CN106635165A - Method and device for preparing clean synthesized gas by gasifying carbon-containing raw material - Google Patents
Method and device for preparing clean synthesized gas by gasifying carbon-containing raw material Download PDFInfo
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- CN106635165A CN106635165A CN201611147150.0A CN201611147150A CN106635165A CN 106635165 A CN106635165 A CN 106635165A CN 201611147150 A CN201611147150 A CN 201611147150A CN 106635165 A CN106635165 A CN 106635165A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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Abstract
The invention belongs to the technical field of energy and chemical industry, and relates to a method and device for preparing clean synthesized gas by gasifying a carbon-containing raw material. According to the method and device, circulation of solid particles which are used as both a heat carrier and a catalyst is utilized to realize decoupled optimization control and re-integration of the carbon-containing raw material gasification and gasified product thermal desulfurization processes, and medium-high temperature clean synthesized gas is obtained. The gaseous product prepared by gasifying a carbon-containing raw material is subjected to thermal desulfurization to prepare the medium-high temperature clean synthesized gas, gas sensible heat can be kept and is convenient for connecting with a downstream synthesized gas conversion and utilization unit, and the heat efficiency is remarkably improved; and based on two parallel independent optimally-controlled solid heat carrier/catalyst circulations, decoupling and optimal reintegration of carbon-containing raw material gasification and gas medium-high temperature purification can be realized, the solid carbon-containing raw material can be directly converted to clean synthesized gas, and the equipment cost and operation cost can be reduced.
Description
Technical field
The invention belongs to derived energy chemical technical field, is related to a kind of solid thermal carriers catalyst using circulation, by carbon containing
The method and apparatus that material gasification produces cleaning synthesis gas.
Background technology
Coal Chemical Industry, coal gasification power generation technology of the development based on coal gasification, is that to solve China's pollution that caused by coal burning, oil gas short
Lack, realize the important channel of energy resources and environment global optimization.Biomass are the novel energy of representative, with carbon it is neutral, can
The features such as regeneration and reserves are big, actively Developing Biomass gasification technology and the utilization channel of expansion biomass synthesis gas, can conduct
The important supplement of traditional fossil energy, effectively reduces carbon emission and realizes energy sustainable development.Sulfide is coal gas/synthesis gas
One of major pollutants, or even biomass synthesis gas also contain a certain amount of sulfide with the difference of gasified raw material, can make
Forming apparatus burn into catalyst poisoning and environmental pollution.Desulfurizing and purifying is that synthesis gas clean utilization and Efficient Conversion are indispensable
Step.
Synthetic gas desulfurization purification techniques is broadly divided into wet desulphurization and dry desulfurization.Conventional wet desulfurization technology, it is such as wet
Formula oxidizing process (anthraquinone disulphonate method, naphthoquinones method, tannin process etc.), alkanolamine method (MEA, DEA etc.) and Physical Absorption method (low temperature
Methyl alcohol is washed, polyglycol dimethyl ether process etc.) etc., although mature technology, invest huge, cross hundred million easily, operation and safeguard
It is costly.Desulfurization by dry method mainly by two kinds of approach, using the metal oxides such as iron, zinc, calcium and cerium or composite oxides
For desulfurizing agent, under high temperature, metal sulfide is generated by there is vulcanization reaction with hydrogen sulfide, desulfurization is realized, after sulfuration
Desulfurizing agent high temperature regeneration under air, vapor or sulfur dioxide atmosphere, the desulfurizing agent after regeneration is recycled；Or in catalysis oxygen
Under changing catalyst action, using coal gas/synthesis gas in a small amount of oxygen be sulphur simple substance by hydrogen sulfide catalysis oxidation, separate then real
Existing desulfurization.Due to downstream cleaning coal gas/synthesis gas using technology such as integrated combination cycle generating (IGCC), synthetic natural gas processed and
Synthesizing methanol etc. is same to be operated under high temperature, and dry desulfurization (thermally desulfurizing) technology avoids coal gas of high temperature/synthesis gas cleaned
Cooling-warming temperature in journey, effectively increases the thermal efficiency of system, and simplification of flowsheet reduces sewage discharge, reduces and set
Standby investment.
