CN103756730B - Heat accumulating type powdered coal entrained bed gasification method - Google Patents
Heat accumulating type powdered coal entrained bed gasification method Download PDFInfo
- Publication number
- CN103756730B CN103756730B CN201410028175.3A CN201410028175A CN103756730B CN 103756730 B CN103756730 B CN 103756730B CN 201410028175 A CN201410028175 A CN 201410028175A CN 103756730 B CN103756730 B CN 103756730B
- Authority
- CN
- China
- Prior art keywords
- group
- gasification
- heat
- accumulation
- thermophore
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Industrial Gases (AREA)
Abstract
The invention discloses a heat accumulating type powdered coal entrained bed gasification method. In the powdered coal entrained bed gasification process in the prior art, sensible heat of untreated gas cannot be well recycled and used for improving the temperature of a gasification agent through any methods. A system adopted by the gasification method disclosed by the invention comprises a gasification reaction unit, A group of heat accumulation and purification units and B group of heat accumulation and purification units, wherein both the A and B groups of heat accumulation and purification units are formed by sequentially-connected slag collectors, filters and heat accumulators; A and B groups of process nozzles are arranged in the gasification reaction unit and are respectively connected with the slag collectors in the A and B groups of heat accumulation and purification units; the gasification agent and carbon-containing flue are introduced into a gasification reactor for reaction from the process nozzle on one end of the gasification reactor; untreated gas after the reaction is discharged out of the gasification reactor from the process nozzle on the other end of the gasification reactor; the functions of the two groups of process nozzles are interchanged in a next process period. By adopting the gasification method disclosed by the invention, high-temperature sensible heat of the untreated gas at the exit of a gasification furnace can be effectively recycled and the gasification agent can be pretreated to a high temperature as the same as the temperature of the untreated gas.
Description
Technical field
The present invention relates to the high temperature gasification agent gasification process being applicable to fine coal or other carbonaceous fuels, especially a kind ofly accumulation of heat is carried out to raw gas and the entrained flow gasification method of heating to vaporized chemical.
Background technology
Coal Gasification Technology is one of gordian technique of the solid carbon-containing fuel clean and effective utilizations such as current coal, biomass, refinery coke, is also main path primary energy source being converted into clean secondary energy.Air-flow bed coal-gasification technology possesses that carbon turnover ratio is high, in coal gas containing many advantages such as tar, less demanding, the full-automatic manipulations of coal, be adapted to very much large-scale gasification industry.But airflow bed gasification furnace temperature of exit gas is higher, cause that vapourizing furnace cold gas efficiency is on the low side, gas heat can not get good utilization, become the biggest obstacle that airflow bed gasification furnace is applied.
In coal chemical industry, cold gas efficiency is the topmost economic and technical norms of gasifying process, and it is used for weighing efficiency coal resources being changed into synthetic gas, and this index directly affects the economic benefit of factory.In coal industrial combustion gas industry, airflow bed gasification furnace temperature of exit gas is high, caloric power of gas is low, and the steam produced after coal gas of high temperature cooling often can not get good utilization and therefore produces huge waste, and these factors all limit the application of entrained flow bed gasification technology in industrial gas preparation.If can develop a kind of can reclaim coal gas of high temperature sensible heat, vaporized chemical can be preheating to the high temperature of working as with export coal gas phase again, just can increase substantially the calorific value of coal gas, and need not lower the temperature to coal gas, gasifier bed gasification technology so just can be made to be more widely used.
It is usually improve gasification agent temperature that current one improves cold gas efficiency method, first utilizes the sensible heat in waste heat boiler recovery raw gas, gas heat is become high-temperature steam, then utilizes high-temperature steam by interchanger preheating vaporized chemical.But such method, equipment of being not only is huge, investment amount is high, and owing to vaporized chemical can not be preheating to very high temperature (being generally less than 300 DEG C) by interchanger, therefore, a lot of steam heats is had to can not get sufficient utilization in systems in which, sensible heat utilization rate in raw gas is not high, and caloric power of gas, cold gas efficiency also can not get larger raising.
