CN109880653A - A kind of the hydrogen-rich synthetic gas preparation method and system of melting slag waste heat driving - Google Patents
A kind of the hydrogen-rich synthetic gas preparation method and system of melting slag waste heat driving Download PDFInfo
- Publication number
- CN109880653A CN109880653A CN201910305887.8A CN201910305887A CN109880653A CN 109880653 A CN109880653 A CN 109880653A CN 201910305887 A CN201910305887 A CN 201910305887A CN 109880653 A CN109880653 A CN 109880653A
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- vapor
- slag
- blast furnace
- reaction
- 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.)
- Granted
Links
- 239000007789 gas Substances 0.000 title claims abstract description 128
- 239000002893 slag Substances 0.000 title claims abstract description 118
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 91
- 239000001257 hydrogen Substances 0.000 title claims abstract description 91
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 83
- 238000002360 preparation method Methods 0.000 title claims abstract description 52
- 239000002918 waste heat Substances 0.000 title claims abstract description 42
- 230000008018 melting Effects 0.000 title claims abstract description 27
- 238000002844 melting Methods 0.000 title claims abstract description 27
- 238000002309 gasification Methods 0.000 claims abstract description 96
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 69
- 239000003818 cinder Substances 0.000 claims abstract description 62
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 62
- 239000004449 solid propellant Substances 0.000 claims abstract description 54
- 238000006243 chemical reaction Methods 0.000 claims abstract description 49
- 239000002002 slurry Substances 0.000 claims abstract description 45
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 33
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 17
- 238000006057 reforming reaction Methods 0.000 claims abstract description 17
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 16
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 9
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 8
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 8
- 238000002407 reforming Methods 0.000 claims description 42
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 30
- 239000002245 particle Substances 0.000 claims description 27
- 238000010521 absorption reaction Methods 0.000 claims description 21
- 238000003860 storage Methods 0.000 claims description 20
- 238000000926 separation method Methods 0.000 claims description 17
- 229910052742 iron Inorganic materials 0.000 claims description 15
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 229910001868 water Inorganic materials 0.000 claims description 11
- 239000003054 catalyst Substances 0.000 claims description 10
- 239000003245 coal Substances 0.000 claims description 10
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims description 7
- 229910052737 gold Inorganic materials 0.000 claims description 7
- 239000010931 gold Substances 0.000 claims description 7
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 6
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 6
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims description 6
- 229910017052 cobalt Inorganic materials 0.000 claims description 6
- 239000010941 cobalt Substances 0.000 claims description 6
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 6
- 229910052802 copper Inorganic materials 0.000 claims description 6
- 239000010949 copper Substances 0.000 claims description 6
- 229910052751 metal Inorganic materials 0.000 claims description 6
- 239000002184 metal Substances 0.000 claims description 6
- 229910052750 molybdenum Inorganic materials 0.000 claims description 6
- 239000011733 molybdenum Substances 0.000 claims description 6
- 229910052697 platinum Inorganic materials 0.000 claims description 6
- 229910052709 silver Inorganic materials 0.000 claims description 6
- 239000004332 silver Substances 0.000 claims description 6
- 230000005587 bubbling Effects 0.000 claims description 5
- 238000002347 injection Methods 0.000 claims description 5
- 239000007924 injection Substances 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 5
- 239000002699 waste material Substances 0.000 claims description 5
- 239000002131 composite material Substances 0.000 claims description 4
- 239000003863 metallic catalyst Substances 0.000 claims description 4
- 239000000178 monomer Substances 0.000 claims description 4
- 239000002028 Biomass Substances 0.000 claims description 3
- 239000007809 chemical reaction catalyst Substances 0.000 claims description 3
- 239000011280 coal tar Substances 0.000 claims description 3
- 210000000262 cochlear duct Anatomy 0.000 claims description 3
- 239000004058 oil shale Substances 0.000 claims description 3
- 239000002006 petroleum coke Substances 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 24
- 230000008569 process Effects 0.000 abstract description 14
- 238000005265 energy consumption Methods 0.000 abstract description 9
- 238000011084 recovery Methods 0.000 abstract description 6
- 229910000831 Steel Inorganic materials 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 9
- 239000010959 steel Substances 0.000 description 9
- 230000035800 maturation Effects 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 238000010791 quenching Methods 0.000 description 4
- 230000000171 quenching effect Effects 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000002817 coal dust Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000000295 complement effect Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000005469 granulation Methods 0.000 description 2
- 230000003179 granulation Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 241000790917 Dioxys <bee> Species 0.000 description 1
- 238000003287 bathing Methods 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000007908 dry granulation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000921 elemental analysis Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000000452 restraining effect Effects 0.000 description 1
- 238000012163 sequencing technique Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Processing Of Solid Wastes (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
Abstract
The invention belongs to hydrogen-rich synthetic gas preparation methods and system that heat recovery technical field more particularly to a kind of melting slag waste heat drive.This method comprises the following steps: S1: blast furnace cinder, vapor and the fine grain slurries of carbonic solid fuels carry out gasification reaction, generate crude synthesis gas and ash content based on carbon monoxide and hydrogen；S2: crude synthesis gas and vapor are subjected to reforming reaction, the synthesis gas of generation includes hydrogen, carbon dioxide and vapor；S3: the carbon dioxide in the synthesis gas generated in S2 is removed, the synthesis gas comprising hydrogen and vapor is generated；S4: by removing comprising the vapor in hydrogen and vapor for generation, hydrogen-rich synthetic gas is formed；Vapor is prepared using the heat that reaction generates clinker in step S1, and required vapor is provided for the reaction process of S1 and S2.The preparation method realizes that process flow is simple, and cost and energy consumption are greatly reduced, and contamination-free generates.
Description
Technical field
The invention belongs to the hydrogen-rich synthetic gas systems that heat recovery technical field more particularly to a kind of melting slag waste heat drive
Preparation Method and system.