Chinese invention patent CN201410205126.2 provides a kind of coal gas/thermally desulfurizing by synthesis gas dry method and sulfur recovery side
Oxidation of Hydrogen Sulfide is elemental sulfur using activated carbon and is adsorbed in activated carbon hole that purified gas goes to pipe network, satisfies by method, the technology
Regenerator is entered with activated carbon, fully desorption Posterior circle is used under 500 DEG C of nitrogen atmospheres, returned after the gaseous sulfur cooling for desorbing
Receive, by-product solid-state sulphur；The technology is capable of achieving recovery of sulfur, non-secondary pollution, but effective desulfurization temperature of activated carbon is interval
Below 120 DEG C, its application under high temperature is limited.Chinese invention patent CN201410771832.3 adopts ferrotitanium moldeed depth
Degree catalyst for selective oxidation carries out dry method to synthesis gas and continuously removes hydrogen sulfide, synthesis gas continuous desulfurization at 200-350 DEG C,
Reacted gas Jing coolings obtain molten sulfur and purified gas；Sulfur removal technology is this technique simplifies, but still adopts cooling means
Elemental sulfur and decontaminating syngas are separated, system thermal efficiency is reduced, heat exchange cost increased.
The content of the invention
The present invention is directed to the problems referred to above, there is provided the method and apparatus for producing cleaning synthesis gas by carbon raw material gasification, utilizes
As the circulation for heat carrier and the solid particle of catalyst, the solution of carbon raw material gasification and gasification product thermally desulfurizing process is realized
Coupling optimal control is integrated again, obtains high temperature cleaning synthesis gas.
Technical scheme：
The method that carbon raw material vaporizing system cleans synthesis gas, step is as follows：
In gasification reactor, carbon raw material is heated with gasifying agent by solid thermal carriers, and pyrolytic reaction, gasification reaction occur
And/or reforming reaction, generating gaseous products, be attached with the solid thermal carriers and semicoke of carbon deposit, the temperature of gasification reactor is
700-950℃；Gaseous products are entered in desulfurization reactor, under catalyst action, remove the sulfur component in gaseous products, raw
Into cleaning synthesis gas and the catalyst for adsorbing/being combined with sulfide, the temperature of desulfurization reactor is 300-850 DEG C；Gasification reaction
The catalyst for adsorbing/being combined with sulfide in solid thermal carriers and semicoke, the desulfurization reactor of device enters lifter；In lifter
In be passed through hot-air, the burning of carbon deposit on semicoke and solid thermal carriers, the heat that process is produced be used to heating solid thermal carriers and
Catalyst, heat smoke carries the ash content after coal-char combustion, solid thermal carriers and the boosted device of catalyst and enters gas-solid separator；
In gas-solid separator, the heat smoke for carrying dust is separated respectively with solid thermal carriers and catalyst；Leave the heat of gas-solid separator
Outer row after flue gas removing dust, removing and harmful gas and heat recovery；The solid thermal carriers and catalyst for leaving gas-solid separator are divided
For two parts, solid thermal carriers Jing burning tanks turn again to gasification reactor, and catalyst is entered and introduced in regenerator and regenerator
Regeneration solid/liquid/gas reactions, realize the abundant regeneration of the catalyst of absorption/combine sulfide, catalyst after regeneration returns desulphurization reaction
Device.
Described catalyst is desulfurizing agent or desulfurization and coke tar reforming bifunctional catalyst, while inert material can be mixed into；
Described inert material is quartz sand, sand or alumina globule.
When catalyst is used as desulfurizing agent, for the sulphur in gaseous products to be transferred in catalyst；Described catalyst
It is cerium system, manganese systems, iron system or nickel fimily desulfurizing agent, zinc oxide or the metal composite oxide containing zinc oxide；
When catalyst is used as desulfurization and coke tar reforming bifunctional catalyst, for the sulphur in described gaseous products to be turned
In moving on to the catalyst, and realize effective removing of tar component in gaseous products；Described catalyst is by desulfurizing agent and Jiao
Oily reforming catalyst is combined, and described desulfurizing agent is cerium system, manganese systems, iron system or nickel fimily desulfurizing agent, zinc oxide or containing oxidation
The metal composite oxide of zinc, described coke tar reforming catalyst is that olivine, olivine nickel-loaded catalyst or olivine carry iron
Catalyst；Described catalyst is the nickel catalyst for possessing desulfurization and coke tar reforming dual-use function；
Temperature is realized in the following way in gasification reactor：(1) adjust into the solid thermal carriers of gasification reactor
Temperature and its mass ratio with carbon raw material, wherein the temperature into the solid thermal carriers of gasification reactor is 750-1000 DEG C,
The mass ratio of solid thermal carriers and carbon raw material in the unit interval into gasification reactor is 10-100:1；(2) in gasified reverse
Answer and be passed through in device oxygen, by the part burning of carbon raw material or the product of carbon raw material heat is provided.
