CN103695040A - Technological process for technology of preparing coal chemical chain oxygen carrier to synthesis gas - Google Patents
Technological process for technology of preparing coal chemical chain oxygen carrier to synthesis gas Download PDFInfo
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- CN103695040A CN103695040A CN201310745124.8A CN201310745124A CN103695040A CN 103695040 A CN103695040 A CN 103695040A CN 201310745124 A CN201310745124 A CN 201310745124A CN 103695040 A CN103695040 A CN 103695040A
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- oxygen carrier
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- oxygen
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 89
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 89
- 239000001301 oxygen Substances 0.000 title claims abstract description 89
- 239000007789 gas Substances 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims abstract description 36
- 239000003245 coal Substances 0.000 title claims abstract description 32
- 230000008569 process Effects 0.000 title claims abstract description 31
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 16
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 16
- 238000005516 engineering process Methods 0.000 title abstract description 17
- 239000000126 substance Substances 0.000 title abstract description 13
- 238000006243 chemical reaction Methods 0.000 claims abstract description 31
- 238000002309 gasification Methods 0.000 claims abstract description 24
- 239000002817 coal dust Substances 0.000 claims abstract description 14
- 239000004381 Choline salt Substances 0.000 claims abstract description 10
- 230000008929 regeneration Effects 0.000 claims abstract description 10
- 238000011069 regeneration method Methods 0.000 claims abstract description 10
- 230000001172 regenerating effect Effects 0.000 claims description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 29
- 239000002918 waste heat Substances 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 9
- 239000008234 soft water Substances 0.000 claims description 8
- 230000009719 regenerative response Effects 0.000 claims description 7
- 238000009826 distribution Methods 0.000 claims description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 239000000376 reactant Substances 0.000 claims description 4
- 238000011084 recovery Methods 0.000 claims description 4
- 239000002912 waste gas Substances 0.000 claims description 4
- 235000014171 carbonated beverage Nutrition 0.000 claims description 3
- 239000011343 solid material Substances 0.000 claims description 3
- 230000005587 bubbling Effects 0.000 claims description 2
- PFRWMMTZXJJCTP-UHFFFAOYSA-L calcium hydrogen sulfate hydrate Chemical compound O.S([O-])(O)(=O)=O.[Ca+2].S([O-])(O)(=O)=O PFRWMMTZXJJCTP-UHFFFAOYSA-L 0.000 claims description 2
- 239000010883 coal ash Substances 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 229910052717 sulfur Inorganic materials 0.000 abstract description 5
- 239000011593 sulfur Substances 0.000 abstract description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 4
- 239000002245 particle Substances 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 238000005243 fluidization Methods 0.000 abstract description 2
- 230000007423 decrease Effects 0.000 abstract 1
- 230000004927 fusion Effects 0.000 abstract 1
- 230000001737 promoting effect Effects 0.000 abstract 1
- 239000000446 fuel Substances 0.000 description 8
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- 239000000969 carrier Substances 0.000 description 4
- 238000002407 reforming Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 239000002956 ash Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- -1 and after heating Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910052755 nonmetal Inorganic materials 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 101150091813 shfl gene Proteins 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
Images
Classifications
-
- 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
- Y02P20/10—Process efficiency
-
- 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
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a technological process for a technology of preparing a coal chemical chain oxygen carrier to synthesis gas. In the process, coal is not directly contacted with air; vapor is adopted as a fluidization and gasification medium; the transfer of oxygen and heat is realized through the circular conversion of oxygen carrier particles between a gasification furnace R1001 and a regeneration furnace R1002; then the gasification reaction of not contacting the coal dust with the air is finished. Main equipment of the complete technological process comprises the gasification furnace R1001, the regeneration furnace R1002, a return valve L1001, cyclone separators (X1001, X1002), afterheat recoverers (E1001, E1002) and the like. The process avoids or reduces the conversion of sulfur in the coal to sulfurous gas, and decreases the emission of Sox. The technology of preparing the coal chemical chain oxygen carrier to the synthesis gas adapts to coal types with high sulfur, high ash specification and high ash fusion point in China, can reduce the gasification energy consumption and improve the economic benefit, and is a gasification technology worthy of promoting.
Description
Technical field
Patent of the present invention relates to gasification field, relates to the technical process that a kind of coal chemistry chain oxygen carrier is prepared synthetic gas.