Background technique
Iron and steel enterprise is the big power consumer in China, and the residual heat resources of iron and steel enterprise account for about the one third of fuel consumption.
With the use of a series of technology so that the waste heat of iron and steel enterprise is recycled, but the sensible heat of blast furnace slag still without
It is recycled to effective.Therefore focus concerned by people in recent years is become to the research that blast furnace slag waste heat recycles.Blast furnace
Slag generates during blast furnace ironmaking, and it is in molten condition that the temperature being discharged from blast furnace, which is about 1500 DEG C, and ton slag heat enthalpy value is about
1770MJ is equivalent to heat caused by 60kg mark coal completely burned.The blast furnace slag yield in China in 2018 has reached 2.5 hundred million
Ton carries the calorific capacity that heat is equivalent to 15,000,000 tons of standard coals.The recycling of blast furnace slag waste heat can be effectively reduced steel
The energy consumption of iron enterprise is advantageously implemented the target of energy-saving and emission-reduction.
Blast furnace slag waste heat complementary energy recycle restraining factors be concentrated mainly on three aspect: the thermal coefficient of blast furnace slag compared with
Low, requirement of quite a few waste heat recovery apparatus to slag fluidity is relatively high, to reach optimal slag flow and air quantity
Proportion；Blast furnace slag waste heat utilize during energy consumption and serious, the traditional wet-treating mode environmental pollution of pollution problem
Than more serious, dry granulation rule requires the investment of device and operating cost larger；The utilization of subsequent cold slag is very important
The problem of, cooling velocity is faster, its property is just closer to the hydraulicity of cement material and intensity.
There are two main classes: water quenching and dry treatment method for the processing method of current blast furnace slag.Water quenching is direct with new water
Impact high-temperature slag makes its temperature reduce rapidly to form a large amount of glass state material, and the raw material as production cement, generation
Hot water is only used for purposes, the waste heat recovery rates such as plant area's heating and the bathing of iron and steel enterprise and only has limited 10% or so.Typically
Water quenching is mainly bottom filter method, Yin Bafa, Tula method, Lhasa method and name Te Kefa.Dry treatment method mainly have mechanical crushing method,
Wind quenching method and centrifugal granulation method, recycle the sensible heat of blast furnace slag, that there are heat recovery rates is low, latent heat is unutilized due to these modes,
The problems such as energy consumption is high, processing is difficult is not widely applied in production reality also in the experimental study stage.
Recycling problem about blast furnace slag waste heat complementary energy receives very big attention, both at home and abroad in relation to iron and steel enterprise and
Colleges and universities, research institute are conducting a research work, but so far and have not seen the reports of the extensive industrial applications of entity device,
Not formed mature technology.
Summary of the invention
(1) technical problems to be solved
For existing blast-furnace slag heat recovery rate low technical problem, the present invention provides a kind of melting slag waste heat
The hydrogen-rich synthetic gas preparation method and system of driving.
(2) technical solution
In order to achieve the above object, the main technical schemes that the present invention uses include:
A kind of hydrogen-rich synthetic gas preparation method of melting slag waste heat driving, includes the following steps:
S1: blast furnace cinder, vapor and the fine grain slurries of carbonic solid fuels carry out gasification reaction, generate with an oxidation
Crude synthesis gas and ash content based on carbon and hydrogen；
S2: crude synthesis gas and vapor are subjected to reforming reaction, the synthesis gas of generation includes that hydrogen, carbon dioxide and water steam
Gas；
S3: the carbon dioxide in the synthesis gas generated in S2 is removed, the synthesis gas comprising hydrogen and vapor is generated；
S4: by removing comprising the vapor in hydrogen and vapor for generation, hydrogen-rich synthetic gas is formed；
Vapor is prepared using the heat that reaction generates clinker in step S1, and is provided for the reaction process of S1 and S2 required
Vapor.
Preferably, after step S1, further include the steps that crude synthesis gas and ash content are separated.
Preferably, the gasification reaction temperature in step S1 is 1450 DEG C -1250 DEG C；
Reforming reaction temperature in step S3 is 350 DEG C -650 DEG C；
Preferably, the concentration of the fine grain slurries of carbonic solid fuels in step S1 is 50%-60%.
Preferably, the carbonic solid fuels fine grained diameter in the fine grain slurries of carbonic solid fuels in step S1 is
100μm-300μm。
Preferably, the carbonic solid fuels fine grained in the fine grain slurries of carbonic solid fuels in step S1 includes height
Rank coal, scala media coal, low-order coal, coal tar, biomass, petroleum coke, oil shale and/or carbonaceous solids waste.
Preferably, reforming reaction catalyst is added in step S3, catalyst includes load type metal catalyst；
Active component in load type metal catalyst include platinum, gold, silver, iron, molybdenum, copper or cobalt metallic monomer or platinum,
Any two kinds or more the composite load type metallic catalysts being combined in gold, silver, iron, molybdenum, copper and cobalt.
A kind of hydrogen-rich synthetic gas preparation system of melting slag waste heat driving, uses melting slag waste heat driving as described above
The preparation of hydrogen-rich synthetic gas preparation method progress hydrogen-rich synthetic gas comprising gasification reactor, reforming reactor and heat exchanger；
Gasification reactor has high-temperature slag entrance, injection point, steam entry, slag outlet and syngas outlet,
Wherein, high-temperature slag is inputted in gasification reactor by slag entrance, and the fine grain slurries of carbonic solid fuels are entered by slurries
Mouth is input in gasification reactor, and vapor is input in gasification reactor by steam entry；
Blast furnace cinder, vapor and the fine grain slurries of carbonic solid fuels are chemically reacted in gasification reactor,
And the crude synthesis gas generated after reaction is input in reforming reactor, clinker is input in heat exchanger, heat exchanger by with
Clinker heat exchange prepares vapor；
The steam outlet of heat exchanger is connected to the steam entry of gasification reactor, reforming reactor.