Carbon raw material into gasification reactor is carbonic solid fuels such as coal, biomass, petroleum coke, coke, charcoal,
Can be for example various liquid hydrocarbons of carbonaceous liquid fuel, or carbonaceous gas fuel such as coke-stove gas and natural gas, or on
State two or more mixture of carbon raw material；
Gasifying agent into gasification reactor is vapor, or the mixture of vapor and oxygen, or vapor and dioxy
Change the mixture of carbon, or the mixture of vapor and carbon dioxide and oxygen.
Temperature in desulfurization reactor is realized in the following way：(1) temperature into the catalyst of desulfurization reactor is adjusted
Urge into the described of the desulfurization reactor in degree and its mass ratio with the carbon raw material into gasification reactor, unit interval
Agent is 5-50 with the mass ratio of the carbon raw material for entering the gasification reactor:1, catalyst enters temperature during desulfurization reactor
Degree control is at 300-850 DEG C；(2) in the preposition regenerator of desulfurization reactor, by introducing regeneration gas, absorption/combination is realized
The abundant regeneration of the catalyst of sulfide, at the same time, using directly or indirectly heat exchange mode control regenerator outlet catalyst
Temperature；(3) in desulfurization reactor, gaseous products are cocurrent, adverse current or cross-flow with the way of contact of catalyst.
By control into the lifting air of lifter temperature and solid thermal carriers, catalyst and semicoke in lifter
The time of staying, make the carbon deposit on semicoke and solid thermal carriers and catalyst complete burn off, solid thermal carriers in lifting process
It is heated with catalyst；Temperature setting into the hot-air of the lifter is that the guarantee semicoke and the carbon deposit can be complete
Full burning, while avoiding the melting of active component sintering and the ash content in the catalyst, the inlet temperature of the hot-air
Control is at 300-800 DEG C；High-temp solid heat carrier Jing gas-solid separators enter burning tank, the maximum temperature of the burning tank and from
The temperature control of solid thermal carriers of burning tank is opened at 800-1100 DEG C, the heat produced when the burning of the semicoke and carbon deposit is not
When being enough to for the solid thermal carriers to be heated to said temperature, by the burning tank add gas or liquid or solid it is auxiliary
Combustion-supporting material, using the burning of the auxiliary fuel come additional heat；
By control into the lifting air of lifter temperature and solid thermal carriers, catalyst and semicoke in lifter
The time of staying, make semicoke divided combustion in the middle part of lifting process, the inlet temperature of the hot-air is controlled at 20-600 DEG C；Solid
Jing after gas-solid separator enters burning tank, the carbon deposit on remaining semicoke and solid thermal carriers is in air gas for heat carrier and remaining semicoke
After-flame under atmosphere, high-temp solid heat carrier returns gasification reactor.
Fresh catalyst entrance is set in lifter bottom, to supplement catalyst loss.
The device of cleaning synthesis gas, including the preposition regeneration of gas-solid separator, desulfurization reactor are produced in carbon raw material gasification
Device, burning tank, gasification reactor, desulfurization reactor and lifter；The catalyst inlet of the preposition regenerator of desulfurization reactor and
Respectively Jing pipelines are connected to two solid matter outlets of gas-solid separator, desulfurization reactor to the solid thermal carriers entrance of burning tank
The catalyst outlet of preposition regenerator be connected with the catalyst inlet of desulfurization reactor, the outlet of the solid thermal carriers of burning tank with
The solid thermal carriers entrance connection of gasification reactor, the solid thermal carriers outlet conduit of gasification reactor and urging for desulfurization reactor
Agent outlet conduit converges rear or each boosted device is connected to the solid thermal carriers/catalyst inlet of gas-solid separator, gasification
The product gas outlet of reactor is connected to the gaseous products entrance of desulfurization reactor.
