CN107151720A - A kind of Lurgi gasifying gas converts the system and method for producing DRI through steam - Google Patents
A kind of Lurgi gasifying gas converts the system and method for producing DRI through steam Download PDFInfo
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- 238000004519 manufacturing process Methods 0.000 title abstract description 38
- 238000006243 chemical reaction Methods 0.000 claims abstract description 134
- 239000003245 coal Substances 0.000 claims abstract description 81
- 239000003034 coal gas Substances 0.000 claims abstract description 72
- 238000002309 gasification Methods 0.000 claims abstract description 65
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 57
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 57
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 56
- 230000009467 reduction Effects 0.000 claims abstract description 56
- 230000009466 transformation Effects 0.000 claims abstract description 53
- 238000000034 method Methods 0.000 claims abstract description 45
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 44
- 230000023556 desulfurization Effects 0.000 claims abstract description 44
- 238000005261 decarburization Methods 0.000 claims abstract description 38
- 238000005406 washing Methods 0.000 claims abstract description 28
- 239000008188 pellet Substances 0.000 claims abstract description 14
- 239000000463 material Substances 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims description 275
- 238000006722 reduction reaction Methods 0.000 claims description 59
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 49
- 229910052799 carbon Inorganic materials 0.000 claims description 49
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 40
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 35
- 239000005864 Sulphur Substances 0.000 claims description 24
- 238000002485 combustion reaction Methods 0.000 claims description 21
- 238000000629 steam reforming Methods 0.000 claims description 20
- 239000000446 fuel Substances 0.000 claims description 18
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 16
- 239000001301 oxygen Substances 0.000 claims description 16
- 229910052760 oxygen Inorganic materials 0.000 claims description 16
- 238000011084 recovery Methods 0.000 claims description 13
- 230000006835 compression Effects 0.000 claims description 12
- 238000007906 compression Methods 0.000 claims description 12
- 239000000779 smoke Substances 0.000 claims description 12
- 229910052717 sulfur Inorganic materials 0.000 claims description 12
- 239000011593 sulfur Substances 0.000 claims description 12
- 239000002918 waste heat Substances 0.000 claims description 11
- 230000008859 change Effects 0.000 claims description 9
- 238000003672 processing method Methods 0.000 claims description 8
- 239000002994 raw material Substances 0.000 claims description 8
- 239000003054 catalyst Substances 0.000 claims description 7
- 239000000428 dust Substances 0.000 claims description 5
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 4
- 238000002347 injection Methods 0.000 claims description 3
- 239000007924 injection Substances 0.000 claims description 3
- 238000005201 scrubbing Methods 0.000 claims description 3
- 238000010025 steaming Methods 0.000 claims description 3
- 238000005516 engineering process Methods 0.000 abstract description 31
- 229910052742 iron Inorganic materials 0.000 abstract description 22
- 238000000746 purification Methods 0.000 abstract description 11
- 239000002184 metal Substances 0.000 abstract description 8
- 229910052751 metal Inorganic materials 0.000 abstract description 8
- 238000002407 reforming Methods 0.000 abstract description 4
- 230000010354 integration Effects 0.000 abstract description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 17
- 239000003077 lignite Substances 0.000 description 15
- 239000000203 mixture Substances 0.000 description 11
- 238000012545 processing Methods 0.000 description 11
- 230000008569 process Effects 0.000 description 10
- 238000010438 heat treatment Methods 0.000 description 9
- 239000003345 natural gas Substances 0.000 description 8
- 239000000047 product Substances 0.000 description 6
- 238000005262 decarbonization Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 3
- 239000003830 anthracite Substances 0.000 description 3
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- 239000004480 active ingredient Substances 0.000 description 2
- 238000005255 carburizing Methods 0.000 description 2
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- 238000004939 coking Methods 0.000 description 2
- 238000007323 disproportionation reaction Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
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- 230000002349 favourable effect Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
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- 238000000227 grinding Methods 0.000 description 1
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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
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0073—Selection or treatment of the reducing gases
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Industrial Gases (AREA)
Abstract
The system and method for producing DRI is converted through steam the invention provides a kind of Lurgi gasifying gas, the system includes the Lurgi coal gasification units being sequentially connected, dedusting washing unit, hydrosphere transformation unit, desulfurization and decarburization unit, the gentle base reduction unit of conversion unit.In the present invention, the coal gas produced by Lurgi gasification furnaces is converted by hydrosphere transformation, desulfurization and decarburization, in reburner, is obtained high temperature and high reduction degree synthesis gas, is passed through in gas-based reduction shaft furnace and pellet is reduced, obtain reducing metal iron.The present invention with fixed bed pressured gasification stove with hydrosphere transformation unit, conversion unit and gas-based reduction shaft furnace by being combined, the effective integration of Coal Gasification Technology, gas reforming technology, gas purification technology and reduction shaft furnace technology can be realized, and there is provided the system and method that a kind of coal gas with more high material and energy utilization rate produces DRI.
Description
Technical field
The invention belongs to DRI production technical field, it is related to a kind of Lurgi gasifying gas and converts production through steam
The system and method for DRI, more particularly to a kind of coal gas produced with Lurgi coal gasifiers and HyL-III gas base are also
Former shaft furnace combines the system and its processing method of production DRI.
Background technology
DRI (DRI) refers to the process of reduction of iron ore under less than fusion temperature into sponge iron.With biography
System blast furnace iron-making method is compared, and eliminates the process such as coking and sintering, with flow is short, pollution is small, consume less and not by excellent
The advantages of matter coking coal shortage influence；Meanwhile, the objectionable impurities content such as sulphur, phosphorus and silicon is low in DRI, is conducive to electric furnace
Smelt the pure steel grade of high-quality.
The research of gas-based shaft kiln technology since the Midrex technologies in 1936, DRI technology development is existing more than 80 years
History.External commercialized Direct Reducing Iron Process has Midrex, HyL and PERED etc..The production of external DRI is main
Using natural gas and the pellet of Iron concentrate preparation as raw material, based on natural gas DRI technology master reduction of iron ore in shaft furnace
Produce DRI.
China is the deficient country of natural gas resource, from the yield and Consumption forecast to Chinese current and following natural gas
From the point of view of analysis, using natural gas as gas base directly reducing iron process gas primary raw material, difficult more, cost is higher, from economy
Property consider almost without feasibility.In China, the cheap source of the gas that can substitute natural gas is found for DRI production, it is right
Capture gas base directly reducing iron technical barrier significant.
Based on the national conditions of the few gas of middle national wealth coal, coal chemical industry is with a long history in Chinese development, almost all coal system in the world
Gas technique has practice to attempt in China, coal gas technique relative maturity.It is used for using mill coal inferior production coal gas direct
Reduced iron, greatly reduces source of the gas cost, and be gas-based shaft kiln technology is applied offer opportunity in China.At present, coal gasification skill
Art is broadly divided into three kinds of fixed bed, fluid bed and air flow bed, wherein fixed bed be divided into atmospheric gasification (such as UGI stoves, the technology due to
It is seriously polluted to have tended to be superseded) and pressurized gasification (the Lurgi stoves of such as dry ash extraction and the BGL stoves of slag tap).
Table 1 lists the typical coal gas composition of Lurgi gasification technologies.Compared with fluid bed or air-flow bed technique, fixed bed
Condensation technique goes for particle size range 5mm~50mm lump coal, it is not necessary to complicated coal-grinding or coal preparation technology.
Table 1：Static bed coal gasification technique representative gases are constituted
US 4205830 and US 4225340 disclose the method and dress of a kind of utilization coal gas production DRI
Put, methods described is reacted coal, oxygen and water vapour in coal gasifier, also Primordial Qi is passed through shaft furnace, a top gas part
As fuel, a part of circularly removing CO2Reheat afterwards and be mixed into shaft furnace with coal gas.Lime is added in coal gasifier
(CaO) it is used to remove sulfide.CH in the gas componant that methods described is provided4Content is below 0.3%, it is clear that be not suitable for place
Manage the high CH that static bed coal gasification is produced4The coal gas of content (8% or so)；And CaO is added in coal gasification apparatus, it can not reach
To preferable desulfurized effect, it is difficult to meet gas emission request instantly.
CN 203034041U disclose a kind of utilization coal gasification gas and gas-based shaft kiln directly reduced metallurgical system,
Which show coal gasification, wash, the basic procedure of hydrosphere transformation, desulfurization and decarburization to reduction shaft furnace, but the patent is not provided
Implementation detail, is only worth with theoretical reference；And the patent does not consider the recycling of top gas after reduction, after reaction
Also a large amount of CO/H2Top gas it is clearly inappropriate directly as fume treatment.
CN 1141402C disclose the device that a kind of utilization water coal slurry pressure gasification produces sponge iron.The patent selects moral
Scholar's Gu stove, by gas conversion, NHD purifications, by being communicated to shaft furnace after two heating stove heats in parallel.This method can be applied
Reclaimed in high sulfur content coal, and to sulphur, but Texaco stove invests high relative to fixed bed coal gasifier, gasification pressure
Power is high；And directly by the way of the laggard shaft furnace of the heated stove heat of gas, easily occur CO gasification carburization reactions, damage boiler tube
Cause adverse consequences.
As can be seen here, coal resources, the development gas base directly reducing iron technology of China's abundant how are made full use of, in realization
The innovation and breakthrough of state's gas base directly reducing iron technology, select suitable Coal Gasification Technology, gas reforming technology, gas purification skill
Art and reduction shaft furnace technology, and the integrated of above-mentioned technology is urgent problem to be solved.
The content of the invention
Problem present in the method and system of DRI is produced for existing coal gas, the invention provides one kind
Lurgi gasifying gas converts the system and method for producing DRI through steam.The present invention is by with fixed bed pressured gasification
Stove (Lurgi coal gasifiers) is combined with hydrosphere transformation unit, conversion unit and gas-based reduction unit, it is possible to achieve coal gasification skill
Art, gas reforming technology, gas purification technology and reduction shaft furnace technology effective integration there is provided one kind have more high material and
The system and method that the coal gas of energy utilization rate produces DRI.
For up to this purpose, the present invention uses following technical scheme：
In a first aspect, the system for producing DRI is converted through steam the invention provides a kind of Lurgi gasifying gas,
The system include be sequentially connected Lurgi coal gasification units, dedusting washing unit, hydrosphere transformation unit, desulfurization and decarburization unit,
The gentle base reduction unit of conversion unit.
In the present invention, fixed bed pressured gasification stove (Lurgi coal gasifiers) is thrown compared with powder coal gasification furnace or water-coal slurry furnace
Provide relatively low, stable operation, it is not necessary to complicated standby coal measures system, less pollution；And in the raw gas of Lurgi coal gasifier outputs
CH4Content is higher, typically more than 8%, and the carbon content that iron product is reduced to increase in production DRI is favourable；And
And, by the conversion of subsequent transformation unit, the H in synthesis gas can be improved2With CO contents, so as to improve reduced iron yield.
Below as currently preferred technical scheme, but the limitation of the technical scheme provided not as the present invention, pass through
Following technical scheme, can preferably reach and realize the technical purpose and beneficial effect of the present invention.
As currently preferred technical scheme, the dedusting washing unit is scrubbing tower；The dedusting washing unit
Effect is to carry out dedusting and cooling to the raw gas that Lurgi coal gasifiers are synthesized, and is that the temperature of raw gas is down to hydrosphere transformation
The treatment temperature of unit, hydro-thermal conversion is carried out so as to follow-up.
Preferably, the hydrosphere transformation unit is hydrosphere transformation device.
In the present invention, hydrosphere transformation unit uses hydrosphere transformation technology, compared with con-ventional insulation is converted, by temperature
Accurate control avoids equipment overtemperature caused by exothermic heat of reaction, improves conversion efficiency, and one section can meet conversion and require, simplify
The equipment of converter unit.
The present invention adjusts the H in coal gas by hydrosphere transformation unit2/ CO mol ratios are to the production for meeting gas-based reduction unit
Index request.
Preferably, the hydrosphere transformation device is using one section of shifting thermal conversion.
Preferably, the transformation catalyst used in the hydrosphere transformation device is wide warm sulfur-resistant transformation catalyst, and it is used
Scope is 190 DEG C~500 DEG C, and the catalyst does not have upper limit requirement to sulfur content.
As currently preferred technical scheme, sulfide containing material and the sulphur recovery unit of the desulfurization and decarburization unit connect
Connect, the sulphur recovery unit is reclaimed using methods such as Claus methods to the sulphur in coal gas.
Preferably, pressure regulation unit is set between the desulfurization and decarburization unit and the conversion unit.The pressure regulation unit
Effect is to be down to the pressure of raw gas into the scope met needed for gas-based reduction cellular manufacture, and carries out energy regenerating simultaneously.
Preferably, the pressure regulation unit uses turbine, and the turbine is typical but non-limiting examples have：Steam turbine,
It is not limited to steam turbine.
Preferably, the fuel of the gas outlet of the pressure regulation unit and the unstripped gas entrance of conversion unit and conversion unit enters
Mouth is connected.The decompression coal gas after pressure regulation cell processing is divided into two parts, a part enters conversion unit as unstripped gas
Conversion reaction is carried out, another part is connected as fuel with the burner of conversion unit, the conduct in driving or unavailable top gas
Fuel supplies conversion unit.
As currently preferred technical scheme, the conversion unit is low steam carbon ratio steam reformer, its H2O and CH4's
Mol ratio is 1.1~1.5, such as 1.1,1.2,1.3,1.4 or 1.5, it is not limited to cited numerical value, the numerical value model
Other unrequited numerical value are equally applicable in enclosing.
In the present invention, the conversion unit using low steam carbon ratio steam reformer for common heating furnace, can reduce due to
The metal boiler tube dirtization that CO disproportionation carburizings are caused is damaged, and can extend the boiler tube life-span, it is more suitable for CH4The high coal gas of content；
Meanwhile, it turn avoid common steam and reform the synthesis gas oxidizability rise problem brought.
Preferably, the conversion unit includes water vapour injection device.
Preferably, the gas-based reduction unit is HyL-III shaft furnaces, and it is provided with pellet entrance, synthesis gas inlet, stove
Top gas is exported and reduced iron outlet.
As currently preferred technical scheme, the system also includes top gas wash mill and top gas compression dress
Put, the top gas outlet of the gas-based reduction unit is connected with the gas access of top gas wash mill, top gas wash mill
Gas vent be connected respectively with the gas access of top gas compression set and the fuel inlet of conversion unit, top gas compression dress
The gas vent put is connected with the gas access of hydrosphere transformation unit.
That is it is divided into two parts, a part of combustion as conversion unit after the top gas of gas-based reduction unit generation is scrubbed
Material, is mixed into hydrosphere transformation unit with coal gas after a part of compressed device compression, participates in reacting as unstripped gas.
The present invention, the top gas that gas-based reduction unit is produced is recycled, can be with the H in optimizing regulation raw gas2With
CO contents, improve the utilization ratio of raw material coal gas.
It is used as currently preferred technical scheme, combustion product gases outlet and the smoke heat exchanging system phase of the conversion unit
Even.
Preferably, the smoke heat exchanging system includes waste heat boiler and combustion air pre-heater, and combustion air pre-heater can
After waste heat boiler, the steam outlet of smoke heat exchanging system steam entry respectively with conversion unit, aqueous vapor
The steam entry and Lurgi coal gasifiers steam entry of converter unit are connected.I.e. by the combustion product gases of conversion unit
Heat reclaimed, with heating boiler aquatic products heat steam, for Lurgi coal gasifiers, hydrosphere transformation unit and conversion
Unit；Meanwhile, compressed air is heated, hot-air is provided for conversion unit.
Second aspect, the invention provides the processing method of said system, the described method comprises the following steps：
(1) feed coal carries out gasification reaction generation raw gas in Lurgi coal gasification units with oxygen and water vapour；
(2) step (1) the raw gas removing dust carries out water gas shift reaction, coal gas after being converted with after washing；
(3) coal gas after desulfurization and decarburization, carries out low steam carbon ratio steam conversion conversion reaction after step (2) described conversion, raw
Into synthesis gas；
(4) step (3) described synthesis gas enters the pellet counter current contacting with addition in gas-based reduction unit, is reduced
Reaction, generates reduced iron, and the reduced iron is sponge iron.
More specifically, methods described is：
(1) feed coal carries out gasification reaction generation raw gas in Lurgi coal gasifiers with oxygen and water vapour；
(2) step (1) described raw gas enters after dedusting washing unit removing dust and washing, enters into hydrosphere transformation unit
Row water gas shift reaction, coal gas after being converted；
(3) coal gas enters desulfurization and decarburization unit after desulfurization and decarburization after step (2) described conversion, is carried out into conversion unit
Low steam carbon ratio steam reforming reaction, generates synthesis gas；
(4) step (3) described synthesis gas enters the pellet counter current contacting with addition in gas-based reduction unit, is reduced
Reaction, generates reduced iron.
Wherein, step (1) the gasification reaction temperature is 1000 DEG C~1600 DEG C, and operating pressure is 1MPaG~3MPaG,
Gasification reaction generation raw gas temperature be 600 DEG C~700 DEG C, raw gas removing dust and washing after temperature be down to 200 DEG C~
350℃；The reaction temperature of step (2) described water gas shift reaction is 200 DEG C~300 DEG C, and reaction pressure is 1MPaG~3MPaG.
As currently preferred technical scheme, CO's mole contains in the raw gas of step (1) gasification reaction generation
Measure as 15%~25%, H2Molar content be 38%~41%, CH4Molar content be 7%~13%, CO2Molar content
For 25%~32%.
Preferably, H in coal gas after step (2) described hydrosphere transformation2It is 7~8 with CO mol ratios.Due to follow-up low steam carbon ratio
Steam conversion can reduce synthesis gas H2/ CO ratios, hydrosphere transformation regulation H2The slightly above HyL-III shaft furnace productions requirement of/CO ratios, with
Just the synthesis gas H after change2/ CO ratios disclosure satisfy that shaft furnace production needs.
In the present invention, the water gas shift reaction is：CO+H2O→CO2+H2+Q；
As currently preferred technical scheme, coal gas is after desulfurization and decarburization after step (3) described conversion, total sulfur content ＜
1mg/m3, CO2Molar content ＜ 1%.
Preferably, coal gas after desulfurization and decarburization, then after pressure regulation, carries out low steam carbon ratio steaming after step (3) described conversion
Vapour conversion reaction.
Preferably, the pressure regulation is regulation pressure to 0.5MPaG~0.8MPaG, and the pressure is to meet gas-based reduction list
The production requirement of member.
Preferably, the coal gas after the adjusted pressure is divided into two parts, and a part participates in low steam carbon ratio as unstripped gas
Steam reforming reaction, another part as low steam carbon ratio steam reforming reaction fuel.
Preferably, H in step (3) the low steam carbon ratio steam reforming reaction2O and CH4Mol ratio 1.1~1.5, for example
1.1st, 1.2,1.3,1.4 or 1.5 etc., it is not limited to other unrequited numerical value in cited numerical value, the number range
It is equally applicable.
In the present invention, by low steam carbon ratio steam reforming reaction, the H in synthesis gas is adjusted2With CO mol ratio, thus H2O
With CH4Mol ratio be the present invention influence reaction result one of key factor.
Preferably, H in step (3) described synthesis gas2With CO total moles content ＞ 90%, such as 91%, 92%,
93%th, 94% or 95% etc., it is not limited to other unrequited numerical value are equally fitted in cited numerical value, the number range
With.
Preferably, H in step (3) described synthesis gas2Be 5.6~6.5, such as 5.6 with CO mol ratio, 5.7,5.8,
5.9th, 6,6.1,6.2,6.3,6.4 or 6.5 etc., it is not limited to other are unrequited in cited numerical value, the number range
Numerical value it is equally applicable.
Preferably, step (3) the synthesis gas temperature be 850 DEG C~1000 DEG C, such as 850 DEG C, 870 DEG C, 900 DEG C, 930
DEG C, 950 DEG C, 970 DEG C or 1000 DEG C etc., it is not limited to other unrequited numbers in cited numerical value, the number range
Value is equally applicable.Preferably, the pressure of step (3) described synthesis gas be 0.5MPaG~0.8MPaG, such as 0.5MPa,
0.55MPa, 0.6MPa, 0.65MPa, 0.7MPa, 0.75MPa or 0.8MPa etc., it is not limited to cited numerical value, the number
Other unrequited numerical value are equally applicable in the range of value.
As currently preferred technical scheme, the burning cigarette that step (3) the low steam carbon ratio steam reforming reaction is produced
Gas is exchanged heat as thermal source with the waste heat boiler and combustion air pre-heater in smoke heat exchanging system, the heated production of waste heat boiler
Raw water vapour, which is returned, participates in gasification reaction, water gas shift reaction and low steam carbon ratio steam reforming reaction, combustion air pre-heater
The preheated air of preheated generation participates in top gas combustion heat supplying.
Preferably, it is divided into two parts after the top gas of step (4) the reduction reaction generation is scrubbed, it is a part of compressed
Afterwards as reaction raw materials return participate in water gas shift reaction, another part as low steam carbon ratio steam reforming reaction fuel recovery
Its heat.
Compared with prior art, the invention has the advantages that：
(1) fixed bed pressured gasification stove (Lurgi coal gasifiers) is used in the present invention, with coal gasification or coal water slurry gasification
Stove is compared to relatively low, the stable operation of investment, it is not necessary to complicated standby coal measures system, less pollution；
(2) hydrosphere transformation uses hydrosphere transformation technology in the present invention, avoids reaction by the accurate control to temperature and puts
Thermally-induced equipment overtemperature, improves conversion efficiency, and one section can meet conversion and require, the equipment for simplifying converter unit；
(3) common heating furnace is substituted with low steam carbon ratio reburner in the present invention, can reduced because CO disproportionation carburizings are caused
Metal boiler tube dirtization damage, the boiler tube life-span can be extended；Meanwhile, it turn avoid common steam and reform the synthesis gas oxidizability brought
Rise problem；
(4) in the present invention by the way of furnace roof gas washing Posterior circle participates in reaction, improve raw material coal gas utilizes effect
Rate, waste heat boiler and combustion air pre-heater are set to reburner, have reclaimed obvious heat of smoke, byproduct steam be available for coal gasifier and
Reburner is used, and improves material and efficiency of energy utilization；
(5) in the present invention, using Lurgi coal gasifier combinations Coal Gasification Technology, gas reforming technology, gas purification technology
Gentle base reduction unit technology, can overcome the limitation of natural gas in gas base directly reducing method, improve production DRI
Yield, production cost can be reduced.
Brief description of the drawings
Fig. 1 is the knot that Lurgi gasifying gas described in the embodiment of the present invention 1 converts the system for producing DRI through steam
Structure schematic diagram；
Wherein, 1-Lurgi coal gasification units, 2- dedusting washing units, 3- hydrosphere transformation units, 4- desulfurization and decarburization units,
5- pressure regulation units, 6- conversion units, 7- gas-based reduction units, 8- top gas wash mills, 9- top gas compression sets, 10- cigarettes
Gas heat-exchange system, 11- sulphur recovery units.
Embodiment
For the present invention is better described, technical scheme is readily appreciated, below to the present invention further specifically
It is bright.But following embodiments is only the simple example of the present invention, the scope of the present invention is not represented or limits, this
Invention protection domain is defined by claims.
Specific embodiment of the invention mode part provides a kind of Lurgi gasifying gas through steam conversion production direct-reduction
The system and its processing method of iron, the system include the Lurgi coal gasification units 1, dedusting washing unit 2, water being sequentially connected
The gentle base reduction unit 7 of gas converter unit 3, desulfurization and decarburization unit 4, conversion unit 6.
Its processing method comprises the following steps：
(1) feed coal carries out gasification reaction generation raw gas in Lurgi coal gasification units 1 with oxygen and water vapour；
(2) step (1) the raw gas removing dust carries out water gas shift reaction, coal gas after being converted with after washing；
(3) coal gas after desulfurization and decarburization, carries out low steam carbon ratio steam reforming reaction after step (2) described conversion, and generation is closed
Into gas；
(4) step (3) described synthesis gas enters the pellet counter current contacting with addition in gas-based reduction unit 7, is gone back
Original reaction, generates reduced iron.
It is below present invention typical case but non-limiting example：
Embodiment 1：
Present embodiments provide a kind of Lurgi gasifying gas and system and its processing for producing DRI are converted through steam
Method, as shown in figure 1, the system includes the Lurgi coal gasification units 1, dedusting washing unit 2, hydrosphere transformation being sequentially connected
The gentle base reduction unit 7 of unit 3, desulfurization and decarburization unit 4, pressure regulation unit 5, conversion unit 6；It also includes top gas wash mill
8 and top gas compression set 9.
Wherein, the Lurgi coal gasification units 1 are provided with lump coal feeding device, steam inlet and oxygen intake；
Dedusting washing unit 2 is scrubbing tower；
Hydrosphere transformation unit 3 is hydrosphere transformation device, and it uses one section of shifting thermal conversion, and its transformation catalyst used is width
Warm sulfur-resistant transformation catalyst, it is 190 DEG C~500 DEG C using scope；
The sulfide containing material of desulfurization and decarburization unit 4 is connected with sulphur recovery unit 11；
Pressure regulation unit 5 uses turbine, its gas outlet and the combustion of the unstripped gas entrance and conversion unit 6 of conversion unit 6
Expect that entrance is connected；
Conversion unit 6 is low steam carbon ratio steam reformer, and it includes water vapour injection device；The burning cigarette of conversion unit 6
Gas outlet is connected with smoke heat exchanging system 10；Smoke heat exchanging system 10 includes waste heat boiler and combustion air pre-heater, and flue gas is changed
The steam outlet of hot systems 10 steam entry respectively with conversion unit 6, the steam entry of hydrosphere transformation unit 3 and
The steam entry of Lurgi coal gasification units 1 is connected.
Gas-based reduction unit 7 be HyL-III shaft furnaces, its provided with pellet entrance, synthesis gas inlet, top gas outlet and
Reduced iron is exported.
The top gas outlet of gas-based reduction unit 7 is connected with the gas access of top gas wash mill 8, furnace roof gas washing dress
The gas vent for putting 8 is connected with the gas access of top gas compression set 9 and the fuel inlet of conversion unit 6 respectively, top gas
The gas vent of compression set 9 is connected with the gas access of hydrosphere transformation unit 3.
Exemplified by producing 1,000,000 tons/year of DRIs, the method handled using said system includes following step
Suddenly：
(1) lignite 63t/h is thrown in Lurgi coal gasification units 1, to Lurgi coal gasification units 1 feed 79t/h steam and
11381Nm3/ h oxygen, lignite carries out gasification reaction generation raw gas with oxygen and water vapour in coal gasifier, raw gas
Yield is 106266Nm3/h；
(2) step (1) described raw gas, which enters, carries out dedusting and washing in dedusting washing unit 2, and is cooled to 250 DEG C,
Subsequently into hydrosphere transformation unit 3, under conditions of 250 DEG C and 2MPaG, 20191Nm is passed through3/ h water vapours carry out aqueous vapor change
Change, and adjust H2It is 7.4, coal gas 126456Nm after being converted with CO mol ratios3/h；
(3) coal gas enters the progress desulfurization and decarburization processing of desulfurization and decarburization unit 4 after step (2) described conversion, makes total sulfur content
It is down to 1mg/m3Hereinafter, CO and is removed completely2, the sulphur of removing enters the Clausius equlity sulphur of sulphur recovery unit 11, to sulphur
The lignite of content 2%, year 1.3 ten thousand tons of sulphur recovery amount；
Coal gas after desulfurization and decarburization is 77362Nm3/ h, it, will after the regulation pressure of pressure regulation unit 5 to 0.6MPaG
Wherein 12378Nm3/ h coal gas makees fuel, is that conversion unit 6 provides heat energy, and by synthesis gas from low-temperature heat to 950 DEG C,
Remaining coal gas 64984Nm3/ h enters conversion unit 6 and carries out low steam carbon ratio steam conversion, by CH in synthesis gas4It is converted into H2
And CO, water vapour and CH4Mol ratio 1.1, generates 83000Nm3/ h synthesis gas, wherein H2It is 5.7, H with CO mol ratios2+ CO moles
Content 92%, meets HyL-III production targets；
(4) step (3) synthesis gas enters from the middle part of gas-based reduction unit 7, with being added from the top of gas-based reduction unit 7
188t/h pellet counter current contactings, carry out reduction reaction, generate reducing metal iron, the DRI of gas-based reduction unit 7 life
Production speed is 125t/h；
The top gas part circulation of gas-based reduction unit 7 participates in low steam carbon ratio steam as reaction raw materials and converted, it is to avoid
Coal gas primary first-order equation in gas-based reduction unit 7 is unable to reach the material waste of higher conversion generation；A part of conduct
Fuel is reaction heat supply, and combustion product gases enter as thermal source with the waste heat boiler and combustion air pre-heater in smoke heat exchanging system 10
Row heat exchange, the water vapour of the heated generation of waste heat boiler, which is returned, participates in coal gasification reaction, water gas shift reaction and low steam carbon ratio steaming
Vapour conversion reaction, the air preheated through combustion air pre-heater participates in combustion reaction.
In the present embodiment, raw gas that each stage of reaction is produced, coal gas after coal gas, desulfurization decarbonization purification after hydrosphere transformation
And the temperature of low steam carbon ratio steam reforming reaction synthesis gas, pressure and gas composition example are as shown in table 2.
Table 2：Lurgi static bed coal gasification techniques representative gases are constituted
The CO+H in coal gas composition after desulfurization and decarburization2Content only accounts for 86.5%, and after low steam carbon ratio is converted, synthesis
Active ingredient CO+H in gas2Up to 92.3%.
Compared with only with common heating furnace, purified gas is changed by low steam carbon ratio steam, improves CH4Utilize
Rate, adds synthesis gas reduction degree；Pass through CH4With H2O reaction generations CO+H2, effective gas output increased 36.4%, can increase also
Former iron yield 45.5t/h.
Produce 1,000,000 tons/year of DRIs day and throw about 1526 tons of lignite amount, 1 day 1800 tons of coal feeding amount Lurgi gas
Demand can be met by changing stove, and it is standby to open one using one during actual production.
Embodiment 2：
Present embodiments provide a kind of Lurgi gasifying gas and system and its processing for producing DRI are converted through steam
Method, the system architecture is in the same manner as in Example 1.
Exemplified by producing 300,000 tons/year of DRIs, the method handled using said system is comprised the following steps：
(1) anthracite 14t/h is put into Lurgi coal gasification units 1, feeding 27t/h to Lurgi coal gasification units 1 steams
Vapour and 6025Nm3/ h oxygen, anthracite carries out gasification reaction generation raw gas, rough coal with oxygen and water vapour in coal gasifier
The yield of gas is 31880Nm3/h；
(2) step (1) described raw gas, which enters, carries out dedusting and washing in dedusting washing unit 2, and is cooled to 250 DEG C,
Subsequently into hydrosphere transformation unit 3, under conditions of 250 DEG C and 2MPaG, 6057Nm is passed through3/ h water vapours carry out hydrosphere transformation,
And adjust H2It is 7.4, coal gas 37937Nm after being converted with CO mol ratios3/h；
(3) coal gas enters the progress desulfurization and decarburization processing of desulfurization and decarburization unit 4 after step (2) described conversion, makes total sulfur content
It is down to 1mg/m3Hereinafter, CO and is removed completely2；
Coal gas after desulfurization and decarburization is 23208Nm3/ h, it adjusts pressure to 0.6MPaG through pressure regulation unit 5, by it
Middle 3713Nm3/ h coal gas makees fuel, is that conversion unit 6 provides heat energy, and by synthesis gas from low-temperature heat to 950 DEG C, its
Remaining coal gas 19495Nm3/ h enters conversion unit 6 and carries out low steam carbon ratio steam reforming reaction, by CH in synthesis gas4It is converted into
H2And CO, water vapour and CH4Mol ratio 1.1, generates 24900Nm3/ h synthesis gas, wherein H2It is 5.7, H with CO mol ratios2+ CO rubs
That content 92%, meets HyL-III production targets；
(4) step (3) synthesis gas enters from the middle part of gas-based reduction unit 7, with being added from the top of gas-based reduction unit 7
56.4t/h pellet counter current contactings, carry out reduction reaction, generate reducing metal iron, the DRI of gas-based reduction unit 7 life
Production speed is 37.5t/h.
In the present embodiment, raw gas that each stage of reaction is produced, coal gas after coal gas, desulfurization decarbonization purification after hydrosphere transformation
And the temperature of low steam carbon ratio steam reforming reaction synthesis gas, pressure and gas composition example are in the same manner as in Example 1.
Compared with only with common heating furnace, purified gas is changed by low steam carbon ratio steam, improves CH4Utilize
Rate, adds synthesis gas reduction degree；Pass through CH4With H2O reaction generations CO+H2, effective gas output increased 36.4%, can increase also
Former iron yield 13.7t/h.
Produce 300,000 tons/year of DRIs day and throw about 336 tons of anthracite amount, 1 day 400 tons of coal feeding amount Lurgi gas
Demand can be met by changing stove, and it is standby to open one using one during actual production.
Embodiment 3：
Present embodiments provide a kind of Lurgi gasifying gas and system and its processing for producing DRI are converted through steam
Method, the system architecture is in the same manner as in Example 1.
Exemplified by producing 1,500,000 tons/year of DRIs, the method handled using said system includes following step
Suddenly：
(1) lignite 92t/h is thrown in Lurgi coal gasification units 1, to Lurgi coal gasification units 1 feed 113t/h steam and
16300Nm3/ h oxygen, lignite carries out gasification reaction generation raw gas with oxygen and water vapour in coal gasifier, raw gas
Yield is 152190Nm3/h；
(2) step (1) described raw gas, which enters, carries out dedusting and washing in dedusting washing unit 2, and is cooled to 250 DEG C,
Subsequently into hydrosphere transformation unit 3, under conditions of 250 DEG C and 2MPaG, 30286Nm is passed through3/ h water vapours carry out aqueous vapor change
Change, and adjust H2It is 8.0, coal gas 182476Nm after being converted with CO mol ratios3/h；
(3) coal gas enters the progress desulfurization and decarburization processing of desulfurization and decarburization unit 4 after step (2) described conversion, makes total sulfur content
It is down to 1mg/m3Hereinafter, CO and is removed completely2, the sulphur of removing enters the Clausius equlity sulphur of sulphur recovery unit 11, to sulphur
The lignite of content 2%, year 1.5 ten thousand tons of sulphur recovery amount；
Coal gas after desulfurization and decarburization is 110794Nm3/ h, it, will after the regulation pressure of pressure regulation unit 5 to 0.8MPaG
Wherein 19943Nm3/ h coal gas makees fuel, is that conversion unit 6 provides heat energy, and by synthesis gas from low-temperature heat to 1000
DEG C, remaining coal gas 90851Nm3/ h enters conversion unit 6 and carries out low steam carbon ratio steam conversion, by CH in synthesis gas4It is converted into
H2And CO, water vapour and CH4Mol ratio 1.5, generates 125000Nm3/ h synthesis gas, wherein H2It is 5.7, H with CO mol ratios2+ CO rubs
That content 92%, meets HyL-III production targets；
(4) step (3) synthesis gas enters from the middle part of gas-based reduction unit 7, with being added from the top of gas-based reduction unit 7
281t/h pellet counter current contactings, carry out reduction reaction, generate reducing metal iron, the DRI of gas-based reduction unit 7 life
Production speed is 187.5t/h；
In the present embodiment, raw gas that each stage of reaction is produced, coal gas after coal gas, desulfurization decarbonization purification after hydrosphere transformation
And the temperature of low steam carbon ratio steam reforming reaction synthesis gas, pressure and gas composition example are as shown in table 3.
Table 3：Each phase gas composition of embodiment 3
The CO+H in coal gas composition after desulfurization and decarburization2Content only accounts for 86.5%, and after low steam carbon ratio is converted, synthesis
Active ingredient CO+H in gas2Up to 92.1%.
Compared with only with common heating furnace, purified gas is changed by low steam carbon ratio steam, improves CH4Utilize
Rate, adds synthesis gas reduction degree；Pass through CH4With H2O reaction generations CO+H2, effective gas output increased 46.4%, can increase also
Former iron yield 87.1t/h.
Produce 1,500,000 tons/year of DRIs day and throw about 2190 tons of lignite amount, 2 day 1200 tons of coal feeding amount Lurgi gas
Demand can be met by changing stove, and it is standby to open one using two during actual production.
Embodiment 4：
Present embodiments provide a kind of Lurgi gasifying gas and system and its processing for producing DRI are converted through steam
Method, the system architecture is in the same manner as in Example 1.
Exemplified by producing 800,000 tons/year of DRIs, the method handled using said system is comprised the following steps：
(1) lignite 50t/h is thrown in Lurgi coal gasification units 1, to Lurgi coal gasification units 1 feed 62t/h steam and
9005Nm3/ h oxygen, lignite carries out gasification reaction generation raw gas, the production of raw gas with oxygen and water vapour in coal gasifier
Rate is 84081Nm3/h；
(2) step (1) described raw gas, which enters, carries out dedusting and washing in dedusting washing unit 2, and is cooled to 250 DEG C,
Subsequently into hydrosphere transformation unit 3, under conditions of 250 DEG C and 2MPaG, 16732Nm is passed through3/ h water vapours carry out aqueous vapor change
Change, and adjust H2It is 8.0, coal gas 100813Nm after being converted with CO mol ratios3/h；
(3) coal gas enters the progress desulfurization and decarburization processing of desulfurization and decarburization unit 4 after step (2) described conversion, makes total sulfur content
It is down to 1mg/m3Hereinafter, CO and is removed completely2, the sulphur of removing enters the Clausius equlity sulphur of sulphur recovery unit 11, to sulphur
The lignite of content 2%, year 0.8 ten thousand tons of sulphur recovery amount；
Coal gas after desulfurization and decarburization is 61211Nm3/ h, it, will after the regulation pressure of pressure regulation unit 5 to 0.5MPaG
Wherein 8570Nm3/ h coal gas makees fuel, is that conversion unit 6 provides heat energy, and by synthesis gas from low-temperature heat to 850 DEG C,
Remaining coal gas 52641Nm3/ h enters conversion unit 6 and carries out low steam carbon ratio steam conversion, by CH in synthesis gas4It is converted into H2
And CO, water vapour and CH4Mol ratio 1.1, generates 667000Nm3/ h synthesis gas, wherein H2It is 6.3, H with CO mol ratios2+ CO rubs
That content 90%, meets HyL-III production targets；
(4) step (3) synthesis gas enters from the middle part of gas-based reduction unit 7, with being added from the top of gas-based reduction unit 7
150t/h pellet counter current contactings, carry out reduction reaction, generate reducing metal iron, the DRI of gas-based reduction unit 7 life
Production speed is 100t/h；
In the present embodiment, raw gas that each stage of reaction is produced, coal gas after coal gas, desulfurization decarbonization purification after hydrosphere transformation
And the temperature of low steam carbon ratio steam reforming reaction synthesis gas, pressure and gas composition example are as shown in table 4.
Table 4：Each phase gas composition of embodiment 4
Produce 800,000 tons/year of DRIs day and throw about 1210 tons of lignite amount, 1 day 1400 tons of coal feeding amount Lurgi gas
Demand can be met by changing stove, and it is standby to open one using one during actual production.
Compared with only with common heating furnace, purified gas is changed by low steam carbon ratio steam, improves CH4Utilize
Rate, adds synthesis gas reduction degree, while reducing carbon distribution risk in stove, increases the boiler tube life-span；Pass through CH4With H2O reaction generations
CO+H2, effective gas output increased 31.7% can increase reduced iron yield 31.7t/h.
Embodiment 5：
Present embodiments provide a kind of Lurgi gasifying gas and system and its processing for producing DRI are converted through steam
Method, the system architecture is in the same manner as in Example 1.
Exemplified by producing 700,000 tons/year of DRIs, the method handled using said system is comprised the following steps：
(1) lignite 44t/h is thrown in Lurgi coal gasification units 1, to Lurgi coal gasification units 1 feed 54t/h steam and
7780Nm3/ h oxygen, lignite carries out gasification reaction generation raw gas, the production of raw gas with oxygen and water vapour in coal gasifier
Rate is 72646Nm3/h；
(2) step (1) described raw gas, which enters, carries out dedusting and washing in dedusting washing unit 2, and is cooled to 250 DEG C,
Subsequently into hydrosphere transformation unit 3, under conditions of 250 DEG C and 2MPaG, 13440Nm is passed through3/ h water vapours carry out aqueous vapor change
Change, and adjust H2It is 7.0, coal gas 86086Nm after being converted with CO mol ratios3/h；
(3) coal gas enters the progress desulfurization and decarburization processing of desulfurization and decarburization unit 4 after step (2) described conversion, makes total sulfur content
It is down to 1mg/m3Hereinafter, CO and is removed completely2；
Coal gas after desulfurization and decarburization is 52886Nm3/ h, it, will after the regulation pressure of pressure regulation unit 5 to 0.5MPaG
Wherein 8462Nm3/ h coal gas makees fuel, is that conversion unit 6 provides heat energy, and by synthesis gas from low-temperature heat to 900 DEG C,
Remaining coal gas 44424Nm3/ h enters conversion unit 6 and carries out low steam carbon ratio steam conversion, by CH in synthesis gas4It is converted into H2
And CO, water vapour and CH4Mol ratio 1.3, generates 58000Nm3/ h synthesis gas, wherein H2It is 5.7, H with CO mol ratios2+ CO moles
Content 90%, meets HyL-III production targets；
(4) step (3) synthesis gas enters from the middle part of gas-based reduction unit 7, with being added from the top of gas-based reduction unit 7
131t/h pellet counter current contactings, carry out reduction reaction, generate reducing metal iron, the DRI of gas-based reduction unit 7 life
Production speed is 87.5t/h；
In the present embodiment, raw gas that each stage of reaction is produced, coal gas after coal gas, desulfurization decarbonization purification after hydrosphere transformation
And the temperature of low steam carbon ratio steam reforming reaction synthesis gas, pressure and gas composition example are as shown in table 5.
Table 5：Each phase gas composition of embodiment 5
Produce 700,000 tons/year of DRIs day and throw about 1045 tons of lignite amount, 1 day 1200 tons of coal feeding amount Lurgi gas
Demand can be met by changing stove, and it is standby to open one using one during actual production.
Compared with only with common heating furnace, purified gas is changed by low steam carbon ratio steam, improves CH4Utilize
Rate, adds synthesis gas reduction degree, while reducing carbon distribution risk in stove, increases the boiler tube life-span；Pass through CH4With H2O reaction generations
CO+H2, effective gas output increased 35.7% can increase reduced iron yield 31.2t/h.
Summary embodiment can be seen that in the present invention, using BGL coal gasification combinations Coal Gasification Technology, hydrosphere transformation
The gentle base reduction technique of technology, gas purification technology, low steam carbon ratio steam-reforming techniques, can overcome in gas base directly reducing method
The limitation of natural gas, reduces production cost.
Applicant states that the present invention illustrates detailed process equipment and the technological process of the present invention by above-described embodiment,
But the invention is not limited in above-mentioned detailed process equipment and technological process, that is, do not mean that the present invention has to rely on above-mentioned detailed
Process equipment and technological process could be implemented.Person of ordinary skill in the field it will be clearly understood that any improvement in the present invention,
Addition, selection of concrete mode of equivalence replacement and auxiliary element to each raw material of product of the present invention etc., all fall within the present invention's
Within the scope of protection domain and disclosure.
Claims (10)
1. a kind of Lurgi gasifying gas converts the system for producing DRI through steam, it is characterised in that the system includes
The Lurgi coal gasification units (1) that are sequentially connected, dedusting washing unit (2), hydrosphere transformation unit (3), desulfurization and decarburization unit (4),
The gentle base reduction unit (7) of conversion unit (6).
2. system according to claim 1, it is characterised in that the dedusting washing unit (2) is scrubbing tower；
Preferably, the hydrosphere transformation unit (3) is hydrosphere transformation device；
Preferably, the hydrosphere transformation device is using one section of shifting thermal conversion；
Preferably, the transformation catalyst used in the hydrosphere transformation device is wide warm sulfur-resistant transformation catalyst, and it uses scope
For 190 DEG C~500 DEG C.
3. system according to claim 1 or 2, it is characterised in that the sulfide containing material and sulphur of the desulfurization and decarburization unit (4)
Sulphur recovery unit (11) is connected；
Preferably, pressure regulation unit (5) is set between the desulfurization and decarburization unit (4) and the conversion unit (6)；
Preferably, the pressure regulation unit (5) uses turbine；
Preferably, the gas outlet of the pressure regulation unit (5) and the unstripped gas entrance of conversion unit (6) and conversion unit (6)
Fuel inlet is connected.
4. the system according to claim any one of 1-3, it is characterised in that the conversion unit (6) is steamed for low steam carbon ratio
Vapour reburner, its H2O and CH4Mol ratio be 1.1~1.5；
Preferably, the conversion unit (6) includes water vapour injection device；
Preferably, the gas-based reduction unit (7) is HyL-III shaft furnaces, and it is provided with pellet entrance, synthesis gas inlet, stove
Top gas is exported and reduced iron outlet.
5. the system according to claim any one of 1-4, it is characterised in that the system also includes top gas wash mill
(8) and top gas compression set (9), the top gas outlet of the gas-based reduction unit (7) and the gas of top gas wash mill (8)
Body entrance is connected, the gas vent of top gas wash mill (8) gas access respectively with top gas compression set (9) and conversion
The fuel inlet of unit (6) is connected, the gas vent of top gas compression set (9) and the gas access of hydrosphere transformation unit (3)
It is connected.
6. the system according to claim any one of 1-5, it is characterised in that the combustion product gases of the conversion unit (6) go out
Mouth is connected with smoke heat exchanging system (10)；
Preferably, the smoke heat exchanging system (10) includes waste heat boiler and combustion air pre-heater, the smoke heat exchanging system
(10) steam outlet steam entry respectively with conversion unit (6), the steam entry of hydrosphere transformation unit (3) and
Lurgi coal gasification units (1) steam entry is connected.
7. the processing method of the system according to claim any one of 1-6, it is characterised in that methods described includes following step
Suddenly：
(1) feed coal carries out gasification reaction generation raw gas in Lurgi coal gasification units (1) with oxygen and water vapour；
(2) step (1) the raw gas removing dust carries out water gas shift reaction, coal gas after being converted with after washing；
(3) coal gas after desulfurization and decarburization, carries out low steam carbon ratio steam reforming reaction after step (2) described conversion, generates synthesis gas；
(4) step (3) described synthesis gas enters the pellet counter current contacting with addition in gas-based reduction unit (7), is reduced
Reaction, generates reduced iron.
8. processing method according to claim 7, it is characterised in that the raw gas of step (1) the gasification reaction generation
Middle CO molar content is 15%~25%, H2Molar content be 38%~41%, CH4Molar content be 7%~13%,
CO2Molar content be 25%~32%；
Preferably, H in coal gas after step (2) described hydrosphere transformation2It is 7~8 with CO mol ratios.
9. the processing method according to claim 7 or 8, it is characterised in that coal gas is de- through desulfurization after step (3) described conversion
After carbon, total sulfur content ＜ 1mg/m3, CO2Molar content ＜ 1%；
Preferably, coal gas after desulfurization and decarburization, then after pressure regulation, carries out low steam carbon ratio steam and turned after step (3) described conversion
Change reaction；
Preferably, the pressure regulation is regulation pressure to 0.5MPaG~0.8MPaG；
Preferably, the coal gas after the adjusted pressure is divided into two parts, and a part participates in low steam carbon ratio steam as unstripped gas
Conversion reaction, another part as low steam carbon ratio steam reforming reaction fuel；
Preferably, H in step (3) the low steam carbon ratio steam reforming reaction2O and CH4Mol ratio 1.1~1.5；
Preferably, H in step (3) described synthesis gas2With CO total moles content ＞ 90%；
Preferably, H in step (3) described synthesis gas2Mol ratio with CO is 5.6~6.5；
Preferably, step (3) the synthesis gas temperature is 850 DEG C~1000 DEG C；
Preferably, the pressure of step (3) described synthesis gas is 0.5MPaG~0.8MPaG.
10. the processing method according to claim any one of 7-9, it is characterised in that step (3) the low steam carbon ratio steam
The combustion product gases that conversion reaction is produced are used as the waste heat boiler and combustion air pre-heater in thermal source and smoke heat exchanging system (10)
Exchanged heat, the water vapour of the heated generation of waste heat boiler, which is returned, participates in gasification reaction, water gas shift reaction and low steam carbon ratio steaming
Vapour conversion reaction, the preheated air of the preheated generation of combustion air pre-heater participates in top gas combustion heat supplying；
Preferably, it is divided into two parts after the top gas of step (4) the reduction reaction generation is scrubbed, a part is made after compression
Returned for reaction raw materials and participate in water gas shift reaction, another part is used as its heat of the fuel recovery of low steam carbon ratio steam reforming reaction
Amount.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109825659A (en) * | 2019-04-08 | 2019-05-31 | 宁夏神耀科技有限责任公司 | A kind of technique and production system of gas-based shaft kiln production direct reduced iron |
| CN112358892A (en) * | 2020-10-19 | 2021-02-12 | 山西晋煤集团技术研究院有限责任公司 | Method for preparing reducing gas by using anthracite as gas-based direct reduced iron system |
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| CN112358892A (en) * | 2020-10-19 | 2021-02-12 | 山西晋煤集团技术研究院有限责任公司 | Method for preparing reducing gas by using anthracite as gas-based direct reduced iron system |
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