CN101358258B - Coal reducing gas direct reduction metallurgical process in gas-based shaft kiln and system - Google Patents
Coal reducing gas direct reduction metallurgical process in gas-based shaft kiln and system Download PDFInfo
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- CN101358258B CN101358258B CN2007101198838A CN200710119883A CN101358258B CN 101358258 B CN101358258 B CN 101358258B CN 2007101198838 A CN2007101198838 A CN 2007101198838A CN 200710119883 A CN200710119883 A CN 200710119883A CN 101358258 B CN101358258 B CN 101358258B
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- 239000003245 coal Substances 0.000 title claims abstract description 84
- 238000010310 metallurgical process Methods 0.000 title description 9
- 239000007789 gas Substances 0.000 claims abstract description 192
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 66
- 238000000034 method Methods 0.000 claims abstract description 52
- 238000001816 cooling Methods 0.000 claims abstract description 38
- 238000006243 chemical reaction Methods 0.000 claims abstract description 25
- 229910052742 iron Inorganic materials 0.000 claims abstract description 19
- 239000000112 cooling gas Substances 0.000 claims abstract description 13
- 238000006722 reduction reaction Methods 0.000 claims description 63
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 56
- 230000002829 reductive effect Effects 0.000 claims description 23
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 21
- 229910052739 hydrogen Inorganic materials 0.000 claims description 20
- 239000001301 oxygen Substances 0.000 claims description 16
- 229910052760 oxygen Inorganic materials 0.000 claims description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 15
- 239000002002 slurry Substances 0.000 claims description 15
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 12
- 238000005261 decarburization Methods 0.000 claims description 11
- 239000003546 flue gas Substances 0.000 claims description 11
- 238000002309 gasification Methods 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 9
- 230000006835 compression Effects 0.000 claims description 7
- 238000007906 compression Methods 0.000 claims description 7
- 238000006477 desulfuration reaction Methods 0.000 claims description 7
- 230000023556 desulfurization Effects 0.000 claims description 7
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims description 6
- 238000010304 firing Methods 0.000 claims description 3
- 230000001590 oxidative effect Effects 0.000 claims description 3
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 claims description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 2
- 235000011089 carbon dioxide Nutrition 0.000 claims description 2
- 238000005272 metallurgy Methods 0.000 claims description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims 1
- 230000035939 shock Effects 0.000 abstract description 7
- 239000006096 absorbing agent Substances 0.000 abstract description 4
- 239000000446 fuel Substances 0.000 abstract description 2
- 239000003638 chemical reducing agent Substances 0.000 abstract 1
- 239000002826 coolant Substances 0.000 abstract 1
- 238000005201 scrubbing Methods 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 23
- 239000007788 liquid Substances 0.000 description 21
- 239000000243 solution Substances 0.000 description 21
- 238000005516 engineering process Methods 0.000 description 16
- 229910052757 nitrogen Inorganic materials 0.000 description 12
- 239000003250 coal slurry Substances 0.000 description 10
- 238000000227 grinding Methods 0.000 description 10
- 238000005406 washing Methods 0.000 description 10
- 238000011946 reduction process Methods 0.000 description 8
- 239000002893 slag Substances 0.000 description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 230000008929 regeneration Effects 0.000 description 6
- 238000011069 regeneration method Methods 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 238000010791 quenching Methods 0.000 description 5
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 4
- 238000003723 Smelting Methods 0.000 description 4
- 238000004939 coking Methods 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 239000010797 grey water Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 239000002585 base Substances 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000000571 coke Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000007701 flash-distillation Methods 0.000 description 3
- 239000006260 foam Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000000536 complexating effect Effects 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 230000006837 decompression Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000013467 fragmentation Methods 0.000 description 2
- 238000006062 fragmentation reaction Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 230000036961 partial effect Effects 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000002441 reversible effect Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000012216 screening Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 241000282326 Felis catus Species 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 235000012538 ammonium bicarbonate Nutrition 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003818 cinder Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
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- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- -1 hydrogen sulfide sulfides Chemical class 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- KSOKAHYVTMZFBJ-UHFFFAOYSA-N iron;methane Chemical group C.[Fe].[Fe].[Fe] KSOKAHYVTMZFBJ-UHFFFAOYSA-N 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000001465 metallisation Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 210000003205 muscle Anatomy 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
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- 239000003507 refrigerant Substances 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 238000005204 segregation Methods 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000010257 thawing Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/02—Making spongy iron or liquid steel, by direct processes in shaft furnaces
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
- C21B2100/28—Increasing the gas reduction potential of recycled exhaust gases by separation
- C21B2100/282—Increasing the gas reduction potential of recycled exhaust gases by separation of carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
- C21B2100/44—Removing particles, e.g. by scrubbing, dedusting
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/60—Process control or energy utilisation in the manufacture of iron or steel
- C21B2100/64—Controlling the physical properties of the gas, e.g. pressure or temperature
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/60—Process control or energy utilisation in the manufacture of iron or steel
- C21B2100/66—Heat exchange
-
- 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
- Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture Of Iron (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a coal-derived reducing gas base shaft furnace direct reduction metallurgical method and a system thereof. Reducing gases with CO and H2 serving as the main components are prepared from coal through a coal-derived reducing gas system, and are treated by the reducing reaction with iron ore through a direct reduction metallurgical system. The reducing gases are mainly used as the reducing agents of the reducing flow, the cooling agents of the cooling flow and the fuel of the direct reducing metallurgical system. The reducing flow is composed of a reducing shaft furnace, a furnace top gas heat exchanger, a furnace top gas shock chilling/scrubbing system, a process gas recycle compressor, a compressor secondary cooler, a CO2 absorber, a process gas humidifier, a process gas heater, etc. The conical part of the lower part of the shaft furnace is the cooling zone of the shaft furnace direct reduction metallurgical furnace. The cooling gases are sprayed in from the conical region of the lower part of the shaft furnace direct reduction metallurgical furnace, and flow upwards across the metallurgical furnace. The hot cooling gases flow away the cooling region and then are cooled, compressed and recycled. The system is simple in structure and low in process cost.
Description
Technical field
The present invention relates to a kind ofly prepare reducing gas and reduce metallurgical technology, relate in particular to a kind of coal reducing gas direct reduction metallurgical process in gas-based shaft kiln and system with coal.
Background technology
British Ya De that adopted the smelting process (as blast furnace) of coke to obtain great advance than the method for having invented coal coking since 1735, had reached unprecedented perfect degree.The coke smelting process depends critically upon coking coal, and along with the exhaustion of coking coal resource, the coking coal metallurgical technology is faced adverse conditions, and exploitation and employing mill coal iron-smelting process are extremely urgent.
The mill coal metallurgical technology is meant and does not use coke to carry out the various processing methodes of metallurgical production, is divided into direct-reduction process and smelting reduction process two big classifications.Wherein, direct-reduction process is the main flow of mill coal metallurgy.Direct-reduction process has gas base and coal-based two kinds.In all gas base directly reducing metallurgical technologies, most by the Sweet natural gas acquisition reducing gas and the energy.Be subjected to the restriction of natural gas source, gas base directly reducing metallurgical technology cost height is not suitable for China's actual conditions.
Summary of the invention
The purpose of this invention is to provide a kind of system architecture is simple, the technology cost is low coal reducing gas direct reduction metallurgical process in gas-based shaft kiln and system.
The objective of the invention is to be achieved through the following technical solutions:
Coal reducing gas direct reduction metallurgical process in gas-based shaft kiln of the present invention comprises step:
A, prepare reducing gas with coal, the main component of described reducing gas is CO and H
2
B, utilize described reducing gas and iron ore to carry out reduction reaction.
The gas-based shaft kiln directly reduced metallurgical system of coal system reducing gas of the present invention comprises coal system reducing gas system and shaft kiln directly reduced metallurgical system,
Described coal system reducing gas system makes coal with CO and H
2Be the reducing gas of main component, and described reducing gas is flowed to shaft kiln directly reduced metallurgical system;
Reducing gas and iron ore that described shaft kiln directly reduced metallurgical system utilizes described coal system reducing gas system to flow to carry out reduction reaction.
As seen from the above technical solution provided by the invention, coal reducing gas direct reduction metallurgical process in gas-based shaft kiln of the present invention and system are CO and H owing to prepare main component by coal system reducing gas system with coal
2Reducing gas, and utilize described reducing gas and iron ore to carry out reduction reaction by direct reduction metallurgical system.System architecture is simple, the technology cost is low.
Description of drawings
Fig. 1 is the process flow sheet of coal system reducing gas system among the present invention;
Fig. 2 is the schematic diagram of reduction metallurgical system among the present invention.
Embodiment
Coal reducing gas direct reduction metallurgical process in gas-based shaft kiln of the present invention and system, its preferable embodiment comprises:
Step 1, prepare reducing gas with coal, the main component of described reducing gas is CO and H
2, H in the reducing gas
2Being generally 1.0～3.0 with the volume ratio of CO, also can be other ratio according to arts demand.
Step 2, utilize described reducing gas and iron ore to carry out reduction reaction.
As shown in Figure 1, described step 1 comprises:
Step 11, with the levigate coal water slurry of making of the mixture of coal and water;
Step 12, described coal water slurry is carried out gasification process: described coal water slurry and oxygen are carried out mixed firing and oxidizing reaction under high temperature, high pressure, obtain containing CO and H
2Raw gas;
Step 13, described raw gas is carried out purifying treatment: described raw gas is taken off processing such as dirt, decarburization, desulfurization, the content that makes CO and H2 when total content meets predetermined requirement, obtains described reducing gas.
In described step 1, be not limited to coal is made the form of coal water slurry, also can be other state of coal dust, coal cinder or arts demand.Coal and oxygen mixed firing and oxidizing reaction also are not limited to carry out under high temperature, high pressure, can be according to the temperature and pressure of the needs selective reaction of technology.
As shown in Figure 2, described step 2 comprises:
Step 21, reduction flow process: described reducing gas is carried out reduction reaction with iron ore after preheating, i.e. CO and H
2Generate direct-reduced iron with the ferric oxide reaction.
Step 22, cooling process: the reducing gas without preheating is cooled off described direct-reduced iron, produces the carburization reaction of part direct-reduced iron simultaneously.
Coal reducing gas direct reduction metallurgical process in gas-based shaft kiln of the present invention and system comprise coal system reducing gas system and direct reduction metallurgical system,
Described coal system reducing gas system makes coal with CO and H
2Be the reducing gas of main component, and described reducing gas is flowed to shaft kiln directly reduced metallurgical system;
Reducing gas and iron ore that described shaft kiln directly reduced metallurgical system utilizes described coal system reducing gas system to flow to carry out reduction reaction.
As shown in Figure 1, described coal system reducing gas system comprises:
Coal water slurry prepares the unit: be used for the levigate coal water slurry of making of the mixture of coal and water;
Gasification unit: be used under high temperature, the high pressure described coal water slurry being carried out gasification process, obtain containing CO and H
2Raw gas;
Clean unit: be used for described raw gas is carried out purifying treatment, obtain CO and H
2Content when total content meet the reducing gas of pre-provisioning request.
Described clean unit comprises: cleaning apparatus, CO and H
2Changing device; Carbonic acid gas and sulfurous gas, hydrogen sulfide sulfides remove device etc.
As shown in Figure 2, described direct reduction metallurgical system comprises reducing gas feed unit, reduction unit and cooling unit, described reduction unit comprises direct reduction shaft furnace, reducing gas humidifier and reducing gas well heater, and described direct reduction shaft furnace comprises zone of reduction and cooling zone
Described well heater is used for the hot spots reducing gas, with the reactive behavior that improves reducing gas, keep the required technological temperature of reduction reaction in the shaft furnace.
Described reduction unit also comprises flue gas heat exchange device, gas water scrubber, process gas compression machine, CO
2Resorber, humidifier and well heater.The unreacted reducing gas of flue gas that generates after the reduction reaction and part is discharged from the top of reduction shaft furnace, and successively through described flue gas heat exchange device, gas water scrubber, process gas compression machine, CO
2After resorber, humidifier and well heater are handled, participate in reduction reaction once more.
Described reduction metallurgical system also comprises cooling unit, and another part in the described reducing gas directly enters described cooling zone, and the direct-reduced iron that furnace reduction is gone out cools off, and produces the carburization reaction of part direct-reduced iron.Described cooling unit comprises cooling gas device for supplying, cooling gas washer, cooling gas compressor, after handling through cooling gas washer, cooling gas compressor successively from described cooling zone expellant gas, participates in cooling process once more.
With specific embodiment coal reducing gas direct reduction metallurgical process in gas-based shaft kiln of the present invention and system are described in detail below:
The method and system that prepare reducing gas with coal mainly comprise following technical process and equipment:
1.1 empty the branch
Air removes dust and the laggard air compressor machine of becoming owner of of other granule foreign through air filter, cools off through entering in the air cooling tower after the stage compression, thereby to reduce the working load that water in air content reduces adsorber as far as possible.The refrigerated water on air cooling tower top utilizes exsiccant to go out in water-cooling tower further to cool off through ammonia evaporator after the useless nitrogen of tower cools off, and then enters air cooling tower top cooling air.By the air admission molecular sieve adsorber that air cooling tower comes, the moisture content in the absorbed air, CO
2And hydrocarbon polymer.Work of two molecular sieve adsorbers, the waste gas regeneration that another is heated by steam.The air that goes out adsorber is divided into two strands after filtering, and one enters Xia Ta after directly entering the cooling of pressure nitrogen interchanger.Another strand air at first enters main heat exchanger and is backflowed air cooling but through being further divided into two the tunnel, the one tunnel after the compression of supercharging air machine, enters Xia Ta then after decompressor expands; Another road air is through after supercharging side supercharging of booster expansion turbine, through the hyperbaric oxygen interchanger be evaporated product---oxygen cooling deutomerite flows to down tower.
Begin to separate behind the tower under the clean and gas-cooled air admission that backflowed, the air that enters down tower bottom passes column plate and carries out caloic and exchange with phegma on the column plate, obtains pure nitrogen gas on Xia Ta top, obtains oxygen-enriched liquid air at the tower still.As the product carrying device, all the other purity nitrogens enter the condensation side of condenser/evaporator after the partial pressure nitrogen re-heat that following top of tower remove to be extracted out, and nitrogen is emitted heat by the liquid oxygen evaporation that will go up tower bottom there, self obtain condensation and mainly as tower phegma down.Wherein part liquid nitrogen is vaporized the back as the product carrying device by the drag flow high-pressure air in interchanger after the liquid nitrogen pump pressurization.
From extracting one liquid nitrogen fraction out in the middle part of the tower down, quilt is cold excessively in supercooler, and enters the phegma of top of tower as last tower after throttling in addition.The oxygen-enriched liquid air of extracting out from the following tower still of tower is sent into tower as last tower phegma through cold excessively after the throttling.Oxygen product finally produces in last tower rectifying.Highly purified liquid oxygen is extracted out after the liquid oxygen pump pressurization from last tower bottom and is delivered to the hyperbaric oxygen interchanger, and by vaporization of drag flow high-pressure air and re-heat, the oxygen of vaporization goes out device as the product pneumatic transmission.
Useless nitrogen is extracted out from last tower top, at first in supercooler by pure liquid nitrogen, liquid nitrogen fraction and oxygen-enriched liquid air re-heat, enter in the interchanger cooling box after the re-heat then.A part is as the resurgent gases of purification system, and rest part is as the low-temperature receiver of cooling column.
1.2 raw material accumulating
The feed coal train enters factory, after the processing (winter) of thawing, at unloading platform, by screw unloader feed coal is discharged in the blow tank, transport by ground belt under the blow tank, by rubber conveyer transhipment and metering, feed coal is delivered to coal yard stack (when needing, also can directly send screening, crushing system) feed coal.
Coal yard is born having bad luck of feed coal by grab crane and dozer.Grab crane is responsible for grasping feed coal, enters delivery system by loading hopper.After two-stage screening, fragmentation, having bad luck, it is stand-by to deliver to the preceding coal bin of grinding machine.
Limestone powder is shipped by tank car, and it is stand-by directly to deliver to the preceding bunker of grinding machine.
Feed coal and limestone powder (low-ash-fusion coal does not add) in the preceding bunker of grinding machine are sent into grinding machine after metering by proportioning.
1.3 coal slurry preparation technology flow process
Deliver to the coal hopper by the feed coal (doing) that coal fortune system sends here, send into rod mill through Weighing feeder control operational throughput, add a certain amount of water, material carries out the wet method coal-grinding in rod mill.For controlling viscosity of coal slurry and keeping the stability of coal slurry can add suitable additive; For adjusting the pH value of coal slurry, add alkali lye or ammoniacal liquor.Grind slurry altogether and meet the requirements of size-grade distribution, the pulp density that makes is about 60～65%.The slip that grinding machine overflows relies on gravity to flow into the grinding machine blow tank after trommel screen is removed macrobead, and grinding machine blow tank agitator makes the slip homogenizing and keeps suspended state.Slip is pumped into the coal slurry groove air feed usefulness of gasification system again by the coal pulverizer blow tank.
The slurrying water is after metering sent into grinding machine with water by the slurrying tank by the slurrying water pump.The slurrying water uses to realize water cycle, and reduces cost of water treatment from the grey water handing unit.Rest part replenishes with former water as required.
1.4 gasification
In this workshop section, coal slurry and oxygen carry out partial oxidation reaction and make thick reducing gas.
The hyperbaric oxygen that coal slurry is sent here together with the sky branch after the pressurization of coal slurry force (forcing) pump by the coal slurry groove enters vapourizing furnace by burner, and following principal reaction takes place for coal slurry and oxygen in vapourizing furnace:
C+O
2→CO
2
C+CO
2→2CO
C+H
2O→CO+H
2
CO+H
2O→H
2+CO
2
Be reflected under the 2.0～6.0MPa (G), 1200～1500 ℃ and carry out.Gasification reaction was finished in vapourizing furnace conversion zone moment, generated by CO, H
2, CO
2, H
2O and a small amount of CH
4, H
2The raw gas of gas compositions such as S.A small amount of unconverted component and the molten slag that formed by part of ash are with raw gas, thin ash particle and flow to shock chamber into the vapourizing furnace bottom in the gasified raw material.
Chilled water is entered by the Quench water pump and is positioned at the vertical chilling ring of shock chamber's downtake, and flows into the shock chamber downwards along the downtake inwall.Slag quenching in water solidifies, and sinks to vapourizing furnace bottom water-bath.After raw gas and water directly contacted and cools off, most of thin ash was stayed in the water.Raw gas after cooling and washing rises along the annular space between downtake and the airway, goes out the moisture of carrying secretly in the part raw gas through shock chamber's upper baffle is baffle separation, draws from the air outlet of vapourizing furnace side, is sent to Venturi tube and washing tower.
Raw gas mixes through Venturi tube with water from the Quench water pump, thin ash is soaked fully by water, enter the wash tower bottoms water-bath through the washing tower downtake then, remove remaining thin ash, then the annular space through between downtake and airway rises, enter the column plate at washing tower top, the water droplet of carrying secretly is separated by the scum dredger above the column plate.The raw gas that is substantially free of thin ash goes out washing tower and delivers to purification system.
Be deposited on thick slag and other solid particulate of bottom, vapourizing furnace shock chamber, bring lock hopper into by circulating water flow.Big clinker carries out fragmentation through dregs breaker.Most of lime-ash of discharging from vapourizing furnace is deposited in the lock hopper bottom, regularly enters slag bath, pulls back entrucking outward transport out by slag removal machine.Extract more clear water from the lock hopper top out, enter the water-bath of vapourizing furnace shock chamber through the circulation of lock hopper recycle pump.
1.5 grey water handing
The Heisui River that this workshop section will gasify is carried out pulp water and is separated the water cycle use after the processing.
Wash the high temperature Heisui River that tower discharges from vapourizing furnace and carbon and enter high pressure flash vessel respectively, the Heisui River after high pressure flash concentrates concentrates the back through vacuum flashing again and is pumped into clarifying tank by slag bath, and the adding flocculation agent makes its accelerate precipitation in the water.The thin slag slurry of clarifying tank bottom is extracted out through pump and is sent to the filter feeding trough, and via delivering to the vacuum filter dehydration after the pressurization of filter feeding pump, a blob of slag is pulled out outside the factory by automobile.
The high pressure gas that flash off reclaim after the heat through grey water heater, fall sour gas by gas-liquid separator separates, and phlegma is as bath water.
The low-pressure gas that flashes off is directly delivered to the washing tower feeding trough, and the clear water overflow of clarifying tank top is delivered to washing tower feeding trough, gasification lock hopper, coal-grinding tank to grey tank respectively by grey water pump, and a small amount of buck is discharged into wastewater treatment as waste water.
1.6 conversion and recovery of heat
Come autopneumatolysis workshop section by the fully saturated unstripped gas of steam (3.74MPa, about 214 ℃), behind 1# gas-liquid separator separates liquid, the incoming stock gas preheater of about 65% raw gas tube side, be transformed the technology conversion gas preheating that stove comes out, temperature enters shift converter after being increased to about 305 ℃ by about 214 ℃.Shift converter divides two sections, and epimere is pre-conversion, at furnace gas following chemical reaction takes place:
CO+H
2O←→CO
2+H
2+Q
Because the carbon monodixe conversion reaction is an exothermic process, the gas temperature that goes out shift converter rises to 463 ℃, pressure 3.64MPa, contains carbon monoxide about 5.45% (wet basis), enter middle pressure steam superheater tube side, middle pressure saturation steam heat exchange with the conversion by-product, temperature is reduced to about 440 ℃, incoming stock then gas preheater shell side and unstripped gas heat exchange, temperature is reduced to about 398 ℃, enter middle pressure steam producer tube side again, temperature is reduced to about 270 ℃, converge with about 35% the raw gas of not participating in transformationreation then, satisfy the required H of reducing gas
2After the ratio of/CO, enter the boiler water-suppling heater shell side, temperature is reduced to about 220 ℃, go NHD regenerator column boiling device to carry out heat exchange, enter the 2# gas-liquid separator then, behind the separating technology phlegma, gas enters low pressure steam generator, by-product low-pressure steam (0.35MPa is saturated), temperature further reduces, the part water vapor condensation is a water in the gas, and gas-liquid mixture enters the 3# gas-liquid separator, behind the separating and condensing liquid, gas enters de-salted water preheater tube side, heating engineering de-salted water enters watercooler again and is cooled with circulating water to about 40 ℃, enters the 4# gas-liquid separator at last.
The top of 4# gas-liquid separator adds de-salted water, be used for the ammonia of trace in the washing gas, prevent to produce bicarbonate of ammonia crystallization blocking pipe and valve, go out about 40 ℃ of the gas temperatures, pressure 3.50MPa, CO20.32% of 4# gas-liquid separator, deliver to the NHD purification system.
1.7 decarburization, desulfurization
Water-gas enters the thionizer bottom after the gas-gas interchanger heat exchange cooling of NHD decarburization workshop section, absorb most H with top-down NHD solution counter current contact in the tower
2S and part SO
2And COS, the raw gas (about normal temperature, 3.65Mpa) that goes out thionizer goes decarbonizing tower to remove remaining CO
2
The rich solution of discharging at the bottom of the thionizer, after entering desulfurization hydraulic turbine recovered energy, decompression, enter the flash distillation of high pressure flash groove, this flashed vapour enters decarburization sudden strain of a muscle press with the high pressure flash gas merging of decarburization workshop section, and desulphurization system is advanced to reclaim the H in the high pressure flash gas together with raw gas in the back of boosting
2High pressure flash tank liquor liquid phase after the low-pressure flashing tank flash distillation is advanced in heat exchange is regenerated through solvent regeneration tower, and regeneration back lean solution is returned thionizer and recycled.Low pressure flash gas and regeneration overhead sour gas come along sulfur recovery unit.
Remove H from thionizer
2S and part SO
2Advance decarbonizing tower with the raw gas of COS and remove CO
2
The NHD lean solution temperature of advancing the decarburization cat head is-5 ℃, absorbs CO in tower
2Process in because CO
2Solution heat solution temperature is raise, go out NHD rich solution temperature at the bottom of the tower and reach about 16.5 ℃, pressure 3.58Mpa.Rich solution enters hydraulic turbine and reclaims static energy, enters decarburization high pressure flash groove after the step-down, partly soluble CO
2With most of H
2Desorb at this.Enter decarburization after the desulfurization flashed vapour of high pressure flash gas and desulfurization workshop section mixes and dodge press, flashed vapour boosts, cools off the back to be mixed with raw gas, and (about normal temperature, 1.3Mpa) goes the circulation of desulfurization workshop section to absorb again after the gas-to-gas heat exchanger cooling.
The rich solution gravity flow of coming out in the poor bottom of decarburization flash distillation enters gas stripping column, and solution and gas are put forward nitrogen counter current contact in packing layer, at this moment dissolved CO in the solution
2Put forward by gas, enter atmosphere.The lean solution (about 6.7 ℃) of coming out at the bottom of the gas stripping column is through decarburization lean pump pressure-raising and enter decarbonizing tower top recycle after ammonia evaporator is cooled to about-5 ℃.
1.8 sulfur recovery
Sour gas is after gas-liquid separation, entered top, absorption tower by complexing iron doctor solution self-priming, gas-liquid two-phase mixes in injector, and constantly upgrade contact area, gas-liquid two-phase enters bottom segregation section, behind the gas phase separation drop, enters packed absorber, behind spray section, packing section absorbing hydrogen sulphide, tail gas is concentrated discharging.
Compile bottom complexing iron doctor solution rich solution self-injection absorption tower, the packed absorber and enter the rich solution groove, squeeze into the injector at regenerator column top through the rich solution pump, enter the air thorough mixing of injector with self-priming, after reaction, enter regenerator column, further oxidation regeneration in regenerator column, lean solution after the regeneration enters the lean solution groove from the overflow of regenerator column top, is boosted by lean pump and sends into spray absorption tower, packed absorber circulation absorption.
The elementary sulfur of separating out in the regenerator column is suspended in the annular column at regenerator column top, and overflow enters foam chute, sends into the sulphur foam chute by the sulphur foam pump again, filters through whizzer, advances the sulfur melting kettle recovery sulphur.
1.9 depressurized system
Coal gas after the purification makes gaseous tension be reduced to about 0.8Mpa by 3.65MPa through decompressor, delivers to circulating water system, uses for Shaft Furnace Direct Reduction Process after the heat exchange.But the decompression acting of expanding drives about mechanical means saves energy 1500Kw, produces about cold 4.75MJ/h.
The reducing gas quality reaches following processing requirement after reducing pressure:
CO+H
2 95.57％
CO
2 3％
CH
4、Ar、N
2 1.43％
Pressure 0.8Mpa
Temperature normal temperature
The system and method that the coal system of utilization reducing gas and iron ore carry out reduction reaction mainly comprises following technical process and equipment:
2.1 the principle of reduction reaction is, passes through H
2With the chemical reaction of CO and iron ore the oxygen in the ore is removed, is produced the direct-reduced iron of high degree of metalization:
Fe
2O
3+3H
2→2Fe+3H
2O
Fe
2O
3+3CO→2Fe+3CO
2
The core of its technology is direct reduction shaft furnace.As shown in Figure 2, from technology point of view, directly reduction mainly is made up of supply, reduction flow process and cooling process three parts of reducing gas.
2.2 the supply of reducing gas
Reducing gas supply flow process is seen Fig. 2.Usually reducing gas is main as reducing the reductive agent of flow process, the refrigerant and the fuel of cooling process in gas-based shaft kiln directly reduced technology.
2.3 reduction flow process
The reduction flow process is by direct reduction shaft furnace, furnace roof flue gas heat exchange device, furnace roof flue gas Quench/washing system, process gas recycle compressor, compressor recooler, CO
2Compositions such as resorber, process gas humidifier and process gas well heater.
The reducing gas of reduction flow process is by the synthetic gas that replenishes and removed CO
2Temperature be that 50 ℃, pressure are 6.4kg/cm
2About recycle gas mix to form.
Be to obtain the optimum control of cementation process, reducing gas adds a spot of water vapor by a humidification jar, then by about process gas heater heats to 930 ℃.
The reducing gas of heat is admitted to the reduction shaft furnace band, and pressure is approximately 4.5kg/cm
2, upwards reverse flow guarantees that through the iron ore moving-bed gas distribution is even, contact is good between the gas-solid.
At the zone of reduction of shaft furnace, the heat transmission of the at first logical superheated reducing gas of iron ore is preheating to the required temperature levels of reduction process.After the pre-heating stage, reducing gas H
2With CO and ferric oxide generation reduction reaction, the oxygen in the ore is removed.The mechanism of reduction reaction comprises the formation of reductive agent gas ion and electron diffusion, cenotype nuclear in the adsorption catalysis of reaction interface, solid-phase layer and grows up etc.
The mechanism of reduction process can be described as:
Fe
2O
3→Fe
3O
4→FeO→Fe
Wherein iron ore and H
2The reduction reaction process be:
3Fe
2O
3+H
2→2Fe
3O
4+H
2O
Fe
3O
4+H
2→3FeO+H
2O
FeO+H
2→Fe+H
2O
The reduction reaction process of iron ore and CO is:
3Fe
2O
3+CO→2Fe
3O
4+CO
2
Fe
3O
4+CO→3FeO+CO
2
FeO+CO→Fe+CO
2
The about 490 ℃ flue gas of temperature that shaft furnace is discharged reclaims heat through furnace roof flue gas heat exchange device, produces to be used for CO
2Remove the steam of device, then by flue gas Quench/washing system.In this link, the water that produces in the reduction process obtains concentrating and removing from air-flow, and the most dust that carries in the gas is also separated goes out.Washed gas recycles after by process gas compressor pressurize.
2.4 cooling gas flow process
The conical section of shaft furnace bottom is shaft kiln directly reduced cooling zone.
For ease of the discharging operation of cold conditions direct-reduced iron, about 40 ℃ of temperature, the about 4.8kg/cm of pressure
2Synthetic gas and the recirculation cooler that comes out of cooling gas compressor mix the back and spray into from the conical region of reactor lower part, upwards the direct-reduced iron moving-bed is crossed in reverse flow.Be cooled at the cooling zone product, produce the carburization reaction of part direct-reduced iron simultaneously:
3Fe+CH
4→Fe
3C+2H
2
3Fe+2CO→Fe
3C+CO
2
3Fe+CO+H
2→Fe
3C+H
2O
CH
4→C+2H
2
Reduced zone also carries out the part carburization reaction.Most of C is with iron carbide (Fe
3C) form enters into product.
The process of cooling of carburization reaction overall height heat absorption behavior reinforcement direct-reduced iron.
The cold gas of heat is left cooled region, and through overcooling, compression, recirculation is used.Direct-reduced iron is discharged the cooling zone of shaft furnace by rotary valve under about 55 ℃ condition.
The present invention comprises CO and H by coal system reducing gas system with the coal preparation
2Reducing gas, and utilize described reducing gas that iron ore is carried out reduction reaction by direct reduction metallurgical system.System architecture is simple, the technology cost is low.
The above; only for the preferable embodiment of the present invention, but protection scope of the present invention is not limited thereto, and anyly is familiar with those skilled in the art in the technical scope that the present invention discloses; the variation that can expect easily or replacement all should be encompassed within protection scope of the present invention.
Claims (2)
1. the gas-based shaft kiln directly reduced metallurgical system of coal system reducing gas is characterized in that, comprises coal system reducing gas system and shaft kiln directly reduced metallurgical system;
Described coal system reducing gas system makes coal with CO and H
2Be the reducing gas of main component, and described reducing gas is flowed to shaft kiln directly reduced metallurgical system;
Reducing gas and iron ore that described shaft kiln directly reduced metallurgical system utilizes described coal system reducing gas system to flow to carry out reduction reaction;
Described coal system reducing gas system comprises:
Coal water slurry prepares the unit: be used for the levigate coal water slurry of making of the mixture of coal and water;
Gasification unit: be used for described coal water slurry is carried out gasification process, obtain containing CO and H
2Raw gas;
Clean unit: be used for described raw gas is carried out purifying treatment, obtain CO and H
2Content when total content meet the reducing gas of pre-provisioning request;
Described clean unit comprises: CO and H
2Changing device, carbonic acid gas and sulfide remove device;
Described shaft kiln directly reduced metallurgical system comprises reducing gas feed unit, reduction unit and cooling unit, and described reduction unit comprises direct reduction shaft furnace, reducing gas humidifier and reducing gas well heater, and described direct reduction shaft furnace comprises zone of reduction and cooling zone;
Described reducing gas well heater is used for the hot spots reducing gas, with the reactive behavior that improves reducing gas, keep the required technological temperature of reduction reaction in the shaft furnace;
Another part in the described reducing gas directly enters described cooling zone, and the direct-reduced iron that furnace reduction is gone out cools off, and produces the carburization reaction of part direct-reduced iron simultaneously;
Described reduction unit also comprises flue gas heat exchange device, gas water scrubber, process gas compression machine, CO
2Resorber; The unreacted reducing gas of flue gas that generates after the reduction reaction and part is discharged from the top of reduction shaft furnace, and successively through described flue gas heat exchange device, gas water scrubber, process gas compression machine, CO
2After resorber, reducing gas humidifier, reducing gas well heater are handled, participate in reduction reaction once more;
Described cooling unit comprises cooling gas washer, cooling gas compressor;
After process cooling gas washer, cooling gas compressor are handled successively from described cooling zone expellant gas, participate in cooling process once more.
2. the method for the gas-based shaft kiln directly reduced metallurgy of the gas-based shaft kiln directly reduced metallurgical system realization coal system reducing gas of the described coal system reducing gas of claim 1 is characterized in that, comprises step:
A, prepare reducing gas with coal, the main component of described reducing gas is CO and H
2
B, utilize described reducing gas and iron ore to carry out reduction reaction;
H in the described reducing gas
2With the volume ratio of CO be 1.0～3.0;
Described steps A comprises step:
A1, with the levigate coal water slurry of making of the mixture of coal and water;
A2, described coal water slurry is carried out gasification process: described coal water slurry and oxygen are carried out mixed firing and oxidizing reaction, obtain containing CO and H
2Raw gas;
A3, described raw gas is carried out purifying treatment: with described raw gas carry out decarburization, desulfurization is handled, and makes CO and H
2The ratio of content and total content meet predetermined requirement, obtain described reducing gas;
Described step B comprises step:
B1, reduction flow process: described reducing gas is carried out reduction reaction with iron ore after preheating, i.e. CO and H
2Generate direct-reduced iron with the ferric oxide reaction;
B2, cooling process: the reducing gas without preheating is cooled off described direct-reduced iron, produces the carburization reaction of part direct-reduced iron simultaneously.
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Denomination of invention: Coal reducing gas direct reduction metallurgical process in gas-based shaft kiln and system Effective date of registration: 20180328 Granted publication date: 20100630 Pledgee: Bank of Beijing, Limited by Share Ltd, Nanjing branch Pledgor: Jiangsu Research & Design Institute of Metallurgical Industry Co., Ltd. Registration number: 2018320000034 |
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