Beneficial effects of the present invention：(1) carbon raw material gasification gained gaseous products Jing thermally desulfurizings are produced high temperature cleaning and are closed
Into gas, gas sensible heat is maintained, and is easy to be docked with downstream syngas conversion and range site, and the thermal efficiency is significantly improved；(2) base
In two parallel connections can independent optimization control solid thermal carriers/catalyst circulation, realize high in carbon raw material gasification and aerogenesis
The decoupling and optimization of temperature purification is integrated again, realizes that solid carbon raw material, to the direct conversion of cleaning synthesis gas, reduces installation cost
With and operating cost.
Description of the drawings
Fig. 1 is the method operation logic schematic diagram that cleaning synthesis gas is produced in carbon raw material gasification of the present invention.
Specific embodiment
The carbon raw material gasification disclosed in this patent is further described below by specific embodiment and produces cleaning synthesis gas
Method and apparatus, but the present invention do not limited by following embodiments.
Embodiment
Kahikatea wood chip gasification experiment, the operation of experimental system are carried out in feed throughput is for the experimental system of 0.5kg/h
Flow process principle is with accompanying drawing 1.Raw material kahikatea wood chip particle diameter is 0.38-0.83mm, and Industrial Analysis and elementary analysis result are as follows：
The kahikatea wood chip Industrial Analysis of table 1. and elementary analysis
Before experiment, raw material is dried 4h for 105-110 DEG C in an oven.Adopt granularity and carry nickel (Ni for 0.38-0.83mm olivines
Carrying capacity is 6wt.%) it is desulfurization and reformation bifunctional catalyst, quartz sand is solid thermal carriers.Kahikatea feed rate is 0.3kg/
H, the cycle rate into the solid thermal carriers of gasification reactor is 3kg/h, into the circulation speed of the catalyst of desulfurization reactor
Rate is 4.5kg/h.Gasification reactor temperature is 780 DEG C, and the temperature of desulfurization reactor is 600 DEG C, the matter of vapor/kahikatea wood chip
Amount compares 0.45, atmospheric operation.
Gasification reactor adopts fluidized bed process form, kahikatea quickly to add with the vapor Jing high-temp solid heat carriers being passed through
After heat, there is pyrolytic reaction, gasification reaction and reforming reaction in gasification reactor；Carbon deposit one on semicoke and solid thermal carriers
Rise and enter burning tank via lifter and gas-solid separator, here is burnt completely, solid thermal carriers are heated, high-temp solid heat is carried
Body returns gasification reactor and completes circulation；Gaseous products are entered in desulfurization reactor.
Desulfurization reactor adopts moving bed operation format, high-temperature gas product here to contact instead with olivine nickel-loaded catalyst
Should, desulfurization and tar conversion removing are realized, obtain cleaning synthesis gas；Reacted catalyst is via lifter and gas-solid separator
Into the preposition regenerator combustive regeneration of methanator, the sulfide for being attached to catalyst surface is converted into oxide, living
Property recovered, regenerated catalyst return desulfurization reactor.
Test result indicate that, using the apparatus and method, compared to inertia silica as desulfurization reactor bed, adopt
Nickel is carried as desulfurization and reformation bifunctional catalyst, be capable of achieving the effective of sulfur component in high-efficiency gasification and aerogenesis and take off with olivine
Remove, the method and device can produce the ideal chose that high temperature cleans synthesis gas as by carbon raw material gasification.
The gasification of biomass of table 2. produces cleaning synthesis gas operation result
Claims (10)
1. a kind of method that carbon raw material vaporizing system cleans synthesis gas, it is characterised in that step is as follows：
In gasification reactor, carbon raw material is heated with gasifying agent by solid thermal carriers, occur pyrolytic reaction, gasification reaction and/
Or reforming reaction, generating gaseous products, be attached with the solid thermal carriers and semicoke of carbon deposit, the temperature of gasification reactor is 700-
950℃；Gaseous products are entered in desulfurization reactor, under catalyst action, remove the sulfur component in gaseous products, are generated clear
Clean synthesis gas and the catalyst for adsorbing/being combined with sulfide, the temperature of desulfurization reactor is 300-850 DEG C；Gasification reactor
The catalyst for adsorbing/being combined with sulfide in solid thermal carriers and semicoke, desulfurization reactor enters lifter；Lead in lifter
Enter hot-air, the carbon deposit burning on semicoke and solid thermal carriers, the heat that process is produced is used to heat solid thermal carriers and catalysis
Agent, heat smoke carries the ash content after coal-char combustion, solid thermal carriers and the boosted device of catalyst and enters gas-solid separator；In gas-solid
In separator, the heat smoke for carrying dust is separated respectively with solid thermal carriers and catalyst；Leave the heat smoke of gas-solid separator
Outer row after removing dust, removing and harmful gas and heat recovery；The solid thermal carriers and catalyst for leaving gas-solid separator are divided into two
Part, solid thermal carriers Jing burning tanks turn again to gasification reactor, and catalyst enters regenerator with introducing in regenerator again
The abundant regeneration of the catalyst of sulfide is adsorbed/is combined in anger reaction, realization, and the catalyst after regeneration returns desulfurization reactor.
2. method according to claim 1, it is characterised in that described catalyst is desulfurizing agent, desulfurization and coke tar reforming
Bifunctional catalyst.
3. method according to claim 2, it is characterised in that when catalyst is used as desulfurizing agent, for by gaseous products
In sulphur be transferred in catalyst；Described catalyst is cerium system, manganese systems, iron system or nickel fimily desulfurizing agent, zinc oxide or containing oxidation
The metal composite oxide of zinc.
4. method according to claim 2, it is characterised in that when catalyst is used as desulfurization and coke tar reforming double-function catalyzing
During agent, for the sulphur in described gaseous products to be transferred in the catalyst, and tar component in gaseous products is realized
Effectively removing；Described catalyst is combined by desulfurizing agent with coke tar reforming catalyst, and described desulfurizing agent is cerium system, manganese
System, iron system or nickel fimily desulfurizing agent, zinc oxide or the metal composite oxide containing zinc oxide, described coke tar reforming catalyst is olive
Olive stone, olivine nickel-loaded catalyst or olivine supported ferric catalyst；Described catalyst is to possess desulfurization and coke tar reforming is dual
The nickel catalyst of function.
5. the method according to claim 3 or 4, it is characterised in that be mixed into inert material simultaneously in described catalyst, institute
The inert material stated is quartz sand, sand or alumina globule.
6. according to the arbitrary described method of claim 1-4, it is characterised in that temperature is real in the following way in gasification reactor
It is existing：(1) temperature and its mass ratio with carbon raw material into the solid thermal carriers of gasification reactor is adjusted, wherein entering gasification
The temperature of the solid thermal carriers of reactor is to enter the solid thermal carriers of gasification reactor and contain in 750-1000 DEG C, unit interval
The mass ratio of carbon raw material is 10-100:1；(2) oxygen is passed through in gasification reactor, by the anti-of carbon raw material or carbon raw material
The part burning for answering product provides heat；
Carbon raw material into gasification reactor is one kind in carbonic solid fuels, carbonaceous liquid fuel, carbonaceous gas fuel
Or two or more mixing；
Gasifying agent into gasification reactor is vapor, or the mixture of vapor and oxygen, or vapor and carbon dioxide
Mixture, or the mixture of vapor and carbon dioxide and oxygen.
7. according to the arbitrary described method of claim 1-4, it is characterised in that the temperature in desulfurization reactor is in the following way
Realize：(1) temperature and its quality with the carbon raw material into gasification reactor into the catalyst of desulfurization reactor is adjusted
Than the matter of the catalyst into the desulfurization reactor and the carbon raw material into the gasification reactor in the unit interval
Amount is than being 5-50:1, catalyst is into temperature control during desulfurization reactor at 300-850 DEG C；(2) before desulfurization reactor
In putting regenerator, by introducing regeneration gas, the abundant regeneration of the catalyst of sulfide is adsorbed/is combined in realization, at the same time, is adopted
Directly or indirectly heat exchange mode controls the temperature of regenerator outlet catalyst；(3) in desulfurization reactor, gaseous products with catalysis
The way of contact of agent is cocurrent, adverse current or cross-flow.
8. according to the arbitrary described method of claim 1-4, it is characterised in that
By control into lifter lifting air temperature with solid thermal carriers, catalyst and semicoke stopping in lifter
Stay the time, make the complete burn off in lifting process of the carbon deposit on semicoke and solid thermal carriers and catalyst, solid thermal carriers with urge
Agent is heated；Temperature setting into the hot-air of the lifter can fire completely to ensure the semicoke and the carbon deposit
Burn, while the melting of active component sintering and the ash content in the catalyst is avoided, the inlet temperature control of the hot-air
At 300-800 DEG C；High-temp solid heat carrier Jing gas-solid separators enter burning tank, the maximum temperature of the burning tank and leave burning
The shortage of heat that the temperature control of the solid thermal carriers of burnt tank is produced at 800-1100 DEG C, when the burning of the semicoke and carbon deposit with
When the solid thermal carriers are heated into said temperature, by adding gas or liquid or solid auxiliary combustion in the burning tank
Material, using the burning of the auxiliary fuel come additional heat；
By control into lifter lifting air temperature with solid thermal carriers, catalyst and semicoke stopping in lifter
The time is stayed, the inlet temperature for making semicoke divided combustion in the middle part of lifting process, the hot-air is controlled at 20-600 DEG C；Solid thermal is carried
Jing after gas-solid separator enters burning tank, the carbon deposit on remaining semicoke and solid thermal carriers is in air atmosphere for body and remaining semicoke
After-flame, high-temp solid heat carrier returns gasification reactor.
9. the device of cleaning synthesis gas is produced in a kind of carbon raw material gasification, it is characterised in that the device includes gas-solid separator, takes off
The preposition regenerator of reaction of Salmon-Saxl device, burning tank, gasification reactor, desulfurization reactor and lifter；Desulfurization reactor it is preposition again
Respectively Jing pipelines are connected to two solids of gas-solid separator for the catalyst inlet of raw device and the solid thermal carriers entrance of burning tank
Material outlet, the catalyst outlet of preposition regenerator of desulfurization reactor is connected with the catalyst inlet of desulfurization reactor, burns
The solid thermal carriers outlet of tank is connected with the solid thermal carriers entrance of gasification reactor, the solid thermal carriers outlet of gasification reactor
The catalyst outlet pipeline of pipeline and desulfurization reactor converges rear or each boosted device is connected to the solid thermal of gas-solid separator
Support/catalyst entrance, the product gas outlet of gasification reactor is connected to the gaseous products entrance of desulfurization reactor.
10. device according to claim 9, it is characterised in that fresh catalyst entrance is set in lifter bottom, to mend
Fill catalyst loss.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109207179A (en) * | 2018-09-18 | 2019-01-15 | 华中科技大学 | A kind of system of Photospot solar fuse salt pyrolysis carbonaceous material preparing synthetic gas |
| CN114574250A (en) * | 2022-04-14 | 2022-06-03 | 河南大学 | Method and device for preparing clean synthesis gas through biomass chemical-looping gasification |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102517098A (en) * | 2012-01-05 | 2012-06-27 | 四川大学 | Method for preparing renewable high-temperature gas desulphurization agent suitable for fluidization system |
| CN104498117A (en) * | 2014-12-04 | 2015-04-08 | 大连理工大学 | Method and device for preparing methane-enriched gas from carbon-containing raw materials |
-
2016
- 2016-12-13 CN CN201611147150.0A patent/CN106635165A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102517098A (en) * | 2012-01-05 | 2012-06-27 | 四川大学 | Method for preparing renewable high-temperature gas desulphurization agent suitable for fluidization system |
| CN104498117A (en) * | 2014-12-04 | 2015-04-08 | 大连理工大学 | Method and device for preparing methane-enriched gas from carbon-containing raw materials |
Non-Patent Citations (3)
| Title |
|---|
| 张蕾: "《烟气脱硫脱硝技术及催化剂的研究进展》", 31 July 2016, 中国矿业大学出版社 * |
| 王永刚等: "《煤气化工艺学》", 30 September 2014, 中国矿业大学出版社 * |
| 王群善等: "《工程物理现代工程技术物理基础》", 31 December 1993, 辽宁科学技术出版社 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109207179A (en) * | 2018-09-18 | 2019-01-15 | 华中科技大学 | A kind of system of Photospot solar fuse salt pyrolysis carbonaceous material preparing synthetic gas |
| CN114574250A (en) * | 2022-04-14 | 2022-06-03 | 河南大学 | Method and device for preparing clean synthesis gas through biomass chemical-looping gasification |
| CN114574250B (en) * | 2022-04-14 | 2023-05-02 | 河南大学 | Method and device for preparing clean synthetic gas by biomass chemical chain gasification |
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