CN103667566B - Middle low-rank coal vaporizing system is for reducing gas fluidized-bed smelting process and system - Google Patents
Middle low-rank coal vaporizing system is for reducing gas fluidized-bed smelting process and system Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 101
- 230000008569 process Effects 0.000 title claims abstract description 74
- 239000003245 coal Substances 0.000 title claims abstract description 42
- 230000008016 vaporization Effects 0.000 title description 4
- 238000003723 Smelting Methods 0.000 title description 2
- 230000009467 reduction Effects 0.000 claims abstract description 271
- 239000007789 gas Substances 0.000 claims abstract description 256
- 239000012530 fluid Substances 0.000 claims abstract description 68
- 238000000746 purification Methods 0.000 claims abstract description 46
- 238000005261 decarburization Methods 0.000 claims abstract description 43
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 43
- 230000023556 desulfurization Effects 0.000 claims abstract description 43
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 17
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 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
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000000843 powder Substances 0.000 claims abstract description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000001301 oxygen Substances 0.000 claims abstract description 10
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 10
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 36
- 239000007788 liquid Substances 0.000 claims description 26
- 238000000926 separation method Methods 0.000 claims description 22
- 229910052742 iron Inorganic materials 0.000 claims description 18
- 229910052757 nitrogen Inorganic materials 0.000 claims description 17
- 239000000428 dust Substances 0.000 claims description 16
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 12
- 238000004140 cleaning Methods 0.000 claims description 12
- 238000005406 washing Methods 0.000 claims description 12
- 238000002309 gasification Methods 0.000 claims description 11
- 239000000446 fuel Substances 0.000 claims description 8
- 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 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 6
- 235000011089 carbon dioxide Nutrition 0.000 claims description 6
- 150000002431 hydrogen Chemical class 0.000 claims description 6
- 229910052759 nickel Inorganic materials 0.000 claims description 6
- 239000002689 soil Substances 0.000 claims description 6
- 238000009997 thermal pre-treatment Methods 0.000 claims description 6
- 239000003077 lignite Substances 0.000 claims description 5
- 239000002245 particle Substances 0.000 claims description 5
- 229910052720 vanadium Inorganic materials 0.000 claims description 5
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 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
- 229910044991 metal oxide Inorganic materials 0.000 claims description 4
- 150000004706 metal oxides Chemical class 0.000 claims description 4
- 239000002893 slag Substances 0.000 claims description 4
- 239000004575 stone Substances 0.000 claims description 4
- 239000003476 subbituminous coal Substances 0.000 claims description 4
- 238000006722 reduction reaction Methods 0.000 description 231
- 238000002360 preparation method Methods 0.000 description 16
- 239000000203 mixture Substances 0.000 description 11
- 238000004064 recycling Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 230000007423 decrease Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 229910052595 hematite Inorganic materials 0.000 description 3
- 239000011019 hematite Substances 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 241001417490 Sillaginidae Species 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 238000005453 pelletization Methods 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000002699 waste material 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
- 241001062472 Stokellia anisodon Species 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
- 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
- 230000008859 change Effects 0.000 description 1
- 239000002817 coal dust 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
- 238000009826 distribution Methods 0.000 description 1
- 238000003912 environmental pollution Methods 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
- 238000010438 heat treatment Methods 0.000 description 1
- 235000003642 hunger Nutrition 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 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
- 239000003921 oil Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 230000037351 starvation Effects 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 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
- JFALSRSLKYAFGM-UHFFFAOYSA-N uranium(0) Chemical compound [U] JFALSRSLKYAFGM-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]
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 in fluid bed reduction reactor, to obtain reduzate and the weary gas of reduction; Weary for reduction gas is carried out desulfurization and decarburization process, to obtain the weary gas of reduction through purification; And the weary gas of reduction through purification is incorporated in fluid bed reduction reactor.Utilize the method effectively to reduce to breeze, the reduction efficiency of breeze while of cost-effective, can be significantly improved.
Description
Technical field
The present invention relates to field of metallurgy.In one, low-rank coal vaporizing system smelts novel method and system for reducing gas fluidized-bed.
Background technology
China's ore reserve inferior is enriched, whole nation iron ore finds out that resource reserve is 613.35 hundred million tons, wherein basic unit price is 223.64 hundred million tons, stock number 389.71 hundred million tons, China's iron ore finds out that the resource reserve overwhelming majority is for lean ore, rich iron ore finds out that resource reserve has 10.02 hundred million tons, account for that whole iron ore finds out resource reserve 1.6%.On the other hand, the iron ore reserves that China has the raw Hubeiwan of companion's (being total to) account for 1/3 of national reserves, and companion's (being total to) is raw, and Hubeiwan has: vanadium, titanium, tungsten, molybdenum, cobalt, antimony, gold, cadmium, gallium, uranium, thorium etc. more than 30 plant rare precious metal.This is the principal feature of China's iron ore deposit.Adopt existing blast-furnace technique to carry out " by force " to complex ore to smelt, cause a large amount of Coexisting Elements reasonably do not utilized and waste, even environmental pollution, such as, in the higher-grade that China is about 4,000,000,000 tons, high-phosphorus iron ore is not utilized.Therefore the comprehensive utilization in ore deposit inferior is a problem that must solve.In addition, along with high grade iron ore resources is reducing day by day in the world, in import resources, fine ore reaches 80%; The average grade of domestic iron ore only has 33%, and product ore deposit, native land 100% is almost breeze entirely.Want simultaneously in the face of or adapt to import resources valency and increase that gesture does not subtract, granularity is more and more thinner, domestic a large amount of compositeon-silicon paragenetic can not get the resource situation such as reasonable development, breeze Direct Reduction Technology is the important channel successfully managing current China iron ore present situation.
