CN103667565B - Middle low-rank coal vaporizing system standby reduction air cooling send fluidized-bed to smelt novel method and system - Google Patents
Middle low-rank coal vaporizing system standby reduction air cooling send fluidized-bed to smelt novel method and system Download PDFInfo
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- 230000009467 reduction Effects 0.000 title claims abstract description 244
- 238000000034 method Methods 0.000 title claims abstract description 111
- 239000003245 coal Substances 0.000 title claims abstract description 42
- 241001062472 Stokellia anisodon Species 0.000 title description 5
- 238000001816 cooling Methods 0.000 title description 4
- 230000008016 vaporization Effects 0.000 title description 4
- 239000007789 gas Substances 0.000 claims abstract description 310
- 230000008569 process Effects 0.000 claims abstract description 80
- 239000012530 fluid Substances 0.000 claims abstract description 70
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 68
- 230000023556 desulfurization Effects 0.000 claims abstract description 68
- 238000005261 decarburization Methods 0.000 claims abstract description 67
- 238000000746 purification Methods 0.000 claims abstract description 42
- 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 15
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000001301 oxygen Substances 0.000 claims abstract description 12
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 12
- 239000000843 powder Substances 0.000 claims abstract description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000007788 liquid Substances 0.000 claims description 41
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 36
- 238000000926 separation method Methods 0.000 claims description 32
- 238000005406 washing Methods 0.000 claims description 24
- 239000000428 dust Substances 0.000 claims description 19
- 229910052742 iron Inorganic materials 0.000 claims description 18
- 229910052757 nitrogen Inorganic materials 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
- 238000002309 gasification Methods 0.000 claims description 12
- 238000004140 cleaning Methods 0.000 claims description 9
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 8
- 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 8
- 150000002431 hydrogen Chemical class 0.000 claims description 7
- 229910052720 vanadium Inorganic materials 0.000 claims description 7
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-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
- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 claims description 6
- 238000009997 thermal pre-treatment Methods 0.000 claims description 6
- 230000006835 compression Effects 0.000 claims description 5
- 238000007906 compression Methods 0.000 claims description 5
- 239000003077 lignite 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
- 229910052595 hematite Inorganic materials 0.000 claims description 4
- 239000011019 hematite Substances 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
- 229910052759 nickel Inorganic materials 0.000 claims description 4
- 239000002245 particle Substances 0.000 claims description 4
- 239000002893 slag Substances 0.000 claims description 4
- 239000002689 soil 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 212
- 238000002360 preparation method Methods 0.000 description 18
- 239000000203 mixture Substances 0.000 description 10
- 238000006243 chemical reaction Methods 0.000 description 6
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- 230000007423 decrease Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
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- 229910052500 inorganic mineral Inorganic materials 0.000 description 3
- 239000011707 mineral Substances 0.000 description 3
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
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- 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
- 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
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- 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
- 238000005262 decarbonization Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
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- 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
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- 239000010931 gold Substances 0.000 description 1
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- 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
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- 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)
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; And weary for reduction gas is incorporated in fluid bed reduction reactor; Wherein, weary for reduction gas is incorporated into fluid bed reduction reactor and comprises further: after being mixed with reducing gas by weary for reduction gas in advance, carry out desulfurization and decarburization process, so as to obtain through purification mixed gas and be 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.Fluidized-bed is sent to smelt novel method and system in particular to middle low-rank coal vaporizing system standby reduction air cooling.
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 standby reduction air cooling with advantages such as production efficiency are high, reducing gas preparation cost is low send fluidized-bed to smelt novel method and system.
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; And weary for described reduction gas is incorporated in described fluid bed reduction reactor; Wherein, weary for described reduction gas is incorporated into described fluid bed reduction reactor and comprises further: after being mixed with described reducing gas by weary for described reduction gas in advance, carry out desulfurization and decarburization process, to obtain the mixed gas through purification; Described mixed gas is incorporated in described fluid bed reduction reactor.