Another kind is the mode adopting raw gas and vaporized chemical direct heat exchange, and such way can improve the temperature of vaporized chemical, but due to coal gas of high temperature contact with vaporized chemical after be highly combustible, possess very large potential safety hazard.Generally, such flow process can not be designed.
In current gasification industry, do not have other can reclaim sensible heat of raw gas very well to improve the method for gasification agent temperature, therefore, develop one also to improve vaporized chemical charging temperature to greatest extent, reduce raw gas temperature out, improve CO, H in coal gas by efficiency utilization sensible heat of raw gas
2, CH
4the gasification process of content, can improve energy utilization rate, reduce and pollute, all possess very important meaning to economical, society.
Summary of the invention
The object of the present invention is to provide a kind of heat accumulating type fine coal entrained flow gasification method, its can efficient recovery entrained flow gasification outlet of still raw gas high temperature sensible heat and vaporized chemical is preheating to the high temperature suitable with exporting raw gas, by improving the temperature into furnace gas agent, improve CO, H in raw gas
2deng the content of available gas, increase substantially cold gas efficiency, caloric power of gas; Reduce the follow-up temperature out of raw gas, decontaminating syngas dust and impurity, save the equipment such as waste heat boiler, dust removal installation follow-up in conventional air bed gasifying process, investment reduction simultaneously.
For this reason, the present invention solves above-mentioned technical problem by the following technical programs: a kind of heat accumulating type fine coal entrained flow gasification method, it is characterized in that, this gasification process system used comprises gasification reaction unit, A group accumulation of heat impurity removing unit and B group accumulation of heat impurity removing unit, and A, B group accumulation of heat impurity removing unit is by crust block device, strainer and the thermophore composition connected successively; Be provided with A, B two groups of technique nozzles in gasification reaction unit, be connected with the crust block device in A group and B group accumulation of heat impurity removing unit respectively; The concrete steps of described gasification process are as follows successively:
Step 1), during work, vaporized chemical enters the thermophore in A group accumulation of heat impurity removing unit and obtains preheating, then successively by the strainer of A group, crust block device enters gasification reaction unit, now vaporized chemical can remain in A set filter before blowback cleaning, ash content in crust block device and carbonaceous particles, and enter gasification reaction unit along with vaporized chemical, react with the vaporising fuel spraying into gasification reaction unit generating gasification of meeting, slag is discharged from the cinder notch of gasification reaction unit, the synthetic gas produced after gasification sprays into the crust block device in B group accumulation of heat impurity removing unit through B group technique nozzle, the slag of the molten in B group crust block device entrained by synthetic gas is cooled, temperature drops to below the texturing temperature DT of ash content, then B set filter is entered, ash content contained in synthetic gas and unreacted carbon granule is completely filtered in B set filter, clean synthetic gas is through the accumulation of heat of B group thermophore, discharge from the outlet of B group thermophore after reducing temperature,
Step 2), after work for some time, treat that thermophore accumulation of heat in B group accumulation of heat impurity removing unit is close to saturated, stop the supply of A group vaporized chemical, vaporized chemical changes into and entering from B group accumulation of heat impurity removing unit, vaporized chemical enters the thermophore of B group and obtains preheating, then successively by the strainer of B group, crust block device enters gasification reaction unit, now vaporized chemical can remain in B set filter before blowback cleaning, ash content in crust block device and carbonaceous particles, and enter gasification reaction unit along with vaporized chemical, react with the vaporising fuel spraying into gasification reaction unit generating gasification of meeting, slag is discharged from the cinder notch of gasification reaction unit, the synthetic gas produced after gasification sprays into the crust block device in A group accumulation of heat impurity removing unit through A group technique nozzle, the slag of the molten in A group crust block device entrained by synthetic gas is cooled, temperature drops to below the texturing temperature DT of ash content, then A set filter is entered, ash content contained in synthetic gas and unreacted carbon granule are completely filtered in the filter, clean synthetic gas is through the accumulation of heat of A group thermophore, discharge from the outlet of A group thermophore after reducing temperature,
Step 3), after work for some time, treats that thermophore accumulation of heat in A group accumulation of heat impurity removing unit is close to saturated, the supply of stopping B group vaporized chemical, and vaporized chemical changes into and entering from A group accumulation of heat impurity removing unit, repeating step 1) and 2) operation, continuous seepage synthetic gas.