Summary of the invention
The present invention is intended to one of solve the problems of the technologies described above at least to a certain extent.For this reason, one object of the present invention is that proposing a kind of middle low-rank coal vaporizing system with advantages such as production efficiency are high, reducing gas preparation cost is low smelts novel method and system for reducing gas fluidized-bed.
For this reason, in first of the present invention, the present invention proposes a kind of ore powder reduction method, this comprises: coal, water vapour and oxygen are reacted in gasifying reactor, to obtain the reducing gas containing carbon monoxide and hydrogen; Described reducing gas and breeze are reacted in fluid bed reduction reactor, to obtain reduzate and the weary gas of reduction; Weary for described reduction gas is carried out desulfurization and decarburization process, to obtain the weary gas of reduction through purification; And the described weary gas of reduction through purification is incorporated in described fluid bed reduction reactor.
Utilize aforesaid method directly to be reduced by breeze, eliminate sintering, prepare the high pollutions such as pelletizing, dynamical operation, thus a large amount of initial costs and running cost can be saved.And the feed coal that the method prepares reducing gas can adopt low-rank coal, significantly reduces the preparation cost of reducing gas.In addition, in the method, the weary gas of reduction being used for reducing after breeze is carried out purifying treatment, the carbon monoxide and hydrogen of wherein not participating in reduction reaction are led back in fluid bed reduction reactor, continues on for reducing breeze, the waste of reducing gas can be avoided thus.Therefore, utilize the method for above-mentioned reduction breeze, reduce the preparation cost of reducing gas, improve the reduction efficiency of breeze further.
In addition, ore powder reduction method according to the above embodiment of the present invention can also have following additional technical characteristic:
According to embodiments of the invention, described breeze is at least one being selected from red soil nickel ore, oolitic hematite, antelope stone ore, vanadium titano-magnetite, rhombohedral iron ore, specularite, limonite, spathic iron ore and nonferrous metal oxides slag.The reduction efficiency of breeze can be improved thus further.
According to a particular embodiment of the invention, the mean particle size of breeze can be below 3.0mm.The reduction efficiency of breeze can be improved thus further.
According to embodiments of the invention, described coal is at least one being selected from brown coal, long-flame coal and sub-bituminous coal.The cost of preparation reducing gas can be reduced thus.
According to embodiments of the invention, the gasification temperature in described gasifying reactor is 750 ~ 1100 degrees Celsius, and vapor pressure is more than 0.3MPa.The efficiency of preparation reducing gas can be improved thus, to improve the efficiency of reduction breeze further.
According to embodiments of the invention, described reducing gas contains hydrogen, carbon monoxide, carbonic acid gas, methane, nitrogen, and wherein, the volume percent of each component meets following condition: H
2/ CO>0.5, (H
2+ CO)/(H
2o+CO
2) >10,3%<CH
4<15%, N
2<10%, 1%≤CO
2≤ 3%.Utilize this reducing gas can improve the reduction efficiency of breeze further thus.Contriver is surprised to find, and when adopting the reducing gas composition of this ratio, can effectively utilize this reducing gas and carrying out reduction treatment to breeze.When employing does not meet the reducing gas of this condition, can significantly decline to the efficiency that breeze reduces.
According to embodiments of the invention, described gasifying reactor is at least one being selected from fixed bed, fluidized-bed and conveying bed.The efficiency of preparation reducing gas can be improved thus, to improve the reduction efficiency of breeze further.Contriver is surprised to find, and only have when adopting fixed bed, fluidized-bed and conveying bed, low-rank coal in just can utilizing, obtain and can be effective to reducing gas breeze being carried out to reduction treatment, namely the composition of reducing gas meets following requirements: H
2/ CO>0.5, (H
2+ CO)/(H
2o+CO
2) >10,3%<CH
4<15%, N
2<10%, 1%≤CO
2≤ 3%.When adopting other gasifying reactor, due to the restriction of gasifying reactor itself, being not suitable for low-rank coal in utilization and obtaining the reducing gas meeting above-mentioned condition.Thus the reducing gas utilizing other gasifying reactors to produce carries out the cost performance of breeze reduction far below employing fixed bed, fluidized-bed and conveying bed.
According to embodiments of the invention, before reducing gas and breeze being reacted, in advance dust removal process is carried out to described reducing gas.The dustiness of reducing gas can be reduced thus, to improve the reduction efficiency of breeze further.
According to embodiments of the invention, the reduction temperature in described fluid bed reduction reactor is 750 ~ 1150 degrees Celsius, and reduction pressure is less than or equal to 1.0MPa.The reduction efficiency of breeze can be improved thus further.
According to embodiments of the invention, before desulfurization and decarburization is carried out to the weary gas of described reduction, in advance dust removal process, heat exchange process, carrying out washing treatment and gas-liquid separation process are carried out successively to the weary gas of described reduction, and carry out described desulfurization and decarburization process after the gas obtained after gas-liquid separation is compressed.The reducing gas not participating in reduction reaction can be carried out purifying rear recycling thus, to improve the utilising efficiency of reducing gas further, and then improve the reduction efficiency of breeze.
According to embodiments of the invention, utilize a part for the described weary gas of reduction through purification to carry out heat exchange process to the weary gas of described reduction, can heat utilization efficiency be improved thus.According to embodiments of the invention, before the described weary gas of reduction through purification is introduced described fluid bed reduction reactor, in process furnace, thermal pretreatment is carried out to the described weary gas of reduction through purification, wherein, described process furnace adopts a part for the described weary gas of reduction through purification as fuel.The utilising efficiency of reducing gas can be improved thus, and then improve the reduction efficiency of breeze.
