CN207987121U - A kind of biomass gasification device - Google Patents
A kind of biomass gasification device Download PDFInfo
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- 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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- 238000002309 gasification Methods 0.000 title claims abstract description 137
- 239000002028 Biomass Substances 0.000 title claims abstract description 34
- 238000006243 chemical reaction Methods 0.000 claims abstract description 69
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 27
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 27
- 238000010438 heat treatment Methods 0.000 claims abstract description 24
- 239000012530 fluid Substances 0.000 claims abstract description 21
- 230000008676 import Effects 0.000 claims description 51
- 239000000463 material Substances 0.000 claims description 45
- 238000006057 reforming reaction Methods 0.000 claims description 44
- 230000005587 bubbling Effects 0.000 claims description 26
- 238000001914 filtration Methods 0.000 claims description 26
- 238000000926 separation method Methods 0.000 claims description 8
- 230000001105 regulatory effect Effects 0.000 claims description 5
- 238000005192 partition Methods 0.000 claims description 4
- 230000008859 change Effects 0.000 claims description 3
- 239000000571 coke Substances 0.000 claims description 3
- 238000005243 fluidization Methods 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 8
- 230000008569 process Effects 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 51
- 239000000047 product Substances 0.000 description 17
- 238000005516 engineering process Methods 0.000 description 9
- 239000003795 chemical substances by application Substances 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 229910052593 corundum Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 238000000197 pyrolysis Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 229910001845 yogo sapphire Inorganic materials 0.000 description 2
- 241000283216 Phocidae Species 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000011120 plywood Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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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
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.
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Cited By (2)
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 |
-
2017
- 2017-10-25 CN CN201721395300.XU patent/CN207987121U/en not_active Expired - Fee Related
Cited By (4)
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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