The present invention arranges gasification reaction unit, and vaporized chemical and vaporising fuel carry out being oxidized and gasification reaction at gasification reaction unit, generates raw gas; Arrange crust block device, the liquid residue after coal gasification carries out collecting and lowering the temperature at crust block device, and liquid slag is down to below texturing temperature; Arrange strainer, the dust carried in raw gas and uncollected solid slag will be filtered completely, and after strainer, raw gas dustiness has reached subsequent technique service requirements; Thermophore is set, mainly realize the heat exchange of raw gas and vaporized chemical, high temperature rough gas flows through thermophore temperature and is reduced to less than 300 DEG C, and heat is stored in thermophore, normal temperature vaporized chemical flows through heat storage device vaporized chemical and is heated to more than 900 DEG C, and thermophore transmission ofenergy is to vaporized chemical.
Gasification reaction unit (i.e. gasifying reactor) arranges two groups of process burners, one group is that gasifying medium sprays into burner, other one group is that gasification product discharges burner, two groups of burners are according to technical process alternate run, be that gasifying medium sprays into burner in this step of reaction, next step of reaction is that gasification product discharges burner.Simultaneously crust block device, strainer and thermophore all arrange two groups, by the alternate run of two groups of devices, realize accumulation of heat when a thermophore raw gas flows through, another thermophore vaporized chemical by time heat release process.The vaporized chemical that such guarantee passes into gasification reaction unit is all more than 900 DEG C high temperature, and syngas outlet temperature below 300 DEG C, thus improves CO, H in the raw gas of gasification reaction
2, CH
4content, has not only increased substantially cold gas efficiency and caloric power of gas, possessed very high efficiency of carbon conversion, and outlet coal gas is low temperature, clean dustless coal gas, eliminates the follow-up waste heat boiler of traditional coal gasifying process and coal gas dust removal treating plant.
Vaporized chemical of the present invention is air, a kind of in the pure oxygen of the oxygen enrichment of oxygen level more than 21 ~ 90%, oxygen level 100%, water vapor, carbonic acid gas or appoint several mixtures; Described vaporising fuel is the mixture of any one or several in all carbonaceous materials such as coal dust, petroleum coke powder, biological particles, mud.
Described crust block device can adopt heat-storing material to make, and the crust block pipe of boiler industry also can be adopted to make; Described strainer can be one or several molectron of the high-temperature gas filters such as the strainer made of granular-bed filter, metal felt or sintered metal mesh, described thermophore can be honeycomb ceramic heat accumulator, also can be the heat storage that other heat-storing materials are made.
Biological particles is mixed with in coal dust of the present invention.
Vaporized chemical of the present invention enters temperature in gasification reaction unit preferably more than 900 DEG C; Clean synthetic gas through thermophore accumulation of heat, reduce temperature after the temperature of discharging from the outlet of thermophore preferably below 150 DEG C.
In sum, the beneficial effect that the present invention has is: first, and the present invention arranges two groups of technique nozzles by gasification reaction unit, often organizes nozzle and connects crust block device, strainer and thermophore respectively, two groups of process burners alternately spray into vaporized chemical and vaporising fuel, ejection raw gas.The one group of thermophore flowing through high temperature rough gas makes raw gas lower the temperature in accumulation of heat, and the one group of thermophore flowing through vaporized chemical makes vaporized chemical heat up in heat release.By improving gasification agent temperature with upper type, reducing raw gas temperature, thus increase substantially the cold gas efficiency of raw gas, and improve the composition of available gas in synthetic gas (carbon monoxide, hydrogen).
Secondly, the synthetic gas utilizing gasification process of the present invention to produce is for through dedusting, clean coal gas, also the coal gas after accumulation of heat, cooling is through, therefore the synthetic gas that gasification reaction unit of the present invention is discharged is high heating value, low temperature, clean synthetic gas, waste heat boiler follow-up in conventional pulverized coal gasifying process, purified synthesis gas device can be save, significantly simplify technical process, reduce the cost of equipment, possess fairly obvious economic benefit.