In second of the present invention, the present invention proposes a kind of for reducing the system of breeze, it is characterized in that, comprise: gasifying reactor, described gasifying reactor is used for coal, water vapour and oxygen are reacted wherein, to obtain the reducing gas containing carbon monoxide and hydrogen; Fluid bed reduction reactor, described fluid bed reduction reactor is connected with described gasifying reactor, for making described reducing gas and breeze react in fluid bed reduction reactor, to obtain reduzate and the weary gas of reduction; Desulfurization and decarburization device, described desulfurization and decarburization device is connected with described fluid bed reduction reactor, and weary for described reduction gas is carried out desulfurization and decarburization process, to obtain the weary gas of reduction through purification; And reducing weary gas return pipeline, described reduction weary gas return pipeline is connected with described fluid bed reduction reactor with described desulfurization and decarburization device respectively, for being incorporated in described fluid bed reduction reactor by the described weary gas of reduction through purification.Utilize and above-mentionedly can effectively to reduce to breeze for reducing the system of breeze, and the reduction efficiency of breeze can be significantly improved.
In addition, according to the above embodiment of the present invention can also have following additional technical characteristic for reducing the system of breeze:
According to embodiments of the invention, the gasification temperature in described gasifying reactor is 750 ~ 1100 degrees Celsius, and vapor pressure is more than 0.3MPa.The efficiency that reducing gas prepared by gasifying reactor can be improved thus, to improve the reduction efficiency of breeze further.
According to embodiments of the invention, described reducing gas contains hydrogen, carbon monoxide, carbonic acid gas, methane, nitrogen, and wherein, the volume percent of each component meets following condition: H
2/ CO>0.5, (H
2+ CO)/(H
2o+CO
2) >10,3%<CH
4<15%, N
2<10%, 1%≤CO
2≤ 3%.The reduction efficiency of reducing gas can be improved thus, to improve the reduction efficiency of breeze further.Contriver is surprised to find, and when adopting the reducing gas composition of this ratio, can effectively utilize this reducing gas and carrying out reduction treatment to breeze.When employing does not meet the reducing gas of this condition, can significantly decline to the efficiency that breeze reduces.
According to embodiments of the invention, described gasifying reactor is at least one being selected from fixed bed, fluidized-bed and conveying bed.The efficiency of preparation reducing gas can be improved thus, to improve the reduction efficiency of breeze further.Contriver is surprised to find, and only have when adopting fixed bed, fluidized-bed and conveying bed, low-rank coal in just can utilizing, obtain and can be effective to reducing gas breeze being carried out to reduction treatment, namely the composition of reducing gas meets following requirements: H
2/ CO>0.5, (H
2+ CO)/(H
2o+CO
2) >10,3%<CH
4<15%, N
2<10%, 1%≤CO
2≤ 3%.When adopting other gasifying reactor, due to the restriction of gasifying reactor itself, being not suitable for low-rank coal in utilization and obtaining the reducing gas meeting above-mentioned condition.Thus the reducing gas utilizing other gasifying reactors to produce carries out the cost performance of breeze reduction far below employing fixed bed, fluidized-bed and conveying bed.
According to embodiments of the invention, may further include for reducing the system of breeze: the first cleaning apparatus, described first cleaning apparatus is connected with described fluid bed reduction reactor with described gasifying reactor respectively, for before reducing gas and breeze being reacted, in advance dust removal process is carried out to described reducing gas.The dustiness of reducing gas can be reduced thus, to improve the reduction efficiency of breeze further.
According to embodiments of the invention, the reduction temperature in described fluid bed reduction reactor is 750 ~ 1150 degrees Celsius, and reduction pressure is less than or equal to 1.0MPa.The reduction efficiency of breeze can be improved thus further.
According to embodiments of the invention, between described fluid bed reduction reactor and described desulfurization and decarburization device, direction along from described fluid bed reduction reactor to described desulfurization and decarburization device, be disposed with the second cleaning apparatus, heat-exchanger rig, washing device, gas-liquid separation device and compression set, so that before carrying out desulfurization and decarburization to the weary gas of described reduction, in advance successively dust removal process is carried out to the weary gas of described reduction, heat exchange process, carrying out washing treatment and gas-liquid separation process, and carry out described desulfurization and decarburization process after the gas obtained after gas-liquid separation is compressed.The reducing gas not participating in reduction reaction can be carried out purifying rear recycling thus, to improve the utilising efficiency of reducing gas further, and then improve the reduction efficiency of breeze.
According to embodiments of the invention, described heat-exchanger rig is connected with described desulfurization and decarburization device, to utilize a part for the described weary gas of reduction through purification to carry out heat exchange process to the weary gas of described reduction.Effectively can reduce thus and reduce the temperature of weary gas, and preliminary preheating is carried out to the weary gas of reduction after purification, avoid heat losses, improve heat utilization efficiency.
According to embodiments of the invention, reduce on weary gas return pipeline and be provided with process furnace, so that before the described weary gas of reduction through purification is introduced described fluid bed reduction reactor, in process furnace, thermal pretreatment is carried out to the described weary gas of reduction through purification, wherein, described process furnace adopts a part for the described weary gas of reduction through purification as fuel.The utilising efficiency of reducing gas can be improved thus, and then improve the reduction efficiency of breeze.
Additional aspect of the present invention and advantage will part provide in the following description, and part will become obvious from the following description, or be recognized by practice of the present invention.
Accompanying drawing explanation
Above-mentioned and/or additional aspect of the present invention and advantage will become obvious and easy understand from accompanying drawing below combining to the description of embodiment, wherein:
Fig. 1 is the schematic flow sheet of ore powder reduction method according to an embodiment of the invention;
Fig. 2 is according to an embodiment of the invention for reducing the structural representation of system of breeze;
Fig. 3 is in accordance with another embodiment of the present invention for reducing the structural representation of system of breeze;
Fig. 4 be according to another embodiment of the present invention for reducing the structural representation of system of breeze.