Preferably, which further includes slag ladle, the fine grain slurries memory of carbonic solid fuels, separation equipment, receipts
Storage, absorption tower, drier, hydrogen storage device and blast furnace slag particle collector；
Slag ladle is connected with slag entrance, and slag ladle is used to store the high-temperature slag of blast furnace discharge, enables high-temperature slag
Enough stable and continuous output；
The fine grain slurries memory of carbonic solid fuels is connected with injection point, the fine grain slurries of carbonic solid fuels
The memory carbonic solid fuels fine grain slurries good for storage configuration, provide instead for the gasification reaction in gasification reactor
Answer object；
Separation equipment is provided between gasification reactor and reforming reactor, separation equipment can receive gasification reactor production
The raw crude synthesis gas and ash content based on carbon monoxide and hydrogen, and crude synthesis gas is exported with ash separation and respectively,
The crude synthesis gas separated is input in reforming reactor；
Collector is connected with the ash outlet end of separation equipment, is used to collect the ash content of separation equipment output；
Absorption tower is connected with the gas outlet end of reforming reactor, and what absorption tower was used to receive reforming reactor output includes
There is the synthesis gas of hydrogen, carbon dioxide and vapor, and absorb carbon dioxide therein, formation includes hydrogen and vapor
Synthesis gas simultaneously exports；
Absorption tower is connected with drier, and what drier was used to receive absorption tower output includes the conjunction of hydrogen and vapor
At gas, vapor therein is absorbed, form hydrogen-rich synthetic gas and is exported；
Hydrogen storage device is connected with drier, hydrogen-rich synthetic gas and storage of the hydrogen storage device for receiving dryer output；
Blast furnace cinder granulator is arranged between heat exchanger and gasification reactor, and blast furnace cinder granulator is for receiving gasification
Blast furnace cinder after the gasification reaction of reactor discharge forms high temperature slag particle and exports；
Heat exchanger is used to receive the high temperature slag particle of blast furnace cinder granulator formation, and vapor is generated by way of heat exchange simultaneously
It is output in gasification reactor and reforming reactor；
Blast furnace slag particle collector is connected with heat exchanger, and blast furnace slag particle collector is used to receive the slag particle of heat exchanger discharge.
Preferably, separation equipment is cyclone separator；Gasification reactor is bubbling bed gasification reactor；Reforming reactor is
Fixed bed reforming reactor；Heat exchanger is indirect type heat exchanger.
(3) beneficial effect
The beneficial effects of the present invention are: the hydrogen-rich synthetic gas preparation method of melting slag waste heat provided by the invention driving and being
System, the waste heat of blast furnace cinder are used for the gasification reaction of solid fuel, and the high-quality latent heat of especially blast furnace cinder has obtained effectively
Utilization, while vapor used in gasification reaction and reforming reaction process passes through the waste heat of blast furnace cinder and generates, in this way
Mode also reduce energy consumption.
Preparation method of the invention has coupled blast furnace cinder UTILIZATION OF VESIDUAL HEAT IN and solid fuel gasification reaction and reforming reaction
Technical advantage, be not only effectively utilized the high-quality residual heat and energy of blast furnace cinder, but also realize the preparation of hydrogen-rich synthetic gas.
In conclusion preparation method of the invention realizes the high-quality blast furnace utilized while the preparation of hydrogen-rich synthetic gas
Melting slag waste heat, process flow is simple, and cost and energy consumption are greatly reduced, and contamination-free generates, to the energy-saving tool of iron and steel enterprise
There is important meaning.
Detailed description of the invention
Fig. 1 is that the structure of the hydrogen-rich synthetic gas preparation system for the melting slag waste heat driving that the specific embodiment of the invention provides is shown
It is intended to；
[description of symbols]
1: slurries memory；2: slag ladle；3: gasification reactor；4: cyclone separator；5: reforming reactor；6: absorbing
Tower；7: drier；8: hydrogen storage device；9: blast furnace cinder granulator；10: heat exchanger；11: ash content collector；12: blast furnace slag particle is collected
Device.
Specific embodiment
In order to preferably explain the present invention, in order to understand, with reference to the accompanying drawing, by specific embodiment, to this hair
It is bright to be described in detail.
As shown in Figure 1, the present embodiment provides the hydrogen-rich synthetic gas preparation system that a kind of melting slag waste heat drives, the system packets
Include the fine grain slurries memory 1 of carbonic solid fuels, slag ladle 2, gasification reactor 3, cyclone separator 4, reforming reactor
5, absorption tower 6, drier 7, hydrogen storage device 8, blast furnace cinder granulator 9, heat exchanger 10, ash content collector 11 and blast furnace slag particle are collected
Device 12.
The fine grain slurries memory 1 of carbonic solid fuels is connected with gasification reactor 3, contains for storage configuration to be good
The fine grain slurries of carbon solid fuel provide reactant for the gasification reaction in gasification reactor 3.
Slag ladle 2 is connected with gasification reactor 3, for storing the high-temperature slag of blast furnace discharge, enables high-temperature slag
Enough stable and continuous output.
Gasification reactor 3 can carry out wherein for blast furnace cinder, vapor and the fine grain slurries of carbonic solid fuels
Chemical reaction generates the crude synthesis gas and ash content based on carbon monoxide and hydrogen and exports.It is mainly sent out in gasification reactor 3
Raw reaction includes:
Disproportionated reaction:
Oxidation reaction:
Partial oxidation reaction:
Aqueous vapor reaction:
Methanation reaction:
Water gas shift reaction:
Methane reforming reaction:
Separation equipment, that is, cyclone separator 4 is connected with gasification reactor 3, can receive gasification reactor 3 generation with
Crude synthesis gas and ash content based on carbon monoxide and hydrogen, and crude synthesis gas is exported with ash separation and respectively.
Ash content collector 11 is connected with cyclone separator 4, for collecting the ash content of the output of cyclone separator 4.
