CN101962575A - Method and device for preparing synthesis gas by coal particle/oxygen carrier chemical chain - Google Patents
Method and device for preparing synthesis gas by coal particle/oxygen carrier chemical chain Download PDFInfo
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- CN101962575A CN101962575A CN2010102908037A CN201010290803A CN101962575A CN 101962575 A CN101962575 A CN 101962575A CN 2010102908037 A CN2010102908037 A CN 2010102908037A CN 201010290803 A CN201010290803 A CN 201010290803A CN 101962575 A CN101962575 A CN 101962575A
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- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 136
- 239000001301 oxygen Substances 0.000 title claims abstract description 133
- 239000007789 gas Substances 0.000 title claims abstract description 74
- 239000003245 coal Substances 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000000126 substance Substances 0.000 title claims abstract description 24
- 239000002245 particle Substances 0.000 title claims abstract description 15
- 230000015572 biosynthetic process Effects 0.000 title abstract description 13
- 238000003786 synthesis reaction Methods 0.000 title abstract description 13
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 title 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 132
- 238000006243 chemical reaction Methods 0.000 claims abstract description 33
- 230000008569 process Effects 0.000 claims abstract description 13
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 7
- 238000001354 calcination Methods 0.000 claims description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 238000000926 separation method Methods 0.000 claims description 10
- 239000007787 solid Substances 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 6
- 235000011089 carbon dioxide Nutrition 0.000 claims description 6
- 230000003647 oxidation Effects 0.000 claims description 6
- 239000002131 composite material Substances 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 230000004048 modification Effects 0.000 claims description 4
- 238000012986 modification Methods 0.000 claims description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- 230000005587 bubbling Effects 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 claims description 3
- 239000010883 coal ash Substances 0.000 claims description 3
- 238000013461 design Methods 0.000 claims description 3
- 238000006477 desulfuration reaction Methods 0.000 claims description 3
- 230000023556 desulfurization Effects 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims description 2
- 238000000746 purification Methods 0.000 abstract description 7
- 238000002360 preparation method Methods 0.000 abstract description 6
- 238000006722 reduction reaction Methods 0.000 abstract description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 abstract 6
- 229910000019 calcium carbonate Inorganic materials 0.000 abstract 3
- 235000010216 calcium carbonate Nutrition 0.000 abstract 3
- 229910052925 anhydrite Inorganic materials 0.000 abstract 1
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 abstract 1
- 238000003912 environmental pollution Methods 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 16
- 238000002309 gasification Methods 0.000 description 7
- 239000000446 fuel Substances 0.000 description 5
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 3
- 229910044991 metal oxide Inorganic materials 0.000 description 3
- 150000004706 metal oxides Chemical class 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 238000013459 approach Methods 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- -1 carrying out also Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000005111 flow chemistry technique Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000006479 redox reaction Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
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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
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Carbon And Carbon Compounds (AREA)
Abstract
The invention belongs to the technical field of clean and efficient utilization of coal and relates to a novel process and a device for producing synthesis gas by coal, in particular to a method and a device for preparing synthesis gas by a coal particle/oxygen carrier chemical chain. In the method, double chemical chain is used to prepare the synthesis gas, the oxygen carrier undergoes a reduction reaction with the coal particles in an oxygen carrier gasifier and an oxidation reaction with air in an air reactor, and the synthesis gas is prepared by the cycle reaction of the oxygen carrier; the purification of the synthesis gas and the collection of CO2 are completed by using a CaCO3/CaO chemical chain; in the preparation of the synthesis gas by combined CaSO4/CaCO3 oxygen chemical chain, the purification and CO2 collection by using the CaCO3/CaO chemical chain are coupled in the preparation process of the synthesis gas by the oxygen carrier chemical chain; therefore, the preparation of the synthesis gas and the preparation of the two chemical chains for the purification of the synthesis gas and the CO2 collection are processed synchronously. The device has a simple structure and is based on a reliable principle; the energy utilization rate of the device is high; the gas prepared by the device has high quality; and the device causes little environmental pollution.