Embodiment
Be described below in detail embodiments of the invention, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has element that is identical or similar functions from start to finish.Be exemplary below by the embodiment be described with reference to the drawings, be intended to for explaining the present invention, and can not limitation of the present invention be interpreted as.
In first of the present invention, the present invention has put forward a kind of ore powder reduction method, is described in detail the ore powder reduction method of the embodiment of the present invention below with reference to Fig. 1.
S100: preparation reducing gas
According to one embodiment of present invention, first 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 can be prepared thus.
According to another embodiment of the invention, for the preparation of the coal of reducing gas type and be not particularly limited, according to a particular embodiment of the invention, coal can for being selected from least one of low-rank coal in brown coal, long-flame coal and sub-bituminous coal etc.The cost of preparation reducing gas can be reduced thus.The energy characteristic distributions of China is " oil starvation, weak breath, rich coal ", therefore traditional processing method has been not suitable for the national conditions of China, the coal reserves of China occupies third place in the world, output ranks first in the world, low-rank coal reserves occupy more than 40% of coal resources total reserves, current annual production accounts for about 30% of national coal weight, therefore, the exploitation of expanding low-rank coal rationally can not only apply the coal resource of China, simultaneously, utilize low-rank coal to prepare reducing gas and significantly can save cost, improve resource utilization.
According to one embodiment of present invention, the gasification temperature in the gasifying reactor in ore powder reduction method is also not particularly limited, and according to a particular embodiment of the invention, can be 750 ~ 1100 degrees Celsius, and vapor pressure can be more than 0.3MPa.The efficiency of preparation reducing gas can be improved thus, to improve the efficiency of reduction breeze further.According to a particular embodiment of the invention, the type of gasifying reactor is also not particularly limited, and according to the concrete example of this law, gasifying reactor can be at least one being selected from fixed bed, fluidized-bed and conveying bed.Contriver is surprised to find, and only have when adopting fixed bed, fluidized-bed and conveying bed, low-rank coal in just can utilizing, obtain and can be effective to reducing gas breeze being carried out to reduction treatment, namely the composition of reducing gas meets following requirements: H
2/ CO>0.5, (H
2+ CO)/(H
2o+CO
2) >10,3%<CH
4<15%, N
2<10%, 1%≤CO
2≤ 3%.When adopting other gasifying reactor, due to the restriction of gasifying reactor itself, being not suitable for low-rank coal in utilization and obtaining the reducing gas meeting above-mentioned condition.Thus the reducing gas utilizing other gasifying reactors to produce carries out the cost performance of breeze reduction far below employing fixed bed, fluidized-bed and conveying bed.The efficiency of preparation reducing gas can be improved thus, to improve the reduction efficiency of breeze further.According to a particular embodiment of the invention, can react in coal, water vapour and oxygen gasifying reactor under these conditions, prepare the reducing gas containing carbon monoxide and hydrogen.
According to another embodiment of the invention, the composition of reducing gas is also not particularly limited, and according to the concrete example of this law, can contain hydrogen, carbon monoxide, carbonic acid gas, methane, nitrogen in reducing gas, wherein, the volume percent of each component meets following condition: H
2/ CO>0.5, (H
2+ CO)/(H
2o+CO
2) >10,3%<CH
4<15%, N
2<10%, 1%≤CO
2≤ 3%.Utilize this reducing gas can improve the reduction efficiency of breeze further thus.Contriver is surprised to find, and when adopting the reducing gas composition of this ratio, can effectively utilize this reducing gas and carrying out reduction treatment to breeze.When employing does not meet the reducing gas of this condition, can significantly decline to the efficiency that breeze reduces.
S200: reduction breeze
According to one embodiment of present invention, the method for reduction breeze comprises further, and the reducing gas of above-mentioned preparation and breeze are reacted in fluid bed reduction reactor, to obtain reduzate and the weary gas of reduction.According to a particular embodiment of the invention, the breeze for reducing can be at least one being selected from red soil nickel ore, oolitic hematite, antelope stone ore, vanadium titano-magnetite, rhombohedral iron ore, specularite, limonite, spathic iron ore and nonferrous metal oxides slag.Above-mentioned breeze complicated component is difficult, utilizes the method for reducing of breeze of the present invention, can effectively reduce to above-mentioned breeze, improves the reduction efficiency of breeze further.
According to another embodiment of the invention, the mean particle size of breeze is also not particularly limited, and according to a particular embodiment of the invention, the mean particle size of breeze can be below 3.0mm.The reduction efficiency of breeze can be improved thus further.
According to still a further embodiment, for reduce breeze fluid bed reduction reactor reactor in reduction temperature and be not particularly limited, according to a particular embodiment of the invention, the reduction temperature in reactor can be 750 ~ 1150 degrees Celsius, and reduction pressure is less than or equal to 1.0MPa.The reduction efficiency of breeze can be improved thus further.
According to one embodiment of present invention, before reducing gas and breeze being reacted, in advance dust removal process is carried out to reducing gas.The dustiness of reducing gas can be reduced thus, to improve the reduction efficiency of breeze further.According to a particular embodiment of the invention, the gasifying reactor cyclonic separator that at least two can be utilized to connect carries out purifying treatment to the reducing gas prepared in gasifying reactor, wherein be separated in each gasifying reactor cyclonic separator and obtain solid impurity and can be back in gasifying reactor successively, continuation can participate in gasification reaction.The efficiency of carbon conversion of reducing gas can be improved thus, to improve the reduction efficiency of breeze further.