Background technology
The eighties in 20th century, Germany scientist Richter etc. propose the concept of burning chemistry chains, and this technology has very high capacity usage ratio, there is no NO
xdischarge Deng pollutent.Chemical chain burning technology is that traditional combustion reactions is decomposed into two chemical reactions: the reduction reaction that the oxygen carrier reaction that the oxygen carrier of reduction-state carries out in air and the oxygen carrier of oxidation state carry out in geseous fuel.The oxygen carrier reaction that cycle alternation carries out under oxidation and two kinds of atmosphere of reduction, realizes the transfer of oxygen and the burning of fuel.Chemical chain reforming hydrogen producing technology (CLR), the hydrogen production of chemical chain process (CLH) of water vapour replacement air, mixed firing-gasification hydrogen production of chemical chain technology (HLG) that the fire coal of take is fuel on the basis of chemical chain burning technology, have been developed again.In recent years, the whole world is prepared synthetic gas technical study to chemical chain oxygen carrier and is comparatively paid close attention to, it is low that this technology has cost of investment, applied range (as coal, chemical industry and power industry etc.), applicable coal many (the especially coals of high-sulfur, ash-rich, high ash melting point), while energy consumption is low, pollute the advantages such as little.([1]Ryden?M，Lyngfelt?A，Mattisson?T.Synthesis?gas?generation?by?chemical-looping?reforming?in?a?continuously?operating?laboratory?reactor[J].Fue1，2006，85(12/13)：1631-1641.[2]Luis?F.de?Diego，Ortiz?M，García-Labiano?F，et?al.Synthesis?gas?generation?by?chemical-looping?reforming?using?a?Ni-based?oxygen?carriers[J].Energy?Procedia，2009，1(1)：3-10.[3]Ortiz?M，Luis?F.de?Diego，Abad?A，et?al.Hydrogen?production?by?auto-thermal?chemical-looping?reforming?in?a?pressurized?fluidized?bed?reactor?using?Ni-based?oxygen?carriers[J].Hydrogen?Energy，2010，35(1)：151-160.)
Carry out coal chemistry chain oxygen carrier and prepare the research of synthetic gas technology, optimize and be applicable to the oxygen carrier that coal chemistry chain oxygen carrier is prepared synthetic gas technology, accumulation coal chemistry chain oxygen carrier is prepared synthetic gas technical experience, significant for exploitation Coal Gasification Technology efficient, super clean feature.
Chemical chain gasification (chemical looping gasification, CLG) technology, be to utilize metal or nonmetal oxide to provide gasification required oxygen element to fuel, the ratio by control lattice oxygen/fuel obtains take the synthetic gas that H2 and CO be main component.Chemical chain gasification system comprises two reactors: vapourizing furnace and regeneratory furnace.Oxygen carrier reacts with airborne oxygen in regeneratory furnace, obtains lattice oxygen; In vapourizing furnace, with fuel reaction, provide gasification reaction requisite oxygen.
Summary of the invention
The object of the present invention is to provide a kind of coal chemistry chain oxygen carrier to prepare the technical process of synthetic gas technology, coal is not directly contacted with air in gasification, but adopt water vapour as fluidisation and gasifying medium, circulation by oxygen carrier granule between vapourizing furnace and regeneratory furnace transforms the transmission that realizes oxygen and heat, completes the discontiguous gasification reaction of solid fuel and air.
For achieving the above object, the technical solution used in the present invention is:
For coal chemistry chain oxygen carrier, prepare a synthesis gas process flow process, its principal character is:
A certain amount of coal dust and oxygen carrier are sent into vapourizing furnace R1001 from vapourizing furnace R1001 middle part, and a certain amount of water vapor enters vapourizing furnace R1001 reaction zone through vapourizing furnace R1001 bottom air compartment, air distribution plate and reacts with coal dust, oxygen carrier;
The crude synthesis gas that vapourizing furnace R1001 generates is sent into the separated coal ash of 1# cyclonic separator X1001 and partial crushing oxygen carrier by syngas outlet pipe, after dedusting, synthetic gas is sent into lower procedure after synthetic gas waste-heat recoverer E1001 reclaims heat, and synthetic gas waste-heat recoverer E1001 reclaims heat in order to thermal regeneration stove R1002 water wall soft water;
Oxygen carrier after vapourizing furnace R1001 oxygen loss enters after returning charge valve L1001 through vapourizing furnace R1001 reaction chamber middle part revert pipe, send into regeneratory furnace R1002 and carry out regenerative response, air is through regeneratory furnace R1002 bottom air compartment, air distribution plate enters in regeneratory furnace and carries out regenerative response with oxygen carrier, after regeneration, oxygen carrier carries out gas solid separation through the air conveying 2# of sending into cyclonic separator X1002, solid materials returns to vapourizing furnace R1001 and carries out gasification reaction, gas material is used for thermal regeneration stove R1002 reaction required air through waste gas residual heat withdrawer E1002 recovery waste heat, tail gas high altitude discharge, regenerative response is emitted a large amount of heat, regeneratory furnace R1002 is designed to water wall structure, a certain amount of soft water enters regeneratory furnace R1002 water wall and further heats by after the separation of drum E1003 carbonated drink after synthetic gas waste-heat recoverer E1001, water vapour is sent into vapourizing furnace R1001 and is done fluidized gas and reactant.
