CN101723812A - Method for preparing dimethyl ether by utilizing tail gas discharged by melting reduction ironmaking - Google Patents
Method for preparing dimethyl ether by utilizing tail gas discharged by melting reduction ironmaking Download PDFInfo
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- CN101723812A CN101723812A CN200910094926A CN200910094926A CN101723812A CN 101723812 A CN101723812 A CN 101723812A CN 200910094926 A CN200910094926 A CN 200910094926A CN 200910094926 A CN200910094926 A CN 200910094926A CN 101723812 A CN101723812 A CN 101723812A
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- 230000009467 reduction Effects 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 43
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 title claims abstract description 26
- 238000002844 melting Methods 0.000 title abstract description 9
- 230000008018 melting Effects 0.000 title abstract description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 71
- 239000007789 gas Substances 0.000 claims abstract description 56
- 238000006243 chemical reaction Methods 0.000 claims abstract description 52
- 238000006722 reduction reaction Methods 0.000 claims abstract description 51
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 48
- 229910052742 iron Inorganic materials 0.000 claims abstract description 34
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 19
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 14
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 14
- 239000003034 coal gas Substances 0.000 claims abstract description 13
- 239000001257 hydrogen Substances 0.000 claims abstract description 13
- 239000000463 material Substances 0.000 claims abstract description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000003054 catalyst Substances 0.000 claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 5
- 230000018044 dehydration Effects 0.000 claims abstract description 4
- 239000007787 solid Substances 0.000 claims abstract description 4
- 238000003723 Smelting Methods 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 13
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- 230000002194 synthesizing effect Effects 0.000 claims description 5
- 229910021536 Zeolite Inorganic materials 0.000 claims description 4
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 239000002808 molecular sieve Substances 0.000 claims description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 4
- 239000010457 zeolite Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000003607 modifier Substances 0.000 claims description 3
- 239000002994 raw material Substances 0.000 claims description 2
- 238000005272 metallurgy Methods 0.000 abstract description 3
- 239000002699 waste material Substances 0.000 abstract description 3
- 230000003749 cleanliness Effects 0.000 abstract 1
- 239000002131 composite material Substances 0.000 abstract 1
- 238000004134 energy conservation Methods 0.000 abstract 1
- 230000007613 environmental effect Effects 0.000 abstract 1
- 239000003245 coal Substances 0.000 description 18
- 230000008569 process Effects 0.000 description 15
- 238000004519 manufacturing process Methods 0.000 description 12
- 230000004927 fusion Effects 0.000 description 10
- 238000004939 coking Methods 0.000 description 8
- 238000001816 cooling Methods 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 229910000831 Steel Inorganic materials 0.000 description 6
- 239000010959 steel Substances 0.000 description 6
- 230000009466 transformation Effects 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 239000004566 building material Substances 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- 239000002893 slag Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000002283 diesel fuel Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000008188 pellet Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003818 cinder Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 238000010310 metallurgical process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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Abstract
The invention discloses a method for preparing dimethyl ether by utilizing tail gas discharged by melting reduction ironmaking, and relates to a method for directly preparing the dimethyl ether by utilizing coal gas output by the melting reduction ironmaking, which belongs to the technical field of metallurgy and energy. The method comprises the steps of: introducing hot coal gas which comes from a melting iron bath furnace into a pre-reduction shaft furnace, and ensuring that the hot coal gas is in countercurrent contact with an ironmaking material added from the top of the pre-reduction shaft furnace to perform a gas-solid reduction reaction; sending a reduced material into the melting iron bath furnace, and converting the unreacted coal gas in the pre-reduction shaft furnace into hydrogen-rich synthetic gas through a water gas shift reaction; and then adopting an one-step method from syngas to directly synthesize the dimethyl ether on a composite catalyst for methanol synthesis and methanol dehydration. The method has the characteristics of energy conservation, consumption reduction, cleanliness and environmental protection, and can avoid the generation of hot spots and three wastes during the reaction.
Description
Technical field
The present invention relates to a kind of method of utilizing fused reduction iron-smelting output coal gas directly to prepare dme, belong to metallurgy and energy technology field.
Background technology
China is a smelting iron and steel big country, but coking coal resource is less relatively, and the coking coal resource of China will face exhaustion later on by 2070, and traditional blast furnace iron-making process can't be produced normally.In contrast, a large amount of mill coal resources but can't be fully used in iron-smelting process, and therefore exploitation and employing mill coal iron-smelting process are imperative.Ironmaking technique of fusion and reduction directly uses non-coking coal, concentrate or lump ore production liquid iron, and it has omitted coking process and sintering circuit, has shortened technical process, has reduced cost, increases the production handiness, has improved molten steel quality.But the very valuable in a large number coal gas of attached product (mainly consists of CO, H in the production process
2And CO
2) need to handle.If it is not used, a large amount of energy will be wasted, and this will certainly have influence on the popularization and the utilization of ironmaking technique of fusion and reduction.
Therefore be necessary to develop and a kind of fused reduction iron-smelting exported the method that coal gas directly prepares dme, when adopting short flow process ironmaking technology, can not only improve efficiency of energy utilization, reduce environmental pollution, also can obtain the fine dimethyl ether liquid fuel, this will be an effective way of China's metallurgy industry Sustainable development and energy strategy development.
Summary of the invention
The purpose of this invention is to provide a kind of fused reduction iron-smelting discharging tail gas that utilizes and prepare the dme method, can reduce pollution significantly, help energy-saving and emission-reduction environment; Can break the thermodynamics equilibrium limit of methyl alcohol building-up reactions, the CO transformation efficiency is significantly improved than independent methyl alcohol building-up reactions in the indirect method; Have that flow process is short, equipment scale is little, working pressure is low and characteristics such as CO per pass conversion height, can make facility investment expense and process cost significantly reduce.
Solving the technical scheme that technical problem of the present invention adopts is: will introduce reduction shaft furnace from the heating gas in the molten iron bath stove, and with the ironmaking material counter current contact that the top of reduction shaft furnace adds, carry out the gas-solid reduction reaction; Reducing material is admitted to the molten pig liquid furnace, and the intact coal gas of the unreacted of reduction shaft furnace changes into hydrogen-rich synthetic gas through water gas shift reaction; With this hydrogen-rich synthetic gas (CO and H
2) be raw material, utilize one-step method from syngas, synthesizing methanol reaction and Dehydration of methanol are finished in a reactor, follow the transformationreation of CO simultaneously, directly dimethyl ether synthesis.Its reaction formula is:
2CO+4H
2＝2CH
3OH
CO+H
2O＝CO
2+H
2
2CH
3OH＝CH
3OCH
3+H
2O
Total reaction: 3CO+3H
2=CH
3OCH
3+ CO
2
Concrete processing method of the present invention is:
Fused reduction iron-smelting tail gas changes into hydrogen-rich synthetic gas behind purification, water gas shift reaction, should be again through modified, and CO in the modified gas and H
2Ratio be made into about 1: 1, enter the dme synthesis reactor again and react; The dual-function catalyst that the catalyzer of dme building-up reactions adopts SCTM-98 catalyzer and HZSM-5 zeolite molecular sieve to make, the air speed of reaction is 2400h
-1, reaction pressure 2.0～10.0Mpa, 230 ℃～280 ℃ of temperature of reaction, hydrogen-carbon ratio 3: 1.The principal feature of this method is the advantage of reacting, and synthesizing methanol reaction and Dehydration of methanol are finished in a reactor, and reaction equilibrium constant is big, has overcome the low weakness of synthesizing methanol reaction conversion ratio.
The present invention mainly separates purifying plant by fused reduction iron-smelting device (reduction shaft furnace and iron-bath molten reduction stove), tail gas separator, water-gas shift device, dme synthesizer and a cover liquid fuel and constitutes.
The present invention utilizes the high-temperature tail gas that discharges in the short flow process fused reduction iron-smelting production process, changes into hydrogen-rich synthetic gas through water gas shift reaction, and synthetic gas is used further to dimethyl ether synthesis.Dme is a kind of important clean energy and environmentfriendly products, and it has the cetane value close with diesel oil, and combustion processes can realize low NO and no sulphur emissions, can be used as the desirable alternative fuel of diesel oil, in order to the deficiency of alleviation China's oil liquefied gas and coal gas.Reach the purpose of energy-saving and cost-reducing and clean environment firendly, and avoided the generation of the reaction process focus and the three wastes again.
In ironmaking technique of fusion and reduction, compounds such as lump ore (pellet ore) or fine ore and Wingdale add the reduction shaft furnace top, and from the heating gas counter current contact in the molten pig liquid furnace, carry out the gas-solid reduction reaction, reducing material is admitted to the molten pig liquid furnace, carries out the reduction at end and separates with slag iron.Mill coal is sent in the molten pig liquid furnace by charging system and is gasified, and carries out gasification reaction with oxygen and less water.The coal gas that goes out iron liquid furnace enters shaft furnace and ore and carries out the prereduction reaction after dedusting.The intact coal gas of unreacted is emitted by shaft furnace, and molten hot metal in the molten pig liquid furnace and liquid slag are sent respectively from iron mouth and cinder notch.
Discharge tail gas in the fused reduction iron-smelting process changes into hydrogen-rich synthetic gas through water gas shift reaction, directly dimethyl ether synthesis.In reaction process, because reaction synergistic effect, methyl alcohol is once generation, carry out dehydration reaction and change into dme at once, broken through the thermodynamics equilibrium limit of simple methyl alcohol in synthetic, increased the reaction impellent, the water that generates in the reaction process can suppress against the current gas shift reaction again to be taken place, and makes height when the simple methyl alcohol of CO transformation efficiency is synthetic.
The Equilibrium limit of multistep in synthetic not only broken in this reaction, improved per pass conversion, and a large amount of reaction heat that produce in the reaction can have been removed the inactivation of having avoided synthetic catalyst to cause owing to overtemperature to a certain extent rapidly.Liquefying reactor can in time be removed reaction heat and keep reaction gas temperature and pressure owing to have good heat conductivity, inertia liquid phase carrier that thermal capacitance is big.
The present invention has the following advantages:
1. realize briquet replacing coke, solved the contradiction of Iron and Steel Production development, can effectively utilize conventional energy resources with the coking coal resource shortage.
Rich coal resources in China, but China's coking coal resource relative shortage only account for about 27% of coal reserves, and skewness, and Coal Transport poses a big pressure to traffic.The production of coke also will be subjected to the restriction of coal washing and coking equipment investment, therefore, adopts the melting and reducing technology, and producing molten iron with mill coal is the metallurgical process that suits Chinese resource situation.，
2. the comprehensive utilization of ironmaking technique of fusion and reduction output tail gas, can come the dme of the direct synthesis clean energy by the synthetic gas behind the water gas shift reaction, be a kind of Steel Production Flow Chart combined preparation clean fuel of cleaning, can reduce pollution significantly, help energy-saving and emission-reduction environment.
3. direct dimethyl ether synthesis process has been broken the thermodynamics equilibrium limit of methyl alcohol building-up reactions, and the CO transformation efficiency is significantly improved than independent methyl alcohol building-up reactions in the indirect method.
4. investment and production cost have been reduced, its flexible operation
This method has that flow process is short, equipment scale is little, working pressure is low and characteristics such as CO per pass conversion height, makes facility investment expense and process cost significantly reduce.Fused reduction iron-smelting has been cancelled coking, sintering circuit, and flow process shortens, and can save Iron and Steel Production capital construction and facility investment more than 15%～20%.
Description of drawings
Fig. 1 is a process flow diagram of the present invention.
Embodiment
Embodiment 1:
Certain annual production is the Steel Plant of 1,000,000 t, adopts ironmaking technique of fusion and reduction and will export the gas preparation dme.Iron ore is crushed to 1～10mm to add from reduction shaft furnace furnace roof material inlet, the coal and the solvent thorough mixing that are crushed to 1～10mm are evenly joined the molten iron bath reduction furnace from the furnace roof material inlet in the back, iron is bathed the reduction furnace fire box temperature and is maintained 1450 ℃～1650 ℃, the jetting pressure of oxygen maintains 0.2～1MPa, obtain the high-quality molten iron, deliver to steel making working procedure.1450 ℃～1650 ℃ the gas of exporting in the iron liquid furnace enters reduction shaft furnace from the bottom, with the iron ore counter current contact, and the pre-reduced iron ore.The tail gas that does not have to have reduced is exported in pre-reducing furnace, goes into the water-gas shift device through dedusting washing is laggard, and the output hydrogen-rich synthetic gas passes through modifier treatment again, makes CO and H in the modified gas
2Ratio be made into convergence 1: 1, directly enter liquid phase synthesizer synthesis of dimethyl ether with synthesis gas one-step then.The dual-function catalyst that the catalyzer of dme building-up reactions adopts SCTM-98 catalyzer and HZSM-5 zeolite molecular sieve to make, the air speed of reaction is 2400h
-1, reaction pressure 2.0～10.0Mpa, 230 ℃～280 ℃ of temperature of reaction, hydrogen-carbon ratio 3: 1.Melting slag is through the broken cooling of gasification cooling shredding unit, and temperature is reduced to 45 ℃, and the waste residue that cooling obtains after pulverizing send Building Materials Factory to produce building materials.This technology consumption coal 1,200,000 t can produce iron 1,000,000 t. dme 500,000 t (being equivalent to 450,000 t diesel oil).Bring considerable economic and social benefit thus, energy utilization rate improves nearly 1 times, and product energy consumption descends 60%, and ton steel cost descends 50%, SO
2Quantity discharged reduces by 99%, has obviously improved the pollution of traditional Iron industry to environment.
Embodiment 2:
Certain annual production is the Steel Plant of 2,000,000 t, adopts ironmaking technique of fusion and reduction and will export the gas preparation dme.The high phosphorus pellet is added from reduction shaft furnace furnace roof material inlet, to be crushed to 1～10mm flux and hard coal thorough mixing and evenly join the molten iron bath reduction furnace from the furnace roof material inlet in the back, iron is bathed reduction furnace injection oxygen enrichment dephosphorization, iron is bathed the reduction furnace fire box temperature and is maintained 1500 ℃～1750 ℃, the jetting pressure of oxygen maintains 0.1～0.8MPa, after obtain containing the high-quality molten iron of P≤0.015%, deliver to steelshop.1500 ℃～1750 ℃ gas of output enters reduction shaft furnace from the bottom in the iron liquid furnace, with the iron ore counter current contact, and the pre-reduced iron ore.The tail gas that does not have to have reduced is exported in pre-reducing furnace, is recovered used heat, dedusting cooling.The unstripped gas hydrogen-rich synthetic gas at first is compressed into high pressure (surpassing synthesis pressure, no longer pressurization before synthesizing) after entering dme factory, enter shift conversion step then.Bypass is set in the transformation system is used for the coal gas short circuit, with the H of control synthetic gas
2/ CO ratio leveled off to 1: 1, and transformation catalyst adopts sulfur resistant catalyst (as Co-Mo type catalyzer).Low-temperature rectisol RectisoI method is adopted in removing of sour gas, and substep removes H
2S and CO
2, to satisfy the requirement of synthetic catalyst, the air speed of catalyzed reaction is 2400h
-1, reaction pressure 2.0～10.0Mpa, 230 ℃～280 ℃ of temperature of reaction, hydrogen-carbon ratio 3: 1.The empty O that obtains that divides
2Deliver to melting and reducing iron and bathe the dephosphorization operation.Synthetic gas then directly enters liquid phase synthesizer dimethyl ether synthesis.N
2Then deliver to Rectisol method sour gas and remove operation.
Melting slag send Building Materials Factory to produce building materials after the broken cooling of gasification cooling shredding unit.
This technology consumption coal 2,500,000 t can produce iron 2,000,000 t, dme 1,000,000 t.Energy utilization rate improves nearly 1.5 times, and product energy consumption descends 70%, SO
2Quantity discharged reduces by 99%, has obviously improved the pollution of traditional Iron industry to environment.
Embodiment 3
Certain annual production is the Steel Plant of 5,000,000 t, adopts ironmaking technique of fusion and reduction and will export the gas preparation dme.To be crushed to 1～25mm iron ore adds from reduction shaft furnace furnace roof material inlet, to be crushed to 1～20mm bituminous coal and flux thorough mixing evenly adds from the fusion reducing furnace furnace roof back, the fusion reducing furnace fire box temperature maintains 1500 ℃～1750 ℃, and side-blown nitrogen injection pressure maintains 0.1～12Mpa; The high-quality molten iron that the fusion reducing furnace furnace bottom is discharged send steelshop, and the gas of furnace roof output enters the reduction shaft furnace bottom, with the iron ore counter current contact, and the pre-reduced iron ore.The tail gas that has not reduced (is rich in CO, H
2And CO
2) in pre-reducing furnace, export, through waste heat recovery, purification cooling, become hydrogen-rich synthetic gas after the separation.Send into shift conversion step after the pressurization of this hydrogen-rich synthetic gas,, control the H of synthetic gas well through modifier treatment
2/ CO ratio is approximately 1: 1, the dual-function catalyst that adopts SCTM-98 catalyzer and HZSM-5 zeolite molecular sieve to make, and the air speed of reaction is 2400h
-1, reaction pressure 2.0～10.0Mpa, 230 ℃～280 ℃ of temperature of reaction, hydrogen-carbon ratio 3: 1, directly dimethyl ether synthesis.
This technology consumption coal 6,500,000 t can produce iron 5,000,000 t. dme 2,000,000 t.Energy utilization rate improves nearly 1.7 times, and product energy consumption descends 74%, SO
2Quantity discharged reduces by 99%, has obviously improved the pollution of traditional Iron industry to environment.
Claims (2)
1. method of utilizing fused reduction iron-smelting discharging tail gas to prepare dme is characterized in that: will introduce reduction shaft furnace from the heating gas in the molten iron bath stove, and with the ironmaking material counter current contact that the top of reduction shaft furnace adds, carry out the gas-solid reduction reaction; Reducing material is admitted to the molten pig liquid furnace, and the intact coal gas of the unreacted of reduction shaft furnace changes into hydrogen-rich synthetic gas through water gas shift reaction; Mainly contain CO and H with this
2Hydrogen-rich synthetic gas be raw material, with one-step method from syngas synthesizing methanol reaction and Dehydration of methanol are finished in a reactor, follow the transformationreation of CO simultaneously, direct dimethyl ether synthesis.
2. the method for utilizing fused reduction iron-smelting discharging tail gas to prepare dme according to claim 1, it is characterized in that: described hydrogen-rich synthetic gas should pass through modifier treatment, makes CO and H in the modified gas
2Ratio be made into convergence and enter the dme synthesis reactor after 1: 1 again and react; The dual-function catalyst that the catalyzer of dme building-up reactions adopts SCTM-98 catalyzer and HZSM-5 zeolite molecular sieve to make, the air speed of reaction is 2400h
-1, reaction pressure 2.0～10.0Mpa, 230 ℃～280 ℃ of temperature of reaction, hydrogen-carbon ratio 3: 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910094926A CN101723812A (en) | 2009-09-03 | 2009-09-03 | Method for preparing dimethyl ether by utilizing tail gas discharged by melting reduction ironmaking |
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|---|---|---|---|
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102864265A (en) * | 2012-09-24 | 2013-01-09 | 中南大学 | Method for recycling gas-base direct reducted tail gas |
| CN104477841A (en) * | 2014-11-17 | 2015-04-01 | 武汉钢铁(集团)公司 | Method using high phosphorous ore reduction exhaust gas to make methanol |
| CN105218326A (en) * | 2014-06-28 | 2016-01-06 | 孙立 | A kind of method of dimethyl ether synthesis |
-
2009
- 2009-09-03 CN CN200910094926A patent/CN101723812A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102864265A (en) * | 2012-09-24 | 2013-01-09 | 中南大学 | Method for recycling gas-base direct reducted tail gas |
| CN102864265B (en) * | 2012-09-24 | 2014-05-28 | 中南大学 | Method for recycling gas-base direct reducted tail gas |
| CN105218326A (en) * | 2014-06-28 | 2016-01-06 | 孙立 | A kind of method of dimethyl ether synthesis |
| CN104477841A (en) * | 2014-11-17 | 2015-04-01 | 武汉钢铁(集团)公司 | Method using high phosphorous ore reduction exhaust gas to make methanol |
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Application publication date: 20100609 |