Description
Technical field:
The invention belongs to the coal clean and effective and utilize technical field, relate to novel process and device that coal prepares synthetic gas, particularly a kind of coal particles/oxygen carrier chemistry chain prepares the method and the device thereof of synthetic gas.
Background technology:
Preparing synthetic gas by gasification of coal is one of coal clean utilization technology, coal prepare the synthetic gas process be coal in High Temperature Furnaces Heating Apparatus and reaction such as a certain amount of oxygen generation mainly comprise H
2, gas such as CO, the synthetic gas of generation can be used for combustion power generation, synthetic number of chemical product and liquid fuel etc.Traditional Coal Gasification Technology mainly utilizes air, water vapour etc. to make vaporized chemical.In order to reduce N in the product gas
2And CO
2Content, the gasification installation front need utilize air separation facility (ASU) to obtain oxygen rich gas, needs complicated unit operations such as gas sweetening after the gasification.Chemistry chain technology (Chemical-Looping technology) is for the clean and effective utilization of the energy has proposed a kind of new approaches, and this technology need not to consume additional energy can realize CO
2Interior separation; Can realize the cascade utilization of energy, the overall thermal efficiency of system is improved; Simultaneously can also control heating power type and fuel type NO
xGenerate, therefore chemical chain technology is the novelty breach that solves energy utilization and environmental problem.The principle of chemistry chain technology is exactly to utilize solid particulate that given chemical reaction is decomposed into several chemical reactions, and wherein chemical media can carry out chemical reaction and regeneration.For example in the burning chemistry chains process, the oxygen carrier reaction in air, carried out of ortho states oxygen carrier and the oxidation state oxygen carrier reduction reaction of in geseous fuel, carrying out also, oxygen carrier cycle alternation under oxidation and two kinds of atmosphere of reduction reacts, realize the transfer of oxygen and the burning of fuel, since fuel not with air in free oxygen directly contact, but with oxygen carrier in the oxygen of chemical combination attitude react, so burning chemistry chains is a kind of aphlogistic combustion system, can realize CO
2Interior separation.CaCO
3CO is caught in/CaO working cycle
2Technology is to utilize CaO and CO
2Reaction generates CaCO
3, CaCO
3Pyrolysis generates CaO once more, and so recycle can be finished CO
2Catch, these two chemical chain process are expressed as follows with reaction equation:
The circulation of oxygen carrier: MeO+C → Me+CO
Me+1/2O
2→MeO
CO
2Circulation: CaO+CO
2→ CaCO
3
CaCO
3→CaO+CO
2
Main flow chemistry chain oxygen carrier type is a metal oxide at present, be proved the oxide compound that the active metal oxide that can be used as oxygen carrier mainly comprises transition metal Ni, Fe, Co, Mn, Cu and Cd, but in practical application in industry, the metal oxygen carrier must have a spot of metal oxide and enter atmosphere in recycling process, and in use there are wearing and tearing, lump and can cause the problems such as heavy metal contamination in the human habitat, make the utilization of metal oxygen carrier be subjected to certain restriction.Study the more CaSO that mainly contains at present
4, BaSO
4, SrSO
4Deng the vitriol oxygen carrier, it has advantages such as oxygen carrying capability is big, inexpensive, is subjected to extensive concern recently.Traditional gasification of coal prepares synthetic gas need provide oxygen rich gas, and CO in the synthetic gas
2Separate complex, chemical chain technology provides new thinking for the coal preparing synthetic gas, replaces airborne free oxygen with the fixed oxygen in the oxygen carrier, saves air separation facility, and the oxygen carrier that is reduced in vapourizing furnace is oxidized again recycle once more in air; Utilize CaCO
3/ CaO circulation can realize CO
2Separation; Chemistry chain oxygen carrier prepares synthetic gas method to be compared with traditional coal gasification method and has great advantage, but present technology also is difficult to reach the effect of the shortcoming that overcomes conventional art fully; Seek the method that a kind of ideal chemistry chain oxygen carrier prepares synthetic gas and not only can improve existing coal process for preparing synthetic gas, but also can develop new technology of combined.