Again, utilize gasification process of the present invention to produce synthetic gas, possess very high efficiency of carbon conversion.Because the flying dust of synthetic gas is exporting through metre filter, unreacted completely carbon granule is filtered, and in circulation next time, these carbon granules are again blown into gasification reaction unit and are reacted fully, and residue is fallen in slag bath by its cinder notch.In addition, owing to have employed high temperature gasification agent gasification, in vapourizing furnace, initial reaction stage temperature is very high, is also very beneficial for the carbon granule of activity compared with lower part to transform completely.Therefore, gasification process of the present invention possesses very high efficiency of carbon conversion (>99.9%).
In addition, the present invention can obtain clean raw gas, low temperature or normal temperature raw gas; Meanwhile, strainer, crust block device also have certain heat accumulation function.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention.
Embodiment
Preferred embodiment of the present invention is provided, to describe technical scheme of the present invention in detail below in conjunction with Figure of description.
embodiment 1
Heat accumulating type fine coal entrained flow gasification method as shown in Figure 1, its system used is by gasification reaction unit, and two groups of crust block devices, strainer and thermophore form.The two ends of gasification reaction unit connect one group of crust block device, strainer and thermophore respectively successively.
Gasification reaction unit is the main reactor of high temperature air gasification reaction, vaporized chemical and carbonaceous fuel react after gasifying reactor one end technique nozzle passes into reactor, discharge gasifying reactor by the other end technique nozzle after completion of the reaction, two groups of process burner functions are exchanged in next process cycle technique.
Crust block device is carbonaceous fuel liquid slag slag collector, and slag is down to below texturing temperature from liquid state.Strainer is for fall all impurity, filtering dust, and it can adopt the material such as wire cloth or metal felt to make.Thermophore for high temperature rough gas gas heat is passed to normal temperature air, high temperature rough gas through time, thermophore heat absorption reduces raw gas temperature, treats to switch through flow process after a while, and normal temperature vaporized chemical is through thermophore, and thermophore release of heat carrys out heat air agent.
embodiment 2
The following examples, by preparing the specific embodiment of high heating value raw gas in conjunction with coal gasification, are further described the present invention.
Step 1: the gasifying reactor of gasification reaction unit is through lighting a fire, being warmed up to suitable temp.
Step 2: vaporized chemical enters gasifying reactor successively after A group thermophore, strainer and crust block device, coal dust also sprays into gasifying reactor from A group process burner, and in gasifying reactor, vaporized chemical and coal dust start to carry out coal gasification reaction.The high temperature rough gas of 1100 ~ 1300 DEG C generated is discharged from B group technique nozzle, and successively through B group crust block device, strainer and thermophore, the raw gas temperature of discharging after the heat exchange of thermophore at regenerator unit is below 150 DEG C.
Step 3: stop spraying into vaporized chemical and coal dust from A group process burner, pass into water vapor or rare gas element from B group gas exit, replaces the raw gas in B group pipeline and equipment.
Step 4: vaporized chemical rises to 900 ~ 1300 DEG C from temperature after B group thermophore, strainer and crust block device, and enter gasifying reactor, coal dust also sprays into gasifying reactor from B group process burner, and in gasifying reactor, vaporized chemical and coal dust start to carry out coal gasification reaction.The high temperature rough gas of 1100 ~ 1300 DEG C generated is discharged from A group technique nozzle, and successively through A group crust block device, strainer and thermophore, the raw gas temperature of discharging after the heat exchange of thermophore is below 150 DEG C.
Step 5: stop spraying into vaporized chemical and coal dust from B group process burner, pass into water vapor or rare gas element from A group gas exit, replaces the raw gas in A group pipeline and equipment.
Step 6: repeating step 2 is to step 5, and system is normally run.
embodiment 3
The following examples will prepare the another kind of method specific embodiment of high heating value raw gas in conjunction with coal gasification, be further described the present invention.