Reforming reactor 5 is connected with separator 4, for receiving the synthesis gas of the output of cyclone separator 4, and certain temperature
Down by the effect of catalyst, so that the carbon monoxide in synthesis gas occurs water gas shift reaction with the vapor being passed through and generates hydrogen
Gas and carbon dioxide.The key reaction occurred in reforming reactor includes:
Absorption tower 6 is connected with reforming reactor 5, for receive reforming reactor 5 output mainly contain hydrogen, dioxy
Change the synthesis gas of carbon and vapor, and absorb carbon dioxide therein, is formed and mainly contain the synthesis gas of hydrogen and vapor simultaneously
Output,.The key reaction occurred in absorption tower includes:
Drier 7 is connected with absorption tower 6, for receiving the conjunction for mainly containing hydrogen and vapor of the output of absorption tower 6
At gas, vapor therein is absorbed, form hydrogen-rich synthetic gas and is exported.
Hydrogen storage device 8 is connected with drier 7, the hydrogen-rich synthetic gas exported for receiving dryer 7 and storage.As a result, may be used
Pass through the fine grain slurries memory 1 of carbonic solid fuels, slag ladle 2, gasification reaction to be interpreted as the preparation of hydrogen-rich synthetic gas
Device 3, cyclone separator 4, reforming reactor 5, absorption tower 6, drier 7, hydrogen storage device 8 are realized.
Blast furnace slag melts granulator 9 and is connected with gasification reactor 3, for receiving the gasification reaction of the discharge of gasification reactor 3
Blast furnace cinder afterwards forms high temperature slag particle and exports, and the temperature of blast furnace cinder drops to 1250 DEG C hereinafter, so in the process
After blast furnace cinder granulator 9 touches slag, the temperature of slag continues to drop to its freezing point blast furnace slag particle formed below.
Heat exchanger 10 is connected with blast furnace cinder granulator 9, for receiving the high temperature sludge of the formation of blast furnace cinder granulator 9
Grain, vapor is generated by way of heat exchange and is output in gasification reactor 3 and reforming reactor 5.
Blast furnace slag particle collector 12 is connected with heat exchanger 10, for receiving the slag particle of the discharge of heat exchanger 10.Thus, it is possible to
Be interpreted as, the recycling of blast furnace cinder residual heat and energy by the fine grain slurries memory 1 of carbonic solid fuels, slag ladle 2,
Gasification reactor 3, blast furnace cinder granulator 9, heat exchanger 10, blast furnace slag particle collector 12 are realized.
To sum up, the preparation system of the present embodiment is reacted using blast furnace cinder containing a large amount of high-quality waste heats and solid fuel gasification
The characteristics of needing heat to supply, a kind of hydrogen-rich synthetic gas preparation system for proposing melting slag waste heat driving of innovation.It devises simultaneously
It is molten to be effectively utilized blast furnace for gasification reactor 3 containing blast furnace cinder, vapor and the fine grain slurries of carbonic solid fuels
The progress of the high-quality waste heat driving gasification reaction of slag, and it is additionally arranged heat exchanger 10, the blast furnace being discharged using gasification reactor 3
The after-heat of slag, in addition reforming reactor 5, which is arranged, is changed into hydrogen-rich synthetic gas for the crude synthesis gas of acquisition.It is of the invention as a result,
The technical advantage of gasification reactor 3, reforming reactor 5 and heat exchanger 10 has been coupled, the height of blast furnace cinder has both been effectively utilized
Quality residual heat and energy, and realize the preparation of hydrogen-rich synthetic gas.To sum up, preparation system of the invention realizes hydrogen-rich synthetic gas
The high-quality blast furnace cinder waste heat utilized while preparation, process flow is simple, and cost and energy consumption are greatly reduced, pollution-free produce
It is raw, have great importance to the energy-saving of iron and steel enterprise.
With further reference to attached drawing 1, in the present embodiment, gasification reactor 3 is bubbling bed gasification reactor.Gasification reactor
3 top is set there are two fixed opening, is separately connected the fine grain slurries memory 1 of carbonic solid fuels and slag ladle 2；Together
When 3 top of gasification reactor be additionally provided with the outlet of crude synthesis gas；The bottom end setting two of gasification reactor 3 is fixed to open
Mouthful, a fixed opening for be passed through heat exchanger 10 generation vapor, another fix open after for be discharged reaction after
Temperature decline blast furnace cinder, the temperature of blast furnace cinder at this time drop to 1250 DEG C hereinafter, its viscosity compared to gasification reaction
It significantly increases before.In the process, the blast furnace cinder of blast furnace discharge enters in slag ladle 2 and continuous with stable flow
Be passed into gasification reactor 3, opened when at 2/3rds positions that blast furnace cinder amount has reached 3 total capacity of gasification reactor
Begin while being passed through the fine grain slurries of carbonic solid fuels and heat exchanger 10 in the fine grain slurries memory 1 of carbonic solid fuels
The vapor of generation.Temperature rises rapidly when the fine grain slurries of carbonic solid fuels and vapor enter in gasification reactor 3
To 1250 DEG C -1450 DEG C, the fine grain slurries of carbonic solid fuels, vapor and blast furnace cinder contact with each other and gasified reverse occur height
Crude synthesis gas should be generated, with being continuously added for the fine grain slurries of carbonic solid fuels, vapor and blast furnace cinder, blast furnace is molten
Slag is continuously gasification reaction supply heat, and gasification reaction is also carrying out rapidly.The thick synthesis constantly generated in this process
Gas and the ash content of carrying have gasification reactor 3 to enter crude synthesis gas and ash separation in cyclone separator 4.As a result, may be used
Gasification reaction is interpreted as to start rapidly with the addition of the fine grain slurries of carbonic solid fuels and vapor, blast furnace cinder
High-quality sensible heat and latent heat are changed into the chemical heat of gasification reaction, and i.e. conduct when vapor is passed through by 3 bottom of gasification reactor
Gasifying agent generates bubbling again, plays the role of being stirred to react area, increases the phase mutual connection of reactant, gasifying agent and blast furnace cinder
Touching.