During the feed coal utilizing aforesaid method to prepare reducing gas can adopt, low-rank coal, significantly reduce 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 above-mentioned method of going back 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 that at least one by 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 prepares.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 in utilization, low-rank coal obtains 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 is carried out desulfurization and decarburization process, in advance dust removal process, carrying out washing treatment and gas-liquid separation process are carried out to described reducing gas.The purity of reducing gas can be improved 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 for being not more than 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, a part for the described mixed gas through purification is utilized to carry out heat exchange process to the weary gas of described reduction.Heat utilization efficiency can be improved thus.
According to embodiments of the invention, before the described mixed gas through purification is introduced described fluid bed reduction reactor, in process furnace, thermal pretreatment is carried out to the described mixed gas through purification, wherein, described process furnace adopts a part for the described mixed gas 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 with described gasifying reactor, and described reducing gas and the weary gas of reduction are carried out desulfurization and decarburization process, to obtain the mixed gas through purification; And mixed gas delivery pipeline, described mixed gas delivery 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 mixed gas 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, between described gasifying reactor and described desulfurization and decarburization device, the first cleaning apparatus, the first washing device and the first gas-liquid separation device is disposed with to described desulfurization and decarburization device direction along described gasifying reactor, for before reducing gas and breeze being reacted, in advance dust removal process, carrying out washing treatment and gas-liquid separation process are carried out to described reducing gas.The purity of reducing gas can be improved 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 not more than 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, second washing device, second 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 mixed gas 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 mixed gas, avoid heat losses, improve heat utilization efficiency.
According to embodiments of the invention, described mixed gas delivery pipeline is provided with process furnace, so that before by the described mixed gas delivery through purification extremely described fluid bed reduction reactor, in process furnace, thermal pretreatment is carried out to the described mixed gas through purification, wherein, described process furnace adopts a part for the described mixed gas through purification as fuel.The utilising efficiency of mixed 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 reacts coal, water vapour and oxygen in gasifying reactor, obtains 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 in being selected from, low-rank coal, such as can be selected from least one of brown coal, long-flame coal and sub-bituminous coal.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, in expansion, the exploitation of low-rank coal rationally can not only apply the coal resource of China, simultaneously, in utilization, low-rank coal prepares reducing gas and significantly can save cost, improves 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 gasification reactor, fluidized bed gasification reactor and conveying bed gasifying reactor.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 concrete example of the present invention, 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.
Particularly, can by controlling add the ratio of coal, water vapour and oxygen, and concrete reduction reactor and its processing parameter control the above-mentioned reducing gas that obtains, to improve the reduction efficiency of reducing gas to breeze.Thus, according to the ore powder reduction method of the embodiment of the present invention, in can selecting, low-rank coal as raw material, by controlling the ratio of the water vapour that adds and oxygen and concrete suitable reduction reactor processing parameter, high-quality reducing gas can be prepared equally.Thus can the cost-effective efficiency simultaneously improving preparation reducing gas.
According to one embodiment of present invention, before the reducing gas of above-mentioned preparation is passed into fluid bed reduction reactor, in advance reducing gas is carried out desulfurization and decarburization process, to improve the purity of reducing gas further, improve the reaction efficiency of reducing gas and breeze.According to a particular embodiment of the invention, before reducing gas is carried out desulfurization and decarburization process, dust removal process, carrying out washing treatment and gas-liquid separation process can also be carried out to reducing gas in advance.The solid impurities such as the flying dust in reducing gas can be removed thus further, can further improve the purity of reducing gas thus, to improve the reduction efficiency of breeze further.According to concrete example of the present invention, above-mentioned dust removal process, carrying out washing treatment and gas-liquid separation process can be undertaken by gasifying reactor cyclonic separator, washing device and gas-liquid separation device, effectively can carry out purifying to reducing gas thus.
According to a particular embodiment of the invention, dust removal process is carried out to reducing gas, 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.
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; And weary for reduction gas is incorporated in fluid bed reduction reactor.
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, carry out reduction reaction after above-mentioned breeze being prepared into breeze, the ultimate compression strength of breeze is also not particularly limited, and according to a particular embodiment of the invention, the mean particle size of breeze is below 3.0mm.The specific surface of breeze can be improved thus, to expand the contact area of breeze and reducing gas, improve the reduction efficiency of breeze 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 for being not more than 1.0MPa.In the work-ing life saving extension device while the energy, and can improve the reduction efficiency of breeze further thus.
S300: the weary gas of purification reduction
According to one embodiment of present invention, before weary for described reduction gas is incorporated into fluid bed reduction reactor, desulfurization and decarburization process is carried out to the weary gas of reduction, purifying can be carried out to the weary gas of reduction thus, to improve the rate of utilization to reducing gas, and then improve reducing gas to the efficiency of breeze.According to a particular embodiment of the invention, aforesaid method comprises further: before carrying out desulfurization and decarburization to the weary gas of reduction, carry out dust removal process, heat exchange process, carrying out washing treatment and gas-liquid separation process successively in advance to the weary gas of 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 a particular 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 mixed gas 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 mixed gas 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 improve further thus and reduce the purity 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, process of gas-liquid desulfurization and decarburization 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, 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.
According to another embodiment of the invention, above-mentioned reducing gas and the weary gas of reduction together can carry out desulfurization and decarburization process, same desulfurization and decarburization device can be adopted thus in aforesaid method jointly to carry out desulfurization and decarburization process to reducing gas and the weary gas of reduction, the desulfurization and decarburization efficiency to reducing gas and the weary gas of reduction can be improved thus further.
S400: the weary gas that will reduce is introduced in fluid bed reduction reactor
According to one embodiment of present invention, the mixed gas after being purified after reducing gas and the weary gas of reduction being carried out desulfurization and decarburization process jointly.According to a particular embodiment of the invention, the part through the mixed gas 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 mixed gas after purification, avoid heat losses, improve heat utilization efficiency.
According to one embodiment of present invention, mixed gas after above-mentioned purification is before passing in fluidized-bed reactor, need to carry out thermal pretreatment to it in process furnace, wherein, process furnace can adopt a part for mixed gas as fuel, a part by mixed gas passes into in process furnace, uses, provide heat as fuel.Reduce the temperature of the inside of fluid bed reduction reactor after the low-temperature mixed gas 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.
In second of the present invention, the present invention proposes a kind of for reducing the system 1000 of breeze, this system comprises: gasifying reactor 100, fluid bed reduction reactor 200, desulfurization and decarburization device 300 and mixed gas delivery pipeline 400.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 with gasifying reactor 100, and reducing gas and the weary gas of reduction are carried out desulfurization and decarburization process, to obtain the mixed gas through purification; Mixed gas delivery pipeline 400 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 mixed gas 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.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 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>0.7, (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 still a further embodiment, as shown in Figure 3, above-mentionedly to comprise further for reducing the system of breeze: between described gasifying reactor 100 and described desulfurization and decarburization device 300, the first cleaning apparatus 110, first washing device 120 and the first gas-liquid separation device 130 is disposed with to described desulfurization and decarburization device 300 direction along described gasifying reactor 100, for before reducing gas and breeze being reacted, in advance dust removal process, carrying out washing treatment and gas-liquid separation process are carried out to described reducing gas.The purity of reducing gas can be improved 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 reducing gas can be improved thus, to improve the reduction efficiency of breeze further.According to embodiments of the invention, after utilizing reducing gas to carry out reduction treatment to breeze, in the weary gas of the reduction produced, also remain a large amount of reducing gas, this part can have been reduced weary gas after purification, then return breeze is reduced.Here used term " purification " refers to the composition removed and be not suitable for reduction treatment in the weary gas of reduction, mainly sulfocompound and carbon compound, thus, utilizes desulfurization and decarburization device 300 can carry out purifying treatment to the weary gas of reduction.
According to a specific embodiment of the present invention, reduction temperature in the reactor of fluid bed reduction reactor 200 is also not particularly limited, according to concrete example of the present invention, the reduction temperature in reactor can be 750 ~ 1150 degrees Celsius, and reduction pressure is for being not more than 1.0MPa.The reduction efficiency of breeze can be improved thus further.
According to another specific embodiment of the present invention, as shown in Figure 3, between described fluid bed reduction reactor 200 and described desulfurization and decarburization device 300, direction along from described fluid bed reduction reactor 200 to described desulfurization and decarburization device 300, be disposed with the second cleaning apparatus 210, heat-exchanger rig 220, second washing device 230, second gas-liquid separation device 240 and compression set 250, 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.According to another specific embodiment of the present 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, be wherein separated the unreduced breeze 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, 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.Heat-exchanger rig 220 is utilized effectively to cool the weary gas of reduction thus, so that by the water vapour liquefaction contained in the weary gas of reduction, 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 particular embodiment of the invention, utilize the second washing device 230 can carry out purifying treatment to the weary gas of reduction, so that the tiny fly ash granule in the weary gas of removing reduction, can improving further thus and reduce the purification efficiency of weary gas, improving reducing the recycling of weary gas.
According to another specific embodiment of the present invention, utilize the second gas-liquid separation device 240 water contained in the weary gas of reduction can be separated, with convenient next step, process of gas-liquid desulfurization and decarburization 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 another embodiment of the invention, utilize above-mentioned desulfurization and decarburization device 300 together can carry out desulfurization and decarburization process to reducing gas and the weary gas of reduction, therefore, the mixed gas after being purified after the above-mentioned reducing gas through rough purification and the weary gas of reduction being carried out desulfurization and decarburization process jointly.By mixed gas delivery pipeline 400 by mixed gas delivery to fluid bed reduction reactor with breeze generation reduction reaction.The purifying treatment to reducing gas and the weary gas of reduction can be improved thus further, to improve the reduction efficiency of breeze further.
According to one embodiment of present invention, heat-exchanger rig 220 is connected with desulfurization and decarburization device 300, to utilize the part through the mixed gas of purification 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 mixed gas after purification, avoid heat losses, improve heat utilization efficiency.According to a particular embodiment of the invention, above-mentionedly need after preheating, be back to fluid bed reduction reactor 200 for the mixed gas after heat exchange process.Reduce the temperature in fluid bed reduction reactor after the low-temperature mixed gas after purifying can be avoided thus to enter fluid bed reduction reactor 200, and then improve the reduction efficiency of breeze.
According to another embodiment of the invention, mixed gas delivery pipeline 400 is provided with process furnace 410, so that before the mixed gas through purification is introduced fluid bed reduction reactor 200, in process furnace 410, thermal pretreatment is carried out to the mixed gas through purification, wherein, described process furnace 410 adopts a part for the mixed gas through purifying as fuel, the temperature in the low-temperature mixed gas reduction fluid bed reduction reactor 200 after purifying can be avoided thus, the reduction efficiency of breeze can be improved thus further.
The advantage of the ore powder reduction method of the embodiment of the present invention:
1, adopt gasifying reactor can to gasify the low-rank coal such as brown coal, long-flame coal, sub-bituminous coal, 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, reducing gas and the weary gas of reduction share a set of desulfurization and decarburization device, and facility investment is few;
3, contain certain methane gas in reducing gas, meet the carburizing requirement of subsequent technique;
4, 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;
5, 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, simultaneous reactions efficiency increases substantially.
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, reducing gas washer; 5, reducing gas gas-liquid separator; 6, desulfurization and decarburization device; 7 process furnace; 8, fluid bed reduction reactor; 9, weary cyclconic wind separator is reduced; 10, weary gas secondary cyclone is reduced; 11, interchanger; 12, weary gas washing device is reduced; 13, weary gas gas-liquid separator is reduced; 14, compressor.
With vanadium titano-magnetite 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 high temperature reduction gas produced removes flying dust through gasifying reactor primary cyclone 2 and gasifying reactor secondary cyclone 3, and then enter reducing gas washer 4 and to wash and after reducing gas gas-liquid separator 5 realizes gas-liquid separation, after clean reducing gas and the gas and vapor permeation from compressor 14, enter desulfurization and decarburization device 6 together and carry out desulfurization and decarburization, desulfurization and decarburization device 6 gas is out divided into two tunnels: first via gas first interchanger 11 with through reducing the weary gas heat exchange of reduction after the dedusting of weary gas secondary cyclone 10, enter process furnace 7 again to heat, enter fluid bed reduction reactor 8 afterwards to use as reducing medium, second road gas enters process furnace 7 and uses as fuel.
Particle diameter is that the vanadium titano-magnetite fine ore of 2.0mm enters by fluid bed reduction reactor 8 side the reducing gas that fluid bed reduction reactor 8 and fluid bed reduction reactor 8 bottom enter and issues raw reduction reaction at 850 degrees Celsius and 0.8MPa pressure, and wherein reducing gas should meet: 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 via bottom fluid bed reduction reactor 8, and metal recovery rate reaches 90%.
The weary gas of reduction of fluid bed reduction reactor 8 is through reducing after weary gas primary cyclone 9 and the dedusting of reduction weary gas secondary cyclone 10, enter interchanger 11 and carry out heat exchange with the road gas from decarbonization desulfurization system 6, wash and reduce weary gas gas-liquid separator 13 except liquid through the weary gas washing device 12 of reduction again, being mixed with the reducing gas from reducing gas gas-liquid separator 5 after compressor 14 supercharging afterwards enters desulfurization and decarburization device 6 and carries out desulfurization and decarburization.
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, wherein, gasification temperature in described gasifying reactor is 750 ~ 1100 degrees Celsius, 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 reducing gas and breeze are reacted in fluid bed reduction reactor, to obtain reduzate and the weary gas of reduction;
A part for the mixed gas through purification is utilized to carry out heat exchange process to the weary gas of described reduction;
Before the described mixed gas through purification is introduced described fluid bed reduction reactor, in process furnace, thermal pretreatment is carried out to the described mixed gas through purification, wherein, described process furnace adopts a part for the described mixed gas through purification as fuel;
Weary for described reduction gas is incorporated in described fluid bed reduction reactor, wherein, weary for described reduction gas is incorporated into described fluid bed reduction reactor comprise further: after being mixed with described reducing gas by weary for described reduction gas in advance, carry out desulfurization and decarburization process, to obtain the mixed gas through purification, wherein, before desulfurization and decarburization is carried out 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, and
Described mixed gas is incorporated in described fluid bed reduction reactor.
2. method according to claim 1, it is characterized in that, described breeze is that at least one by 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 prepares.
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 is carried out desulfurization and decarburization process, carries out dust removal process, carrying out washing treatment and gas-liquid separation 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 with described gasifying reactor, and described reducing gas and the weary gas of reduction are carried out desulfurization and decarburization process, to obtain the mixed gas through purification; And
Mixed gas delivery pipeline, described mixed gas delivery pipeline is connected with described fluid bed reduction reactor with described desulfurization and decarburization device respectively, for the described mixed gas through purification 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,
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, the second washing device, the second 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 mixed gas through purification to carry out heat exchange process to the weary gas of described reduction,
Described mixed gas delivery pipeline is provided with process furnace, so that before by the described mixed gas delivery through purification extremely described fluid bed reduction reactor, in process furnace, thermal pretreatment is carried out to the described mixed gas through purification, wherein, described process furnace adopts a part for the described mixed gas through purification as fuel.
8. system according to claim 7, it is characterized in that, between described gasifying reactor and described desulfurization and decarburization device, the first cleaning apparatus, the first washing device and the first gas-liquid separation device is disposed with to described desulfurization and decarburization device direction along described gasifying reactor, for before reducing gas and breeze being reacted, in advance dust removal process, carrying out washing treatment and gas-liquid separation process are carried out 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 not more than 1.0MPa.
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| WO2014187328A1 (en) * | 2013-05-23 | 2014-11-27 | 北京神雾环境能源科技集团股份有限公司 | New method and system for cold conveying fluidized bed smelting of reducing gas prepared by using medium/low-rank coal gasification |
| CN104451163A (en) * | 2014-12-15 | 2015-03-25 | 湖南省加嘉锑业科技有限公司 | Heavy metal treatment device |
| CN104805248A (en) * | 2015-03-31 | 2015-07-29 | 攀钢集团攀枝花钢铁研究院有限公司 | Device and method for reduction of coal-based pellets |
| CN106244751A (en) * | 2016-09-08 | 2016-12-21 | 江苏省冶金设计院有限公司 | A kind of low order coal dust gas-made technology for blast furnace blowing |
| CN106811595A (en) * | 2017-03-24 | 2017-06-09 | 江苏省冶金设计院有限公司 | The system and method for processing vanadium titano-magnetite |
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