Step 1: the gasifying reactor of gasification reaction unit is through lighting a fire, being warmed up to suitable temp.
Step 2: air enters gasifying reactor successively after A group thermophore, strainer and crust block device, coal dust also sprays into gasifying reactor from A group process burner, and in gasifying reactor, air and coal dust start to carry out the reaction of fine coal oxidizing fire.The high-temperature flue gas of 1100 ~ 1300 DEG C generated is discharged from B group technique nozzle, successively through B group crust block device, strainer and thermophore, the raw gas temperature of discharging after the heat exchange of thermophore is below 120 DEG C, and this process Main Function is heating B group thermophore, and flue gas is emptying.
Step 3: stop spraying into vaporized chemical and coal dust from A group process burner, water vapor is passed into from B group gas exit, water vapour temperature after thermophore, strainer and crust block device rises to 900 ~ 1300 DEG C, enter gasifying reactor, coal dust also sprays into gasifying reactor from B group process burner, and in gasifying reactor, water vapour and coal dust start to carry out coal gasification reaction.The high temperature rough gas of 1100 ~ 1300 DEG C generated is discharged from A group technique nozzle, and successively through A group crust block device, strainer and thermophore, the raw gas temperature of discharging after the heat exchange of thermophore is below 120 DEG C.
Step 4: stop spraying into water vapour and coal dust from B group process burner, pass into water vapor or rare gas element from A group gas exit, replaces the raw gas in A group pipeline and equipment.
Step 5: repeating step 2 is to step 4, and system is normally run.
Claims (4)
1. a heat accumulating type fine coal entrained flow gasification method, it is characterized in that, this gasification process system used comprises gasification reaction unit, A group accumulation of heat impurity removing unit and B group accumulation of heat impurity removing unit, and A, B group accumulation of heat impurity removing unit is by crust block device, strainer and the thermophore composition connected successively; Be provided with A, B two groups of technique nozzles in gasification reaction unit, be connected with the crust block device in A group and B group accumulation of heat impurity removing unit respectively; The concrete steps of described gasification process are as follows successively:
Step 1), during work, vaporized chemical enters the thermophore in A group accumulation of heat impurity removing unit and obtains preheating, then successively by the strainer of A group, crust block device enters gasification reaction unit, now vaporized chemical can remain in A set filter before blowback cleaning, ash content in crust block device and carbonaceous particles, and enter gasification reaction unit along with vaporized chemical, react with the vaporising fuel spraying into gasification reaction unit generating gasification of meeting, slag is discharged from the cinder notch of gasification reaction unit, the synthetic gas produced after gasification sprays into the crust block device in B group accumulation of heat impurity removing unit through B group technique nozzle, the slag of the molten in B group crust block device entrained by synthetic gas is cooled, temperature drops to below the texturing temperature DT of ash content, then B set filter is entered, ash content contained in synthetic gas and unreacted carbon granule is completely filtered in B set filter, clean synthetic gas is through the accumulation of heat of B group thermophore, discharge from the outlet of B group thermophore after reducing temperature,
Step 2), after work for some time, treat that thermophore accumulation of heat in B group accumulation of heat impurity removing unit is close to saturated, stop the supply of A group vaporized chemical, vaporized chemical changes into and entering from B group accumulation of heat impurity removing unit, vaporized chemical enters the thermophore of B group and obtains preheating, then successively by the strainer of B group, crust block device enters gasification reaction unit, now vaporized chemical can remain in B set filter before blowback cleaning, ash content in crust block device and carbonaceous particles, and enter gasification reaction unit along with vaporized chemical, react with the vaporising fuel spraying into gasification reaction unit generating gasification of meeting, slag is discharged from the cinder notch of gasification reaction unit, the synthetic gas produced after gasification sprays into the crust block device in A group accumulation of heat impurity removing unit through A group technique nozzle, the slag of the molten in A group crust block device entrained by synthetic gas is cooled, temperature drops to below the texturing temperature DT of ash content, then A set filter is entered, ash content contained in synthetic gas and unreacted carbon granule are completely filtered in the filter, clean synthetic gas is through the accumulation of heat of A group thermophore, discharge from the outlet of A group thermophore after reducing temperature,
Step 3), after work for some time, treats that thermophore accumulation of heat in A group accumulation of heat impurity removing unit is close to saturated, the supply of stopping B group vaporized chemical, and vaporized chemical changes into and entering from A group accumulation of heat impurity removing unit, repeating step 1) and 2) operation, continuous seepage synthetic gas.