With further reference to attached drawing 1, in the present embodiment, the fine grain slurries memory 1 of carbonic solid fuels with do not have
Specific limitation, it is only necessary to use technology maturation, operating aspect and widely used relevant apparatus.
With further reference to attached drawing 1, in the present embodiment, slag ladle 2 does not have specific limitation, it is only necessary to using technology at
It is ripe, operating aspect and widely used relevant apparatus.The selection of slag ladle 2 should match with blast furnace bed drain purge, in system
The quantity for being equipped with slag ladle 2 is not limited only to 1, can carry out storage blast furnace cinder, the use of slag ladle 2 using multiple slag ladles
It needs to guarantee that stablizing for slag stream is flowed out in the process, prevents slag blocking outlet, should have certain preventing clogging up device；Simultaneously because
The temperature of blast furnace cinder is high, and corrosivity is stronger, and the slag ladle of use need to have good thermal insulation property and corrosion resistance, to protect
Demonstrate,prove the trouble-free operation of whole system.
With further reference to attached drawing 1, in the present embodiment, the bottom of gasification reactor 3 is equipped with fixed steam entry, this
Invention is not limited to that the steam entry of multiple uniform/uneven distributions can also be used using an entrance.It is multiple uniformly/
The steam entry of uneven distribution is more advantageous to the mutual of the fine grain slurries of carbonic solid fuels, vapor and blast furnace cinder
Contact.
With further reference to attached drawing 1, in the present embodiment, the invention is not limited to be gasification with bubbling bed gasification reactor
Reactor 3, it is any that the reactor of blast furnace cinder, carbonic solid fuels fine grain slurries and vapor can be provided simultaneously
As gasification reactor 3, and the inlet/outlet of each position is also not limited to the position of gasification reactor 3, and each position enters
Mouth/outlet can be different according to the structure of different gasification reactors, guarantee blast furnace cinder, carbonic solid fuels in the process
The intake of fine grain slurries and vapor matches.
With further reference to attached drawing 1, in the present embodiment, cyclone separator 4 and gasification reactor 3, reforming reactor 5 and
Ash content collector 11 is connected.Specifically, being provided with entrance in the side wall surface of cyclone separator 4, crude synthesis gas and ash content pass through
This entrance enters in cyclone separator；And outlet is provided on the other side upper wall surface of cyclone separator 4, the outlet is for revolving
The exclusion for the synthesis gas without containing ash content that wind separator 4 has been handled；The bottom of cyclone separator 4 is provided with ash outlet, should
Outlet is used for the discharge of ash content.From above it is to be understood that the crude synthesis gas containing synthesis gas and ash content is entered by gas access
Into cyclone separator, then it is discharged by isolated synthesis gas by gas vent, ash content is discharged by outlet at bottom.The invention patent
Cyclone separator 4 be not specifically designed, the size and treating capacity of cyclone separator 4 and gasification reactor 3 match.
With further reference to attached drawing 1, in the present embodiment, ash content collector 11 does not have specific limitation, it is only necessary to use skill
Art is mature, operating aspect and widely used relevant apparatus.
With further reference to attached drawing 1, in the present embodiment, reforming reactor 5 be fixed bed reactors, reforming reactor 5 with
Cyclone separator 4 is connected to receive the synthesis gas of removal ash content.Specifically, the side wall surface setting fixation of reforming reactor 5
Air intake removes the synthesis gas of ash content to receive, after another side wall surface is also provided with a fixed air intake so that reforming reaction is discharged
Synthesis gas, in bottom, the fixed air intake of setting is to receive the synthesis gas generated by heat exchanger 10.Inside reforming reactor
Placed load type metal catalyst, wherein active component be mainly the metallic monomers such as platinum, gold, silver, iron, molybdenum, copper and cobalt or
Wherein any two kinds or more the composite load type metallic catalysts being combined.
With further reference to attached drawing 1, in the present embodiment, the invention is not limited to using fixed bed reactors as reforming reaction
Device 5, any reforming reactor that can complete water gas shift reaction can be used as reforming reactor 5, and the entrance of each position/
Outlet is also not limited to the position of reforming reactor 5, and the inlet/outlet of each position can be according to the knot of different reforming reactors
Structure and it is different, in the process guarantee carbon monoxide transformation efficiency with higher.
With further reference to attached drawing 1, in the present embodiment, absorption tower 6 is connected with reforming reactor 5, does not have specific
Limitation, it is only necessary to use technology maturation, operating aspect and widely used relevant apparatus.Specifically, the side wall surface on absorption tower 6
Fixed air intake is set to receive the synthesis gas of the preparation of reforming reactor 5, center of top is provided with spray equipment to absorb and close
At the carbon dioxide in gas, in the fixed gas outlet of the another side setting on absorption tower 6 carbon dioxide gas is discharged away
Synthesis gas, main become in synthesis gas is hydrogen and vapor at this time.
With further reference to attached drawing 1, in the present embodiment, drier 7 is connected with absorption tower 6, does not there is specific limitation,
It only needs using technology maturation, operating aspect and widely used relevant apparatus.Specifically, the side wall surface of drier 7 is equipped with
Dry hydrogen-rich synthetic gas is discharged to complete the drying of synthesis gas in air intake and gas outlet.
With further reference to attached drawing 1, in the present embodiment, hydrogen storage device 8 is connected with drier 7, does not there is specific limitation,
It only needs using technology maturation, operating aspect and widely used relevant apparatus.
With further reference to attached drawing 1, in the present embodiment, blast furnace cinder granulator 9 is connected with gasification reactor 3, will
The blast furnace cinder of gasification reactor discharge forms slag particle.Specifically, there are two opposed steerings for setting in blast furnace cinder granulator
Opposite rotary drum, blast furnace cinder are flowed into two rotary drum middle positions after being discharged by gasification reactor, go forward side by side through drum rotating drive
One step cools down to form the slag particle of surface scull.
With further reference to attached drawing 1, in the present embodiment, blast furnace cinder granulator 9 is not limited in the rotary drum in attached drawing 1
Formula, any granulated slag granulator of dry type blast furnace cinder that can complete can be used as blast furnace cinder granulator 9, protect in the process
Demonstrate,prove granulation efficiency with higher and more uniform blast furnace slag grain diameter.
With further reference to attached drawing 1, in the present embodiment, heat exchanger 10 is connected with blast furnace cinder granulator 9, to recycle height
Residual heat and energy entrained by the blast furnace slag particle being discharged in furnace slag granulating device.Specifically, the slag particle that blast furnace cinder granulator is formed
It enters in heat exchanger 10, the side wall of heat exchanger 10 is water-cooling wall, and high temperature slag particle is formed with the cold water indirect heat exchange in water-cooling wall
Vapor is in gasification reactor 3 and reforming reactor 5.
With further reference to attached drawing 1, in the present embodiment, the invention is not limited to using indirect heat exchanger as heat exchanger 10,
Any heat exchanger that can effectively recycle slag particle waste heat and form vapor can be used as heat exchanger 10, and the position of water-cooling wall
It is not limited to the position of heat exchanger 10, can be different according to various heat exchange device structure, guarantee heat exchange efficiency in the process.
With further reference to attached drawing 1, in the present embodiment, blast furnace slag particle collector 12 is connected with heat exchanger 10, does not have
Specific limitation, it is only necessary to use technology maturation, operating aspect and widely used relevant apparatus.
A kind of hydrogen-rich synthetic gas preparation method of melting slag waste heat driving is additionally provided in the present embodiment, in the present embodiment
In, preparation method can refer to above-mentioned preparation system and be implemented.Specifically comprise the following steps:
S1. blast furnace cinder, vapor and the fine grain slurries of carbonic solid fuels carry out gasification reaction, generate with an oxidation
Crude synthesis gas and ash content based on carbon and hydrogen.
S2. separating treatment is carried out to the crude synthesis gas of formation and ash content.
S3. crude synthesis gas is passed into reforming reactor and carries out reforming reaction with vapor, the gas of generation mainly wraps
Include hydrogen, carbon dioxide and vapor.
S4. the synthesis gas of formation is passed into absorption tower and removes carbon dioxide, generated comprising hydrogen and vapor
Synthesis gas.
S5. the synthesis gas comprising hydrogen and vapor of generation is passed through in drying tower, forms hydrogen-rich synthetic gas.
S6. the heat of blast furnace slag particle is formed by way of heat exchange vapor, and sends back in S1 and S3 step and uses.
In conclusion the preparation method of the present embodiment contains a large amount of high-quality waste heats and solid fuel gasification using blast furnace cinder
The characteristics of reaction needs heat to supply, the hydrogen-rich synthetic gas preparation method for proposing a kind of melting slag waste heat driving of innovation, by blast furnace
The waste heat of slag is used for the gasification reaction of solid fuel, and the high-quality latent heat of especially blast furnace cinder has obtained effective utilization,
The waste heat that gasification reaction passes through blast furnace cinder with vapor used in reforming reaction process simultaneously generates, such mode
Reduce energy consumption.As a result, preparation method of the invention coupled blast furnace cinder UTILIZATION OF VESIDUAL HEAT IN and solid fuel gasification reaction and
The technical advantage of reforming reaction, had not only been effectively utilized the high-quality residual heat and energy of blast furnace cinder, but also realized hydrogen-rich synthetic gas
Preparation.To sum up, preparation method of the invention realizes more than the high-quality blast furnace cinder utilized while the preparation of hydrogen-rich synthetic gas
Heat, process flow is simple, and cost and energy consumption are greatly reduced, and contamination-free generates, to the energy-saving with important of iron and steel enterprise
Meaning.
Further, in the present embodiment, the gasification reaction temperature in step S1 is 1250 DEG C -1450 DEG C；In step S3
Reforming reaction temperature is 350 DEG C -650 DEG C.
Further, in the present embodiment, the concentration of the fine grain slurries of carbonic solid fuels in step S1 is 50%-
60%.
Further, in the present embodiment, the carbonaceous solids combustion in the fine grain slurries of carbonic solid fuels in step S1
Expect that fine grained diameter is 100 μm -300 μm.
Further, in the present embodiment, the carbonaceous solids combustion in the fine grain slurries of carbonic solid fuels in step S1
Expect that fine grained includes high-order coal, scala media coal, low-order coal, coal tar, biomass, petroleum coke, oil shale and carbonaceous solids waste.
Further, in the present embodiment, reforming reaction catalyst is added in step S3, catalyst is mainly load type gold
Metal catalyst, wherein active component be mainly the metallic monomers such as platinum, gold, silver, iron, molybdenum, copper and cobalt or wherein any two kinds and
The composite load type metallic catalyst being combined above.
Using above-mentioned preparation method and preparation system, by taking carbonic solid fuels coal dust as an example, the Industrial Analysis and member of coal dust
As shown in table 1, the component for the hydrogen-rich synthetic gas prepared and the concentration of each component are as shown in table 2 for element analysis.
The Industrial Analysis and elemental analysis of 1 coal dust of table
The component and concentration of component of 2 hydrogen-rich synthetic gas of table
| Synthesis gas components | H2 | CO | CO2 | CH4 |
| Concentration of component (%) | 94.13 | 5.64 | 0.23 | - |
As shown in Table 2, the hydrogen-rich synthetic gas preparation method and be that the melting slag waste heat provided in above-mentioned two embodiment drives
System had both realized the preparation of hydrogen-rich synthetic gas, concentration of component has reached 94.13%, and effective recycling blast furnace cinder
High-quality residual heat and energy.
