CN207727036U - A kind of device of biomass production high-grade synthesis gas - Google Patents
A kind of device of biomass production high-grade synthesis gas Download PDFInfo
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- CN207727036U CN207727036U CN201721395496.2U CN201721395496U CN207727036U CN 207727036 U CN207727036 U CN 207727036U CN 201721395496 U CN201721395496 U CN 201721395496U CN 207727036 U CN207727036 U CN 207727036U
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Abstract
The utility model is related to the devices that a kind of biomass produces high-grade synthesis gas, including multifunctional gasification reactor, fluid bed heat carrier heating device, heat carrier separator, catalyst regeneration classification piece-rate system and synthesis gas collector.The device uses " W " type reactor by biomass pyrogenation gasification, pyrolysis gas is reformed and synthesis gas filter process organic coupling, with equipment volume is small, the reaction was complete, synthesis gas grade is high and remarkable advantage without tar and dust.
Description
Technical field
The utility model belongs to Biomass Energy Utilization field, and in particular to a kind of biomass production high-grade synthesis gas
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, improve synthesis gas grade become critical issue, therefore, gasification reactor and reaction work
Skill is designed to for emphasis.
In addition, the development of limitation biomass gasification technology and industrialized major obstacle are that the elimination of by-product tar is asked at present
Topic.The presence of tar is easy to cause the damage of the blocking of gasification system, corrosion and equipment, cause downstream catalyst inactivation 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, providing a kind of biomass production high-grade synthesis gas
Device, the device using " W " type reactor by biomass pyrogenation gasification, pyrolysis gas reform and the organic coupling of synthesis gas filter process
It closes, with equipment volume is small, the reaction was complete, synthesis gas grade is high and remarkable advantage without tar and dust.
Technical solution provided by the utility model is：
A kind of device of biomass production high-grade synthesis gas, including multifunctional gasification reactor, fluid bed heat carrier liter
Warm device, heat carrier separator, catalyst regeneration classification piece-rate system and synthesis gas collector；
The multifunctional gasification reactor includes pyrolytic gasification reaction zone, the reformation in pyrolytic gasification reaction zone side is arranged
Reaction zone and reformation filtering area；Material inlet and the ash with heat carrier separator are equipped at the top of the pyrolytic gasification reaction zone
Struggle against the heat carrier import connected, and bottom is equipped with the first returning charge valve, and the first returning charge valve passes through material returning device and fluid bed heat carrier
Heating device import connects；
Top is detached by partition board between the pyrolytic gasification reaction zone and reforming reaction area, and lower part is detached by grid,
The partition board and grid are connected with each other；Be respectively equipped at the top of the reforming reaction area product gas outlet and the first catalyst into
Mouthful, bottom is equipped with the second returning charge valve, and the second returning charge valve is connect with catalyst regeneration classification piece-rate system import, the gas
Product exit is connect with synthesis gas collector；The reformation filtering area is arranged between reforming reaction area and product gas outlet,
Top is equipped with the second catalyst inlet, and lower part is equipped with regulating valve；
The fluid bed heat carrier heating device outlet is connect with heat carrier separator import；The catalyst regeneration classification point
It is connect respectively with the first catalyst inlet and the second catalyst inlet from system outlet.
In above-mentioned technical proposal, biomass starting material and vapor are entered by material inlet, heat carrier by heat carrier import into
Enter, pyrolytic gasification reaction zone realize mixing heat up and react, pyrolytic gasification reaction zone generate gas-phase product by grid into
Enter in reforming reaction area, is contacted with the catalyst in reforming reaction area and continue reforming reaction.Gas phase production after reforming reaction
Object continues through reformation filtering area, while reforming the effect that filtering area also plays dust in filtering gas-phase product.
Fluidisation is entered by material returning device by the heat carrier reacted and the semicoke not reacted completely in pyrolytic gasification reaction zone
Bed heat carrier heating device, is again introduced into pyrolytic gasification reaction zone by carrier separator later.By reaction in reforming reaction area
Catalyst heating device is burnt into fluidized bed by the second returning charge valve, sequentially enter later the first cyclone separator and second rotation
Wind separator respectively enters after reduction and reforms filtering area and reforming reaction area.
Preferably, catalyst regeneration classification piece-rate system include fluid bed burn heating device, the first cyclone separator,
Second cyclone separator, the first fixed bed reductor and the second fixed bed reductor；
The fluid bed burns heating device import and is connect with the second returning charge valve of reforming reaction area bottom, outlet and the first rotation
Wind separator import connects, and the first Cyclone outlet is connect with the second cyclone inlet, and the second cyclone separator goes out
Row outside mouthful；The ash bucket of first cyclone separator is connect by the first fixed bed reductor with the second catalyst inlet；It is described
The ash bucket of second cyclone separator is connect by the second fixed bed reductor with the first catalyst inlet.
It is classified piece-rate system by catalyst regeneration, catalyst can be divided into 2 sections by grain diameter and put into respectively
Different workshop sections, respectively：Lower catalyst of the grain size more than 0.5mm is detached by the first cyclone separator to restore by the first fixed bed
Device enters reformation filtering area, and isolate the catalyst less than 0.5mm by second level cyclone separator restores by the second fixed bed
Device enters reforming reaction area.
Preferably, the wall surface that the reformation filtering 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 for reforming catalyst in filtering area.
Preferably, reactiveness is moving bed in the reformation filtering area, and catalyst 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 8-30 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 8~11 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 3-10 layers.Material mixed plate can
Increase contact area between gas-phase product and catalyst, the reaction was complete for promotion.Further preferably 3~5 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, the catalyst is Ni base catalyst.
Preferably, the reaction temperature of the pyrolytic gasification reaction zone is 800-950 DEG C, and heat carrier is by being gravitationally fallen to first
Returning charge valve, the first returning charge valve should have self-sealing function.
Preferably, the reaction temperature of the fluid bed heat carrier heating device is 850-1000 DEG C；The fluid bed burns liter
The reaction temperature of warm device is 700-800 DEG C.
Preferably, the grid is alternatively arranged by inverted v-shaped flase floor and is formed；The inverted v-shaped flase floor is asymmetry
Structure, be located at pyrolytic gasification reaction zone side edges of boards and vertical direction angle be less than side edges of boards positioned at reforming reaction area with
The angle of vertical direction.
Preferably, the angular range for being located at pyrolytic gasification reaction zone side edges of boards and vertical direction is 15-45 °；Positioned at weight
The angular range of whole reaction zone side edges of boards and vertical direction is 15-75 °.
Preferably, the inverted v-shaped flase floor is located at the bottom position of pyrolytic gasification reaction zone side edges of boards less than next
The top position of layer inverted v-shaped flase floor；The bottom position that the inverted v-shaped flase floor is located at reforming reaction area side edges of boards is neat
It puts down in the top position of next layer of inverted v-shaped flase floor.
Preferably, the spacing distance between the inverted v-shaped flase floor is less than the grain of heat carrier in pyrolytic gasification reaction zone
Diameter.
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.
Preferably, the heat carrier import is vertically arranged at the top of pyrolytic gasification reaction zone；The material inlet includes two
It is a, it 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 is carried with heat
The angle of body import is 15-75 °.
Preferably, the first heat carrier import and the second 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.
Compared with the existing technology, the beneficial effects of the utility model are embodied in：
The device of biomass production high-grade synthesis gas provided by the utility model, will be biological using " W " type reactor
Matter pyrolytic gasification, pyrolysis gas is reformed and synthesis gas filter process organic coupling, with equipment volume is small, the reaction was complete, synthesis gas
Grade is high and is free of the remarkable advantage of tar and dust.
Description of the drawings
Fig. 1 is the apparatus structure schematic diagram that biomass produces high-grade synthesis gas in embodiment；
Fig. 2 is the structural schematic diagram of multifunctional gasification reactor in embodiment.
Wherein, 1, multifunctional gasification reactor；101, pyrolytic gasification reaction zone；102, reforming reaction area；103, reformed
Filter area；104, partition board；105, grid；106, material mixed plate；107, heat carrier import；108, material inlet；109, it first urges
Agent import；110, the second catalyst inlet；111, sieve；112, product gas outlet；113, the first returning charge valve；114, second
Returning charge valve；115, regulating valve；2, fluid bed heat carrier heating device；3, fluid bed burns heating device；4, synthesis gas collector；5, hot
Carrier separator；6, the first cyclone separator；7, the second cyclone separator；8, the first fixed bed reductor；9, the second fixed bed
Reductor；10, material returning device；11, steam gasification device.
Specific implementation mode
With reference to specific embodiment, the utility model is described in further detail.
Embodiment
As shown in Figure 1, the device of biomass production high-grade synthesis gas includes multifunctional gasification reactor 1, fluid bed heat
Carrier heating device 2, heat carrier separator 5, catalyst regeneration classification piece-rate system and synthesis gas collector 4.
As shown in Fig. 2, multifunctional gasification reactor 1 includes pyrolytic gasification reaction zone 101, is arranged in pyrolytic gasification reaction zone
The reforming reaction area 102 of 101 both sides and reformation filtering area 103.
Wherein, can be vertical cuboid in the global shape actual production of pyrolytic gasification reaction zone 101, top is equipped with two
A material inlet 108 and the heat carrier import 107 being connect with the ash bucket of heat carrier separator 5, bottom are equipped with the first returning charge valve
113, the first returning charge valve 113 is connect by material returning device 10 with 2 import of fluid bed heat carrier heating device.Heat carrier import 107 is vertical
It is set to 101 top of pyrolytic gasification reaction zone, and two material inlets 108 are then respectively symmetrically inclined at pyrolytic gasification reaction
101 top of area, material inlet 108 and the angle of heat carrier import 107 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-
Top between area 101 and reforming reaction area 102 is answered to be detached by partition board 104, lower part is detached by grid 105, partition board 104 and lattice
The interconnection of grid 105 separates two regions.
Partition board 104 uses solid slab, and pyrolytic gasification reaction zone 101 and the reforming reaction area 102 of both sides are kept apart.And lattice
Grid 105 are alternatively arranged by inverted v-shaped flase floor and are formed, and inverted v-shaped flase floor is dissymmetrical structure, is located at pyrolytic gasification reaction zone
The angle of 101 side edges of boards and vertical direction is less than the angle of the side edges of boards and vertical direction positioned at reforming reaction area 102.Position
In the angular range of 101 side edges of boards of pyrolytic gasification reaction zone and vertical direction be 30 °；Side positioned at reforming reaction area 102
The angular range of edges of boards and vertical direction is 45 °.Inverted v-shaped flase floor is located at the bottom of 101 side edges of boards of pyrolytic gasification reaction zone
Position is set low in the top position of next layer of inverted v-shaped flase floor；Inverted v-shaped flase floor is located at 102 side plate of reforming reaction area
The bottom position on side is flush to the top position of next layer of inverted v-shaped flase floor.In addition, the interval between inverted v-shaped flase floor
Distance is less than the grain size of heat carrier in pyrolytic gasification reaction zone 101.
102 top of reforming reaction area is respectively equipped with product gas outlet 112 and the first catalyst inlet 109, gaseous product
Outlet 112 is connect with synthesis gas collector 4, and bottom is equipped with the second returning charge valve 114, and the second returning charge valve 114 is burnt with fluid bed
Heating device 3 connects.And reform filtering area 103 and be then arranged between reforming reaction area 102 and product gas outlet 112, top is set
There are the second catalyst inlet 110, lower part to be equipped with regulating valve 115, it is moving bed, catalyst to reform reactiveness in filtering area 103
Falling speed is controlled by adjusting regulating valve 115.
It reforms the wall surface that filtering area 103 is contacted with reforming reaction area 102 and product gas outlet 112 and uses sieve 111, sieve
The aperture of net 111 is less than the grain size for reforming catalyst in filtering area 103.In addition, the first catalyst inlet 109 and the second catalyst
110 parallel connection of import is vertically arranged at 102 top of reforming reaction area.
If in addition, being equipped with dry material mixed plate 106 in pyrolytic gasification reaction zone 101 and reforming reaction area 102, material is mixed
The shape of plywood 106 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 is isosceles triangle, and corner angle is 90 °, is arranged in parallel between each other and is layered dislocation row
It arranges, the number of plies of the material mixed plate 106 in pyrolytic gasification reaction zone 101 is 11 layers, the material mixed plate in reforming reaction area 102
106 number of plies is 3 layers.
2 import of fluid bed heat carrier heating device is connect with material returning device 10, is internally provided with steam gasification device 11, vapor gas
The heat that the biomass semicoke not reacted completely generates can be effectively utilized by changing device 11, and for the vapor that gasifies, vapor is then
Raw material as gasification reaction comes into operation.And the outlet of fluid bed heat carrier heating device 2 then connects with 5 import of heat carrier separator
It connects, the ash bucket of heat carrier separator 5 is connect with heat carrier import, and the outlet of heat carrier separator 5 is then outer to arrange.
It includes that fluid bed burns heating device 3, the first cyclone separator 6, the second whirlwind that catalyst regeneration, which is classified piece-rate system,
Separator 7, the first fixed bed reductor 8 and the second fixed bed reductor 9.Fluid bed burns 3 import of heating device and reforms instead
The second returning charge valve 114 of 102 bottom of area is answered to connect, outlet is connect with 6 import of the first cyclone separator, the first cyclone separator 6
Outlet is connect with 7 import of the second cyclone separator, and the second cyclone separator 6 exports outer row.The ash bucket of first cyclone separator 6 is logical
It crosses the first fixed bed reductor 8 to connect with the second catalyst inlet 110, the ash bucket of the second cyclone separator 7 is fixed by second
Bed reductor 9 is connect with the first catalyst inlet 109.
The course of work is as follows：
Biomass and vapor are passed into material inlet 108, and heat carrier Al2O3It is passed into heat carrier import 107, is entered
Into pyrolytic gasification reaction zone 101, reactiveness is fluid bed, and reaction temperature is 800-950 DEG C, on material mixed plate 106
Quickly mixing heating is realized by mutually colliding, and starts vigorous reaction.
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 from 101 bottom of pyrolytic gasification reaction zone by grid 105 in reforming reaction area 102,
It is contacted with the Ni base catalyst in reforming reaction area 102 and continues reforming reaction, the Ni base catalyst in reforming reaction area 102
It is passed through by the first heat carrier import 109.And if the dry material mixed plate 106 in reforming reaction area 102 equally also promotes gas phase
The haptoreaction of product and Ni base catalyst.
Gas-phase product after reaction, which enters, reforms the further reaction of filtering area 103, enters synthesis after obtained synthesis gas
Gas collector 4, catalyst are passed through by the second heat carrier import 110, and play the role of filtering dust in gas-phase product.
Entered by material returning device 10 by the heat carrier reacted and the semicoke not reacted completely in pyrolytic gasification reaction zone 101
Fluid bed heat carrier heating device 2, reaction temperature are 850-1000 DEG C, are again introduced into pyrolytic gasification by carrier separator 5 later
Reaction zone 101.
Catalyst in reforming reaction area 102 by reaction burns heating device by the second returning charge valve 114 into fluidized bed
3, reaction temperature is 700-800 DEG C, the first cyclone separator 6 and the second cyclone separator 7 is sequentially entered later, after reduction
It respectively enters and reforms filtering area 103 and reforming reaction area 102.It is classified piece-rate system by catalyst regeneration, it can be by catalyst
It is divided into 2 sections by grain diameter and puts into different workshop sections respectively, respectively：Lower grain size is detached by the first cyclone separator 6 to be more than
The catalyst of 0.5mm enters by the first fixed bed reductor 8 reforms filtering area 103, is isolated by second level cyclone separator 7
Catalyst less than 0.5mm enters reforming reaction area 102 by the second fixed bed reductor 9.
Claims (9)
1. a kind of device of biomass production high-grade synthesis gas, which is characterized in that including multifunctional gasification reactor, fluid bed
Heat carrier heating device, heat carrier separator, catalyst regeneration classification piece-rate system and synthesis gas collector；
The multifunctional gasification reactor includes pyrolytic gasification reaction zone, the reforming reaction in pyrolytic gasification reaction zone side is arranged
Area and reformation filtering area；It is equipped with material inlet at the top of the pyrolytic gasification reaction zone and connects with the ash bucket of heat carrier separator
The heat carrier import connect, bottom are equipped with the first returning charge valve, and the first returning charge valve is heated up by material returning device and fluid bed heat carrier
Device import connects；
Top is detached by partition board between the pyrolytic gasification reaction zone and reforming reaction area, and lower part is detached by grid, described
Partition board and grid are connected with each other；It is respectively equipped with product gas outlet and the first catalyst inlet, bottom at the top of the reforming reaction area
Portion is equipped with the second returning charge valve, and the second returning charge valve is connect with catalyst regeneration classification piece-rate system import, the gaseous product
Outlet is connect with synthesis gas collector；The reformation filtering area is arranged between reforming reaction area and product gas outlet, top
Equipped with the second catalyst inlet, lower part is equipped with regulating valve；
The fluid bed heat carrier heating device outlet is connect with heat carrier separator import；The catalyst regeneration is classified segregative line
System outlet is connect with the first catalyst inlet and the second catalyst inlet respectively.
2. the device of biomass production high-grade synthesis gas according to claim 1, which is characterized in that the catalyst is again
Grade piece-rate system estranged includes that fluid bed burns heating device, the first cyclone separator, the second cyclone separator, the first fixed bed also
Prototype and the second fixed bed reductor；
The fluid bed burns heating device import and is connect with the second returning charge valve of reforming reaction area bottom, outlet and the first whirlwind point
It is connected from device import, the first Cyclone outlet is connect with the second cyclone inlet, outside the second Cyclone outlet
Row；The ash bucket of first cyclone separator is connect by the first fixed bed reductor with the second catalyst inlet；Described second
The ash bucket of cyclone separator is connect by the second fixed bed reductor with the first catalyst inlet.
3. the device of biomass production high-grade synthesis gas according to claim 1, which is characterized in that the reformation filtering
The wall surface that area is contacted with reforming reaction area and product gas outlet uses sieve；The aperture of the sieve, which is less than, reforms in filtering area
The grain size of catalyst.
4. the device of biomass production high-grade synthesis gas according to claim 1, which is characterized in that the pyrolytic gasification
If being equipped with dry material mixed plate in reaction zone；The shape of the material mixed plate is triangular prism, is arranged in parallel and divides between each other
The number of plies of layer Heterogeneous Permutation, the material mixed plate is 8-30 layers.
5. the device of biomass production high-grade synthesis gas according to claim 1, which is characterized in that the reforming reaction
If being equipped with dry material mixed plate in area；The shape of the material mixed plate is triangular prism, is arranged in parallel between each other and is layered mistake
The number of plies of position arrangement, the material mixed plate is 3-10 layers.
6. the device of biomass production high-grade synthesis gas according to claim 1, which is characterized in that the grid is by falling
V-shaped flase floor is alternatively arranged composition；The inverted v-shaped flase floor is dissymmetrical structure, is located at pyrolytic gasification reaction zone side
The angle of edges of boards and vertical direction is less than the angle of the side edges of boards and vertical direction positioned at reforming reaction area.
7. the device of biomass production high-grade synthesis gas according to claim 1, which is characterized in that the fluid bed heat
Steam gasification device is equipped in carrier heating device.
8. the device of biomass according to claim 1 production high-grade synthesis gas, which is characterized in that the heat carrier into
Mouth is vertically arranged at the top of pyrolytic gasification reaction zone；The material inlet includes two, is obliquely installed respectively anti-in pyrolytic gasification
It answers at the top of area.
9. the device of biomass production high-grade synthesis gas according to claim 1, which is characterized in that the reforming reaction
Area includes two, is symmetricly set on pyrolytic gasification reaction zone both sides.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721395496.2U CN207727036U (en) | 2017-10-25 | 2017-10-25 | A kind of device of biomass production high-grade synthesis gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721395496.2U CN207727036U (en) | 2017-10-25 | 2017-10-25 | A kind of device of biomass production high-grade synthesis gas |
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| Publication Number | Publication Date |
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| CN207727036U true CN207727036U (en) | 2018-08-14 |
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ID=63091138
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| CN201721395496.2U Expired - Fee Related CN207727036U (en) | 2017-10-25 | 2017-10-25 | A kind of device of biomass production high-grade synthesis gas |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107964427A (en) * | 2017-10-25 | 2018-04-27 | 浙江科技学院 | A kind of device and technique of biomass production high-grade synthesis gas |
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2017
- 2017-10-25 CN CN201721395496.2U patent/CN207727036U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107964427A (en) * | 2017-10-25 | 2018-04-27 | 浙江科技学院 | A kind of device and technique of biomass production high-grade synthesis gas |
| CN107964427B (en) * | 2017-10-25 | 2023-09-15 | 浙江科技学院 | Device and process for producing high-grade synthesis gas by biomass |
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Granted publication date: 20180814 Termination date: 20181025 |