Summary of the invention:
The objective of the invention is to overcome the shortcoming that prior art exists, seek to design a kind of novel serve as processing method and the device thereof that reaction component utilization chemistry chain technology prepares synthetic gas with coal particles/oxygen carrier, improve gasification efficiency and energy utilization efficiency to reach, effectively separation of C O
2Function.
Agent structure of the present invention comprises cyclonic separator, oxygen carrier vapourizing furnace, feeding screw, jet pipe, loop seal, loop seal, turbine, cyclonic separator, CaCO
3Calcining furnace, cyclonic separator and air reactor; Carbonic acid gas and/or water vapour through the air reactor preheating enter the oxygen carrier vapourizing furnace in the bottom of oxygen carrier vapourizing furnace, be shaped on jet pipe on the lower sides of oxygen carrier vapourizing furnace, jet pipe axis and oxygen carrier vapourizing furnace linkage section place vertical direction angle are respectively 90 °, 60 °, 45 ° and 30 °, be shaped on feeding screw on the side, middle part of oxygen carrier vapourizing furnace, the top expanded section of oxygen carrier vapourizing furnace is connected with cyclonic separator by pipeline and communicates; The top end of cyclonic separator connects another cyclonic separator, place, bottom and CaCO
3The calcining furnace pipeline is communicated with; The top exit gas of cyclonic separator obtains the refrigerative synthetic gas after by turbine, and the bottom is shaped on the coal ash mouth; CaCO
3The top of calcining furnace is shaped on the carbonic acid gas outlet and is communicated with the water vapour mouth; CaCO
3The calcining furnace bottom is communicated with the air reactor pipeline by loop seal, and the air reactor bottom is shaped on air scoop; Top one side of air reactor is communicated with cyclonic separator by pipeline, the upper end of cyclonic separator is shaped on the nitrogen mouth, the bottom is communicated with the back by loop seal and forms the device that integral type prepares synthetic gas, oxygen carrier vapourizing furnace, air reactor and CaCO with oxygen carrier vapourizing furnace pipeline
3The calcining furnace outside is equipped with heating unit.
The ultimate principle of the inventive method prepares synthetic gas for utilizing two chemical chains, and oxygen carrier carries out reduction reaction with coal particles in the oxygen carrier vapourizing furnace, then in air reactor with air generation oxidizing reaction, the circulating reaction of oxygen carrier makes synthetic gas; The purification of synthetic gas and CO
2Capture utilize CaCO
3/ CaO chemistry chain is finished; Compound CaSO
4/ CaCO
3Oxygen carrier chemistry chain prepares synthetic gas CaCO
3/ CaO chemistry chain purifies and captures CO
2Be coupled to oxygen carrier chemistry chain and prepare in the synthetic gas process, both preparing synthetic gas and purified synthesis gas and CO
2Two chemical chain process carry out simultaneously; Technological process of its preparation synthetic gas is: coal and oxygen carrier are reacted in the oxygen carrier vapourizing furnace, separate through the secondary of cyclonic separator and do not contained CO
2Synthetic gas; The solid that cyclonic separation is obtained enters CaCO
3Calcining furnace is calcined, and the solid that obtains enters the oxygen carrier that obtains oxidation state behind air reactor and the air reaction; Enter the oxygen carrier vapourizing furnace by cyclonic separator and loop seal then, so circulation; The CO that obtains in the calcining furnace
2Gas is stored standby or is entered oxygen carrier vapourizing furnace by air reactor heating back as fluidizing medium with water vapour; Employed oxygen carrier is CaSO
4/ CaCO
3Composite type oxygen carrier obtains by mechanical mixing and through the chemical treatment modification; Its oxygen carrier vapourizing furnace is a bubbling fluidized bed, and its fluidizing medium is CO
2And water vapour, service temperature is 800～1000 ℃, and working pressure is 1～3atm, and the chemical reaction that takes place in the oxygen carrier vapourizing furnace comprises:
CaSO
4+C→CaS+CO
H
2O+C→H
2+CO
H
2O+CO→H
2+CO
2
CO
2+CaO→CaCO
3
CaO+H
2S→CaS+H
2O
CaO+COS→CaS+CO
2
Wherein latter two reaction is desulfurization reaction, and coal particles and oxygen carrier are pressed the carbon content of coal and 1: 1 the amount charging of oxygen carrier amount mol ratio of oxygen carrier; Air reactor is a fast fluidized bed, and fluidizing medium is an air, and service temperature is 950 ℃～1200 ℃, and working pressure is a normal pressure, gasifying gas H
2O and CO
2The preheating of process air reactor earlier before entering the oxygen carrier vapourizing furnace; The chemical reaction that carries out in air reactor is:
CaS+2O
2→CaSO
4。
The oxygen carrier vapourizing furnace that the present invention relates to is the reactor that has four different jet angle jet pipes, jet pipe improves oxygen carrier vapourizing furnace inner fluid flow characteristics, flow angle is respectively 30 ℃, 45 ℃, 60 ℃ and 90 ℃, grid distributor adopts the convex shape design, make that reaction mass is heated evenly on the grid distributor, gas is heated before entering the oxygen carrier vapourizing furnace once more.
The present invention compared with prior art, the one, adopt chemical chain notion to utilize oxygen carrier to transmit oxygen, save air separation plant, the redox reaction of a chemical reaction by oxygen carrier resolved into two reactions, reduce the loss of (fire is used), improved energy utilization efficiency; The 2nd, adopt chemical chain notion to utilize CaCO
3Following of/CaO caught CO
2Obtain high-quality synthetic gas; The 3rd, the purification of synthetic gas and CO
2Catch simultaneously and finish, saved synthesis gas purification, optimized technology, improved the efficient of whole technology; The 4th, utilize CaSO
4Compound oxygen carrier replace metal oxygen carrier, the heavy metal contamination of having avoided the metal oxygen carrier to bring.
Description of drawings:
Fig. 1 is the agent structure technological principle synoptic diagram of apparatus of the present invention.
Fig. 2 is the jet pipe mounting structure principle schematic that the present invention relates to.
Fig. 3 is the convex shape distributing plate structure principle schematic of oxygen carrier vapourizing furnace of the present invention.
Embodiment:
Be described further below in conjunction with accompanying drawing and by embodiment.
Embodiment:
The ultimate principle of present embodiment prepares synthetic gas for utilizing two chemical chains, and oxygen carrier carries out reduction reaction with coal particles in the oxygen carrier vapourizing furnace, then in air reactor with air generation oxidizing reaction, the synthetic gas of the circulating reaction system of oxygen carrier; The purification of synthetic gas and CO
2Capture utilize CaCO
3/ CaO chemistry chain is finished; Compound CaSO
4/ CaCO
3Oxygen carrier chemistry chain prepares synthetic gas CaCO
3/ CaO chemistry chain purifies and captures CO
2Be coupled in the oxygen carrier chemistry chain synthetic gas production process, both preparing synthetic gas and purified synthesis gas and CO
2Two chemical chain process carry out simultaneously; Technology of its preparation synthetic gas is: coal and oxygen carrier are reacted in the oxygen carrier vapourizing furnace, separate through the secondary of cyclonic separator and do not contained CO
2Synthetic gas; The solid that cyclonic separation is obtained enters CaCO
3Calcining furnace is calcined, and the solid that obtains enters the oxygen carrier that obtains oxidation state behind air reactor and the air reaction; Enter the oxygen carrier vapourizing furnace by cyclonic separator and loop seal then, so circulation; The CO that obtains in the calcining furnace
2Gas be stored he with or entered oxygen carrier vapourizing furnace by air reactor heating back as fluidizing medium with water vapour; Its oxygen carrier that uses is CaSO
4/ CaCO
3Composite type oxygen carrier obtains by mechanical mixing and through the chemical treatment modification; Its oxygen carrier vapourizing furnace is a bubbling fluidized bed, and its fluidizing medium is CO
2And water vapour, service temperature is at 800～1000 ℃, and working pressure is 1～3atm, and the main body that takes place in oxygen carrier vapourizing furnace reaction is:
CaSO
4+C→CaS+CO
H
2O+C→H
2+CO
H
2O+CO→H
2+CO
2
CO
2+CaO→CaCO
3
CaO+H
2S→CaS+H
2O
CaO+COS→CaS+CO
2
Wherein latter two reaction is desulfurization reaction, and coal particles and oxygen carrier are pressed the carbon content of coal and 1: 1 the amount charging of oxygen carrier amount mol ratio of oxygen carrier; Air reactor is a fast fluidized bed, and fluidizing medium is an air, and service temperature is 950 ℃～1200 ℃, and working pressure is a normal pressure, gasifying gas H
2O and CO
2The preheating of process air reactor earlier before entering the oxygen carrier vapourizing furnace; The main body reaction of carrying out in air reactor is:
CaS+2O
2→CaSO
4。
The agent structure of present embodiment comprises cyclonic separator 1, oxygen carrier vapourizing furnace 2, feeding screw 3, jet pipe 4, loop seal 5, loop seal 6, turbine 7, cyclonic separator 8, CaCO
3Calcining furnace 9, cyclonic separator 10 and air reactor 11; Carbonic acid gas and/or water vapour through air reactor 11 preheatings enter oxygen carrier vapourizing furnace 2 in the bottom of oxygen carrier vapourizing furnace, be shaped on jet pipe 4 on the lower sides of oxygen carrier vapourizing furnace 2, jet pipe 4 and oxygen carrier vapourizing furnace 2 linkage section place vertical direction angles are respectively 90 °, 60 °, 45 ° and 30 ° (as 13,14,16 and 15 in accompanying drawing 2), be shaped on feeding screw 3 on the side, middle part of oxygen carrier vapourizing furnace 2, the top expanded section of oxygen carrier vapourizing furnace 2 is connected with cyclonic separator 1 by pipeline and communicates; The top end of cyclonic separator 1 connects another cyclonic separator 8, place, bottom and CaCO
3Calcining furnace 9 pipelines are communicated with; The top exit gas of cyclonic separator 8 obtains the refrigerative synthetic gas after by turbine, and the bottom is shaped on coal ash mouth f; CaCO
3The top of calcining furnace 9 is shaped on carbonic acid gas outlet c and is communicated with water vapour mouth b; CaCO
3Calcining furnace 9 bottoms are communicated with air reactor 11 pipelines by loop seal 6, and air reactor 11 bottoms are shaped on air scoop a; Top one side of air reactor 11 is communicated with cyclonic separator 10 by pipeline, and the upper end of cyclonic separator 10 is shaped on nitrogen mouth d, and the bottom is communicated with back composition integral type by loop seal 5 and prepares the synthetic gas device with oxygen carrier vapourizing furnace 2 pipelines.Coal particles and CaSO
4/ CaCO
3Composite type oxygen carrier is entered in the oxygen carrier vapourizing furnace 2 by feeding screw 3 and reacts, and separates with 8 secondary through cyclonic separator 1 and is not contained CO
2Synthetic gas; The solid that cyclonic separator 1 obtains enters CaCO
3Calcining furnace is calcined, and the solid that obtains enters oxygen carrier and the CaO that air reactor 11 and air reaction obtain oxidation state, enters oxygen carrier vapourizing furnace 2 by cyclonic separator 10 and loop seal 6, the CO that obtains in the calcining furnace 9
2Gas and water vapour are entered the oxygen carrier vapourizing furnace by air reactor 11 heating backs as fluidizing medium, oxygen carrier vapourizing furnace specification is Φ 60 * 600mm, expanding reach Φ 100, the percentage of open area 0.94% of grid distributor, hole diameter Φ 1mm, coal adopts Shenmu County's coal, obtains median size and is being 0.67mm through crushing and screening; Oxygen carrier adopts the CaSO of modification
4/ CaCO
3Composite type oxygen carrier, its median size are 0.1mm, and fluidizing medium adopts water vapour, quiet height of bed 100mm, CaCO
3The calcining furnace specification is Φ 40 * 300mm, and the air reactor specification is Φ 60 * 1000mm, expanding reach Φ 100, the percentage of open area 0.94% of grid distributor, hole diameter Φ 1mm; Fluidizing medium is an air, and proximate analysis of coal sees Table 1, obtains the CO=35% that consists of of synthetic gas, H
2=51.4%, CO
2=6%, H
2O=0%, other=7.6%.
Table 1: the technical analysis index inventory of the used coal of present embodiment
Claims (3)
1. a coal particles/oxygen carrier chemistry chain prepares the method for synthetic gas, it is characterized in that making earlier coal and oxygen carrier to react in the oxygen carrier vapourizing furnace, separates through the secondary of cyclonic separator and is not contained CO
2Synthetic gas; The solid that cyclonic separation is obtained enters CaCO
3Calcining furnace is calcined, and the solid that obtains enters the oxygen carrier that obtains oxidation state behind air reactor and the air reaction; Enter the oxygen carrier vapourizing furnace by cyclonic separator and loop seal then, so circulation; The CO that obtains in the calcining furnace
2Gas is stored standby or is entered oxygen carrier vapourizing furnace by air reactor heating back as fluidizing medium with water vapour; Employed oxygen carrier is CaSO
4/ CaCO
3Composite type oxygen carrier obtains by mechanical mixing and through the chemical treatment modification; The oxygen carrier vapourizing furnace is a bubbling fluidized bed, and fluidizing medium is CO
2And water vapour, service temperature is 800～1000 ℃, and working pressure is 1～3atm, and the chemical reaction that takes place in the oxygen carrier vapourizing furnace comprises: CaSO
4+ C → CaS+CO; H
2O+C → H
2+ CO; H
2O+CO → H
2+ CO
2CO
2+ CaO → CaCO
33CaO+H
2S → CaS+H
2O and CaO+COS → CaS+CO
2Wherein latter two reaction is for desulfurization reaction, and coal particles and oxygen carrier are 1: 1 amount charging by the oxygen carrier amount mol ratio of the carbon content of coal and oxygen carrier; Air reactor is a fast fluidized bed, and fluidizing medium is an air, and service temperature is 950 ℃～1200 ℃, and working pressure is a normal pressure, gasifying gas H
2O and CO
2The preheating of process air reactor earlier before entering the oxygen carrier vapourizing furnace; The chemical reaction that carries out in air reactor is: CaS+2O
2→ CaSO
4
One kind according to claim 1 coal particles/oxygen carrier chemistry chain of using of method prepare the device of synthetic gas, it is characterized in that agent structure comprises cyclonic separator, oxygen carrier vapourizing furnace, feeding screw, jet pipe, loop seal, loop seal, turbine, cyclonic separator, CaCO
3Calcining furnace, cyclonic separator and air reactor; Carbonic acid gas and/or water vapour through the air reactor preheating enter the oxygen carrier vapourizing furnace in the bottom of oxygen carrier vapourizing furnace, be shaped on jet pipe on the lower sides of oxygen carrier vapourizing furnace, jet pipe axis and oxygen carrier vapourizing furnace linkage section place vertical direction angle are respectively 90 °, 60 °, 45 ° and 30 °, be shaped on feeding screw on the side, middle part of oxygen carrier vapourizing furnace, the top expanded section of oxygen carrier vapourizing furnace is connected with cyclonic separator by pipeline and communicates; The top end of cyclonic separator connects another cyclonic separator, place, bottom and CaCO
3The calcining furnace pipeline is communicated with; The top exit gas of cyclonic separator obtains the refrigerative synthetic gas after by turbine, and the bottom is shaped on the coal ash mouth; CaCO
3The top of calcining furnace is shaped on the carbonic acid gas outlet and is communicated with the water vapour mouth; CaCO
3The calcining furnace bottom is communicated with the air reactor pipeline by loop seal, and the air reactor bottom is shaped on air scoop; Top one side of air reactor is communicated with cyclonic separator by pipeline, and the upper end of cyclonic separator is shaped on the nitrogen mouth, and the bottom is communicated with the back by loop seal and forms the device that integral type prepares synthetic gas with oxygen carrier vapourizing furnace pipeline; Oxygen carrier vapourizing furnace, air reactor and CaCO
3The calcining furnace outside is equipped with heating unit.
3. coal particles according to claim 2/oxygen carrier chemistry chain prepares the device of synthetic gas, it is characterized in that the oxygen carrier vapourizing furnace is the reactor that has four different jet angle jet pipes, jet pipe improves oxygen carrier vapourizing furnace inner fluid flow characteristics, flow angle is respectively 30 ℃, 45 ℃, 60 ℃ and 90 ℃, grid distributor adopts the convex shape design, make that reaction mass is heated evenly on the grid distributor, gas is heated before entering the oxygen carrier vapourizing furnace once more.
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| CN103017155A (en) * | 2012-12-15 | 2013-04-03 | 华中科技大学 | Method and device for desulfurization and decarburization combustion of coal |
| CN103695040A (en) * | 2013-12-17 | 2014-04-02 | 兖矿集团有限公司 | Technological process for technology of preparing coal chemical chain oxygen carrier to synthesis gas |
| CN106423132A (en) * | 2016-09-22 | 2017-02-22 | 新奥科技发展有限公司 | Catalyst for catalytic coal gasification as well as catalytic coal gasification method and device |
| CN106675655A (en) * | 2016-12-06 | 2017-05-17 | 西安交通大学 | Device and method for biomass chemical chain gasification hydrogen production based on calcium-based carbon supporting body |
| CN107057797A (en) * | 2017-03-28 | 2017-08-18 | 大连理工大学 | A kind of composite oxygen carrier, preparation method and its application in solid fuel gasification |
| CN108569676A (en) * | 2018-05-10 | 2018-09-25 | 哈尔滨理工大学 | Using flue gas as the chemical chain air separation oxygenerator and method of heat source |
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| CN111534332A (en) * | 2020-04-28 | 2020-08-14 | 东南大学 | Microwave-assisted chemical-looping gasification soil heavy metal restoration plant heat treatment method |
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| CN103017155A (en) * | 2012-12-15 | 2013-04-03 | 华中科技大学 | Method and device for desulfurization and decarburization combustion of coal |
| CN103695040A (en) * | 2013-12-17 | 2014-04-02 | 兖矿集团有限公司 | Technological process for technology of preparing coal chemical chain oxygen carrier to synthesis gas |
| CN106423132A (en) * | 2016-09-22 | 2017-02-22 | 新奥科技发展有限公司 | Catalyst for catalytic coal gasification as well as catalytic coal gasification method and device |
| CN106675655A (en) * | 2016-12-06 | 2017-05-17 | 西安交通大学 | Device and method for biomass chemical chain gasification hydrogen production based on calcium-based carbon supporting body |
| CN106675655B (en) * | 2016-12-06 | 2019-06-11 | 西安交通大学 | A kind of biomass chemical chain gasification device for producing hydrogen and method based on calcium base carbon carrier |
| CN107057797A (en) * | 2017-03-28 | 2017-08-18 | 大连理工大学 | A kind of composite oxygen carrier, preparation method and its application in solid fuel gasification |
| CN107057797B (en) * | 2017-03-28 | 2019-05-14 | 大连理工大学 | A kind of composite oxygen carrier, preparation method and its application in solid fuel gasification |
| CN108569676A (en) * | 2018-05-10 | 2018-09-25 | 哈尔滨理工大学 | Using flue gas as the chemical chain air separation oxygenerator and method of heat source |
| CN110484300A (en) * | 2019-08-16 | 2019-11-22 | 东南大学 | Couple the restoring heavy metal-polluted soil by plants annealing device of medium temperature gasification and high temeperature chemistry chain |
| CN110643382A (en) * | 2019-10-28 | 2020-01-03 | 华南理工大学 | Biomass oil-gas co-production device and method based on chemical chain |
| CN111534332A (en) * | 2020-04-28 | 2020-08-14 | 东南大学 | Microwave-assisted chemical-looping gasification soil heavy metal restoration plant heat treatment method |
| CN111534332B (en) * | 2020-04-28 | 2021-06-11 | 东南大学 | Microwave-assisted chemical-looping gasification soil heavy metal restoration plant heat treatment method |
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