Further, described vapourizing furnace R1001 is bubbling fluidized bed, and the reaction between oxygen carrier, coal dust, water vapour occurs in stove, and temperature of reaction is 960-1000 ℃, and pressure is 0.1-0.3MPa, with calcium sulphate oxygen carrier, and its principal reaction:
CaSO
4+C→CaS+CO
H
2O+C→H
2+CO
H
2O+CO→H
2+CO
2；
Regeneratory furnace R1002 is fast bed, and reacting between oxygen carrier and oxygen occurs in stove, and temperature of reaction is 1100-1200 ℃, and pressure is 0.1-0.3MPa, and principal reaction is:
CaS+2O
2→CaSO
4。
Further, described vapourizing furnace R1001 charging is oxygen carrier, coal dust, water vapour, in vapourizing furnace R1001 charging oxygen carrier, the molar ratio of oxygen and carbon content in coal is: 0.5-1.5: 1, in water vapour, the molar ratio computing of oxygen element and carbon content in coal element is 0.5-1.25: 1, and the median size of oxygen carrier and coal dust is 0.15mm.
Further, described oxygen carrier is CaSO
4oxygen carrier.
Further, the feeding temperature of described vapourizing furnace water vapour is 500-600 ℃, and the feeding temperature of vapourizing furnace coal dust and oxygen carrier is normal temperature, and the feeding temperature of regeneratory furnace air is 25-200 ℃.
Advantage of the present invention is: recycling as gasification provides oxygen element of oxygen carrier, save process prepared by pure oxygen, and saved preparation cost; The heat that oxygen carrier generation oxidizing reaction is emitted in regeneratory furnace is brought back vapourizing furnace, for the gasification of fuel provides heat, can reduce energy loss, without external heat, just can make gasification reaction continue to carry out.By to the improvement of this technique oxygen carrier used (patent: a kind ofly suppress the method for preparing oxygen carrier particles that sulfurous gas discharges, CN201010254752.2), can play the effect of furnace sulfur fixation, reduce the discharge of sulfurous gas, avoid the pollution to environment.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention.
Fig. 2 is that soft water is through the schematic diagram of regeneratory furnace and drum separation.
Embodiment
Below in conjunction with accompanying drawing to further illustrating.By being prepared by coal chemistry chain oxygen carrier to the simulation of synthetic gas technical matters flow process, with the device of the scale in 24 tons of coal/skies, set forth.
The present invention is that a kind of coal chemistry chain oxygen carrier is prepared synthesis gas process flow process: vapourizing furnace R1001 charging is oxygen carrier (1t/h), coal dust (0.97t/h), water vapour (0.63t/h, 0.3MPa, 500 ℃), wherein water vapour enters in vapourizing furnace R1001 through vapourizing furnace bottom air distribution plate, do reactant, do again fluidized gas; Regeneratory furnace R1002 charging is air (1553Nm
3/ h, 25 ℃, 0.2MPa), through regeneratory furnace R1002 bottom, air distribution plate enters in regeneratory furnace.
The oxygen carrier of certain particle size adds in vapourizing furnace R1001 and reacts, reacted oxygen carrier enters in returning charge valve L1001 through vapourizing furnace R1001 middle part returning charge mouth, fluidized gas (water vapour 0.2Mpa in returning charge valve L1001, 500 ℃) send into regeneratory furnace R1002, in regeneratory furnace R1002, there is the regenerative response of oxygen carrier and airborne oxygen, oxygen carrier after regeneration is through the air conveying 2# cyclonic separator X1002 that enters, solid materials after cyclonic separator X1002 separation enters in vapourizing furnace R1001, waste gas after 2# cyclonic separator X1002 separation enters waste gas residual heat withdrawer E1002 recovery waste heat, heat enters stove air for thermal regeneration stove R1002, discharge in tail gas after cooling (being mainly nitrogen) high-altitude.