2. heat accumulating type fine coal entrained flow gasification method according to claim 1, it is characterized in that, described vaporized chemical is air, a kind of in the pure oxygen of the oxygen enrichment of oxygen level 21 ~ 90%, oxygen level 100%, water vapor, carbonic acid gas or appoint several mixtures; Described vaporising fuel is the mixture of any one or several in coal dust, petroleum coke powder, biological particles, mud.
3. heat accumulating type fine coal entrained flow gasification method according to claim 1, is characterized in that, described crust block device adopts heat-storing material to make or adopt the crust block pipe of boiler industry to make; Described strainer is one or several molectron in the strainer made of granular-bed filter, metal felt or sintered metal mesh, and described thermophore is honeycomb ceramic heat accumulator.
4. heat accumulating type fine coal entrained flow gasification method according to claim 1 and 2, is characterized in that, vaporized chemical enters temperature in gasification reaction unit more than 900 DEG C; Clean synthetic gas through thermophore accumulation of heat, reduce temperature after the temperature of discharging from the outlet of thermophore below 150 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410028175.3A CN103756730B (en) | 2014-01-22 | 2014-01-22 | Heat accumulating type powdered coal entrained bed gasification method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410028175.3A CN103756730B (en) | 2014-01-22 | 2014-01-22 | Heat accumulating type powdered coal entrained bed gasification method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103756730A CN103756730A (en) | 2014-04-30 |
| CN103756730B true CN103756730B (en) | 2015-02-04 |
Family
ID=50524060
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410028175.3A Active CN103756730B (en) | 2014-01-22 | 2014-01-22 | Heat accumulating type powdered coal entrained bed gasification method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103756730B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105694975A (en) * | 2014-11-27 | 2016-06-22 | 琳德股份公司 | Improved gasification technology |
| CN105779007B (en) * | 2016-03-25 | 2019-02-01 | 北京澳柯清洁煤气工程技术有限公司 | The method that the flyash utilized that has surplus heat regasifies into coal gas |
| CN107176464B (en) * | 2017-05-27 | 2018-10-26 | 鲁西化工集团股份有限公司 | A kind of fine coal pressurization fluidization conveying device |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4199327A (en) * | 1978-10-30 | 1980-04-22 | Kaiser Engineers, Inc. | Process for gasification of coal to maximize coal utilization and minimize quantity and ecological impact of waste products |
| CN1587354A (en) * | 2004-07-06 | 2005-03-02 | 杜三民 | Intermittent gas making method and device with bituminous coal fixing layer |
| CN101100607A (en) * | 2006-07-05 | 2008-01-09 | 中国科学院工程热物理研究所 | Coking technique using coal external burning to replace gas fuel burning |
| JP2008150463A (en) * | 2006-12-15 | 2008-07-03 | Mitsubishi Heavy Ind Ltd | Two-stage entrained bed gasification oven and method for controlling operation of the same |
| CN101629108A (en) * | 2008-07-20 | 2010-01-20 | 黄德夫 | Method for preparing coal gas through gasification of pulverized coal |
| CN102585905A (en) * | 2012-02-29 | 2012-07-18 | 湖北双环科技股份有限公司 | Bituminous coal fixed bed continuous gasification method |
| CN102888251A (en) * | 2012-09-17 | 2013-01-23 | 北京神雾环境能源科技集团股份有限公司 | Coal-based synthetic gas waste heat recovery system and method |
-
2014
- 2014-01-22 CN CN201410028175.3A patent/CN103756730B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4199327A (en) * | 1978-10-30 | 1980-04-22 | Kaiser Engineers, Inc. | Process for gasification of coal to maximize coal utilization and minimize quantity and ecological impact of waste products |
| CN1587354A (en) * | 2004-07-06 | 2005-03-02 | 杜三民 | Intermittent gas making method and device with bituminous coal fixing layer |
| CN101100607A (en) * | 2006-07-05 | 2008-01-09 | 中国科学院工程热物理研究所 | Coking technique using coal external burning to replace gas fuel burning |
| JP2008150463A (en) * | 2006-12-15 | 2008-07-03 | Mitsubishi Heavy Ind Ltd | Two-stage entrained bed gasification oven and method for controlling operation of the same |
| CN101629108A (en) * | 2008-07-20 | 2010-01-20 | 黄德夫 | Method for preparing coal gas through gasification of pulverized coal |
| CN102585905A (en) * | 2012-02-29 | 2012-07-18 | 湖北双环科技股份有限公司 | Bituminous coal fixed bed continuous gasification method |
| CN102888251A (en) * | 2012-09-17 | 2013-01-23 | 北京神雾环境能源科技集团股份有限公司 | Coal-based synthetic gas waste heat recovery system and method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103756730A (en) | 2014-04-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US10208948B2 (en) | Solid fuel grade gasification-combustion dual bed poly-generation system and method thereof | |
| US9410095B2 (en) | Method of gasification of biomass using gasification island | |
| CN101391746B (en) | Small-sized coal gasification hydrogen making method | |
| CN204400934U (en) | A kind of biomass gasification burning deep purifying device | |
| CN102146301A (en) | Method for two-stage coal gasification on composite external heat fixed bed and gas furnace | |
| CN102676229A (en) | Combined rotational flow bed gasification furnace | |
| CN103756730B (en) | Heat accumulating type powdered coal entrained bed gasification method | |
| CN101665724A (en) | Water-coal-slurry gasification method and gasification furnace | |
| JP5646966B2 (en) | Method and apparatus for producing gas mainly containing hydrogen | |
| MX2014007755A (en) | Biomass syngas purification process under positive pressure for producing oil and system configuration thereof. | |
| CN101570699B (en) | Gasification device for solid fuel and method for producing synthetic gas | |
| CN108774548A (en) | A kind of high temperature air steam gasification system and the method for producing high-quality synthesis gas | |
| CN105444180B (en) | A kind of refuse gasification boiler and its application process | |
| CN105441131B (en) | A kind of method of coal gasification lime-ash oxidation and decarbonization ash content coproduction steam | |
| CN106987279A (en) | A kind of U-shaped coal gasification reaction device of secondary separation slagging-off and the coal gasifying process that secondary separation slagging-off is carried out using the device | |
| CN107099337A (en) | A kind of U-shaped coal gasification reaction device and the technique for carrying out coal gasification using the device | |
| CN106947541A (en) | A kind of combined method and system based on low order pyrolysis of coal water vapour quenching water-gas hydrogen manufacturing | |
| CN103965966B (en) | A kind of dry powder pressurizing gasifying apparatus with treatment of Organic Wastewater | |
| CN105779020B (en) | A kind of raw gas purifying and waste heat recycling system and method | |
| CN108179029A (en) | A kind of cleaning Coal Gasification Technology of carbon cycle | |
| CN210711404U (en) | Pyrolysis-gasification integrated device | |
| KR101764302B1 (en) | Method and apparatus for removing tar in synthetic gas by using steel-making slag | |
| CN2167094Y (en) | Water gas generation furnace with up and low blower | |
| CN202595066U (en) | Combined-type rotating fluidized bed gasifier | |
| CN105623740B (en) | Clean coal gas preparation and preparation system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20190305 Address after: 311815 Dingqiao Village, Ciwu Town, Zhuji City, Shaoxing City, Zhejiang Province Patentee after: Zhejiang Asroad Highway Construction & Maintenance Machinery Co., Ltd. Address before: 310004 Room 106, Building 4, Building 1, No. 5, Third Road, Genshan Branch, Jianggan District, Hangzhou City, Zhejiang Province Patentee before: Hangzhou Quanhe Technology Co., Ltd. |
|
| TR01 | Transfer of patent right |