CN1576379A - Effective utilizing method for carbon resource - Google Patents
Effective utilizing method for carbon resource Download PDFInfo
- Publication number
- CN1576379A CN1576379A CNA2004100545828A CN200410054582A CN1576379A CN 1576379 A CN1576379 A CN 1576379A CN A2004100545828 A CNA2004100545828 A CN A2004100545828A CN 200410054582 A CN200410054582 A CN 200410054582A CN 1576379 A CN1576379 A CN 1576379A
- Authority
- CN
- China
- Prior art keywords
- reducing gas
- furnace
- gas
- reducing
- coal
- 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
- 238000000034 method Methods 0.000 title claims abstract description 35
- 229910052799 carbon Inorganic materials 0.000 title description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title description 2
- 239000007789 gas Substances 0.000 claims abstract description 234
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 205
- 239000003245 coal Substances 0.000 claims abstract description 89
- 229910052742 iron Inorganic materials 0.000 claims abstract description 71
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 58
- 239000011593 sulfur Substances 0.000 claims abstract description 58
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 57
- 239000007787 solid Substances 0.000 claims abstract description 37
- 239000002994 raw material Substances 0.000 claims abstract description 36
- 238000010248 power generation Methods 0.000 claims abstract description 33
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 28
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000001257 hydrogen Substances 0.000 claims abstract description 24
- 238000004519 manufacturing process Methods 0.000 claims abstract description 20
- 230000009467 reduction Effects 0.000 claims description 71
- 238000002309 gasification Methods 0.000 claims description 51
- 238000001816 cooling Methods 0.000 claims description 40
- 239000002028 Biomass Substances 0.000 claims description 25
- 239000002699 waste material Substances 0.000 claims description 23
- 239000004033 plastic Substances 0.000 claims description 17
- 229920003023 plastic Polymers 0.000 claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 238000010521 absorption reaction Methods 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 239000003575 carbonaceous material Substances 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 3
- 239000010419 fine particle Substances 0.000 claims 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 abstract 1
- 238000006722 reduction reaction Methods 0.000 description 73
- 239000000428 dust Substances 0.000 description 27
- 238000006477 desulfuration reaction Methods 0.000 description 24
- 230000023556 desulfurization Effects 0.000 description 24
- 229910002092 carbon dioxide Inorganic materials 0.000 description 18
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 14
- 238000011084 recovery Methods 0.000 description 10
- 239000000843 powder Substances 0.000 description 9
- 239000001569 carbon dioxide Substances 0.000 description 7
- 239000000446 fuel Substances 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 230000005855 radiation Effects 0.000 description 6
- 239000003638 chemical reducing agent Substances 0.000 description 5
- 239000000571 coke Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 3
- -1 coal Chemical compound 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000010276 construction Methods 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000001465 metallisation Methods 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- QVGXLLKOCUKJST-IGMARMGPSA-N oxygen-16 atom Chemical compound [16O] QVGXLLKOCUKJST-IGMARMGPSA-N 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 238000010298 pulverizing process Methods 0.000 description 3
- 239000010959 steel Substances 0.000 description 3
- 238000010792 warming Methods 0.000 description 3
- 239000002023 wood Substances 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 229910000805 Pig iron Inorganic materials 0.000 description 2
- 239000004698 Polyethylene Substances 0.000 description 2
- 239000004743 Polypropylene Substances 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 239000000112 cooling gas Substances 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000002093 peripheral effect Effects 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 229920000573 polyethylene Polymers 0.000 description 2
- 229920001155 polypropylene Polymers 0.000 description 2
- 239000004800 polyvinyl chloride Substances 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 244000068988 Glycine max Species 0.000 description 1
- 235000010469 Glycine max Nutrition 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 239000004793 Polystyrene Substances 0.000 description 1
- 241000209140 Triticum Species 0.000 description 1
- 235000021307 Triticum Nutrition 0.000 description 1
- 239000002154 agricultural waste Substances 0.000 description 1
- 238000009933 burial Methods 0.000 description 1
- VTVVPPOHYJJIJR-UHFFFAOYSA-N carbon dioxide;hydrate Chemical compound O.O=C=O VTVVPPOHYJJIJR-UHFFFAOYSA-N 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 239000010903 husk Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 125000001967 indiganyl group Chemical group [H][In]([H])[*] 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 229920000915 polyvinyl chloride Polymers 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 239000011369 resultant mixture Substances 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 230000001568 sexual effect Effects 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 239000003476 subbituminous coal Substances 0.000 description 1
- 150000003464 sulfur compounds Chemical class 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
-
- 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
- Y02P10/00—Technologies related to metal processing
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
- Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/20—Waste processing or separation
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/62—Plastics recycling; Rubber recycling
Abstract
The invention provides a method where carbonaceous resources such as coal are gasified so as to produce a reducing gas, and reduced iron, hydrogen and electric power are simultaneously produced with high efficiency using the reducing gas.In the efficient application method of carbonaceous resources, a sulfur component-containing carbonaceous raw material 15 (such as coal) is partially burned with oxygen 16 to produce a reducing gas 11; the reducing gas 11 and iron ore 2 are brought into contact in a solid reducing furnace 4 to reduce the iron ore, so that sulfur component-containing solid reduced iron 3 is produced; and further, the desulfurized reducing gas 11 is produced. The sulfur component included in the reducing gas 11 is moved to the reduced iron 3 in the solid reducing furnace 4, so that the desulfurized reducing gas 11 is obtained. The sulfur-containing solid reduced iron 3 is charged to a blast furnace. The desulfurized reducing gas 11 is utilized for gaseous hydrogen production and/or combined power generation.
Description
Technical Field
The present invention relates to a method for producing a reducing gas by gasifying a carbonaceous resource such as coal, and efficiently producing reduced iron, hydrogen, and electricity simultaneously using the reducing gas.
Background
It is known to use CO gas and H in solid reduction furnaces2A method for producing reduced iron from a reducing gas containing a gas as a main component. The solid reduction furnace uses a shaft furnace and a fluidized bed. FIG. 2 shows an example of a reduction method using a shaft furnace. The natural gas is reformed by steam in the reducing gas generator 1 to produce H2In a solid reducing furnace 4, iron ore 2 is directly contacted with reducing gas of 700-900 ℃ with gas and CO gas as main components, and CO and H2Conversion to CO2And H2And O, removing oxygen in the iron ore to reduce. The gas for reducing iron ore contains iron powder dust, CO and H due to high temperature2Therefore, the heat is recovered by the heat recovery device 5, the dust is removed by the dust collecting device 6, the cooled gas is cooled by the gascooling device 7, the carbon dioxide is removed by the carbon dioxide removing device 9, and then the gas is reheated by the gas heating furnace 10 and reused as the reducing gas.
As a raw material for producing the reducing gas, it is appropriate to use coal instead of natural gas. Because of abundant coal burial quantity, stable supply and low price, the coal can be stably used for a long time. FIG. 3 shows an example of a process for producing reduced iron using coal as a raw material. The reducing gas is produced in a coal gasifier 12. Pulverized coal obtained by pulverizing coal 15 is introduced into gasification furnace 12 from a gasification combustion furnace together with oxygen 16 (steam 17 is added as needed) and gasified. In order to melt and separate ash in coal, the gasification temperature is generally 1400-1700 ℃. The gasified gas enters the cooling furnace 13 through the upper part of the gasification furnace. Most of the ash in the coal is melted and falls from the lower part of the gasification furnace to become solidified slag. In the cooling furnace 13, a radiation boiler is disposed inside, and the gas is cooled by radiation heat transfer, or the gas discharged from the cooling furnace is heat-recovered, dust-removed, cooled, and then introduced into the cooling furnace.
Patent document 1 describes an invention in which the production of a reducing gas by coal gasification and the reduction of iron ore by the gas are effectively combined. When a reducing gas produced from natural gas is used, the gas used for reduction is heat-recovered, dedusted, cooled, decarbonized, and then reheated to be reused as the reducing gas. When the reducing gas gasified by coal is used, as shown in fig. 3, a part of the reducing gas discharged from the reducing furnace 4 is heat-recovered by the heat recovery device 5, dust is removed by the dust collecting device 6, the gas is cooled by the gas cooling device 7, and the gas is decarbonized by the decarbonizing device 9, and then the gas is introduced into the cooling furnace without reheating. The high-temperature gas gasified by the gasification furnace and the recycled low-temperature reducing gas are mixed in the cooling furnace, and the temperature of 700-900 ℃ suitable for reducing the iron ore can be adjusted.
In the invention described in patent document 1, carbon dioxide is removed from the gas used for reduction, and a part of the gas is discharged to the outside of the system. In the production of reducing gas by coal gasification, the sulfur in the coal contains converted hydrogen sulfide gas. Therefore, it is preferable to provide a desulfurization device or the like for removing sulfur in the gas as necessary for the treatment of the gas discharged to the outside of the system.
Non-patent document 1 describes integrated coal gasification combined cycle power generation using a gas produced from a coal gasifier as a fuel. One example is shown in figure 5. The gasified reducing gas is roughly collected by a cyclone dust collector, then heat-recovered by a heat recovery unit 5, dust-removed by a dust collector 6, cooled by a gas cooler 7, desulfurized and purified by a desulfurizer 21, and then supplied to a combined power generation unit 22 of a gas turbine or a steam turbine.
[ patent document 1]
Japanese laid-open patent publication No. 2000-212620
[ patent document 2]
Japanese laid-open patent publication No. 2002-146420
[ patent document 3]
Japanese patent laid-open publication No. Hei 8-253801
[ non-patent document 1]
"gasification Combined cycle Power Generation" thermal atomic Power Generation Vol.52, No.10(2001), pp 1244-
Disclosure of Invention
Since the coal gasifier and its peripheral equipment are expensive to construct, it is an obstacle to commercialization of coal gasification direct reduction iron-making or coal gasification combined cycle power generation. The first object of the present invention is to improve the equipment investment efficiency and enable commercialization of coal gasification direct reduction iron making and coal gasification combined cycle power generation.
The coal gasification gas contains sulfur. On the other hand, reduced iron produced by reduction iron making is generally used as a raw material for electric furnaces, and it is required to have a low sulfur content as an impurity. Therefore, in the coal gasification direct reduction iron making, as described in patent document 2, a gas desulfurization device 20 needs to be installed in front of the reduction furnace. Therefore, the steel sheet must be cooled once to a temperature of 400 to 500 ℃ at which desulfurization is possible, desulfurized, and then heated to about 900 ℃ and charged into a reduction furnace. In the integrated coal gasification combined cycle power generation, as described in non-patent document 1, desulfurization of gas is performed by the desulfurizer 21 before the integrated power generation. When the reducing gas used in coal gasification direct reduction iron making is discharged to the outside of the system and reused, it is preferable to provide a desulfurization device for removing sulfur in the gas, as described in patent document 1. In this way, when the coal gasification gas is used, a desulfurization unit is required, which is a factor of high construction cost of the peripheral equipment of the coal gasification furnace. The second purpose of the invention is to eliminate the need of a desulfurization device in the coal gasification direct reduction iron making or coal gasification combined cycle power generation. Meanwhile, the purpose is to simplify the additional equipment except the desulfurization equipment.
In response to the problem of global warming, development and practical use of new energy, conversion to low-carbon dioxide-generating energy, improvement of atomic energy ratio, efficient and rational utilization of primary energy, utilization of unused energy and waste energy, and the like have been advanced. In particular, biomass is carbon neutral, and it can be said that it is a resource to be substituted for petroleum, coal, and the like. Further, it can be said that waste plastics are actively utilized as resources to be substituted for petroleum, coal, and the like. The third object of the present invention is to reduce the emission of carbon dioxide by using biomass and waste plastic instead of coal.
Namely, the gist of the present invention is as follows:
(1) a method for effectively utilizing a carbonaceous material 15 containing sulfur by partially combusting a carbonaceous material with oxygen 16 to produce a reducing gas 11, and bringing the reducing gas11 into contact with an iron ore 2 in a solid reducing furnace 4 to reduce the iron ore to produce a solid reduced iron 3 containing sulfur and to produce a desulfurized reducing gas 11.
(2) The method for effectively utilizing a carbonaceous resource according to the above (1), wherein the reducing gas 11 discharged from the solid reducing furnace 4 and the fine iron ore and reduced iron powder discharged together with the reducing gas 11 are separated.
(3) The method for effectively utilizing a carbonaceous resource according to the above (1) or (2), characterized in that the desulfurized reducing gas 11 is obtained by transferring sulfur content contained in the reducing gas 11 to the reduced iron 3.
(4) The method for effectively utilizing a carbonaceous resource according to any one of the above (1) to (3), wherein the carbonaceous raw material 15 is coal.
(5) The method for effectively utilizing a carbonaceous resource according to any one of the above (1) to (4), wherein the carbonaceous raw material 15 contains one or both of biomass and waste plastics in addition to coal.
(6) The method for effectively utilizing carbonaceous resources according to item (5) above, characterized in that a cooling furnace 13 is connected to the gasification furnace 12 for producing the reducing gas 11, and a carbonaceous raw material containing one or both of biomass and waste plastics is charged into the cooling furnace 13.
(7) The method for effectively utilizing a carbonaceous resource according to any one of the above (1) to (6), wherein the solid reducing furnace 4 is a shaft furnace or a fluidized bed furnace.
(8) The method for effectively utilizing a carbonaceous resource according to any one of the above (1) to (7), wherein the reduced iron 3 containing the sulfur-containing solidis charged into a blast furnace.
(9) The method for effectively utilizing a carbonaceous resource according to any one of the above (1) to (8), wherein the desulfurized reducing gas 11 is used for hydrogen production and/or combined power generation.
(10) The method for effectively utilizing carbonaceous resources according to item (9) above, wherein the CO gas in the reducing gas is reformed into H by adding water and/or steam to the desulfurized reducing gas 11 to use sensible heat of the reducing gas as a heat source2Gas and CO2Gas, absorption separation of the CO2Gas to produce hydrogen.
In the present invention, sulfur in the reducing gas produced by using a carbonaceous raw material containing sulfur, particularly coal, is characterized in that the reducing gas is moved to reduced iron in the reduction furnace 4 from the reducing gas to produce reduced iron containing a solid containing sulfur, and as a result, the reducing gas discharged from the reduction furnace 4 is desulfurized. Therefore, when the reducing gas discharged from the reduction furnace 4 is used as a hydrogen production raw material and a composite power generation fuel, it is not necessary to provide a desulfurization facility for removing sulfur from the reducing gas. Further, since sulfur content in the reducing gas moves to the reduced iron, it is not necessary to provide a desulfurization facility for removing sulfur content from the reducing gas before charging into the reduction furnace.
In the present invention, the produced solid reduced iron is preferably charged into a blast furnace as a blast furnace charging raw material. Since the blast furnace itself has a desulfurization function, the sulfur content of the pig iron produced by the blast furnace increases very little even if sulfur is contained in the charged reduced iron. Therefore, even the reduced iron containing sulfur content produced according to the present invention can be used as an iron-making raw material without any problem.
The reducing agent for reducing iron ore in the blast furnace is coke, and the coal for preparing the coke can hardly use cheap common coal. And cheap common coal can be used in the coal gasification direct reduction iron making. Therefore, by charging reduced iron produced by coal gasification reduction iron making according to the present invention into a blast furnace, the cost of coal used for iron making can be reduced as a whole.
In the present invention, the reducing gas produced by gasifying the carbonaceous material is first used for reducing iron ore in the solid reduction furnace and then used for hydrogen production and combined power generation. Therefore, the heat recovery device, the dust collecting device, and the like of the reducing gas can be shared. Therefore, the incidental equipment can be effectively used as compared with the equipment for separately performing reduction iron making and combined power generation.
Drawings
FIG. 1 is a view showing a method for effectively utilizing a carbonaceous resource according to the present invention.
FIG. 2 is a diagram showing a conventional method for producing reduced iron.
FIG. 3 is a diagram showing a conventional method for producing reduced iron.
FIG. 4 is a diagram showing a conventional method for producing reduced iron.
Fig. 5 is a diagram showing a conventional integrated coal gasification combined cycle power generation method.
Description of the symbols
1 reducing gas generator 2 iron ore
3 reduced iron 4 solid reduction furnace (shaft furnace)
5 Heat recovery device 6 dust collecting device
7 gas cooling device 8 compressor
9 decarbonation device 10 gas heating furnace
11 reducing gas 12 coal gasifier
13 cooling furnace 14 cyclone dust collector
15 carbonaceous feedstock (coal) 16 oxygen
17 steam 18 coal moisture control device
19 gas washing cooling device 20, 21 desulphurization device
22 power generation device 23
24 shift reactor 25 hydrogen
26 carbonaceous 27 system effluent gas
Detailed Description
The invention is illustrated with reference to figure 1.
First, a description will be given of a gasification furnace for producing a reducing gas by partially combusting a carbonaceous raw material containing sulfur components with oxygen. In particular, since the case where the carbonaceous material is coal is explained, it may be referred to as a coal gasifier 12.
Pulverized coal obtained by pulverizing coal 15 is introduced into gasification furnace 12 from a gasification combustion furnace together with a gas containing oxygen 16 and steam 17 as needed. The gasification temperature is set to 1400-1700 ℃ for melting and separating ash in coal. Thereby, CO and H are prepared in the gasification furnace2A reducing gas as a main component. The reducing gas 11 contains 500 to 5000ppm of H derived from sulfur carried in from coal2S (partial COS). The gasified gas enters the cooling furnace 13 through the upper part of the gasification furnace. Most of the ash in the coal is melted, falls from the lower part of the gasification furnace, and is changed into solidified slag in the water tank.
The cooling furnace 13 is provided with a radiation boiler therein, and a cooling gas is transferred by radiation, or a part of a gas generated in the cooling furnace and a part of a reducing gas discharged from the reduction furnace is subjected to heat recovery, dust collection, and gas cooling is introduced into the cooling furnace. The present invention in which the carbonaceous raw material containing biomass and waste plastics is introduced into the cooling furnace will be described in detail later.
Since some solid components remain in the gas, the solid components are removed by the cyclone 14 as necessary. The solid component is used as a gasification raw material. The reduction furnace 4, if in the form of a fluidized bed, does not require a cyclone.
Next, the solid reduction furnace 4 that reduces iron ore by bringing the reducing gas 11 generated in the gasification furnace 12 into contact with the iron ore 2 will be described. The solid reduction furnace 4 may use a shaft furnace or a fluidized bed furnace. The shaft furnace is described here as an example.
The shaft furnace 4 is filled with granular iron ore or iron ore block, is successively reduced by the reducing gas 11 while descending in the shaft furnace 4, and is discharged as reduced iron 3 from the lower end of the shaft furnace. Iron ore 2 is charged from the upper end of the shaft furnace 4 to replenish the iron ore in the shaft furnace. On the other hand, a reducing gas 11 of about 900 ℃ is fed from the lower end of the shaft furnace 4, and during the ascent in the shaft furnace, the iron ore directly contacts the reducing gas, and CO and H in the reducing gas2Conversion to CO2、H2And O, removing oxygen in the iron ore to reduce. The reducing gas rises in the shaft furnace while undergoing the reduction reaction, and is discharged from the upper end of the shaft furnace.
The temperature of the reducing gas fed from the lower end of the shaft furnace is set to 700 to 900 ℃, and the temperature of the solid (reduced iron, iron ore) in the lower end of the shaft furnace is maintained at a temperature slightly lower than the gas temperature. The temperature is selected so that the reduction reaction in the shaft furnace can be efficiently performed. In the vertical temperature distribution in the shaft furnace, the temperatures of the reducing gas and the solid (reduced iron and iron ore) are lower as the temperature rises. The temperature of the gas and the solids in the upper end of the shaft furnace can be adjusted by adjusting the ratio (Ws/Wg) of the product Ws of the flow rate (kg/h) of the solids and the specific heat (kcal/kg/deg) of the solids to the product Wg of the flow rate (kg/h) of the gas and the specific heat (kcal/kg/deg) of the gas, and the temperature of the reducing gas fed from the lower end of the shaft furnace.
Conventionally, reduced iron produced by direct reduction iron making by coal gasification has been mainly used as a raw material for electric furnace steel making. Since steel produced by an electric furnace requires a low sulfur content, it is needless to say that reduced iron as a raw material also requires a low sulfur content.
Therefore, conventionally, it has been necessary to provide a desulfurization facility before the reduction furnace is charged, and to remove sulfur in the reducing gas.
On the other hand, the reaction of sulfur content in the furnace when no desulfurization facility is provided in front of the reduction furnace will be described. H in reducing gas in reduction furnace2The reaction of S and iron ore to produce FeS is carried out at a temperature of 400-600 ℃. Conventionally, in order to prevent the reaction from proceeding as much as possible, a temperature distribution in which the temperature in the shaft furnace reaches a range of 400 to 600 ℃ has been adopted. Specifically, the temperature of the reducing gas at the upper end of the shaft furnace is set to be in the temperature range of 550-700 ℃. Thus, 50% of the sulfur in the reducing gas fed into the shaft furnace is moved to the reduced iron, and the remaining 50% of the sulfur remains in the reducing gas and is discharged from the reducing furnace as it is.
In the present invention, as much sulfur content as possible in the reducing gas fed into the shaft furnace 4 is transferred to the reduced iron. Therefore, in the present invention, the temperature of the reducing gas in the upper end of the shaft furnace is set to 400 to 600 ℃, and more preferably 400 to 500 ℃. Thus, the temperature range of 400 to 600 ℃ in which desulfurization is performed by transferring sulfur from the reducing gas to the reduced iron can be expanded. As a result, the sulfur content in the reducing gas fed into the shaft furnace was shifted to about 90% to the reduced iron, and the sulfur content remaining in the reducing gas and discharged from the reducing furnace as it was controlled to 10% or less.
The reducing gas 11 discharged from the reduction furnace 4 is accompanied by fine iron ore and reduced iron powder. The reducing gas 11 is introduced into the dust collector 6, and the fine powder in the reducing gas is collected by the dust collector 6. However, the temperature of the reducing gas 11 is maintained at a high temperature of 400 ℃ or higher from the upper end of the reducing furnace 4 to the dust collecting device 6,and the temperatures of the fine iron ore and the reduced iron powder contained in the reducing gas are also maintained at the same temperature. Due to the fact thatThe temperature is in a temperature range in which desulfurization of the reducing gas is further carried out, and H remaining in the reducing gas2The fine iron ore and the fine reduced iron powder that have moved into the reducing gas while reaching the dust collector 6 are collected by the dust collector 6, and therefore the sulfur content of the reducing gas after passing through the dust collector 6 can be further reduced.
As described above, since the present invention is characterized in that the desulfurized reducing gas is obtained by transferring the sulfur component contained in the reducing gas to the reduced iron, a desulfurization facility for desulfurizing the reducing gas discharged from the solid reduction furnace is not required.
The carbonaceous raw material containing sulfur in the present invention means a carbonaceous raw material containing sulfur in an amount of 0.1% or more. A typical example of the carbonaceous raw material containing sulfur is coal. As described later, either or both of biomass and waste plastics may be contained therein. Coal may also be used. These carbonaceous resources are used in the form of fine powder or granules. As long as CO and H can be generated2The kind of gas and carbonaceous resource is not limited. Thus, various carbonaceous resources can be utilized.
In the present invention, the solid reduced iron containing sulfur means reduced iron containing sulfur in an amount of 0.03% or more by weight.
Further, the desulfurized reducing gas is a reducing gas in which the sulfur content in the reducing gas is 70ppm or less. Thus, the fuel can be directly used as fuel for a combustion furnace. More preferably, the sulfur content is 50ppm or less. This can be used as a fuel for hybrid power generation. However, even when high-sulfur coal containing several% of sulfur content is used, a desulfurization unit is sometimes required, but the capacity thereof may be significantly reduced.
In the present invention, the carbonaceous raw material may contain one or both of biomass and waste plastic in addition to coal. In the present invention, woody and agricultural biomass which is easily transported by air flow is used as biomass. The definition of biomass is according to the definition of FAO (Federation food and agriculture organization). That is, woody biomass refers to a part of forestry biomass and waste biomass in FAO definition, and is suitable for papermaking waste, wood-making waste, construction waste such as thinning wood, firewood, court wood, and the like. The agricultural biomass refers to agricultural wastes such as wheat straws and rice husks, and agricultural energy crops such as vegetable seeds and soybeans. These are used because they contain a small amount of water (up to 50% by mass), generate a high heat amount in a wet basis, and can be easily processed into particles that can be transported by an air stream. The waste plastic is a material containing, for example, a paraffin polymer such as Polyethylene (PE), polypropylene (PP), Polystyrene (PS), and polyvinyl chloride (PVC). However, in order to avoid corrosion of the equipment and to reduce the PVC as much as possible, it is preferable to control the content of the carbonaceous raw material other than coal to 10% or less. By using biomass and waste plastics as carbonaceous raw materials, the amount of carbon dioxide emissions can be reduced instead of coal, and global warming can be achieved.
When biomass and waste plastics are charged into a gasification furnace, in addition to coal, the particle size must be processed or granulated to 5mm or less.
As described above, in the coal gasification furnace 12, coal is gasified at a temperature of 1400 to 1700 ℃ to generate a reducing gas, and then the generated reducing gas is sent to the cooling furnace 13, and the reducing gas is cooled to about 1000 ℃ in the cooling furnace 13. In general, the cooling furnace 13 is provided with a radiation boiler therein as described above, and the cooling gas is transferred by radiation heat, or part of the gas generated in the cooling furnace 13 and the reducing gas discharged from the reduction furnace is introduced into the cooling furnace 13 to be cooled by heat recovery, dust collection, and gas cooling.
In the present invention, it is preferable that the carbonaceous raw material containing biomass and waste plastics is introduced into the cooling furnace 13 and cooled. The temperature range in the cooling furnace may be such that the carbonaceous raw material is gasified, and the reaction proceeds while heat is removed from the gas, so that cooling is possible. On the other hand, since the ash is solidified at the temperature in the cooling furnace, a carbonaceous raw material having a large ash content, for example, coal, is not preferable as the carbonaceous raw material introduced into the cooling furnace. However, since the biomass and waste plastic have a low ash content and there is no problem caused by ash even when they are introduced into the cooling furnace, they are most preferable as carbonaceous raw materials introduced into the cooling furnace. That is, by charging a carbonaceous raw material containing one or both of biomass and waste plastic into a cooling furnace, it is possible to increase the production of reducing gas while cooling the reducing gas without causing ash problems.
The above description has been made of the case where the solid reduction furnace uses the shaft furnace, but the solid reduction furnace may use a fluidized bed furnace. A plurality of fluidized bed reducers are prepared, and raw iron ore powder is put into the fluidized bed reducer at the initial stage and is sequentially sent into the fluidized bed reducer at the lower stage. On the other hand, the reducing gas is fed from below the fluidized bed reduction vessel in the final stage, and the iron ore powder is fluidized and layered in the reduction vessel to carry out the reduction reaction, and is fed to the fluidized bed reduction vessel in the upper stage in the order opposite to the flow of the iron ore powder.
Particularly, it is preferable to charge the reduced iron 3 containing the sulfur-containing solid produced by the present invention into a blast furnace. As described above, since the blast furnace itself has a desulfurization function, even if the charged reduced iron contains sulfur, the increase in the sulfur content of the pig iron produced in the blast furnace is very small. Therefore, even the reduced iron containing sulfur content produced according to the present invention can be used as an iron-making raw material without any problem. Further, since the raw material is charged into the blast furnace, as described in patent document 3, the metallization ratio (amount of metallic iron/total amount of iron in the iron ore × 100 (%)) in the reduction furnace does not need to be 90% or more. The metallization rate in the invention is preferably 40-80%.
In addition, the reducing agent for reducing iron ore in the blast furnace is coke, and expensive caking coal is used as coal for producing coke, and the use ratio of inexpensive ordinary coal is limited. And the coal gasification direct reduction iron making can only use cheap common coal. Therefore, by charging reduced iron produced by coal gasification reduction iron making according to the present invention into a blast furnace, the cost of coal used for iron making can be reduced as a whole.
It is particularly preferred that the desulphurised reducing gas produced by the present invention is used in hydrogen production and/or cogeneration. Since the sulfur content in the reducing gas is low, it can be applied to hydrogen production and/or hybrid power generation as it is even without passing through a desulfurization facility. In addition, most of the water vapor is removed in the cooling process, and CO in the reducing gas is removed by a decarbonation device2Can be made of CO and H2Reducing gas as main component. The reducing gas of this composition is suitable as a gas for hydrogen production and/or combined power generation.
In the present invention, it is preferable that the CO gas in the reducing gas is reformed into H by adding water and/or steam to the desulfurized reducing gas and using the sensible heat of the reducing gas as a heat source2Gas and CO2Gas, absorption separation of the CO2Gas to produce hydrogen.
The desulfurized reducing gas is discharged from the reduction furnace 4 at a high temperature of about 400 ℃ or higher, is collected by the dust collector 6, is added with water and steam in the shift reactor 24, and is subjected to shift reaction by catalytic reaction using sensible heat of the reducing gas as a heat source, whereby CO gas in the reducing gas can be reformed into H2Gas and CO2A gas. Then, the reducing gas is cooled by the heat recovery unit 5, and CO is absorbed and separated by the decarbonation unit 92Gas, as a result of which hydrogen can be produced. Due to CO in the reducing gas after the reduction of the iron ore2The concentration is more than 20%, and CO after the shift reaction2Since the concentration is high, i.e., 50% or more, CO can be separated with high efficiency by an amine absorption method or the like2. The heat required for regeneration of the absorption liquid may be low-pressure steam generated by heat recovery in the production process or low-pressure steam generated by burning municipal refuse or the like.
The hydrogen gas thus produced can be used as a reducing gas for heat treatment of steel products or a raw material for fuel cells directly in iron works. The hydrogen can be further compressed for composite power generation. Further, even if the shift reaction is not performed, the gas can be compressed and supplied to the hybrid power generation.
That is, as the application of the reducing gas discharged from the reduction furnace, any of a method of subjecting the reducing gas to shift reaction, decarbonizing, and then using the gas for hydrogen production or hybrid power generation, a method of decarbonizing the reducing gas and then using the gas for hybrid power generation, and a method of directly using the reducing gas for hybrid power generation can be employed. Of course, a part or all of the reducing gas discharged from the reduction furnace 4 may be returned to the cooling furnace 13, and the reducing gas may be cooled and reused as the reducing gas in the reduction furnace 4.
In the present invention, as for the reducing gas produced by gasifying the carbonaceous raw material, it is first used for reducing iron ore in the solid reducing furnace and then used for hydrogen production and combined power generation. Therefore, the heat recovery device, the dust collecting device, and the like of the reducing gas can be shared. Therefore, the incidental equipment can be effectively used as compared with the equipment for separately performing reduction iron making and combined power generation. In particular, in the coal gasification furnace having a high facility investment, the larger the reducing gas production capacity is, the smaller the facility investment amount for the average production amount of reducing gas is. Therefore, the present invention can improve the overall equipment investment efficiency by performing the reduction iron making and the combined power generation together using one coal gasifier of a larger scale, as compared with the case where coal gasifiers are separately constructed for the reduction iron making and the combined power generation.
As described above, the present invention can efficiently produce reduced iron, hydrogen, and electric power from carbonaceous resources containing coal as a main component.
Examples
As shown in fig. 1, the solid reducing furnace 4 uses a shaft type reducing furnace to produce reduced iron (DRI). The reducing gas 11 is produced using a two-stage gasification furnace having a gasification furnace 12 and a cooling furnace 13. Pulverizing Indonesia-produced sub-bituminous coal into 0.67 ton/t-DRI of pulverized coal having average particle diameter of 50 μm and 560Nm of oxygen3the/t-DRI is fed into the lower gasification furnace 12 and is partially combusted, and is gasified at 1500 ℃ and 5 ata. Further, in the upper stage cooling furnace 13, 0.3 ton/t-DRI of biomass (construction waste wood chips) pulverized to 5mm or less was charged into the reducing gas having a high temperature of 1500 ℃ and the biomass was cooled to 1000 ℃ and simultaneously subjected to thermal decomposition to increase the amount of the reducing gas generated. 20-30% of reducing gas can be used in carbonAnd (3) supplying sexual biomass and waste plastics. 35g/Nm in reducing gas3Is dusted to 5g/Nm by a cyclone 143Thereafter, the resultant mixture is charged into a reduction furnace 4.
In the reduction furnace 4, conditions such as the reducing gas amount and the reducing gas temperature are set so that the metallization ratio (the amount of metallic iron/the total amount of iron in the iron ore × 100 (%)) becomes 80%.Since the reduced iron 3 is charged into the blast furnace together with the sintered ore in order to be used as a raw material of molten iron, the reduction rate of 60 to 90% can be sufficient.
The amount of reducing gas, properties of the reducing gas at the inlet and outlet of the reduction furnace, and the temperature are shown in Table 1.
TABLE 1
| Reduction furnace inlet | Reducing furnace outlet (after dust collection) | ||
| Amount (Nm)3/t-DRI) | 2000 | 2000 | |
| Gas composition (vol%) | CO H2 CO2 H2O Others | 30 54 7 6 2 | 39 27 22 10 2 |
| S concentration (ppm) | As H2S As COS | 520 20 | 30 20 |
| Gas temperature (. degree.C.) | 900 | 420 | |
The reducing gas at the inlet of the reduction furnace contains H2S520 ppm (COS 20ppm), and H after passing through a dust removal device at an outlet of the reduction furnace2S was reduced to 30ppm (COS did not change). On the other hand, the extremely small amount of S in the iron ore 2 increased to 0.15 mass% in the reduced iron 3, and it was confirmed that the S in the reducing gas moved to the reduced iron. Usually, the market deals with the reduced iron containing SThe standard is required to be about 0.015 mass%, and in this example, reduced iron is charged into a blast furnace having a desulfurization function and used, so that it can be used without any problem. In this example, the gas temperature at the outlet of the reduction furnace was set to 420 ℃, so that H in the reducing gas was contained2S reacts with the reduced iron, and sulfur components move from the reducing gas to the reduced iron.
The S concentration in the dust obtained from the dust collector 6 after the reduction furnace was 0.3 mass%. Since the temperature of 400 ℃ or higher is maintained even after the discharge from the reduction furnace 4, it is judged whether the iron powder and the remaining H in the reducing gas are present2S continues to react.
The reducing gas 11 discharged from the reduction furnace 4 consumes about 1/3 of the latent heat held in front of the reduction furnace in the reduction furnace, and still maintains a very high energy. Here, the shift reaction(s) possessed by the reducing gas 11 is utilized ) The effective temperature of 400 ℃ is obtained by removing dust from the reducing gas 11 by the dust collector 6, and then introducing the gas into the shift reactor 24 without cooling, where the gas is shifted to hydrogen and carbon dioxide to separate and utilize the hydrogen. As a result, 1400Nm of hydrogen can be recovered3/t-DRI、CO22.4 tons/t-DRI. By shift reaction, CO2The concentration becomes high exceeding 50%, the absorption efficiency by the amine method and CO2The exhaust gas of the boiler with the concentration of about 10% is improved by 5-10%. With the future CO2The development of immobilization technology is expected to be a promising technology for global warming. The separated hydrogen gas 25 is used as a gas for heat treatment in an iron works. Further, it was confirmed that the iron ore can be used as a reducing gas for the iron ore by pressurizing for combined power generation and circulating in the present production process.
In the following, as a comparative example, the temperature of the reducing gas at the outlet of the reduction furnace was set to 550 ℃. Other conditions were the same as in the above-described examples. H in reducing gas after dust collector at outlet of reduction furnace2S was reduced only to 200ppm (COS did not change). On the other hand, the extremely small amount of S in the iron ore was increased to 0.08 mass% in the reduced iron, and it was confirmed that a part of S in the reducing gas was containedAnd the reaction proceeds to reduced iron. Since the sulfur content in the reducing gas discharged from the reduction furnace is not sufficiently reduced, it cannot be directly used for hydrogen production or hybrid power generation. On the other hand, reduced iron has a high sulfur content and can be used as a blast furnace charging material, but it is difficult to use it as a main material for electric furnace iron making.
ADVANTAGEOUS EFFECTS OF INVENTION
The invention can effectively produce reduced iron, hydrogen and electric power, improves the equipment investment efficiency, and can commercialize coal gasification direct reduction iron making and coal gasification combined power generation.
In addition, the invention can eliminate the need of a desulfurization device in the coal gasification direct reduction iron making and the coal gasification combined power generation.
Further, the present invention can use biomass and waste plastics instead of coal, thereby reducing the amount of carbon dioxide discharged.
Claims (10)
1. A method for effectively utilizing a carbonaceous materialcontaining sulfur components, characterized in that a carbonaceous material containing sulfur components is partially combusted with oxygen to produce a reducing gas, and the reducing gas is brought into contact with an iron ore in a solid reduction furnace to reduce the iron ore, thereby producing a solid reduced iron containing sulfur components and simultaneously producing a desulfurized reducing gas.
2. The method according to claim 1, wherein the reducing gas discharged from the solid reducing furnace and the fine particles of iron ore and reduced iron discharged together with the reducing gas are separated.
3. The method according to claim 1, wherein the desulfurized reducing gas is obtained by transferring sulfur components contained in the reducing gas to the reduced iron.
4. The method according to claim 1, wherein the carbonaceous material is coal.
5. The method according to claim 1, wherein the carbonaceous raw material contains one or both of biomass and waste plastics in addition to coal.
6. The method according to claim 5, wherein a cooling furnace is connected to the gasification furnace for producing the reducing gas, and the carbonaceous raw material containing one or both of biomass and waste plastics is charged into the cooling furnace.
7. The method according to claim 1, wherein the solid reducing furnace is a shaft furnace or a fluidized bed furnace.
8. The method according to claim 1, wherein the reduced iron containing the sulfur-containing solid is charged into a blast furnace.
9. The method according to claim 1, wherein the desulfurized reducing gas is used for hydrogen production and/or combined power generation.
10. The method according to claim 9, wherein the reducibility is improved by adding water and/or steam to the desulfurized reducing gasThe sensible heat of the gas is used as a heat source to upgrade the CO gas in the reducing gas into H2Gas and CO2Gas, absorption separation of the CO2Gas to produce hydrogen.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP201216/2003 | 2003-07-24 | ||
| JP2003201216A JP4250472B2 (en) | 2003-07-24 | 2003-07-24 | Method for producing reduced iron and reducing gas for blast furnace charge, method for using reduced iron, and method for using reducing gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1576379A true CN1576379A (en) | 2005-02-09 |
| CN1576379B CN1576379B (en) | 2010-04-28 |
Family
ID=34261377
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2004100545828A Expired - Fee Related CN1576379B (en) | 2003-07-24 | 2004-07-23 | Effective utilizing method for carbon resource |
Country Status (2)
| Country | Link |
|---|---|
| JP (1) | JP4250472B2 (en) |
| CN (1) | CN1576379B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102482724A (en) * | 2009-05-25 | 2012-05-30 | 蒂森克虏伯伍德有限公司 | Method for the simultaneous production of iron and crude syngas containing co and h2 |
| CN102712959A (en) * | 2009-07-31 | 2012-10-03 | 伊尔技术有限公司 | Method for producing direct reduced iron with limited CO2 emissions |
| CN106906328A (en) * | 2017-04-25 | 2017-06-30 | 本钢板材股份有限公司 | A kind of steelmaking converter technique |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102005027158A1 (en) * | 2005-06-11 | 2006-12-28 | Klaus Dr.-Ing. Scheidig | Process for producing pig iron in the blast furnace while supplying reducing gas into the blast furnace shaft |
| JP4979940B2 (en) * | 2005-12-27 | 2012-07-18 | 新日本製鐵株式会社 | Method for producing reduced iron |
| JP4901668B2 (en) * | 2007-09-21 | 2012-03-21 | 中国電力株式会社 | Coal-fired power generation system and hexavalent chromium elution control method |
| JP4712082B2 (en) * | 2008-09-26 | 2011-06-29 | 株式会社神戸製鋼所 | Coal gasification and direct iron making method and system |
| LU91547B1 (en) * | 2009-04-03 | 2010-10-04 | Wurth Paul Sa | Method and installation for producing direct reduced iron |
| AT508523B1 (en) * | 2009-07-31 | 2011-04-15 | Siemens Vai Metals Tech Gmbh | REFORM GAS-BASED REDUCTION PROCESS AND DEVICE WITH DECARBONIZING THE COMBUSTION GAS FOR THE REFORMER |
| CN114657304B (en) * | 2022-04-15 | 2023-06-27 | 黑龙江建龙钢铁有限公司 | Device and method for preparing gas-based shaft furnace reducing gas by purifying biomass gas |
| KR102642964B1 (en) * | 2023-03-31 | 2024-02-29 | 현대제철 주식회사 | Biogas Generating Apparatus and Reduction System, and Raw Material Reduction Method Using the Same |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1035955C (en) * | 1995-06-23 | 1997-09-24 | 宝山钢铁(集团)公司 | Method for production of sponge iron by using gas-making shaft furnace method of coal-base melting bed |
| CN1107727C (en) * | 1999-05-25 | 2003-05-07 | 雷少军 | Technology of two-stage reduction method producing sponge iron |
-
2003
- 2003-07-24 JP JP2003201216A patent/JP4250472B2/en not_active Expired - Fee Related
-
2004
- 2004-07-23 CN CN2004100545828A patent/CN1576379B/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102482724A (en) * | 2009-05-25 | 2012-05-30 | 蒂森克虏伯伍德有限公司 | Method for the simultaneous production of iron and crude syngas containing co and h2 |
| CN102482724B (en) * | 2009-05-25 | 2015-11-25 | 蒂森克虏伯伍德有限公司 | Produce iron simultaneously and contain CO and H 2the method of crude synthesis gas |
| CN102712959A (en) * | 2009-07-31 | 2012-10-03 | 伊尔技术有限公司 | Method for producing direct reduced iron with limited CO2 emissions |
| CN102712959B (en) * | 2009-07-31 | 2014-06-25 | 伊尔技术有限公司 | Method for producing direct reduced iron with limited CO2 emissions |
| CN106906328A (en) * | 2017-04-25 | 2017-06-30 | 本钢板材股份有限公司 | A kind of steelmaking converter technique |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2005042142A (en) | 2005-02-17 |
| CN1576379B (en) | 2010-04-28 |
| JP4250472B2 (en) | 2009-04-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1249207C (en) | Power generation system based on gasification of combustible material | |
| CN1179149C (en) | Method and apparatus for treating wastes by gasification | |
| CN1167896C (en) | Method and device for treating refuse by gasification | |
| CN1039653C (en) | Integrated carbonaceous fuel drying and gasification process and apparatus | |
| US5980858A (en) | Method for treating wastes by gasification | |
| JP4259777B2 (en) | Biomass gasification method | |
| US20100305220A1 (en) | Method and apparatus for producing liquid biofuel from solid biomass | |
| CN102796561B (en) | Anaerobic gasification method and device for biomass fuels by carbon dioxide circulation | |
| CN1010480B (en) | Fuels containing carbon, particularly gasification of coal | |
| CN102417831A (en) | Biomass gasification generation system | |
| CN87106233A (en) | Make the method for high methane content gas mixture by coal | |
| CN1673317A (en) | Carbonization and gasification of biomass and power generation system | |
| JP4547244B2 (en) | Organic gasifier | |
| JP2004149556A (en) | Method for gasifying biomass and gasifying apparatus therefor | |
| CN211367490U (en) | Material pyrolysis gasification system | |
| CN1576379A (en) | Effective utilizing method for carbon resource | |
| CN107474859B (en) | Coal pyrolysis gasification process coupling device and method thereof | |
| CN110903855A (en) | Material pyrolysis gasification process, system and application | |
| CN1137249C (en) | Method and apparatus for treating wastes by gasification | |
| AU2008252051A1 (en) | Process and plant for producing char and fuel gas | |
| WO2011128513A1 (en) | A waste refining method | |
| CN1017060B (en) | Process for conversion of coal and gypsum to valuable products | |
| CN101597663B (en) | Energy recovery system for preparing sponge iron by gasification of high-pressure pulverized coal and method thereof | |
| CN1042955C (en) | Sponge iron production process and plant | |
| CN1053898A (en) | High-temperature reductibility gas process for purification and gasifying combined generating apparatus |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| CI01 | Publication of corrected invention patent application |
Correction item: First inventor Correct: Onoda Masami False: ONODA MASAMI Number: 6 Volume: 21 |
|
| CI02 | Correction of invention patent application |
Correction item: First inventor Correct: Onoda Masami False: ONODA MASAMI Number: 6 Page: The title page Volume: 21 |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: THE FIRST INVENTOR; FROM: ONODA ZHENGYI TO: ONODA ZHENGJI |
|
| ERR | Gazette correction |
Free format text: CORRECT: THE FIRST INVENTOR; FROM: ONODA ZHENGYI TO: ONODA ZHENGJI |
|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: NIPPON STEEL + SUMITOMO METAL CORPORATION Free format text: FORMER OWNER: SHIN NIPPON STEEL LTD. Effective date: 20130401 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20130401 Address after: Tokyo, Japan Patentee after: NIPPON STEEL & SUMITOMO METAL Corp. Patentee after: Kobe Steel, Ltd. Address before: Tokyo, Japan Patentee before: NIPPON STEEL Corp. Patentee before: Kobe Steel, Ltd. |
|
| CP01 | Change in the name or title of a patent holder | ||
| CP01 | Change in the name or title of a patent holder |
Address after: Tokyo, Japan Co-patentee after: Kobe Steel, Ltd. Patentee after: NIPPON STEEL & SUMITOMO METAL Corp. Address before: Tokyo, Japan Co-patentee before: Kobe Steel, Ltd. Patentee before: NIPPON STEEL & SUMITOMO METAL Corp. |
|
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20100428 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |