 10 are reacted, and reaction temperature is 800-1100 DEG C, the heat carrier after reaction Enter fluid bed heat carrier heating device 3 again by the second material returning device 11 to be recycled, and obtained synthesis gas then enters Second synthesis gas collector 12.

Claims (9)

1. a kind of biomass gasification device, which is characterized in that including gasification reactor, semicoke and heat carrier separator, fluid bed Heat carrier heating device, heat carrier classification piece-rate system and the first synthesis gas collector;
The gasification reactor includes pyrolytic gasification reaction zone, be arranged pyrolytic gasification reaction zone side reforming reaction area and Gas filtration area;Material inlet and the first heat carrier import are equipped at the top of the pyrolytic gasification reaction zone;The pyrolytic gasification is anti- Area is answered to be detached by partition board with reforming reaction area, and the pyrolytic gasification reaction zone is connected to form connection with reforming reaction area bottom Area, returning charge valve are set to the connected region lower end;The returning charge valve, semicoke and heat carrier separator, the first material returning device and fluidisation Bed heat carrier heating device import is sequentially connected;
It is respectively equipped with product gas outlet and the second heat carrier import at the top of the reforming reaction area;The gas filtration area setting Between reforming reaction area and product gas outlet, top is equipped with third heat carrier import, and lower part is equipped with regulating valve;Described first Heat carrier import, the second heat carrier import and the import of third heat carrier are connect with heat carrier classification piece-rate system respectively, the gas Body product exit is connect with the first synthesis gas collector;The fluid bed heat carrier heating device outlet is classified segregative line with heat carrier The import of system connects.
2. biomass gasification device according to claim 1, which is characterized in that the heat carrier is classified piece-rate system by three Grade cyclone separator is composed in series, and the outlet of upper level cyclone separator is connect with next stage cyclone inlet;
The ash bucket of first order cyclone separator is connect with the third heat carrier import at the top of gas filtration area, second level cyclonic separation The ash bucket of device is connect with the first heat carrier import and the second heat carrier import respectively, the ash bucket of third-stage cyclone separator and outlet Outer row respectively.
3. biomass gasification device according to claim 2, which is characterized in that further include that bubbling fluidized bed char Gasification is anti- Answer device and the second synthesis gas collector;
The semicoke is exported with the semicoke of heat carrier separator and is connect with bubbling fluidized bed char Gasification reactor, the bubble flow Change bed char Gasification reactor to connect with fluid bed heat carrier heating device import by the second material returning device;The bubbling fluidized bed half The syngas outlet of coke gasification reactor is connect with the second synthesis gas collector;The first order cyclone separator is revolved with the second level The ash bucket of wind separator is also connect with bubbling fluidized bed char Gasification reactor respectively.
4. biomass gasification device according to claim 1, which is characterized in that the gas filtration area and reforming reaction area Sieve is used with the wall surface of product gas outlet contact;The aperture of the sieve is less than the grain size of heat carrier in gas filtration area.
5. biomass gasification device according to claim 1, which is characterized in that if being equipped in the pyrolytic gasification reaction zone Dry material mixed plate;The shape of the material mixed plate is triangular prism, is arranged in parallel and is layered Heterogeneous Permutation between each other, described The number of plies of material mixed plate is 2-30 layers.
6. biomass gasification device according to claim 1, which is characterized in that if being equipped with dry in the reforming reaction area Expect mixed plate;The shape of the material mixed plate is triangular prism, is arranged in parallel and is layered Heterogeneous Permutation, the material between each other The number of plies of mixed plate is 2-30 layers.
7. biomass gasification device according to claim 1, which is characterized in that the first heat carrier import is vertically arranged At the top of pyrolytic gasification reaction zone;The material inlet includes two, is obliquely installed respectively at the top of pyrolytic gasification reaction zone.
8. biomass gasification device according to claim 1, which is characterized in that the second heat carrier import and third heat Carrier inlet parallel is vertically arranged at the top of reforming reaction area.
9. biomass gasification device according to claim 1, which is characterized in that the reforming reaction area includes two, right Claim to be arranged in pyrolytic gasification reaction zone both sides.
CN201721395300.XU 2017-10-25 2017-10-25 A kind of biomass gasification device Expired - Fee Related CN207987121U (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107723032A (en) * 2017-10-25 2018-02-23 浙江科技学院 A kind of biomass gasification device and technique
CN112552961A (en) * 2019-09-25 2021-03-26 中国石油化工股份有限公司 Biomass gasification device and application thereof

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107723032A (en) * 2017-10-25 2018-02-23 浙江科技学院 A kind of biomass gasification device and technique
CN107723032B (en) * 2017-10-25 2023-10-20 浙江科技学院 Biomass gasification device and process
CN112552961A (en) * 2019-09-25 2021-03-26 中国石油化工股份有限公司 Biomass gasification device and application thereof
CN112552961B (en) * 2019-09-25 2021-11-30 中国石油化工股份有限公司 Biomass gasification device and application thereof

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Granted publication date: 20181019