S300: the weary gas of purification reduction
According to one embodiment of present invention, before desulfurization and decarburization is carried out to the weary gas of reduction, in advance dust removal process, heat exchange process, carrying out washing treatment and gas-liquid separation process are carried out successively to the weary gas of reduction, and carry out desulfurization and decarburization process after the gas obtained after gas-liquid separation is compressed.The reducing gas not participating in reduction reaction can be carried out purifying rear recycling thus, to improve the utilising efficiency of reducing gas further, and then improve the reduction efficiency of breeze.
According to another embodiment of the invention, dust removal process can carry out dedusting by the weary cyclconic wind separator of reduction to the weary gas of reduction, at least two reduction of connecting weary cyclconic wind separators specifically can be adopted to carry out dedusting to the weary gas of reduction, be wherein separated the unreduced mineral obtained and be back to continuation participation reduction reaction in fluid bed reduction reactor successively.The utilising efficiency of mineral can be improved thus further.
According to a particular embodiment of the invention, the weary gas of reduction after dust removal process carries out heat exchange process further, heat exchange process can adopt interchanger to carry out, and particularly, the weary gas of reduction through desulfurization and decarburization process can be adopted to carry out heat exchange process to the weary gas of the reduction after dust removal process.Effectively can reduce thus and reduce the temperature of weary gas, and preliminary preheating is carried out to the weary gas of reduction after purification, avoid heat losses, improve heat utilization efficiency.According to a particular embodiment of the invention, further carrying out washing treatment and gas-liquid separation process are carried out to the weary gas of the reduction after heat exchange process, can reduce further thus and reduce the dustiness of weary gas, the weary gas of reduction after purification can be back in fluid bed reduction reactor thus and participate in reduction reaction, the utilization ratio of reducing gas can be improved thus, avoid the wasting of resources.
According to another specific embodiment of the present invention, gas-liquid separation process can be undertaken by gas-liquid separator, the water contained in the weary gas of reduction can be separated thus, with convenient next step, desulfurization and decarburization process is carried out to the weary gas of reduction, and then can improve further and reduce the desulfurization and decarburization efficiency of weary gas.
According to a specific embodiment of the present invention, after the gas obtained is compressed, carry out desulfurization and decarburization process after gas-liquid separation.The reducing gas not participating in reduction reaction can be carried out purifying rear recycling thus, to improve the utilising efficiency of reducing gas further, and then improve the reduction efficiency of breeze.
S400: the weary gas that will reduce is introduced in fluid bed reduction reactor
According to one embodiment of present invention, the part through the weary gas of reduction of purification is utilized to carry out heat exchange process to the weary gas of reduction.Effectively can reduce thus and reduce the temperature of weary gas, and preliminary preheating is carried out to the weary gas of reduction after purification, avoid heat losses, improve heat utilization efficiency.According to a particular embodiment of the invention, above-mentionedly need to be back to after preheating in fluid bed reduction reactor for the weary gas of the reduction after heat exchange process, reduce the temperature of fluid bed reduction reactor after the weary gas of reduction after purifying can be avoided thus to enter fluid bed reduction reactor, cause reduction efficiency to reduce.And then improve the reduction efficiency of breeze.
According to one embodiment of present invention, before the weary gas of reduction through purification is introduced fluid bed reduction reactor, need to carry out thermal pretreatment to the weary gas of reduction through purification in process furnace, wherein, process furnace can adopt a part for the weary gas of reduction through purifying as fuel, the temperature in the weary gas reduction of the low-temperature reduction after purifying fluid bed reduction reactor can be avoided thus, the utilising efficiency of reducing gas can be improved thus, and then improve the reduction efficiency of breeze.
In second of the present invention, the present invention proposes a kind of for reducing the system 1000 of breeze, this comprises: gasifying reactor 100, fluid bed reduction reactor 200, desulfurization and decarburization device 300 and the weary gas return pipeline 400 that reduces.As shown in Figure 2.
Wherein, gasifying reactor 100 reacts wherein for making coal, water vapour and oxygen, to obtain the reducing gas containing carbon monoxide and hydrogen; Fluid bed reduction reactor 200 is connected with gasifying reactor 100, for making reducing gas and breeze react in fluid bed reduction reactor 200, to obtain reduzate and the weary gas of reduction; Desulfurization and decarburization device 300 is connected with fluid bed reduction reactor 200, and weary for reduction gas is carried out desulfurization and decarburization process, to obtain the weary gas of reduction through purification; The weary gas return pipeline 400 that reduces is connected with fluid bed reduction reactor 200 with desulfurization and decarburization device 300 respectively, for being incorporated in fluid bed reduction reactor 200 by the weary gas of reduction through purification.Utilize and above-mentionedly can effectively to reduce to breeze for reducing the system of breeze, and the reduction efficiency of breeze can be significantly improved.
According to one embodiment of present invention, the gasification temperature in gasifying reactor 100 is also not particularly limited, and according to a particular embodiment of the invention, can be 750 ~ 1100 degrees Celsius, and vapor pressure can be more than 0.3MPa.The efficiency of preparation reducing gas can be improved thus, to improve the efficiency of reduction breeze further.According to a particular embodiment of the invention, the type of gasifying reactor 100 is also not particularly limited, and according to the concrete example of this law, gasifying reactor 100 can be at least one being selected from fixed bed, fluidized-bed and conveying bed.The efficiency of preparation reducing gas can be improved thus, to improve the reduction efficiency of breeze further.Contriver is surprised to find, and only have when adopting fixed bed, fluidized-bed and conveying bed, low-rank coal in just can utilizing, obtain and can be effective to reducing gas breeze being carried out to reduction treatment, namely the composition of reducing gas meets following requirements: H
2/ CO>0.5, (H
2+ CO)/(H
2o+CO
2) >10,3%<CH
4<15%, N
2<10%, 1%≤CO
2≤ 3%.When adopting other gasifying reactor, due to the restriction of gasifying reactor itself, being not suitable for low-rank coal in utilization and obtaining the reducing gas meeting above-mentioned condition.Thus the reducing gas utilizing other gasifying reactors to produce carries out the cost performance of breeze reduction far below employing fixed bed, fluidized-bed and conveying bed.
