CN101528948A - Method and device for producing molten material - Google Patents
Method and device for producing molten material Download PDFInfo
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- CN101528948A CN101528948A CNA2007800376484A CN200780037648A CN101528948A CN 101528948 A CN101528948 A CN 101528948A CN A2007800376484 A CNA2007800376484 A CN A2007800376484A CN 200780037648 A CN200780037648 A CN 200780037648A CN 101528948 A CN101528948 A CN 101528948A
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0006—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0006—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state
- C21B13/0013—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state introduction of iron oxide into a bath of molten iron containing a carbon reductant
- C21B13/002—Reduction of iron ores by passing through a heated column of carbon
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
- C21B13/143—Injection of partially reduced ore into a molten bath
-
- 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
- C21B2100/22—Increasing the gas reduction potential of recycled exhaust gases by reforming
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- 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
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- 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
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
- C21C2100/00—Exhaust gas
- C21C2100/06—Energy from waste gas used in other processes
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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
- Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- 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
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture Of Iron (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention relates to a method for producing molten material, wherein oxygen, reducing agents and iron that has been reduced in a reduction reactor (1) are introduced into a melter gasifier (3). The reducing agent is gasified with the oxygen and the heat thereby produced melts the reduced iron. The coupling gas from the melter gasifier (3) is used at least as a portion of the reduction gas, reacted top gas is withdrawn from the reduction reactor (1). The aim of the invention is to increase energy efficiency and raw material efficiency as well as productivity while at the same time obtaining metallurgically improved properties of the product. For this purpose, at least a portion of the top gas is branched off from the line (9) for the withdrawal of the top gas from the reduction reactor (1) and is returned via at least one return line (13, 18) leading to the melter gasifier (3) and is introduced into the melter gasifier (3).
Description
The present invention relates to a kind of method that is used to make molten metal, wherein with oxygen, reductive agent and in reduction reactor reductive iron be incorporated in the melting gasifier, reductive agent is gasified by oxygen, and the heat that utilizes produce this moment melts through reductive iron, wherein the cupola furnace gas (Kuppelgas) from melting gasifier is used as at least a portion reducing gas, wherein reacted furnace top gas is discharged from from reduction reactor, the invention still further relates to a kind of equipment that is used to implement described method, it has reduction reactor, have the melting gasifier and the reductive agent delivery system of curing by oxygen therapy mechanism, at least one pipeline is used for that cupola furnace gas is transported to reduction reactor at least one pipeline that neutralizes from melting gasifier and is used for discharging furnace top gas from reduction reactor.
With regard to blast furnace, with different carbonaceous gass, be blown into through the air port or on the furnace bosh plane as Sweet natural gas, coke-oven gas etc., so that save coke and improve economy, this point is record to some extent in GB 883 998 A for example.Because CO
2Content, N
2Higher and the H of content
2Content is lower, so spray into blast furnace gas and uneconomical.
With regard to melting and reducing equipment, for example in DE 36 28 102 A1, put down in writing, with temperature is that 25 ℃, the oxygen of purity 〉=95% (volume) are blown in the melting gasifier via nozzle, so that, and be provided for the essential heat of fusion through reductive iron with reductive agent (mainly being coal and briquet) gasification.The cupola furnace gas of melting gasifier (ESV) is used for carrying out indirect reduction at fixed bed reduction blast furnace stack (FBRS) or fluidized-bed reactor (WSR).Since in FBRS or WSR gas use not enough, so in output gas unit coal or briquet consumes higher and energy surplus is higher.
The operation of melting gasifier combined with reduction reactor, and to cause the metallized fluctuation ratio of sponge iron be 70-90%.For example, the coal tar bed tempertaure in the melting gasifier and the rising of cupola furnace temperature can cause needed oxygen amount to reduce, thereby but also can cause reducing gas to reduce.Because described minimizing, the degree of metallization in fixed bed reduction blast furnace stack or fluidized-bed reactor also reduces, and this causes coal tar bed tempertaure and cupola furnace decrease of temperature in the melting gasifier again.Yet this point can cause needing greater amount oxygen, thereby has increased the reducing gas scale of construction, and degree of metallization also increases.Therefore, because the regulation and control section is longer, melting gasifier can't steady operation (particularly decomposed by coal and cause), and the result is that the consumption rate of reductive agent is higher.
In addition, the adiabatic flame temperature (RAFT) that is produced when utilizing oxygen to make gasification was positioned at more than 3000 ℃ (in theory), helped SiO thus
2Be reduced into Si, so the pig iron can have high-load silicon.Therefore need additional aftertreatment usually, so that reach the Si content of desirable 0.4-0.5% (weight).
By depressing CO at 1.5 crust tables with following analysis component: CO of 45% (volume), 30% (volume) from the blast furnace gas of direct reduction unit with from the output gas of the purification of the cupola furnace gas composition of melting gasifier
2, 19% (volume) H
2, 3% (volume) H
2The N of O and 3% (volume)
2Because must being fed to, gas surplus, described output gas utilize mechanism and total energy to optimize mechanism.
Therefore, the objective of the invention is, propose wherein under the situation that improves energy efficiency and starting material efficient, can also boost productivity, wherein improve the metallurgy characteristic of product simultaneously as at the described a kind of method of the beginning part or a kind of equipment.
In order to realize described purpose, method of the present invention is characterised in that, the furnace top gas of at least a portion through discharging is sent in the melting gasifier.Can obviously save coal and briquet as the reductive agent in the melting gasifier thus, described coal and briquet are by supplying reduzate (CO, H from recycle gas
2) replaced.In addition, realize cooling to vortex cavity and coal tar bed by on purpose reducing flame temperature, described cooling produces owing to the thermo-negative reaction of coal, briquet or coke and gaseous fraction and the cracking of methane.
At the gas of this suitable compression through pump around circuit.
According to the another kind of favourable flexible program of described method, will preferably be cooled to 30 to 50 ℃ through the gas cooling of pump around circuit in compression with between being incorporated in the melting gasifier, and reduce carbon dioxide content, preferably be reduced to 2 to 3% (volumes).The advantage here is, increased the gas volume of the coal tar bed that is used for indirect gas reduction, promptly increased the reduction workload in melting gasifier.
According to another kind of flexible program, if at least a portion only is compressed through the gas of pump around circuit, at least another part only is cooled through the gas of pump around circuit, and minimizing carbon dioxide content, and before in being incorporated into melting gasifier the described compressed gas and the gas of carbonic acid gas minimizing are mixed, then can more accurately measure the performance of influence in melting gasifier.
Also can stipulate for this reason, in being incorporated into melting gasifier before with described pump around circuit and gas heating that reduce through refrigerative, carbonic acid gas in case of necessity, the shunting of preferably using pump around circuit gas is as combustion gases.By to the preheating of recycle gas, can make the gas volume maximum of backflow capable of circulation, and it is undesirable to below the disadvantageous lower limit of metallurgy to need not to make that adiabatic flame temperature (RAFT) drops to.Realize thus employed raw-material additional favourable reduction, and CONTROL PROCESS process additionally.
A kind of flexible program of the method according to this invention makes at least a portion pump around circuit gas communication cross higher hydrocarbon and uses another part pump around circuit gas stream to be transformed as combustion gases.
Before in being incorporated into melting gasifier, suit to make pump around circuit gas to mix with the gas of compression separately and/or with the gas of refrigerative and carbonic acid gas minimizing through transforming.
In addition according to a kind of advantageous method flexible program, the particle separation that in cupola furnace gas, carry together, and with its pump around circuit in melting gasifier, wherein a part separately the gas stream that reduces of the gas stream of compression and/or refrigerative and carbonic acid gas be mixed for carrying particle through pump around circuit.
According to a kind of method flexible program of the present invention, utilize amount and/or the temperature and/or the CO of pump around circuit gas
2Become to assign to be controlled at the theoretical adiabatic flame temperature in the vortex cavity, can on purpose control metallurgical process thus.
Adopt the combination of described various scheme and described scheme, can be controlled at the theoretical adiabatic flame temperature in the vortex cavity effectively.
In order to realize described purpose, according to the present invention, the described equipment of the beginning part is characterised in that at least one comes out and be passed into the return line of melting gasifier from the line branching that is used for furnace top gas.
In order to make the dangerous minimum of burning or blast, the gas backstreaming pipeline is parallel to the outlet that oxygen therapy mechanism extends to oxygen therapy mechanism in this case.
Suit in feedback pipe, to install compressor.
According to the present invention, a kind of favourable embodiment of described equipment is characterised in that, between compressor and oxygen therapy mechanism refrigerating unit and carbon dioxide reduction level (Reduktionsstufe) are installed, wherein the carbon dioxide reduction level can also reduce or eliminate vapour content fully.
Can stipulate that at this output terminal of the output terminal of compressor and carbon dioxide reduction level is passed in the common transfer line, this transfer line leads to the oxygen therapy mechanism of melting gasifier.
In order to make the gas volume maximum of backflow capable of circulation by preheating to recycle gas, and can not be unfavorable for metallurgy, after the place of converging of the output terminal of the output terminal of compressor and carbon dioxide reduction level, heating unit is set owing to adiabatic flame temperature (RAFT) reduces greatly.Additionally advantageously reduce the starting material consumption thus, and CONTROL PROCESS process additionally.
Utilize the inventive features of following favourable other, be heating unit combustion gases work, wherein before compressor, branch out branch road, and this branch road leads to the combustion gases joint of heating unit from return line, the starting material consumption can be reduced, and then plant efficiency can be further improved.
Can advantageously between compressor and oxygen therapy mechanism, convertor be installed.
Also can reduce raw-material consumption at this, its mode is according to a kind of favourable embodiment, branch out branch road from return line, and this branch road to lead to the combustion gases joint of convertor.
Another embodiment of equipment of the present invention is characterised in that, refrigerating unit and carbon dioxide reduction level both be set in the parallel legs of return line, transmodulator is set again, and described parallel legs is passed in the common transfer line, and this transfer line leads to the oxygen therapy mechanism of melting gasifier.
Preferably at least one pipeline that is used for cupola furnace gas particle separator is set, the particle re-circulation means is led to melting gasifier from the particle output mechanism of this particle separator, and one of them branch road is passed into the particle feedback mechanism from return line.
To contrast accompanying drawing by preferred embodiment below and describe the present invention in detail.
Blocky or globular iron ore are transported in the reduction blast furnace stack 1 together with unburned fusing assistant in case of necessity.The sponge iron that will be produced in reduction blast furnace stack 1 by dumping device 2 is transported in the head of melting gasifier 3.Gather the pig iron that liquid state is arranged in the bottom of melting gasifier 3, gathering on the pig iron has liquid slag, and these slags are preferably discharged off and on by the tapping mechanism of oneself respectively.Carry vaporized chemicals from standby blast furnace stack 4 to melting gasifier 3, preferred coal and/or briquet mix the iron ore undersize to be sifted out in case of necessity, this iron ore otherwise can not be used for reduction process.In the lower region of melting gasifier 3, carry the gas that contains aerobic by gas piping 5.
The reducing gas that is produced is removed solid-state component, particularly powdered and the granuliform coal that is outgased by the head output of pipeline 6 from melting gasifier 3 in hot gas cyclonic separator 7, enter into reduction blast furnace stack 1 by pipeline 8 then.In this reduction blast furnace stack 1, reducing gas is the column form object that is made of iron ore and fusing assistant of percolation upstream, and in this case reduction of iron ore is become sponge iron.
The coal dust of the isolating degassing and other granular contained material are transferred melt back and melt gasifier 3 in hot gas cyclonic separator 7, preferably the grey powder burner of the wall by being arranged on melting gasifier 3 is gasified when entering into this melting gasifier 3, and oxygen containing gas also is fed to described grey powder burner.
Reducing gas to small part consumption is output by furnace top gas pipeline 9 in the upper end of reduction blast furnace stack 1, is utilized mechanism and total energy to optimize mechanism as output gas owing to the gas surplus is fed to after the gas washing in wet scrubbing device 10.Be used for the pressure controlled reducing gas of equipment and after wet scrubbing device 11 is by gas washing or with output gas, mix, perhaps loop back in the pipeline 6 before hot gas cyclonic separator 7 as cooling gas by pipeline 12.
Particularly advantageously be, return in the technology itself,, and utilize exporting gas to the furnace top gas of at least a portion output or gas washing after promptly by recirculation and be input in the melting gasifier 3 by recirculation.For this reason, remaining the furnace top gas of pump around circuit is shunted by the compressor 14 with high as far as possible suction pressure via pipeline 13 after wet scrubbing device 10 and is compressed.Advantageously also can so that unwanted reducing gas after wet scrubbing device 11 via another pipeline 15 with just shunted and pump around circuit before output gas mixes.
According to first kind of flexible program, can be in water cooler 16 intercooling to 30-50 ℃ and be used to remove CO
2Equipment 17 in make CO
2Content is reduced to 2-3% (volume) afterwards, will be injected in the melting gasifier 3 by the jet pipe 18 that is passed in the oxygen jet through the furnace top gas of pump around circuit, and the return line that wherein is used for furnace top gas is parallel to the outlet that oxygen therapy mechanism extends to oxygen therapy mechanism.Part through this gas so handled can be shunted, and in order to carry from the particle of hot gas cyclonic separator 7 pump around circuits and by blending.Except because from furnace top gas supply such as the CO or the H of pump around circuit
2Reduzate and save outside the coal and briquet in the melting gasifier as reductive agent, can also be because the cracking of the thermo-negative reaction of coal, briquet or coke and gaseous fraction and methane realize cooling to vortex cavity and coal tar bed by on purpose reducing flame temperature, wherein following reaction plays a decisive role:
C+CO
2→2CO ΔH
298＝+173kJ/mol
C+H
2O→CO+H
2 ΔH
298＝+132kJ/mol
CH
4→2H
2+C ΔH
298＝+74kJ/mol
Owing to compressor 14 is installed and the CO that has preposition heat exchanger 16 is installed in case of necessity
2Remover 17 is perhaps installed convertor/reducing gas stove 21, also produces following advantage, promptly can realize higher melt capacity, and then boost productivity, and can also realize reducing the CO of unit of the pig iron per ton by the consumption that reduces reductive agent
2Quantity discharged can be looked the reductive agent cost that is used for coal, briquet, coke and realize reducing running cost, and then be reclaimed additional cost of investment apace.Also can consider when combusting coal fines, alternatively to use nitrogen.
Also can utilize the tangible heat of compression directly to introduce furnace top gas in case of necessity.In order for example to regulate and control CO according to coal tar bed tempertaure or cupola furnace temperature
2Content also can mix two air-flows.
The furnace top gas of pump around circuit also can be at CO
2Randomly be heated after removing by reducing gas stove 19 (convection type, heat accumulating type), electricradiator, plasma burner or heat exchanger (utilizing for example tangible heat of furnace top gas of gas wash tower process gas before) etc.Here the furnace top gas of when using reducing gas process furnace 19 part being shunted is used as combustion gases by pipeline 20.
When passing through the furnace top gas of heat exchanger heats pump around circuit before in being incorporated into melting gasifier 3, preferably utilize the heat energy of wet scrubbing device 10 furnace top gas before.Owing to the advantage of the energy efficiency of the less technology that is improved of needed process water amount for the cooling furnace top gas, this energy requirement that also means the process water pump reduces thus.In addition, the heat that is drained into the process water from furnace top gas reduces, and described heat is drained by cooling tower, perhaps causes that by evaporation the damage by water that must continue compensation in the system consumes.
Perhaps, the furnace top gas through pump around circuit also can be transformed the furnace top gas that wherein uses a part to import as combustion gases by pipeline 22 for the reaction heat that absorbs heat by higher hydrocarbon (for example Sweet natural gas) in convertor 21.
The reducing gas scale of construction from melting gasifier 3 that increases owing to the gas circulation backflow is used to increase production and/or is used for the constant metallization in reduction phase 1 (blast furnace stack or fluidized-bed).The constant metallization realizes by the decoupling zero of melting gasifier 3 with reduction blast furnace stack 1.The whenever all abundant reducing gas scale of construction allows the constant metallization in reduction blast furnace stack 1.Need not in order to satisfy thermal budget to change in large quantities the oxygen amount that remains to be flowed to melting gasifier 3 thus, this causes constant coal tar bed tempertaure, and less coal decomposes, and then causes melting gasifier 3 stably to be worked with the reductive agent consumption of a spot of unit.It is less that the optimization of melting gasifier work is caused being used for fixing bed reduction blast furnace stack 1 essential reduction dosage (FBRS) or in the fluidized-bed reactor (WSR) of equipment, and this pump around circuit by furnace top gas is compensated fully.
In addition,, can control apace thus, reduce the silicone content in the pig iron because the adiabatic flame temperature is low and melting gasifier is stably worked, so that farthest reduce the Si reduction that at high temperature carries out according to following formula:
SiO
2+2C→Si+2CO ΔH
298＝+690kJ/mol
Except silicone content, can also reduce the sulphur content in the pig iron, because because the furnace top gas of pump around circuit only has 1 to 100ppm H
2S is so than the situation of only using coal, briquet or coke, the sulphur of being introduced reduces widely.
At last, reflux, obviously be convenient to regulate needed jet velocity and be convenient to be adjusted in penetrating fully the vortex cavity under the lower situation of melt rate by gas circulation.
Claims (16)
1. be used to make the method for molten metal, wherein with oxygen, reductive agent and in reduction reactor (1) reductive iron be sent in the melting gasifier (3), described reductive agent is gasified by described oxygen, and the heat that utilizes produce this moment melts through reductive iron, wherein the cupola furnace gas from described melting gasifier (3) is used as at least a portion reducing gas, and wherein reacted furnace top gas is discharged from from described reduction reactor (1), the furnace top gas of at least a portion through discharging is sent in the described melting gasifier (3), and the gas of recirculated compressed, it is characterized in that, in compression and between being sent in the melting gasifier (3) with the gas cooling of recirculation, and the minimizing carbon dioxide content, and/or make at least a portion stream of recycled gases by higher hydrocarbon and use another part stream of recycled gases to be transformed as combustion gases.
2. the method for claim 1 is characterized in that, makes at least a portion only be compressed through the gas of recirculation, makes another part at least only be cooled and reduce its carbon dioxide content through the gas of recirculation; With in being sent to described melting gasifier (3) before the gas mixing that reduces of will be described compressed gas and carbonic acid gas.
3. as each described method in claim 1 and 2, it is characterized in that, with described recirculation and gas heating that reduce through refrigerative, carbonic acid gas in case of necessity, preferably used the part stream of recycled gases before in being sent to described melting gasifier (3) as combustion gases.
4. as each described method in the claim 1 to 3, it is characterized in that, in being sent to described melting gasifier (3) before, make through transforming recycle gas with only be compressed and/or the gas of cooling and carbonic acid gas minimizing mixes.
5. as each described method in the claim 1 to 4, it is characterized in that, the particle separation that in cupola furnace gas, carry together, and it is recycled in the described melting gasifier (3), mix wherein that a part only is compressed and/or gas stream that cooling and carbonic acid gas reduce, be used to carry particle through recirculation.
6. as each described method in the claim 1 to 5, it is characterized in that, utilize amount and/or the temperature and/or the CO of recycle gas
2Become the theoretical adiabatic flame temperature in the controlled vortex flow district that assigns to.
7. as each described method in the claim 1 to 6, it is characterized in that, in compression with will be between being sent in the described melting gasifier (3) through the gas cooling to 30 of recirculation to 50 ℃.
8. as each described method in the claim 1 to 7, it is characterized in that, carbon dioxide content is reduced to 2 to 3 volume %.
9. be used to make the equipment of molten metal, has reduction reactor (1), the melting gasifier (3) and the reductive agent delivery system (4) that have oxygen therapy mechanism (5), at least one is used for cupola furnace gas is transported to from described melting gasifier (3) pipeline (6 of described reduction reactor (1), 8) and at least one be used for discharging the pipeline (9) of furnace top gas from described reduction reactor (1), the return line (13 that is passed into described melting gasifier (3) that at least one goes out from the line branching that is used for described furnace top gas, 18), wherein at described return line (13, compressor (14) is installed 18), it is characterized in that, between described compressor (14) and oxygen therapy mechanism (5), refrigerating unit (16) and carbon dioxide reduction level (17) are installed; And/or between described compressor (14) and described oxygen therapy mechanism (5), convertor (21) is installed.
10. equipment as claimed in claim 9 is characterized in that, described gas backstreaming pipeline (13,18) is parallel to described oxygen therapy mechanism (5) and extends to described outlet of curing by oxygen therapy mechanism.
11. as each described equipment in claim 9 and 10, it is characterized in that, the output terminal of the output terminal of described compressor (14) and described carbon dioxide reduction level (17) is passed in the common transfer line (18), and this transfer line leads to the oxygen therapy mechanism (5) of described melting gasifier.
12. equipment as claimed in claim 11 is characterized in that, after the place of converging of the output terminal of the output terminal of described compressor (14) and described carbon dioxide reduction level (17) heating unit (19) is set.
13. equipment as claimed in claim 12, it is characterized in that, described heating unit (19) is worked with combustion gases, wherein before or after described compressor (14), branch out branch road (20), and this branch road leads to the combustion gases joint of described heating unit (19) from described return line (13).
14. equipment as claimed in claim 9 is characterized in that, branches out branch road (22) from described return line (13), and this branch road leads to the combustion gases joint of described convertor (21).
15. as claim 9 or 10 described equipment, it is characterized in that, refrigerating unit (16) and carbon dioxide reduction level (17) both be set in the parallel legs of described return line (13,18), transmodulator (21) is set again, described parallel legs is passed in the common transfer line (18), and this transfer line leads to the oxygen therapy mechanism (5) of described melting gasifier (3).
16. as each described equipment in the claim 9 to 15, it is characterized in that, at at least one pipeline (6) that is used for cupola furnace gas particle separator (7) is set, the particle re-circulation means feeds described melting gasifier (3) from the particle output mechanism of this particle separator, and one of them branch road is passed into the described particle re-circulation means from described recirculating line (18).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102006048601A DE102006048601A1 (en) | 2006-10-13 | 2006-10-13 | Method and device for producing molten material |
| DE102006048601.3 | 2006-10-13 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101528948A true CN101528948A (en) | 2009-09-09 |
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ID=38912104
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2007800376484A Pending CN101528948A (en) | 2006-10-13 | 2007-10-01 | Method and device for producing molten material |
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| Country | Link |
|---|---|
| US (1) | US20100024599A1 (en) |
| EP (1) | EP2082066A1 (en) |
| JP (1) | JP2010506046A (en) |
| KR (1) | KR20090068351A (en) |
| CN (1) | CN101528948A (en) |
| AR (1) | AR063265A1 (en) |
| AU (1) | AU2007312665A1 (en) |
| BR (1) | BRPI0719172A2 (en) |
| CA (1) | CA2665763A1 (en) |
| CL (1) | CL2007002941A1 (en) |
| DE (1) | DE102006048601A1 (en) |
| MX (1) | MX2009003725A (en) |
| RU (1) | RU2009117865A (en) |
| TW (1) | TW200827452A (en) |
| WO (1) | WO2008046503A1 (en) |
| ZA (1) | ZA200902093B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102586530A (en) * | 2012-01-04 | 2012-07-18 | 中冶南方工程技术有限公司 | Method for producing sponge iron by using coke-oven gas |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AT507823B1 (en) * | 2009-01-30 | 2011-01-15 | Siemens Vai Metals Tech Gmbh | METHOD AND APPARATUS FOR PRODUCING RAW IRONS OR LIQUID STEEL PREPARED PRODUCTS |
| AT507955B1 (en) | 2009-02-20 | 2011-02-15 | Siemens Vai Metals Tech Gmbh | METHOD AND APPARATUS FOR MANUFACTURING SUBSTITUTE GAS |
| CN110578029B (en) * | 2019-09-25 | 2020-11-10 | 山东大学 | Two-section type descending entrained flow iron-making system and iron-making process |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB883998A (en) * | 1958-04-01 | 1961-12-06 | Mckee & Co Arthur G | Method of operating blast furnaces |
| DE3438487A1 (en) * | 1984-10-17 | 1986-04-24 | Korf Engineering GmbH, 4000 Düsseldorf | METHOD FOR THE PRODUCTION OF RAW IRON |
| DE3504346C2 (en) * | 1985-02-06 | 1986-11-27 | Korf Engineering GmbH, 4000 Düsseldorf | Method and device for the production of sponge iron particles and liquid pig iron |
| US4685964A (en) * | 1985-10-03 | 1987-08-11 | Midrex International B.V. Rotterdam | Method and apparatus for producing molten iron using coal |
| DE3603894A1 (en) * | 1986-02-05 | 1987-08-06 | Korf Engineering Gmbh | METHOD FOR PRODUCING LIQUID PIPE IRON OR STEEL PRE-MATERIAL |
| US5958107A (en) * | 1993-12-15 | 1999-09-28 | Bechtel Croup, Inc. | Shift conversion for the preparation of reducing gas |
| US5582029A (en) * | 1995-10-04 | 1996-12-10 | Air Products And Chemicals, Inc. | Use of nitrogen from an air separation plant in carbon dioxide removal from a feed gas to a further process |
| AT406380B (en) * | 1996-03-05 | 2000-04-25 | Voest Alpine Ind Anlagen | METHOD FOR PRODUCING LIQUID GUT IRON OR LIQUID STEEL PRE-PRODUCTS AND SYSTEM FOR IMPLEMENTING THE METHOD |
| BRPI0414335B8 (en) * | 2003-12-05 | 2017-05-23 | Posco | cast iron fabrication method, integrated steel fabrication method, cast iron fabrication equipment and integrated steel mill |
-
2006
- 2006-10-13 DE DE102006048601A patent/DE102006048601A1/en not_active Withdrawn
-
2007
- 2007-10-01 ZA ZA200902093A patent/ZA200902093B/en unknown
- 2007-10-01 BR BRPI0719172-3A2A patent/BRPI0719172A2/en not_active IP Right Cessation
- 2007-10-01 EP EP07818594A patent/EP2082066A1/en not_active Withdrawn
- 2007-10-01 AU AU2007312665A patent/AU2007312665A1/en not_active Abandoned
- 2007-10-01 JP JP2009531734A patent/JP2010506046A/en active Pending
- 2007-10-01 CN CNA2007800376484A patent/CN101528948A/en active Pending
- 2007-10-01 RU RU2009117865/02A patent/RU2009117865A/en unknown
- 2007-10-01 CA CA002665763A patent/CA2665763A1/en not_active Abandoned
- 2007-10-01 WO PCT/EP2007/008514 patent/WO2008046503A1/en active Application Filing
- 2007-10-01 MX MX2009003725A patent/MX2009003725A/en unknown
- 2007-10-01 US US12/445,349 patent/US20100024599A1/en not_active Abandoned
- 2007-10-01 KR KR1020097008757A patent/KR20090068351A/en not_active Application Discontinuation
- 2007-10-03 TW TW096136997A patent/TW200827452A/en unknown
- 2007-10-12 AR ARP070104522A patent/AR063265A1/en unknown
- 2007-10-12 CL CL200702941A patent/CL2007002941A1/en unknown
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102586530A (en) * | 2012-01-04 | 2012-07-18 | 中冶南方工程技术有限公司 | Method for producing sponge iron by using coke-oven gas |
Also Published As
| Publication number | Publication date |
|---|---|
| US20100024599A1 (en) | 2010-02-04 |
| BRPI0719172A2 (en) | 2014-04-15 |
| AU2007312665A1 (en) | 2008-04-24 |
| AR063265A1 (en) | 2009-01-14 |
| KR20090068351A (en) | 2009-06-26 |
| RU2009117865A (en) | 2010-11-20 |
| ZA200902093B (en) | 2010-06-30 |
| EP2082066A1 (en) | 2009-07-29 |
| CA2665763A1 (en) | 2008-04-24 |
| WO2008046503A1 (en) | 2008-04-24 |
| MX2009003725A (en) | 2009-04-22 |
| JP2010506046A (en) | 2010-02-25 |
| TW200827452A (en) | 2008-07-01 |
| CL2007002941A1 (en) | 2008-05-30 |
| DE102006048601A1 (en) | 2008-04-17 |
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