Synthetic gas (0.1Mpa, 1000 ℃, gaseous constituent: CO43.7%, H that vapourizing furnace R1001 generates
247.7%, CO
210.43%, mol ratio) after entering 1# cyclonic separator X1001 dedusting, synthetic gas outlet pipe enters synthetic gas waste-heat recoverer E1001 recovery waste heat; Synthetic gas waste-heat recoverer E1001 heat-eliminating medium is soft water, and after heating, soft water is sent into the water wall of regeneratory furnace R1002; Regeneratory furnace R1002 is water wall structure, can make full use of system thermal.The flow process of regeneratory furnace R1002 water is: certain flow normal temperature soft water enters synthetic gas waste-heat recoverer E1001, as shown in Figure 2, send into regeneratory furnace R1002 water wall and carry out carbonated drink separation by drum E1003, institute's Separation of Water steam enters vapourizing furnace R1001 and returning charge valve L1001 continues to be utilized as reactant or fluidized gas.Returning charge valve L1001 is loop seal, take water vapour as fluidizing medium.
As shown in table 1, it is as follows that 24 tons of/day coal chemistry chain oxygen carriers are prepared synthesis gas process flowsheeting result.
24 tons of/day coal chemistry chain oxygen carriers of table 1 are prepared synthesis gas process flowsheeting result
This technical process tool has the following advantages: recycling as gasification provides oxygen element of oxygen carrier, save process prepared by pure oxygen, and saved preparation cost; The heat that oxygen carrier generation oxidizing reaction is emitted in regeneratory furnace is brought back vapourizing furnace, for the gasification of fuel provides heat, can reduce energy loss, without external heat, just can make gasification reaction continue to carry out.By the improvement to this technique oxygen carrier used, can play the effect of furnace sulfur fixation, reduced the discharge of sulfurous gas, avoided the pollution to environment.
Claims (5)
1. for coal chemistry chain oxygen carrier, prepare a synthesis gas process flow process, it is characterized in that:
A certain amount of coal dust and oxygen carrier are sent into vapourizing furnace R1001 from vapourizing furnace R1001 middle part, and a certain amount of water vapor enters vapourizing furnace R1001 reaction zone through vapourizing furnace R1001 bottom air compartment, air distribution plate and reacts with coal dust, oxygen carrier;
The crude synthesis gas that vapourizing furnace R1001 generates is sent into the separated coal ash of 1# cyclonic separator X1001 and partial crushing oxygen carrier by syngas outlet pipe, after dedusting, synthetic gas is sent into lower procedure after synthetic gas waste-heat recoverer E1001 reclaims heat, and synthetic gas waste-heat recoverer E1001 reclaims heat in order to thermal regeneration stove R1002 water wall soft water;
Oxygen carrier after vapourizing furnace R1001 oxygen loss enters after returning charge valve L1001 through vapourizing furnace R1001 reaction chamber middle part revert pipe, send into regeneratory furnace R1002 and carry out regenerative response, air is through regeneratory furnace R1002 bottom air compartment, air distribution plate enters in regeneratory furnace and carries out regenerative response with oxygen carrier, after regeneration, oxygen carrier carries out gas solid separation through the air conveying 2# of sending into cyclonic separator X1002, solid materials returns to vapourizing furnace R1001 and carries out gasification reaction, gas material is used for thermal regeneration stove R1002 reaction required air through waste gas residual heat withdrawer E1002 recovery waste heat, tail gas high altitude discharge, regenerative response is emitted a large amount of heat, regeneratory furnace R1002 is designed to water wall structure, a certain amount of soft water enters regeneratory furnace R1002 water wall and further heats by after the separation of drum E1003 carbonated drink after synthetic gas waste-heat recoverer E1001, water vapour is sent into vapourizing furnace R1001 and is done fluidized gas and reactant.
2. according to claim 1ly a kind ofly for coal chemistry chain oxygen carrier, prepare synthesis gas process flow process, it is characterized in that: described vapourizing furnace R1001 is bubbling fluidized bed, in stove, there is the reaction between oxygen carrier, coal dust, water vapour, temperature of reaction is 960-1000 ℃, pressure is 0.1-0.3MPa, with calcium sulphate oxygen carrier, its principal reaction:
CaSO
4+C→CaS+CO
H
2O+C→H
2+CO
H
2O+CO→H
2+CO
2；
Regeneratory furnace R1002 is fast bed, and reacting between oxygen carrier and oxygen occurs in stove, and temperature of reaction is 1100-1200 ℃, and pressure is 0.1-0.3MPa, and principal reaction is:
CaS+2O
2→CaSO
4。
3. according to claim 1ly a kind ofly for coal chemistry chain oxygen carrier, prepare synthesis gas process flow process, it is characterized in that: described vapourizing furnace R1001 charging is oxygen carrier, coal dust, water vapour, in vapourizing furnace R1001 charging oxygen carrier, the molar ratio of oxygen and carbon content in coal is: 0.5-1.5: 1, in water vapour, the molar ratio computing of oxygen element and carbon content in coal element is 0.5-1.25: 1, and the median size of oxygen carrier and coal dust is 0.15mm.
4. according to claim 1ly a kind ofly for coal chemistry chain oxygen carrier, prepare synthesis gas process flow process, it is characterized in that: described oxygen carrier is CaSO
4oxygen carrier.
5. according to claim 1ly a kind ofly for coal chemistry chain oxygen carrier, prepare synthesis gas process flow process, it is characterized in that: the feeding temperature of described vapourizing furnace water vapour is 500-600 ℃, the feeding temperature of vapourizing furnace coal dust and oxygen carrier is normal temperature, and the feeding temperature of regeneratory furnace air is 25-200 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310745124.8A CN103695040A (en) | 2013-12-17 | 2013-12-17 | Technological process for technology of preparing coal chemical chain oxygen carrier to synthesis gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310745124.8A CN103695040A (en) | 2013-12-17 | 2013-12-17 | Technological process for technology of preparing coal chemical chain oxygen carrier to synthesis gas |
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|---|---|
| CN103695040A true CN103695040A (en) | 2014-04-02 |
Family
ID=50356710
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104560211A (en) * | 2015-01-22 | 2015-04-29 | 兖矿集团有限公司 | Gasification furnace |
| CN107435952A (en) * | 2017-09-13 | 2017-12-05 | 兖矿集团有限公司 | A kind of energy-saving environment protection fire coal cooking and heating furnace and cooking heating method and purposes |
| CN107619694A (en) * | 2017-11-02 | 2018-01-23 | 兖矿集团有限公司 | A kind of digestion system and method for preparing ultra-clean coal |
| CN109355108A (en) * | 2018-09-18 | 2019-02-19 | 华中科技大学 | A kind of Photospot solar gasified bio-matter system of synthesis gas preparation and metal smelt |
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| CN101216175A (en) * | 2007-11-23 | 2008-07-09 | 东南大学 | Oxygen carrier gasifying combustion method for loading oxygen and device |
| CN101962575A (en) * | 2010-09-18 | 2011-02-02 | 青岛科技大学 | Method and device for preparing synthesis gas by coal particle/oxygen carrier chemical chain |
| US20110024687A1 (en) * | 2006-09-21 | 2011-02-03 | Eltron Research & Development, Inc. | Cyclic catalytic upgrading of chemical species using metal oxide materials |
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2013
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20110024687A1 (en) * | 2006-09-21 | 2011-02-03 | Eltron Research & Development, Inc. | Cyclic catalytic upgrading of chemical species using metal oxide materials |
| CN101216175A (en) * | 2007-11-23 | 2008-07-09 | 东南大学 | Oxygen carrier gasifying combustion method for loading oxygen and device |
| CN101962575A (en) * | 2010-09-18 | 2011-02-02 | 青岛科技大学 | Method and device for preparing synthesis gas by coal particle/oxygen carrier chemical chain |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104560211A (en) * | 2015-01-22 | 2015-04-29 | 兖矿集团有限公司 | Gasification furnace |
| CN107435952A (en) * | 2017-09-13 | 2017-12-05 | 兖矿集团有限公司 | A kind of energy-saving environment protection fire coal cooking and heating furnace and cooking heating method and purposes |
| CN107619694A (en) * | 2017-11-02 | 2018-01-23 | 兖矿集团有限公司 | A kind of digestion system and method for preparing ultra-clean coal |
| CN107619694B (en) * | 2017-11-02 | 2023-12-08 | 山东能源集团有限公司 | Digestion system and method for preparing ultra-clean coal |
| CN109355108A (en) * | 2018-09-18 | 2019-02-19 | 华中科技大学 | A kind of Photospot solar gasified bio-matter system of synthesis gas preparation and metal smelt |
| CN109355108B (en) * | 2018-09-18 | 2020-02-21 | 华中科技大学 | Concentrating solar gasification biomass system for synthesis gas preparation and metal smelting |
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Application publication date: 20140402 |