According to a particular embodiment of the invention, can react in coal, water vapour and oxygen gasifying reactor 100 under these conditions, prepare the reducing gas containing carbon monoxide and hydrogen.
According to another embodiment of the invention, the composition of reducing gas is also not particularly limited, and according to the concrete example of this law, can contain hydrogen, carbon monoxide, carbonic acid gas, methane, nitrogen in reducing gas, wherein, the volume percent of each component meets following condition: H
2/ CO>0.5, (H
2+ CO)/(H
2o+CO
2) >10,3%<CH
4<15%, N
2<10%, 1%≤CO
2≤ 3%.Utilize this reducing gas can improve the reduction efficiency of breeze further thus.Contriver is surprised to find, and when adopting the reducing gas composition of this ratio, can effectively utilize this reducing gas and carrying out reduction treatment to breeze.When employing does not meet the reducing gas of this condition, can significantly decline to the efficiency that breeze reduces
According to one embodiment of present invention, as shown in Figure 3, above-mentionedly to comprise further for reducing the system of breeze: the first cleaning apparatus 110, first cleaning apparatus 110 is connected with fluid bed reduction reactor 200 with gasifying reactor 100 respectively, for before reducing gas and breeze being reacted, in advance dust removal process is carried out to reducing gas.The dustiness of reducing gas can be reduced thus, to improve the reduction efficiency of breeze further.According to a particular embodiment of the invention, first cleaning apparatus 110 can be the gasifying reactor cyclonic separator of at least two series connection, this gasifying reactor cyclonic separator is utilized to carry out purifying treatment to the reducing gas prepared in gasifying reactor 100, wherein be separated in each gasifying reactor cyclonic separator and obtain solid impurity and can be back to successively in gasifying reactor 100, continuation can participate in gasification reaction, the efficiency of carbon conversion of gasifying process can be improved thus, to improve the reduction efficiency of breeze further.
According to still a further embodiment, reduction temperature in the reactor of fluid bed reduction reactor 200 is also not particularly limited, according to a particular embodiment of the invention, the reduction temperature in reactor can be 750 ~ 1150 degrees Celsius, and reduction pressure is less than or equal to 1.0MPa.The reduction efficiency of breeze can be improved thus further.
According to still a further embodiment, as shown in Figure 3, between fluid bed reduction reactor 200 and desulfurization and decarburization device 300, direction along from fluid bed reduction reactor 200 to desulfurization and decarburization device 300, be disposed with the second cleaning apparatus 210, heat-exchanger rig 220, washing device 230, gas-liquid separation device 240 and compression set 250, so that before carrying out desulfurization and decarburization to the weary gas of reduction, in advance successively dust removal process is carried out to the weary gas of reduction, heat exchange process and gas-liquid separation process, and carry out desulfurization and decarburization process after the gas obtained after gas-liquid separation is compressed.
According to another embodiment of the invention, second cleaning apparatus 210 can be the weary cyclconic wind separator of reduction of at least two series connection, according to a particular embodiment of the invention, at least two reduction of connecting weary cyclconic wind separators specifically can be adopted to carry out dedusting to the weary gas of reduction, wherein be separated the impurity obtained can be back to successively in fluid bed reduction reactor 200, the purification efficiency to the weary gas of reduction can be improved thus further, to improve the utilising efficiency of reducing gas further, and then improve the reduction efficiency of breeze.
According to a particular embodiment of the invention, heat-exchanger rig 220 can be interchanger, particularly, the weary gas of reduction after utilizing the second cleaning apparatus 210 dedusting is passed into heat-exchanger rig 220 further and carries out heat exchange process.Utilize heat-exchanger rig 220 effectively can carry out heat exchange to the weary gas of reduction thus, reduce the temperature of the weary gas of reduction, and preliminary preheating is carried out to the weary gas of reduction after purification, avoid heat losses, improve heat utilization efficiency.According to a particular embodiment of the invention, washing device 230 and gas-liquid separation device 240 is utilized to carry out carrying out washing treatment and gas-liquid separation process to the weary gas of the reduction after heat exchange process further, can reduce further thus and reduce the dustiness of weary gas, the weary gas of reduction after purification can be back in fluid bed reduction reactor thus and participate in reduction reaction, the utilization ratio of reducing gas can be improved thus, avoid the wasting of resources.
According to another specific embodiment of the present invention, utilize gas-liquid separation device 240 water contained in the weary gas of reduction can be separated, with convenient next step, gas-liquid separation process is carried out to the weary gas of reduction, and then can improve further and reduce the purification efficiency of weary gas.
According to a specific embodiment of the present invention, utilize compression set 250 can compress by weary gas the reduction after gas-liquid separation, carry out desulfurization and decarburization process with the weary gas of convenient reduction.The reducing gas not participating in reduction reaction can be carried out purifying rear recycling thus, to improve the utilising efficiency of reducing gas further, and then improve the reduction efficiency of breeze.
According to still a further embodiment, heat-exchanger rig 220 is connected with desulfurization and decarburization device 300, to utilize the part through the weary gas of reduction of purification to carry out heat exchange process to the weary gas of reduction.The purification efficiency to the weary gas of reduction can be improved thus, to improve the utilising efficiency of reducing gas further, and then improve the reduction efficiency of breeze.According to a particular embodiment of the invention, need to be back to reduction reactor after preheating for the weary gas of the reduction after heat exchange process.Reduce the temperature of fluid bed reduction reactor after the weary gas of reduction after purifying can be avoided thus to enter fluid bed reduction reactor 200, cause reduction efficiency to reduce.And then improve the reduction efficiency of breeze.
Yet another embodiment of the present invention, reduce on weary gas return pipeline 400 and be provided with process furnace 410, so that before the weary gas of reduction through purification is introduced fluid bed reduction reactor 200, in process furnace 410, thermal pretreatment is carried out to the weary gas of reduction through purification, wherein, described process furnace 410 adopts a part for the weary gas of reduction through purifying as fuel, and the another part being about to the weary gas of reduction passes into process furnace, uses as fuel.The temperature in the weary gas reduction of the low-temperature reduction after purifying fluid bed reduction reactor 200 can be avoided thus, the utilising efficiency of reducing gas can be improved thus, and then improve the reduction efficiency of breeze.
The advantage of the ore powder reduction method of the embodiment of the present invention:
1, adopt gasifying reactor can to gasify low-rank coal in brown coal, long-flame coal, sub-bituminous coal etc., be applicable to the resource general layout of the few oily deficency of the rich coal of China, reduce the preparation cost of reducing gas;
2, the weary gas of reduction of preheating after direct after reducing gas purification and purification is mixed into fluid bed reduction reactor 200, coal gas heat and available gas composition are fully utilized;
3, contain certain methane in reducing gas, meet the carburizing requirement of subsequent technique;
4, adopt the reduction weary gas of process furnace to purification to heat, thermo-efficiency is very high;
5, the direct-reduction of low-grade complex refractory ore and the nonferrous metal oxides slags etc. such as red soil nickel ore, oolitic hematite, antelope stone ore, vanadium titano-magnetite, rhombohedral iron ore, specularite, limonite, spathic iron ore can be realized.
6, directly use fine ore, eliminate high pollution, the highly energy-consuming operations such as sintering, pelletizing, save a large amount of initial costs and running cost.
In addition, term " first ", " second " only for describing object, and can not be interpreted as instruction or hint relative importance or imply the quantity indicating indicated technical characteristic.Thus, be limited with " first ", the feature of " second " can express or impliedly comprise one or more these features.In describing the invention, the implication of " multiple " is two or more, unless otherwise expressly limited specifically.
In the present invention, unless otherwise clearly defined and limited, the term such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or connect integratedly; Can be mechanical connection, also can be electrical connection; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals.For the ordinary skill in the art, above-mentioned term concrete meaning in the present invention can be understood as the case may be.
Embodiment
As shown in Figure 4,1, gasifying reactor; 2, gasifying reactor primary cyclone; 3, gasifying reactor secondary cyclone; 4, fluid bed reduction reactor; 5, one-level reduces weary cyclconic wind separator; 6, the weary cyclconic wind separator of second-stage reduction; 7, interchanger; 8, washer; 9, gas-liquid separator; 10, compressor; 11, desulfurization and decarburization device; 12, process furnace.
With red soil nickel ore treatment capacity 80 × 10
4the industrial scale of t/h is example, brown coal coal dust enters fluidized bed gasification reactor 1, react with the gasifying medium generating gasification of water vapor and oxygen under 900 degrees Celsius and 1.0MPa pressure, the coal gas of high temperature produced removes flying dust through one-level gasifying reactor cyclonic separator 2 and secondary gasifying reactor cyclonic separator 3, and reducing gas clean is afterwards mixed into fluid bed reduction reactor 4 with the weary gas of reduction from process furnace 12.
Particle diameter is that the red soil nickel ore breeze of 2.0mm enters by fluid bed reduction reactor 4 top the reducing gas that fluid bed reduction reactor 4 and fluid bed reduction reactor 4 bottom enter and issues raw reduction reaction at 850 DEG C and 0.8MPa pressure, and wherein in reducing gas, the volume percent of each component meets: H
2/ CO=1.0, (H
2+ CO)/(H
2o+CO
2)=13, CH
4=5%, N
2=7%, CO
2content 2%, reduzate is discharged by bottom fluid bed reduction reactor 4 after gas converting heat, and metal recovery rate reaches 90%,
The weary gas of second-stage reduction of fluid bed reduction reactor 4 reduces weary cyclconic wind separator 5 through firsts and seconds, after 6 dedustings, enter interchanger 7 and carry out heat exchange with the road gas from desulfurization and decarburization device 11, liquid is removed again through washer 8 washing and gas-liquid separator 9, after compressor 10 supercharging, enter desulfurization and decarburization device 11 afterwards carry out desulfurization and decarburization, then two-way gas is divided into: first via gas is first in interchanger 7 and the weary gas heat exchange of reduction after the dedusting of second-stage reduction weary cyclconic wind separator 6, after entering process furnace 12 heating again, fluid bed reduction reactor 4 is mixed into the reducing gas after purifying from fluidized bed gasification reactor 1, second road gas enters process furnace 12 and uses as fuel.
In the description of this specification sheets, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means to describe in conjunction with this embodiment or example are contained at least one embodiment of the present invention or example.In this manual, identical embodiment or example are not necessarily referred to the schematic representation of above-mentioned term.And the specific features of description, structure, material or feature can combine in an appropriate manner in any one or more embodiment or example.
Although illustrate and describe embodiments of the invention above, be understandable that, above-described embodiment is exemplary, can not be interpreted as limitation of the present invention, those of ordinary skill in the art can change above-described embodiment within the scope of the invention when not departing from principle of the present invention and aim, revising, replacing and modification.
Claims (9)
1. an ore powder reduction method, is characterized in that, comprising:
Coal, water vapour and oxygen are reacted in gasifying reactor, to obtain the reducing gas containing carbon monoxide and hydrogen;
Described reducing gas and breeze are reacted in fluid bed reduction reactor, to obtain reduzate and the weary gas of reduction;
Weary for described reduction gas is carried out purifying treatment, to obtain the weary gas of reduction through purification;
A part for the described weary gas of reduction through purification is utilized to carry out heat exchange process to the weary gas of described reduction,
Before the described weary gas of reduction through purification is introduced described fluid bed reduction reactor, in process furnace, thermal pretreatment is carried out to the described weary gas of reduction through purification, wherein, described process furnace adopts a part for the described weary gas of reduction through purification as fuel, the weary gas of the described reduction through preheating is incorporated in described fluid bed reduction reactor
Wherein,
Gasification temperature in described gasifying reactor is 750 ~ 1100 degrees Celsius, and vapor pressure is more than 0.3MPa,
Described reducing gas contains hydrogen, carbon monoxide, carbonic acid gas, methane, nitrogen, and wherein, the volume percent of each component meets following condition: H
2/ CO>0.5, (H
2+ CO)/(H
2o+CO
2) >10,3%<CH
4<15%, N
2<10%, 1%≤CO
2≤ 3%,
Described gasifying reactor is at least one being selected from fixed bed, fluidized-bed and conveying bed,
Described purifying treatment comprises further: carry out dust removal process, heat exchange process, carrying out washing treatment, gas-liquid separation process, processed compressed and desulfurization and decarburization process successively to the weary gas of described reduction.
2. method according to claim 1, is characterized in that, described breeze is at least one being selected from red soil nickel ore, antelope stone ore, vanadium titano-magnetite, rhombohedral iron ore, specularite, limonite, spathic iron ore and nonferrous metal oxides slag.
3. method according to claim 2, is characterized in that, the mean particle size of described breeze is below 3.0mm.
4. method according to claim 1, is characterized in that, described coal is at least one being selected from brown coal, long-flame coal and sub-bituminous coal.
5. method according to claim 1, is characterized in that, before reducing gas and breeze being reacted, carries out dust removal process in advance to described reducing gas.
6. method according to claim 1, is characterized in that, the reduction temperature in described fluid bed reduction reactor is 750 ~ 1150 degrees Celsius, and reduction pressure is for being not more than 1.0MPa.
7., for reducing the system of breeze, it is characterized in that, comprise:
Gasifying reactor, described gasifying reactor is used for coal, water vapour and oxygen are reacted wherein, to obtain the reducing gas containing carbon monoxide and hydrogen;
Fluid bed reduction reactor, described fluid bed reduction reactor is connected with described gasifying reactor, for making described reducing gas and breeze react in fluid bed reduction reactor, to obtain reduzate and the weary gas of reduction;
Desulfurization and decarburization device, described desulfurization and decarburization device is connected with described fluid bed reduction reactor, and weary for described reduction gas is carried out desulfurization and decarburization process, to obtain the weary gas of reduction through purification; And
Reduce weary gas return pipeline, described reduction weary gas return pipeline is connected with described fluid bed reduction reactor with described desulfurization and decarburization device respectively, for the described weary gas of reduction through purification is incorporated in described fluid bed reduction reactor,
Gasification temperature in described gasifying reactor is 750 ~ 1100 degrees Celsius, and vapor pressure is more than 0.3MPa,
Described reducing gas contains hydrogen, carbon monoxide, carbonic acid gas, methane, nitrogen, and wherein, the volume percent of each component meets following condition: H
2/ CO>0.5, (H
2+ CO)/(H
2o+CO
2) >10,3%<CH
4<15%, N
2<10%, 1%≤CO
2≤ 3%,
Described gasifying reactor is at least one being selected from fixed bed, fluidized-bed and conveying bed,
Between described fluid bed reduction reactor and described desulfurization and decarburization device, direction along from described fluid bed reduction reactor to described desulfurization and decarburization device, be disposed with the second cleaning apparatus, heat-exchanger rig, washing device, gas-liquid separation device and compression set, so that before carrying out desulfurization and decarburization to the weary gas of described reduction, in advance dust removal process, heat exchange process, carrying out washing treatment and gas-liquid separation process are carried out successively to the weary gas of described reduction, and carry out described desulfurization and decarburization process after the gas obtained after gas-liquid separation is compressed
Described heat-exchanger rig is connected with described desulfurization and decarburization device, to utilize a part for the described weary gas of reduction through purification to carry out heat exchange process to the weary gas of described reduction,
Reduce on weary gas return pipeline and be provided with process furnace, so that before the described weary gas of reduction through purification is introduced described fluid bed reduction reactor, in process furnace, thermal pretreatment is carried out to the described weary gas of reduction through purification, wherein, described process furnace adopts a part for the described weary gas of reduction through purification as fuel.
8. system according to claim 7, is characterized in that, comprises further:
First cleaning apparatus, described first cleaning apparatus is connected with described fluid bed reduction reactor with described gasifying reactor respectively, for before reducing gas and breeze being reacted, carries out dust removal process in advance to described reducing gas.
9. system according to claim 7, is characterized in that, the reduction temperature in described fluid bed reduction reactor is 750 ~ 1150 degrees Celsius, and reduction pressure is less than or equal to 1.0MPa.
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| PCT/CN2014/078060 WO2014187324A1 (en) | 2013-05-23 | 2014-05-21 | New method and system for fluidized bed smelting of reducing gas prepared by using medium/low-rank coal gasification |
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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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