Obviously, preparation method of the invention be not limited to the embodiment one shown by preparation system, as long as can complete to walk
Rapid S1 and step S3.Simultaneously, it is emphasized that, although being sorted in preparation method with S1-S6, not structure
The restriction of pairs of step sequencing, except non-post step must utilize product or this professional domain the relevant technologies people of first step
The case where needing first step to first carry out well known to member, is otherwise not limited to sequence listed by above-described embodiment.
The technical principle of the invention is described above in combination with a specific embodiment, these descriptions are intended merely to explain of the invention
Principle shall not be construed in any way as a limitation of the scope of protection of the invention.Based on explaining herein, those skilled in the art
It can associate with other specific embodiments of the invention without creative labor, these modes fall within this hair
Within bright protection scope.
Claims (10)
1. a kind of hydrogen-rich synthetic gas preparation method of melting slag waste heat driving, includes the following steps:
S1: blast furnace cinder, vapor and the fine grain slurries of carbonic solid fuels carry out gasification reaction, generate with carbon monoxide and
Crude synthesis gas and ash content based on hydrogen；
S2: crude synthesis gas and vapor are subjected to reforming reaction, the synthesis gas of generation includes hydrogen, carbon dioxide and vapor；
S3: the carbon dioxide in the synthesis gas generated in S2 is removed, the synthesis gas comprising hydrogen and vapor is generated；
S4: by removing comprising the vapor in hydrogen and vapor for generation, hydrogen-rich synthetic gas is formed；
Vapor is prepared using the heat that reaction generates clinker in step S1, and required water is provided for the reaction process of S1 and S2
Steam.
2. the hydrogen-rich synthetic gas preparation method of melting slag waste heat driving according to claim 1, it is characterised in that:
After step S1, further include the steps that crude synthesis gas and ash content are separated.
3. the hydrogen-rich synthetic gas preparation method of melting slag waste heat driving according to claim 1, it is characterised in that:
Gasification reaction temperature in step S1 is 1450 DEG C -1250 DEG C；
Reforming reaction temperature in step S3 is 350 DEG C -650 DEG C.
4. the hydrogen-rich synthetic gas preparation method of melting slag waste heat driving according to claim 1, it is characterised in that:
The concentration of the fine grain slurries of carbonic solid fuels in step S1 is 50%-60%.
5. the hydrogen-rich synthetic gas preparation method of melting slag waste heat driving according to claim 1, it is characterised in that:
The carbonic solid fuels fine grained diameter in the fine grain slurries of carbonic solid fuels in step S1 is 100 μm of -300 μ
m。
6. the hydrogen-rich synthetic gas preparation method of melting slag waste heat driving according to claim 1, it is characterised in that:
The carbonic solid fuels fine grained in the fine grain slurries of carbonic solid fuels in step S1 includes high-order coal, scala media
Coal, low-order coal, coal tar, biomass, petroleum coke, oil shale and/or carbonaceous solids waste.
7. the hydrogen-rich synthetic gas preparation method of melting slag waste heat driving according to claim 1, it is characterised in that:
Reforming reaction catalyst is added in step S3, catalyst includes load type metal catalyst；
Active component in load type metal catalyst include platinum, gold, silver, iron, molybdenum, copper or cobalt metallic monomer or platinum, gold,
Any two kinds or more the composite load type metallic catalysts being combined in silver, iron, molybdenum, copper and cobalt.
8. a kind of hydrogen-rich synthetic gas preparation system of melting slag waste heat driving, which is characterized in that it is used as claim 1-7 is any
The hydrogen-rich synthetic gas preparation method of the driving of melting slag waste heat described in one carries out the preparation of hydrogen-rich synthetic gas comprising gasification reaction
Device, reforming reactor and heat exchanger；
Gasification reactor has high-temperature slag entrance, injection point, steam entry, slag outlet and syngas outlet, wherein
High-temperature slag is inputted in gasification reactor by slag entrance, and the fine grain slurries of carbonic solid fuels are inputted by injection point
Into gasification reactor, vapor is input in gasification reactor by steam entry；
Blast furnace cinder, vapor and the fine grain slurries of carbonic solid fuels are chemically reacted in gasification reactor, and will
The crude synthesis gas generated after reaction is input in reforming reactor, and clinker is input in heat exchanger, heat exchanger by with clinker
Heat exchange prepares vapor；
The steam outlet of heat exchanger is connected to the steam entry of gasification reactor, reforming reactor.
9. the hydrogen-rich synthetic gas preparation system of melting slag waste heat driving according to claim 8, which is characterized in that
The system further include slag ladle, the fine grain slurries memory of carbonic solid fuels, separation equipment, collector, absorption tower,
Drier, hydrogen storage device and blast furnace slag particle collector；
Slag ladle is connected with slag entrance, and slag ladle is used to store the high-temperature slag of blast furnace discharge, enables high-temperature slag steady
Fixed and continuous output；
The fine grain slurries memory of carbonic solid fuels is connected with injection point, the fine grain slurries storage of carbonic solid fuels
The device carbonic solid fuels fine grain slurries good for storage configuration, provide reaction for the gasification reaction in gasification reactor
Object；
Separation equipment is provided between gasification reactor and reforming reactor, separation equipment can receive gasification reactor generation
Crude synthesis gas and ash content based on carbon monoxide and hydrogen, and crude synthesis gas is exported with ash separation and respectively, will point
The crude synthesis gas come is separated out to be input in reforming reactor；
Collector is connected with the ash outlet end of separation equipment, is used to collect the ash content of separation equipment output；
Absorption tower is connected with the gas outlet end of reforming reactor, and what absorption tower was used to receive reforming reactor output includes hydrogen
The synthesis gas of gas, carbon dioxide and vapor, and carbon dioxide therein is absorbed, formation includes the synthesis of hydrogen and vapor
Gas simultaneously exports；
Absorption tower is connected with drier, and what drier was used to receive absorption tower output includes the synthesis of hydrogen and vapor
Gas absorbs vapor therein, forms hydrogen-rich synthetic gas and exports；
Hydrogen storage device is connected with drier, hydrogen-rich synthetic gas and storage of the hydrogen storage device for receiving dryer output；
Blast furnace cinder granulator is arranged between heat exchanger and gasification reactor, and blast furnace cinder granulator is for receiving gasification reaction
Blast furnace cinder after the gasification reaction of device discharge forms high temperature slag particle and exports；
Heat exchanger is used to receive the high temperature slag particle of blast furnace cinder granulator formation, and vapor is generated by way of heat exchange and is exported
Into gasification reactor and reforming reactor；
Blast furnace slag particle collector is connected with heat exchanger, and blast furnace slag particle collector is used to receive the slag particle of heat exchanger discharge.
10. the hydrogen-rich synthetic gas preparation system of melting slag waste heat driving according to claim 9, it is characterised in that:
Separation equipment is cyclone separator；Gasification reactor is bubbling bed gasification reactor；Reforming reactor is fixed bed reformation
Reactor；Heat exchanger is indirect type heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910305887.8A CN109880653B (en) | 2019-04-16 | 2019-04-16 | Preparation method and system of hydrogen-rich synthesis gas driven by residual heat of molten slag |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910305887.8A CN109880653B (en) | 2019-04-16 | 2019-04-16 | Preparation method and system of hydrogen-rich synthesis gas driven by residual heat of molten slag |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109880653A true CN109880653A (en) | 2019-06-14 |
| CN109880653B CN109880653B (en) | 2020-09-15 |
Family
ID=66937696
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910305887.8A Expired - Fee Related CN109880653B (en) | 2019-04-16 | 2019-04-16 | Preparation method and system of hydrogen-rich synthesis gas driven by residual heat of molten slag |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109880653B (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3841851A (en) * | 1974-02-12 | 1974-10-15 | E Kaiser | Process and apparatus for the gasification of organic matter |
| CN101665724A (en) * | 2008-09-05 | 2010-03-10 | 绿色煤电有限公司 | Water-coal-slurry gasification method and gasification furnace |
| CN105087835A (en) * | 2015-08-26 | 2015-11-25 | 中冶南方工程技术有限公司 | System and method for recycling high-temperature slag waste heat in coal gasification manner |
| CN107057767A (en) * | 2017-03-17 | 2017-08-18 | 北京交通大学 | One kind is based on CO before chemical chain making oxygen by air separation and burning2The electricity generation system of trapping |
-
2019
- 2019-04-16 CN CN201910305887.8A patent/CN109880653B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3841851A (en) * | 1974-02-12 | 1974-10-15 | E Kaiser | Process and apparatus for the gasification of organic matter |
| CN101665724A (en) * | 2008-09-05 | 2010-03-10 | 绿色煤电有限公司 | Water-coal-slurry gasification method and gasification furnace |
| CN105087835A (en) * | 2015-08-26 | 2015-11-25 | 中冶南方工程技术有限公司 | System and method for recycling high-temperature slag waste heat in coal gasification manner |
| CN107057767A (en) * | 2017-03-17 | 2017-08-18 | 北京交通大学 | One kind is based on CO before chemical chain making oxygen by air separation and burning2The electricity generation system of trapping |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109880653B (en) | 2020-09-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110872531B (en) | Step waste heat recovery device and method utilizing pyrolysis gasification of solid particle heat carrier | |
| BRPI0920029B1 (en) | PROCESS FOR DIRECT REDUCTION OF IRON ORE | |
| CN103014202B (en) | Device and method for recovering high-temperature sensible heat of liquid blast furnace slag | |
| MXPA05000222A (en) | Method for the production of hydrogen-containing gaseous mixtures. | |
| CN102183152A (en) | Steel enterprise associated energy combined cycle power generation system and method | |
| CN103911179B (en) | Coal gasification method and device | |
| WO2012068930A1 (en) | Medium to low temperature pyrolysis system for upgrading the quality of coal or biomass, and method of producing upgraded coal, high calorific value pyrolysis gas and tar or liquefied synthetic oil by using the system | |
| CN111979371A (en) | Method for distributed utilization of heat in process of producing direct reduced iron by dry quenching coupled shaft furnace | |
| CN105885953A (en) | Device and method for preparing reducing gas through lignite gasification poly-generation | |
| CN110591745A (en) | Pyrolysis-gasification integrated device and process | |
| CN104745222A (en) | Moving bed self-heating type pressure gasification hydrogen-rich environment dry distillation furnace and dry distillation method thereof | |
| CN104945215B (en) | Method and system for preparing ethylene from powdered coal | |
| CN109401794B (en) | Staged conversion combined fluidized bed reaction device and reaction method | |
| JP4250472B2 (en) | Method for producing reduced iron and reducing gas for blast furnace charge, method for using reduced iron, and method for using reducing gas | |
| CN109880653A (en) | A kind of the hydrogen-rich synthetic gas preparation method and system of melting slag waste heat driving | |
| CN206428193U (en) | A kind of system of coal hydrogenation pyrolysis | |
| CN115717090A (en) | Method for preparing synthesis gas from semi-coke oven gas | |
| CN204981692U (en) | System for fine coal preparation ethylene | |
| CN210711404U (en) | Pyrolysis-gasification integrated device | |
| CN106497594A (en) | A kind of system and method for coal hydrogenation pyrolysis | |
| CN108486304B (en) | A kind of coal gasification heating gas is directly used in the device and method of gas-based shaft kiln production direct reduced iron | |
| CN207121422U (en) | A kind of preparation system of gas-based shaft kiln also Primordial Qi | |
| CN111733322A (en) | Device system and method for absorbing copper slag waste heat in stepped manner based on coal gasification reaction | |
| CN205933213U (en) | System for carbide slag preparation hydrogen -rich gas and carbide | |
| CN105531355A (en) | Method and system for gasifying carbon carriers and further treating the produced gases |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20200915 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |