CN103667567B - Middle low-rank coal vaporizing system is for reducing gas conveying bed smelting technology and system - Google Patents
Middle low-rank coal vaporizing system is for reducing gas conveying bed smelting technology and system Download PDFInfo
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- 239000003245 coal Substances 0.000 title claims abstract description 35
- 238000003723 Smelting Methods 0.000 title description 5
- 238000005516 engineering process Methods 0.000 title description 3
- 230000008016 vaporization Effects 0.000 title 1
- 239000007789 gas Substances 0.000 claims abstract description 263
- 230000009467 reduction Effects 0.000 claims abstract description 260
- 239000000843 powder Substances 0.000 claims abstract description 74
- 238000011282 treatment Methods 0.000 claims abstract description 69
- 238000000034 method Methods 0.000 claims abstract description 37
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 16
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 16
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 16
- 239000001257 hydrogen Substances 0.000 claims abstract description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 12
- 239000001301 oxygen Substances 0.000 claims abstract description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 10
- 238000000746 purification Methods 0.000 claims abstract description 10
- 238000002309 gasification Methods 0.000 claims description 83
- 238000006477 desulfuration reaction Methods 0.000 claims description 39
- 230000023556 desulfurization Effects 0.000 claims description 39
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 38
- 239000011707 mineral Substances 0.000 claims description 38
- 238000005261 decarburization Methods 0.000 claims description 32
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 30
- 239000000428 dust Substances 0.000 claims description 30
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 26
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 26
- 239000007788 liquid Substances 0.000 claims description 25
- 238000000926 separation method Methods 0.000 claims description 18
- 238000010438 heat treatment Methods 0.000 claims description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- LIKBJVNGSGBSGK-UHFFFAOYSA-N iron(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[Fe+3].[Fe+3] LIKBJVNGSGBSGK-UHFFFAOYSA-N 0.000 claims description 11
- 238000005406 washing Methods 0.000 claims description 11
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 8
- 239000000446 fuel Substances 0.000 claims description 8
- 229910052595 hematite Inorganic materials 0.000 claims description 7
- 239000011019 hematite Substances 0.000 claims description 7
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims description 6
- 239000001569 carbon dioxide Substances 0.000 claims description 6
- 150000002431 hydrogen Chemical class 0.000 claims description 6
- 229910052759 nickel Inorganic materials 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 6
- 239000003077 lignite Substances 0.000 claims description 5
- 239000002245 particle Substances 0.000 claims description 5
- 241000282817 Bovidae Species 0.000 claims description 4
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 4
- 230000006835 compression Effects 0.000 claims description 4
- 238000007906 compression Methods 0.000 claims description 4
- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 claims description 4
- 229910021646 siderite Inorganic materials 0.000 claims description 4
- 239000002893 slag Substances 0.000 claims description 4
- 239000003476 subbituminous coal Substances 0.000 claims description 4
- 229910052720 vanadium Inorganic materials 0.000 claims description 4
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 15
- 238000006722 reduction reaction Methods 0.000 description 223
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 22
- 229910052742 iron Inorganic materials 0.000 description 11
- 239000000203 mixture Substances 0.000 description 11
- 230000008569 process Effects 0.000 description 9
- 238000005262 decarbonization Methods 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 7
- 238000002360 preparation method Methods 0.000 description 6
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- ZSLUVFAKFWKJRC-IGMARMGPSA-N 232Th Chemical compound [232Th] ZSLUVFAKFWKJRC-IGMARMGPSA-N 0.000 description 1
- GYHNNYVSQQEPJS-UHFFFAOYSA-N Gallium Chemical compound [Ga] GYHNNYVSQQEPJS-UHFFFAOYSA-N 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- 229910052776 Thorium Inorganic materials 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 229910052770 Uranium Inorganic materials 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 229910052787 antimony Inorganic materials 0.000 description 1
- WATWJIUSRGPENY-UHFFFAOYSA-N antimony atom Chemical compound [Sb] WATWJIUSRGPENY-UHFFFAOYSA-N 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 1
- 238000005255 carburizing Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 230000010485 coping Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 229910052733 gallium Inorganic materials 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910001710 laterite Inorganic materials 0.000 description 1
- 239000011504 laterite Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 238000005453 pelletization Methods 0.000 description 1
- DPTATFGPDCLUTF-UHFFFAOYSA-N phosphanylidyneiron Chemical compound [Fe]#P DPTATFGPDCLUTF-UHFFFAOYSA-N 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- GFNGCDBZVSLSFT-UHFFFAOYSA-N titanium vanadium Chemical compound [Ti].[V] GFNGCDBZVSLSFT-UHFFFAOYSA-N 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- DNYWZCXLKNTFFI-UHFFFAOYSA-N uranium Chemical compound [U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U] DNYWZCXLKNTFFI-UHFFFAOYSA-N 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
- Y02P10/00—Technologies related to metal processing
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
- Y02P10/143—Reduction of greenhouse gas [GHG] emissions of methane [CH4]
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- Industrial Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The present invention proposes ore powder reduction method and system thereof.Wherein, ore powder reduction method comprises: coal, water vapour and oxygen are reacted in gasifying reactor, to obtain the reducing gas containing carbon monoxide and hydrogen; Reducing gas and breeze are reacted, to obtain reduzate and the weary gas of reduction carrying in bed reduction reactor; Weary for reduction gas is carried out purifying treatment, to obtain the weary gas of reduction through purification; And the weary gas of reduction through purification is incorporated in conveying bed reduction reactor.Utilize the method effectively to reduce to breeze, the reduction efficiency of breeze while of cost-effective, can be significantly improved.<!-- 2 -->
Description
Technical Field
The invention relates to the field of metallurgy. In particular to a novel process and a novel system for conveying bed smelting of reducing gas prepared by medium-low-grade coal gasification.
Background
The reserves of inferior ores in China are abundant, the reserves of the found resources of iron ores in China are 613.35 hundred million tons, wherein the basic reserves are 223.64 million tons, the resources are 389.71 million tons, the vast majority of the reserves of the found resources of iron ores in China are lean ores, the reserves of the found resources of rich iron ores are 10.02 million tons, and the reserves of the found resources of rich iron ores account for 1.6 percent of the reserves of the found resources of all iron ores. On the other hand, the reserves of iron ore with the concomitant (co) production beneficial components in China account for 1/3 of the reserves in China, and the concomitant (co) production beneficial components comprise: more than 30 rare precious metals such as vanadium, titanium, tungsten, molybdenum, cobalt, antimony, gold, cadmium, gallium, uranium, thorium and the like. This is the main characteristic of iron ore resources in China. The existing blast furnace technology is adopted to carry out 'forced' smelting on the composite ore, so that a large amount of symbiotic elements are not reasonably utilized, the waste is useless, and even the environmental pollution is caused, for example, about 40 hundred million tons of high-grade medium and high phosphorus iron ore in China is not utilized. Therefore, comprehensive utilization of inferior ores is a problem which must be solved. In addition, with the increasingly reduced world high-grade iron ore resources, the fine ore in imported ore reaches 80 percent; the average grade of the domestic iron ore is only 33 percent, and almost 100 percent of the domestic iron ore is mineral powder. In order to simultaneously face or adapt to the resource situations that the growth potential of the imported ore price is not reduced, the granularity is thinner and thinner, a large amount of domestic composite paragenic ores cannot be reasonably developed and the like, the direct ore powder reduction technology is an important way for effectively coping with the current state of iron ores in China.
Disclosure of Invention
The present invention aims to solve at least one of the above technical problems to a certain extent. Therefore, the invention aims to provide a novel process and a novel system for conveying bed smelting of medium-low-order coal gasification reduced gas, which have the advantages of high production efficiency, low reduced gas preparation cost and the like.
To this end, in a first aspect of the invention, the invention proposes a method for ore fines reduction, comprising: reacting coal, steam and oxygen in a gasification reactor to obtain a reducing gas comprising carbon monoxide and hydrogen; reacting the reducing gas with the ore powder in a conveying bed reduction reactor so as to obtain a reduction product and reduction exhaust gas; purifying the reduction exhaust gas to obtain purified reduction exhaust gas; and introducing the purified reducing exhaust gas into the transport bed reduction reactor.
The method can directly reduce the mineral powder, and saves the working procedures of high pollution and high efficiency, such as sintering, pellet preparation and the like, thereby saving a large amount of capital investment and operation cost. And the raw material coal for preparing the reducing gas by the method can adopt medium and low rank coal, so that the preparation cost of the reducing gas is obviously reduced. In addition, the method purifies the reduction exhaust gas used for reducing the ore powder, and leads the carbon monoxide and the hydrogen which do not participate in the reduction reaction back to the conveying bed reduction reactor to be continuously used for reducing the ore powder, thereby avoiding the waste of the reduction gas. Therefore, the method for reducing the ore powder reduces the preparation cost of the reducing gas and further improves the reduction efficiency of the ore powder.
In addition, the ore powder reduction method according to the above embodiment of the present invention may have the following additional technical features:
according to an embodiment of the present invention, the mineral powder is at least one selected from the group consisting of laterite-nickel ore, oolitic hematite, antelope quarry, vanadium titano magnetite, hematite, specularite, limonite, siderite and non-ferrous oxide slag. Thereby further improving the reduction efficiency of the ore powder.
According to an embodiment of the invention, the average particle size of the ore fines may be 1.0mm or less. Thereby further improving the reduction efficiency of the ore powder.
According to an embodiment of the present invention, the coal is at least one selected from medium and low rank coals such as lignite, long flame coal, and subbituminous coal. Thereby reducing the cost of producing the reducing gas.
According to the embodiment of the invention, the gasification temperature in the gasification reactor is 750-1100 ℃, and the gasification pressure is more than 0.3 MPa. This increases the efficiency of the production of the reducing gas, so that the efficiency of the reduction of the ore fines is increased further.
According to an embodiment of the present invention, the reducing gas contains hydrogen, carbon monoxide, carbon dioxide, methane, and nitrogen, wherein the volume percentages of the components satisfy the following conditions: h2/CO>0.5，(H2+CO)/(H2O+CO2)>10，3％<CH4<15％，N2<10％，1％≤CO2Less than or equal to 3 percent. The reduction efficiency of the ore fines can thus be further increased by means of the reducing gas. The inventors have surprisingly found that, when a reducing gas composition of this proportion is used, the ore fines can be effectively subjected to a reduction treatment with the reducing gas. When a reducing gas that does not satisfy this condition is used, the efficiency of reducing the ore fines is significantly reduced.
According to an embodiment of the invention, the gasification reactor is at least one selected from the group consisting of a fixed bed, a fluidized bed and a transport bed. Thereby improving the efficiency of producing the reducing gas to further improve the reduction efficiency of the ore powder. The inventors have surprisingly found that only when using fixed, fluidized and transport beds, it is possible to use medium-low rank coals to obtain a reducing gas which can be effectively used for the reduction treatment of ore fines, i.e. the composition of the reducing gas meets the following requirements: h2/CO>0.5，(H2+CO)/(H2O+CO2)>10，3％<CH4<15％，N2<10％，1％≤CO2Less than or equal to 3 percent. When other gasification reactors are used, it is not suitable to use medium-low rank coals to obtain a reducing gas satisfying the above conditions due to the limitations of the gasification reactors themselves. Therefore, the cost performance of the reduction of the mineral powder by using the reducing gas generated by other gasification reactors is far lower than that of the reduction by using a fixed bed, a fluidized bed and a conveying bed.
According to an embodiment of the invention, the reducing gas is dedusted before it is reacted with the ore fines. This reduces the dust content of the reducing gas, so that the reduction efficiency of the ore fines is further increased.
According to the embodiment of the invention, the reduction temperature in the conveying bed reduction reactor is 750-1150 ℃, and the reduction pressure is less than or equal to 1.0 MPa. Thereby further improving the reduction efficiency of the ore powder.
According to the embodiment of the invention, before desulfurization and decarburization are performed on the reduction exhaust gas, dust removal treatment, heat exchange treatment, washing treatment and gas-liquid separation treatment are performed on the reduction exhaust gas in sequence in advance, and the desulfurization and decarburization treatment is performed after compression is performed on the gas obtained after gas-liquid separation. Therefore, the reducing gas which does not participate in the reduction reaction can be purified and reused, so that the utilization efficiency of the reducing gas is further improved, and the reduction efficiency of the mineral powder is further improved.
According to the embodiment of the invention, the part of the purified reduction exhaust gas is used for carrying out heat exchange treatment on the reduction exhaust gas, so that the heat utilization rate can be improved.
According to an embodiment of the invention, the cleaned reducing exhaust gas is preheated in a furnace before being introduced into the transport bed reduction reactor, wherein the furnace uses a part of the cleaned reducing exhaust gas as fuel. Therefore, the utilization efficiency of the reducing gas can be improved, and the reduction efficiency of the mineral powder is further improved.
In a second aspect of the invention, the invention proposes a system for reducing ore fines, characterized in that it comprises: a gasification reactor for reacting coal, steam and oxygen therein to obtain a reducing gas containing carbon monoxide and hydrogen; a transport bed reduction reactor connected with the gasification reactor for reacting the reducing gas with the ore powder in the transport bed reduction reactor to obtain a reduction product and a reduction exhaust gas; the desulfurization and decarburization device is connected with the conveying bed reduction reactor and is used for performing desulfurization and decarburization treatment on the reduction exhaust gas so as to obtain purified reduction exhaust gas; and the reduction exhaust gas return pipeline is respectively connected with the desulfurization and decarburization device and the conveying bed reduction reactor and is used for introducing the desulfurization and decarburization reduction exhaust gas into the conveying bed reduction reactor. The system for reducing the mineral powder can effectively reduce the mineral powder and can obviously improve the reduction efficiency of the mineral powder.
In addition, the system for reducing ore fines according to the above-described embodiment of the invention may also have the following additional technical features:
according to the embodiment of the invention, the gasification temperature in the gasification reactor is 750-1100 ℃, and the gasification pressure is more than 0.3 MPa. Therefore, the efficiency of the gasification reactor for preparing the reducing gas can be improved, so that the reduction efficiency of the ore powder is further improved.
According to an embodiment of the present invention, the reducing gas contains hydrogen, carbon monoxide, carbon dioxide, methane, and nitrogen, wherein the volume percentages of the components satisfy the following conditions: h2/CO>0.5，(H2+CO)/(H2O+CO2)>10，3％<CH4<15％，N2<10％，1％≤CO2Less than or equal to 3 percent. Thereby improving the reduction efficiency of the reducing gas so as to further improve the reduction efficiency of the ore powder. The inventors have surprisingly found that, when a reducing gas composition of this proportion is used, the ore fines can be effectively subjected to a reduction treatment with the reducing gas. When a reducing gas that does not satisfy this condition is used, the efficiency of reducing the ore fines is significantly reduced.
According to an embodiment of the invention, the gasification reactor is at least one selected from the group consisting of a fixed bed, a fluidized bed and a transport bed. Thereby improving the efficiency of producing the reducing gas to further improve the reduction efficiency of the ore powder. The inventors have surprisingly found that fixation is only usedThe medium and low rank coals can be utilized to obtain the reducing gas which can be effectively used for reducing the mineral powder, namely the composition of the reducing gas meets the following requirements: h2/CO>0.5，(H2+CO)/(H2O+CO2)>10，3％<CH4<15％，N2<10％，1％≤CO2Less than or equal to 3 percent. When other gasification reactors are used, it is not suitable to use medium-low rank coals to obtain a reducing gas satisfying the above conditions due to the limitations of the gasification reactors themselves. Therefore, the cost performance of the reduction of the mineral powder by using the reducing gas generated by other gasification reactors is far lower than that of the reduction by using a fixed bed, a fluidized bed and a conveying bed.
According to an embodiment of the present invention, the system for reducing ore fines may further comprise: and the first dust removal device is respectively connected with the gasification reactor and the conveying bed reduction reactor and is used for carrying out dust removal treatment on the reducing gas in advance before the reducing gas is reacted with the mineral powder.
According to the embodiment of the invention, the reduction temperature in the conveying bed reduction reactor is 750-1150 ℃, and the reduction pressure is less than or equal to 1.0 MPa. Thereby further improving the reduction efficiency of the ore powder.
According to an embodiment of the present invention, a second dust removing device, a heat exchanging device, a washing device, a gas-liquid separating device, and a compressing device are sequentially disposed between the transport bed reduction reactor and the desulfurization and decarburization device in a direction from the transport bed reduction reactor to the desulfurization and decarburization device, so that the reduction exhaust gas is subjected to dust removing treatment, heat exchanging treatment, washing treatment, and gas-liquid separating treatment in advance before being subjected to desulfurization and decarburization, and the gas obtained after gas-liquid separation is compressed and then subjected to desulfurization and decarburization treatment. Therefore, the reducing gas which does not participate in the reduction reaction can be purified and reused, so that the utilization efficiency of the reducing gas is further improved, and the reduction efficiency of the mineral powder is further improved.
According to an embodiment of the invention, the heat exchange device is connected with the desulfurization and decarburization device so as to exchange heat with a part of the purified reduction exhaust gas. Therefore, the temperature of the reduction exhaust gas can be effectively reduced, the purified reduction exhaust gas is preliminarily preheated, the heat loss is avoided, and the heat utilization rate is improved.
According to an embodiment of the invention, a furnace is arranged on the reduction exhaust gas return line in order to preheat the purified reduction exhaust gas in the furnace before it is introduced into the transport bed reduction reactor, wherein the furnace uses a part of the purified reduction exhaust gas as fuel. Therefore, the utilization efficiency of the reducing gas can be improved, and the reduction efficiency of the mineral powder is further improved.
Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
The above and/or additional aspects and advantages of the present invention will become apparent and readily appreciated from the following description of the embodiments, taken in conjunction with the accompanying drawings of which:
FIG. 1 is a schematic flow diagram of a process for ore fines reduction according to an embodiment of the invention;
fig. 2 is a schematic structural view of a system for reducing ore fines according to an embodiment of the present invention;
fig. 3 is a schematic structural view of a system for reducing ore fines according to another embodiment of the present invention;
fig. 4 is a schematic structural view of a system for reducing ore fines according to still another embodiment of the present invention.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are illustrative and intended to be illustrative of the invention and are not to be construed as limiting the invention.
In a first aspect of the invention, a method for ore fines reduction is proposed, which is described in detail below with reference to fig. 1.
S100: preparation of reducing gas
According to one embodiment of the invention, the ore fines reduction process first comprises: coal, steam and oxygen are reacted in a gasification reactor to obtain a reducing gas comprising carbon monoxide and hydrogen. Whereby a reducing gas can be produced.
According to another embodiment of the present invention, the type of coal used for the production of the reducing gas is not particularly limited, and according to a specific embodiment of the present invention, the coal may be at least one selected from medium and low rank coals such as lignite, long flame coal, and subbituminous coal. Thereby reducing the cost of producing the reducing gas. The energy distribution characteristics of China are 'oil shortage, gas shortage and coal enrichment', so the traditional process method is not suitable for the national situation of China, the coal reserves of China are in the third world, the yield is in the first world, the medium and low-rank coal reserves account for more than 40% of the total reserves of coal resources, and the annual output at present accounts for about 30% of the total reserves of the national coal, so that the development and utilization of the medium and low-rank coal can be expanded, the coal resources of China can be reasonably applied, and meanwhile, the cost can be remarkably saved and the resource utilization rate can be improved by utilizing the medium and low-rank coal to prepare the reducing gas.
According to an embodiment of the present invention, the gasification temperature in the gasification reactor in the fine ore reduction method is not particularly limited, and according to an embodiment of the present invention, the temperature may be 750 to 1100 degrees celsius, and the gasification pressure may be 0.3MPa is above. This increases the efficiency of the production of the reducing gas, so that the efficiency of the reduction of the ore fines is increased further. The type of gasification reactor according to a specific embodiment of the present invention is not particularly limited, and according to a specific example of the present method, the gasification reactor may be at least one selected from the group consisting of a fixed bed, a fluidized bed, and a transport bed. The inventors have surprisingly found that only when using fixed, fluidized and transport beds, it is possible to use medium-low rank coals to obtain a reducing gas which can be effectively used for the reduction treatment of ore fines, i.e. the composition of the reducing gas meets the following requirements: h2/CO>0.5，(H2+CO)/(H2O+CO2)>10，3％<CH4<15％，N2<10％，1％≤CO2Less than or equal to 3 percent. When other gasification reactors are used, it is not suitable to use medium-low rank coals to obtain a reducing gas satisfying the above conditions due to the limitations of the gasification reactors themselves. Therefore, the cost performance of the reduction of the mineral powder by using the reducing gas generated by other gasification reactors is far lower than that of the reduction by using a fixed bed, a fluidized bed and a conveying bed. Thereby improving the efficiency of producing the reducing gas to further improve the reduction efficiency of the ore powder. According to an embodiment of the present invention, coal, steam and oxygen may be reacted in a gasification reactor under the above conditions to produce a reducing gas containing carbon monoxide and hydrogen.
According to another embodiment of the present invention, the composition of the reducing gas is not particularly limited, and according to a specific example of the present method, the reducing gas may contain hydrogen, carbon monoxide, carbon dioxide, methane, and nitrogen, wherein the volume percentages of the respective components satisfy the following conditions: h2/CO>0.5，(H2+CO)/(H2O+CO2)>10，3％<CH4<15％，N2<10％，1％≤CO2Less than or equal to 3 percent. The reduction efficiency of the ore fines can thus be further increased by means of the reducing gas. The inventors have surprisingly found that, when a reducing gas composition of this proportion is used, the ore fines can be effectively subjected to a reduction treatment with the reducing gas. When a reducing gas that does not satisfy this condition is used, the efficiency of reducing the ore fines is significantly reduced.
Specifically, the above-mentioned reducing gas obtained can be controlled by controlling the ratio of the coal, the steam and the oxygen added, as well as the specific reduction reactor and the process parameters thereof, so as to improve the reduction efficiency of the reducing gas on the ore powder. Therefore, according to the method for reducing the mineral powder provided by the embodiment of the invention, the medium-low rank coal can be selected as a raw material, and high-quality reducing gas can be prepared by controlling the ratio of the added water vapor and the added oxygen and the specific and suitable process parameters of the reduction reactor. Thereby improving the efficiency of producing the reducing gas while saving costs.
S200: reduced ore powder
According to an embodiment of the present invention, the method of reducing fine ore further includes reacting the above-prepared reducing gas with fine ore in the transport bed reduction reactor to obtain a reduction product and a reduction offgas. According to an embodiment of the present invention, the ore powder used for reduction may be at least one selected from the group consisting of laterite-nickel ore, oolitic hematite, antelope quarry, vanadium titano-magnetite, hematite, specularite, limonite, siderite, and non-ferrous oxide slag. The components of the mineral powder are complex and difficult to treat, and the mineral powder can be effectively reduced by using the mineral powder reducing method, so that the reducing efficiency of the mineral powder is further improved.
According to another embodiment of the present invention, the average particle size of the ore fines is not particularly limited, and according to a specific embodiment of the present invention, the average particle size of the ore fines may be 1.0mm or less. Thereby further improving the reduction efficiency of the ore powder.
According to still another embodiment of the present invention, the reduction temperature in the reactor of the transport bed reduction reactor for reducing the fine ore is not particularly limited, and according to an embodiment of the present invention, the reduction temperature in the reactor may be 750 to 1150 degrees celsius and the reduction pressure may be less than or equal to 1.0 MPa. Thereby further improving the reduction efficiency of the ore powder.
According to one embodiment of the invention, the reducing gas is dedusted before it is reacted with the ore fines. According to the embodiment of the invention, at least two gasification reactor cyclone separators connected in series can be used for dedusting the reducing gas prepared in the gasification reactors, wherein the solid impurities separated in each gasification reactor cyclone separator can be sequentially returned to the gasification reactors and can continuously participate in the gasification reaction, so that the reduction efficiency of the mineral powder is further improved.
S300: purifying and reducing exhaust gas
According to the embodiment of the invention, after the ore powder is subjected to reduction treatment by using the reducing gas, a large amount of reducing gas remains in the generated reducing exhaust gas, and the part of the reducing exhaust gas can be purified and then returned to reduce the ore powder. The term "purification" as used herein means to remove components unsuitable for reduction treatment, mainly sulfur-containing compounds and carbon-containing compounds, from the reduction exhaust gas, thereby enabling desulfurization and decarburization treatment.
According to one embodiment of the invention, before purifying the reduction exhaust gas, the reduction exhaust gas is subjected to dust removal treatment, heat exchange treatment, washing treatment and gas-liquid separation treatment in sequence in advance, and the gas obtained after the gas-liquid separation is compressed and then subjected to purification treatment. Therefore, the reducing gas which does not participate in the reduction reaction can be purified and reused, so that the utilization efficiency of the reducing gas is further improved, and the reduction efficiency of the mineral powder is further improved.
According to another embodiment of the invention, the dust removal treatment can remove dust from the reduction exhaust gas by means of a reactor overhead gas cyclone separator, and particularly, at least two reduction exhaust gas cyclones connected in series can be used for removing dust from the reduction exhaust gas, wherein the separated unreduced minerals are sequentially returned to the conveying bed reduction reactor to continue to participate in the reduction reaction. This can further improve the efficiency of mineral utilization.
According to the specific embodiment of the invention, the reduction exhaust gas after the dust removal treatment is further subjected to heat exchange treatment, and the heat exchange treatment can be performed by using a heat exchanger, and specifically, the reduction exhaust gas after the dust removal treatment can be subjected to heat exchange treatment by using the reduction exhaust gas after the purification treatment. Therefore, the temperature of the reduction exhaust gas can be effectively reduced, the purified reduction exhaust gas is preliminarily preheated, the heat loss is avoided, and the heat utilization rate is improved. According to the specific embodiment of the invention, the reducing exhaust gas after heat exchange treatment is further subjected to washing treatment and gas-liquid separation treatment, so that the dust content of the reducing exhaust gas can be further reduced, and the purified reducing exhaust gas can be returned to the conveying bed reduction reactor to participate in reduction reaction, so that the utilization rate of the reducing gas can be improved, and resource waste is avoided.
According to another embodiment of the present invention, the gas-liquid separation process may be performed by a gas-liquid separator, so that water contained in the reduction exhaust gas may be separated to facilitate the next desulfurization and decarburization process for the reduction exhaust gas, thereby further improving the purification efficiency of the reduction exhaust gas.
According to an embodiment of the present invention, the gas obtained after the gas-liquid separation is compressed and then subjected to desulfurization and decarburization treatment. Therefore, the reducing gas which does not participate in the reduction reaction can be purified and reused, so that the utilization efficiency of the reducing gas is further improved, and the reduction efficiency of the mineral powder is further improved.
S400: introducing the reduction exhaust gas into the transport bed reduction reactor
According to one embodiment of the invention, the reduced exhaust gas is heat exchanged with a portion of the purified reduced exhaust gas. Therefore, the temperature of the reduction exhaust gas can be effectively reduced, the purified reduction exhaust gas is preliminarily preheated, the heat loss is avoided, and the heat utilization rate is improved. According to the specific embodiment of the invention, the reduction exhaust gas after heat exchange treatment needs to be preheated and then returned to the conveying bed reduction reactor. Therefore, the reduction efficiency can be prevented from being reduced due to the fact that the temperature of the conveying bed reduction reactor is reduced after the purified reduction exhaust gas enters the conveying bed reduction reactor. Thereby improving the reduction efficiency of the mineral powder.
According to one embodiment of the invention, the cleaned reducing exhaust gas is preheated in a furnace before it is introduced into the transport-bed reduction reactor, wherein the furnace can use a part of the cleaned reducing exhaust gas as fuel, so that the temperature in the transport-bed reduction reactor can be prevented from being lowered by the temperature of the cleaned reducing exhaust gas, and the reduction efficiency of the ore dust can be further increased.
In a second aspect of the invention, the invention proposes a system 1000 for reducing ore fines, comprising: a gasification reactor 100, a transport bed reduction reactor 200, a desulfurization and decarbonization apparatus 300, and a reduction offgas return line 400. As shown in fig. 2.
Wherein the gasification reactor 100 is used to react coal, steam and oxygen therein to obtain a reducing gas containing carbon monoxide and hydrogen; the transport bed reduction reactor 200 is connected to the gasification reactor 100 for reacting the reducing gas with the ore powder in the transport bed reduction reactor 200 to obtain a reduction product and a reduction exhaust gas; the desulfurization and decarbonization device 300 is connected with the transport bed reduction reactor 200, and performs desulfurization and decarbonization treatment on the reduction exhaust gas so as to obtain purified reduction exhaust gas; a reducing exhaust gas return line 400 is connected to the desulfurization and decarbonization apparatus 300 and the transport bed reduction reactor 200, respectively, for introducing the purified reducing exhaust gas into the transport bed reduction reactor 200. The system for reducing the mineral powder can effectively reduce the mineral powder and can obviously improve the reduction efficiency of the mineral powder.
According to the embodiment of the invention, after the ore powder is subjected to reduction treatment by using the reducing gas, a large amount of reducing gas remains in the generated reducing exhaust gas, and the part of the reducing exhaust gas can be purified and then returned to reduce the ore powder. The term "purification" as used herein means that components unsuitable for the reduction treatment, mainly sulfur-containing compounds and carbon-containing compounds, in the reduction exhaust gas are removed, and thus the desulfurization and decarburization apparatus 300 mainly performs the desulfurization and decarburization treatment.
According to an embodiment of the present invention, the gasification temperature in the gasification reactor 100 is not particularly limited, and according to an embodiment of the present invention, the gasification temperature may be 750 to 1100 degrees celsius, and the gasification pressure may be 0.3MPa or more. This increases the efficiency of the production of the reducing gas, so that the efficiency of the reduction of the ore fines is increased further. The type of the gasification reactor 100 according to a specific embodiment of the present invention is not particularly limited, and the gasification reactor 100 may be at least one selected from the group consisting of a fixed bed, a fluidized bed, and a transport bed according to a specific example of the present method. Thereby improving the efficiency of producing the reducing gas to further improve the reduction efficiency of the ore powder. The inventors have surprisingly found that only when using fixed, fluidized and transport beds, it is possible to use medium-low rank coals to obtain a reducing gas which can be effectively used for the reduction treatment of ore fines, i.e. the composition of the reducing gas meets the following requirements: h2/CO>0.5，(H2+CO)/(H2O+CO2)>10，3％<CH4<15％，N2<10％，1％≤CO2Less than or equal to 3 percent. When other gasification reactors are used, it is not suitable to use medium-low rank coals to obtain a reducing gas satisfying the above conditions due to the limitations of the gasification reactors themselves. Therefore, the cost performance of the reduction of the mineral powder by using the reducing gas generated by other gasification reactors is far lower than that of the reduction by using a fixed bed, a fluidized bed and a conveying bed.
According to an embodiment of the present invention, coal, steam and oxygen may be reacted in the gasification reactor 100 under the above-described conditions to produce a reducing gas containing carbon monoxide and hydrogen.
According to another embodiment of the present invention, the composition of the reducing gas is not particularly limited, and according to a specific example of the present method, the reducing gas may contain hydrogen, carbon monoxide, carbon dioxide, methane, and nitrogen, wherein the volume percentages of the respective components satisfy the following conditions: h2/CO>0.5，(H2+CO)/(H2O+CO2)>10，3％<CH4<15％，N2<10％，1％≤CO2Less than or equal to 3 percent. The reduction efficiency of the ore fines can thus be further increased by means of the reducing gas. The inventors have surprisingly found that, when a reducing gas composition of this proportion is used, the ore fines can be effectively subjected to a reduction treatment with the reducing gas. When a reducing gas that does not satisfy this condition is used, the efficiency of reducing the ore fines is significantly reduced.
According to an embodiment of the invention, the gasification reactor is at least one selected from the group consisting of a fixed bed, a fluidized bed and a transport bed. Thereby improving the efficiency of producing the reducing gas to further improve the reduction efficiency of the ore powder. The inventors have surprisingly found that only when using fixed, fluidized and transport beds, it is possible to use medium-low rank coals to obtain a reducing gas which can be effectively used for the reduction treatment of ore fines, i.e. the composition of the reducing gas meets the following requirements: h2/CO>0.5，(H2+CO)/(H2O+CO2)>10，3％<CH4<15％，N2<10％，1％≤CO2Less than or equal to 3 percent. When other gasification reactors are used, it is not suitable to use medium-low rank coals to obtain a reducing gas satisfying the above conditions due to the limitations of the gasification reactors themselves. Therefore, the cost performance of the reduction of the mineral powder by using the reducing gas generated by other gasification reactors is far lower than that of the reduction by using a fixed bed, a fluidized bed and a conveying bed.
According to an embodiment of the present invention, as shown in fig. 3, the system for reducing ore powder further includes: the first dust removing device 110 is connected to the gasification reactor 100 and the transport bed reduction reactor 200, and is used for removing dust from the reducing gas before the reducing gas reacts with the ore powder. This reduces the dust content of the reducing gas, so that the reduction efficiency of the ore fines is further increased. According to an embodiment of the present invention, the first dust removing device 110 may be at least two gasification reactor cyclones connected in series, and the gasification reactor cyclones are used to remove dust from the reducing gas prepared in the gasification reactor 100, wherein the solid impurities separated in each gasification reactor cyclone may be sequentially returned to the gasification reactor 100 to continue to participate in the gasification reaction. The carbon conversion of the reducing gas can thereby be increased, so that the reduction efficiency of the ore dust is further increased.
According to still another embodiment of the present invention, the reduction temperature in the reactor of the transport bed reduction reactor 200 is not particularly limited, and according to an embodiment of the present invention, the reduction temperature in the reactor may be 750 to 1150 degrees celsius and the reduction pressure is less than or equal to 1.0 MPa. Thereby further improving the reduction efficiency of the ore powder.
According to still another embodiment of the present invention, as shown in fig. 3, a second dust removing device 210, a heat exchanging device 220, a washing device 230, a gas-liquid separating device 240 and a compressing device 250 are sequentially disposed between the transport bed reduction reactor 200 and the desulfurization and decarburization device 300 in the direction from the transport bed reduction reactor 200 to the desulfurization and decarburization device 300, so that the reduction exhaust gas is subjected to dust removal, heat exchange and gas-liquid separation in sequence before being subjected to desulfurization and decarburization, and the gas obtained after gas-liquid separation is compressed and then subjected to desulfurization and decarburization.
According to another embodiment of the present invention, the second dust removing device 210 may be at least two reducing exhaust gas cyclones connected in series, and according to an embodiment of the present invention, at least two reducing exhaust gas cyclones connected in series may be used to remove dust from the reducing exhaust gas, wherein the separated impurities may be sequentially returned to the transport bed reduction reactor 200. Therefore, the dedusting treatment efficiency can be improved, and the purification efficiency of the reduction exhaust gas can be further improved, so that the utilization efficiency of the reduction gas can be further improved, and the reduction efficiency of the ore powder can be further improved.
According to an embodiment of the present invention, the heat exchanging device 220 may be a heat exchanger, and specifically, the reduction exhaust gas dedusted by the second dedusting device 210 is further introduced into the heat exchanging device 220 for heat exchanging treatment. Therefore, the heat exchange device 220 can be used for effectively exchanging heat for the reduction exhaust gas, reducing the temperature of the reduction exhaust gas, preliminarily preheating the purified reduction exhaust gas, avoiding heat loss and improving the heat utilization rate. According to the specific embodiment of the present invention, the washing device 230 and the gas-liquid separation device 240 are further utilized to perform washing treatment and gas-liquid separation treatment on the reduction exhaust gas after heat exchange treatment, so that the dust content of the reduction exhaust gas can be further reduced, and the purified reduction exhaust gas can be returned to the transport bed reduction reactor to participate in the reduction reaction, thereby improving the utilization rate of the reduction gas and avoiding resource waste.
According to another embodiment of the present invention, the gas-liquid separation device 240 can be used to separate water contained in the reduction exhaust gas, so as to facilitate the next step of desulfurization and decarburization treatment on the reduction exhaust gas, and further improve the purification efficiency of the reduction exhaust gas.
According to an embodiment of the present invention, the reducing exhaust gas after gas-liquid separation can be compressed by the compression device 250, so as to facilitate the desulfurization and decarburization treatment of the reducing exhaust gas. Therefore, the reducing gas which does not participate in the reduction reaction can be purified and reused, so that the utilization efficiency of the reducing gas is further improved, and the reduction efficiency of the mineral powder is further improved.
According to another embodiment of the present invention, the heat exchanging device 220 is connected to the desulfurization and decarbonization device 300 to exchange heat with a portion of the purified reduction exhaust gas. Therefore, the utilization efficiency of the reducing gas can be improved, and the reduction efficiency of the mineral powder is further improved. According to the specific embodiment of the invention, the reduction exhaust gas after heat exchange treatment needs to be preheated and then returned to the reduction reactor. Thus, it is possible to prevent the reduction efficiency from being lowered due to the temperature of the transport bed reduction reactor being lowered after the purified reduction offgas enters the transport bed reduction reactor 200. Thereby improving the reduction efficiency of the mineral powder.
In a further embodiment of the present invention, a heating furnace 410 is provided on the reducing exhaust gas return line 400 to preheat the purified reducing exhaust gas in the heating furnace 410 before introducing the purified reducing exhaust gas into the transport bed reduction reactor 200, wherein the heating furnace 410 uses a portion of the purified reducing exhaust gas as fuel, i.e., another portion of the reducing exhaust gas is introduced into the heating furnace for use as fuel. This prevents the purified low-temperature reduction offgas from lowering the temperature in the transport-bed reduction reactor 200, and thus the reduction efficiency of the ore fines can be further improved.
The mineral powder reduction method provided by the embodiment of the invention has the advantages that:
1. the gasification reactor can be used for gasifying medium-low-rank coal such as brown coal, long-flame coal, sub-bituminous coal and the like, is suitable for the resource pattern of rich coal, less oil and gas shortage in China, and reduces the preparation cost of reducing gas;
2. the purified reducing gas is directly mixed with the purified preheated reducing exhaust gas and enters a conveying bed reduction reactor 200, so that the heat of the coal gas and the effective gas components are fully utilized;
3. the reducing gas contains certain methane, so that the carburizing requirement of the subsequent process is met;
4. the purified reduction exhaust gas is heated by a heating furnace, so that the heat efficiency is very high;
5. can realize the direct reduction of low-grade complex refractory ores such as laterite-nickel ore, oolitic hematite, antelope stone ore, vanadium-titanium magnetite ore, hematite, specularite, limonite, siderite and the like, nonferrous metal oxide furnace slag and the like.
6. The direct use of fine ore saves the working procedures of sintering, pelletizing and the like with high pollution and high energy consumption, and saves a large amount of capital investment and operation cost.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless specifically defined otherwise.
In the present invention, unless otherwise expressly specified or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Examples
As shown in fig. 4, 1, a gasification reactor; 2. a first-stage cyclone separator of the gasification reactor; 3. a secondary cyclone separator of the gasification reactor; 4. a transport bed reduction reactor; 5. a reducing product distributing bin; 6. a first-stage reduction exhaust gas cyclone separator; 7. a secondary reduction exhaust gas cyclone separator; 8. a heat exchanger; 9. a scrubber; 10. a gas-liquid separator; 11. a compressor; 12. a desulfurization and decarburization device; 13. and (5) heating the furnace.
With the laterite nickel ore handling capacity of 100 × 104For example, pulverized lignite enters a fluidized bed gasification reactor 1, is subjected to gasification reaction with a gasification medium of water vapor and oxygen at 900 ℃ and 1.0MPa, the generated high-temperature reducing gas passes through a primary cyclone separator 2 of the gasification reactor and a secondary cyclone separator 3 of the gasification reactor to remove fly ash, and then the clean reducing gas is mixed with reducing exhaust gas from a heating furnace 13 and enters a conveying bed reduction reactor 4.
Laterite-nickel ore powder with the particle size of 0.5mm enters the conveying bed reduction reactor 4 from the top of the conveying bed reduction reactor 4 and undergoes reduction reaction with reducing gas entering the lower part of the conveying bed reduction reactor 4 at 850 ℃ and 0.8MPa, wherein the reducing gas meets the following requirements: h2/CO＝1.2、(H2+CO)/(H2O+CO2)＝13、CH4＝5％、N2＝7％、CO2The content of the reduction product is 2 percent, and the reduction product is subjected to gas heat exchangeThe bottom of the conveying bed reduction reactor 4 is discharged, the metal recovery rate reaches 90 percent,
the reduction exhaust gas of the conveying bed reduction reactor 4 is dedusted by primary and secondary reduction exhaust gas cyclone separators 6 and 7, enters a heat exchanger 8 to exchange heat with one path of gas from a desulfurization and decarbonization device 12, is washed by a washer 9 and a gas-liquid separator 10 to remove liquid, then enters the desulfurization and decarbonization device 12 after being pressurized by a compressor 11, and then is divided into two paths of gas: the first path of gas exchanges heat with the reducing exhaust gas dedusted by the secondary reducing exhaust gas cyclone separator 7 through the heat exchanger 8, enters the heating furnace 13 for heating, is mixed with the reducing gas purified by the fluidized bed gasification reactor 1, and enters the conveying bed reduction reactor 4; the second path of gas enters the heating furnace 13 to be used as fuel.
In the description herein, references to the description of the term "one embodiment," "some embodiments," "an example," "a specific example," or "some examples," etc., mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made in the above embodiments by those of ordinary skill in the art without departing from the principle and spirit of the present invention.
Claims (9)
1. A mineral powder reduction method is characterized by comprising the following steps:
reacting coal, steam and oxygen in a gasification reactor to obtain a reducing gas comprising carbon monoxide and hydrogen;
reacting the reducing gas with the ore powder in a conveying bed reduction reactor so as to obtain a reduction product and reduction exhaust gas;
purifying the reduction exhaust gas to obtain purified reduction exhaust gas;
utilizing a part of the purified reduction exhaust gas to carry out heat exchange treatment on the reduction exhaust gas,
preheating the purified reducing exhaust gas in a heating furnace, wherein the heating furnace uses a part of the purified reducing exhaust gas as fuel,
introducing the preheated reducing off-gas into the transport bed reduction reactor,
wherein,
the gasification temperature in the gasification reactor is 750-1100 ℃, the gasification pressure is more than 0.3MPa,
the reducing gas contains hydrogen, carbon monoxide, carbon dioxide, methane and nitrogen, wherein the volume percentage of each component meets the following conditions: h2/CO>0.5，(H2+CO)/(H2O+CO2)>10，3％<CH4<15％，N2<10％，1％≤CO2≤3％，
The gasification reactor is at least one selected from a fixed bed, a fluidized bed and a transport bed,
the purification process further comprises: and sequentially carrying out dust removal treatment, heat exchange treatment, washing treatment, gas-liquid separation treatment, compression treatment and desulfurization and decarburization treatment on the reduction exhaust gas.
2. The method according to claim 1, wherein the mineral powder is at least one selected from lateritic nickel ore, antelope ore, vanadium titano-magnetite, hematite, specularite, limonite, siderite, and non-ferrous oxide slag.
3. The method according to claim 2, characterized in that the average particle size of the ore fines is below 1.0 mm.
4. The method of claim 1, wherein the coal is at least one selected from the group consisting of lignite, long-flame coal, and subbituminous coal.
5. The method according to claim 1, characterized in that the reducing gas is dedusted before it is reacted with the ore fines.
6. The method according to claim 1, wherein the reduction temperature in the transport bed reduction reactor is 750 to 1150 ℃ and the reduction pressure is less than or equal to 1.0 MPa.
7. A system for reducing ore fines, comprising:
a gasification reactor for reacting coal, steam and oxygen therein to obtain a reducing gas containing carbon monoxide and hydrogen;
a transport bed reduction reactor connected with the gasification reactor for reacting the reducing gas with the ore powder in the transport bed reduction reactor to obtain a reduction product and a reduction exhaust gas;
the desulfurization and decarburization device is connected with the conveying bed reduction reactor and is used for performing desulfurization and decarburization treatment on the reduction exhaust gas so as to obtain purified reduction exhaust gas; and
a reduction exhaust gas return pipeline which is respectively connected with the desulfurization and decarburization device and the conveying bed reduction reactor and is used for introducing the purified reduction exhaust gas into the conveying bed reduction reactor,
the gasification temperature in the gasification reactor is 750-1100 ℃, the gasification pressure is more than 0.3MPa,
the reducing gas contains hydrogen, carbon monoxide, carbon dioxide, methane and nitrogen, wherein the volume percentage of each component meets the following conditions: h2/CO>0.5，(H2+CO)/(H2O+CO2)>10，3％<CH4<15％，N2<10％，1％≤CO2≤3％，
The gasification reactor is at least one selected from a fixed bed, a fluidized bed and a transport bed,
a second dust removal device, a heat exchange device, a washing device, a gas-liquid separation device and a compression device are sequentially arranged between the conveying bed reduction reactor and the desulfurization and decarburization device along the direction from the conveying bed reduction reactor to the desulfurization and decarburization device, so that the reduction exhaust gas is subjected to dust removal treatment, heat exchange treatment, washing treatment and gas-liquid separation treatment in advance before being subjected to desulfurization and decarburization, and the gas obtained after gas-liquid separation is compressed and then subjected to desulfurization and decarburization treatment,
the heat exchange device is connected with the desulfurization and decarburization device so as to carry out heat exchange treatment on the reduction exhaust gas by using a part of the purified reduction exhaust gas,
the reduction exhaust gas return line is provided with a heating furnace for preheating the purified reduction exhaust gas in the heating furnace before introducing the purified reduction exhaust gas into the transport bed reduction reactor, wherein the heating furnace uses a part of the purified reduction exhaust gas as fuel.
8. The system of claim 7, further comprising:
and the first dust removal device is respectively connected with the gasification reactor and the conveying bed reduction reactor and is used for carrying out dust removal treatment on the reducing gas in advance before the reducing gas is reacted with the mineral powder.
9. The system of claim 7, wherein the reduction temperature in the transport bed reduction reactor is 750-1150 degrees Celsius and the reduction pressure is less than or equal to 1.0 MPa.
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| CN106367647B (en) * | 2016-09-05 | 2018-06-01 | 中南大学 | A kind of method that gas-based reduction manganese iron axinite prepares high carbon ferromanganese |
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Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1109911A (en) * | 1995-03-11 | 1995-10-11 | 宝山钢铁(集团)公司 | Method for producing spongy iron by coal-base gas-making in vertical furnace |
| CN101397597A (en) * | 2007-09-26 | 2009-04-01 | 宝山钢铁股份有限公司 | Method for producing spongy iron by direct reduction of dry coal powder gasification and hot coal gas fine ore fluidized bed |
| CN101597663A (en) * | 2009-06-30 | 2009-12-09 | 上海锅炉厂有限公司 | A kind of energy recovery system for preparing sponge iron by gasification of high-pressure pulverized coal and method |
| CN101831517A (en) * | 2010-05-26 | 2010-09-15 | 王林 | Blast furnace coal gasification air heating furnace smelting method |
| CN102010924A (en) * | 2010-12-31 | 2011-04-13 | 中冶赛迪上海工程技术有限公司 | Method for producing directly reduced iron from coal |
| CN102127611A (en) * | 2011-01-25 | 2011-07-20 | 吴道洪 | Method for reducing vanadium-titanium magnetite powder by coal reducing gas and fluidized beds |
| CN102206723A (en) * | 2011-01-13 | 2011-10-05 | 北京首钢国际工程技术有限公司 | Air-base direct reduction iron-making method for reducing iron concentrate powder by self-reforming of gas rich in methane |
| CN102994678A (en) * | 2012-11-21 | 2013-03-27 | 北京神雾环境能源科技集团股份有限公司 | Method and system for pulverized coal gasification for gas generation and direct reduction metallurgy of gas-based shaft furnace |
| CN203373371U (en) * | 2013-05-23 | 2014-01-01 | 北京神雾环境能源科技集团股份有限公司 | Conveying bed smelting system for preparing reducing gases through medium-low-rank coal gasification |
-
2013
- 2013-05-23 CN CN201310195770.1A patent/CN103667567B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1109911A (en) * | 1995-03-11 | 1995-10-11 | 宝山钢铁(集团)公司 | Method for producing spongy iron by coal-base gas-making in vertical furnace |
| CN101397597A (en) * | 2007-09-26 | 2009-04-01 | 宝山钢铁股份有限公司 | Method for producing spongy iron by direct reduction of dry coal powder gasification and hot coal gas fine ore fluidized bed |
| CN101597663A (en) * | 2009-06-30 | 2009-12-09 | 上海锅炉厂有限公司 | A kind of energy recovery system for preparing sponge iron by gasification of high-pressure pulverized coal and method |
| CN101831517A (en) * | 2010-05-26 | 2010-09-15 | 王林 | Blast furnace coal gasification air heating furnace smelting method |
| CN102010924A (en) * | 2010-12-31 | 2011-04-13 | 中冶赛迪上海工程技术有限公司 | Method for producing directly reduced iron from coal |
| CN102206723A (en) * | 2011-01-13 | 2011-10-05 | 北京首钢国际工程技术有限公司 | Air-base direct reduction iron-making method for reducing iron concentrate powder by self-reforming of gas rich in methane |
| CN102127611A (en) * | 2011-01-25 | 2011-07-20 | 吴道洪 | Method for reducing vanadium-titanium magnetite powder by coal reducing gas and fluidized beds |
| CN102994678A (en) * | 2012-11-21 | 2013-03-27 | 北京神雾环境能源科技集团股份有限公司 | Method and system for pulverized coal gasification for gas generation and direct reduction metallurgy of gas-based shaft furnace |
| CN203373371U (en) * | 2013-05-23 | 2014-01-01 | 北京神雾环境能源科技集团股份有限公司 | Conveying bed smelting system for preparing reducing gases through medium-low-rank coal gasification |
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