CN105129800B - A kind of oxygen/coal injection prepares the technique and system of calcium carbide and ethene - Google Patents
A kind of oxygen/coal injection prepares the technique and system of calcium carbide and ethene Download PDFInfo
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- CN105129800B CN105129800B CN201510431289.7A CN201510431289A CN105129800B CN 105129800 B CN105129800 B CN 105129800B CN 201510431289 A CN201510431289 A CN 201510431289A CN 105129800 B CN105129800 B CN 105129800B
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- calcium carbide
- acetylene
- oxygen
- hydrogen
- calcium
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- 239000005997 Calcium carbide Substances 0.000 title claims abstract description 98
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 title claims abstract description 98
- 238000000034 method Methods 0.000 title claims abstract description 48
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 45
- 239000001301 oxygen Substances 0.000 title claims abstract description 45
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 45
- 239000003245 coal Substances 0.000 title claims abstract description 42
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 32
- 238000002347 injection Methods 0.000 title claims abstract description 32
- 239000007924 injection Substances 0.000 title claims abstract description 32
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 claims abstract description 84
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 claims abstract description 84
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 45
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 34
- 238000006243 chemical reaction Methods 0.000 claims abstract description 34
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 34
- 239000001257 hydrogen Substances 0.000 claims abstract description 34
- 230000008569 process Effects 0.000 claims abstract description 27
- 238000003723 Smelting Methods 0.000 claims abstract description 26
- 239000002817 coal dust Substances 0.000 claims abstract description 21
- 238000004519 manufacturing process Methods 0.000 claims abstract description 17
- 238000000926 separation method Methods 0.000 claims abstract description 17
- 239000000571 coke Substances 0.000 claims abstract description 16
- 238000005261 decarburization Methods 0.000 claims abstract description 16
- 239000007789 gas Substances 0.000 claims description 42
- 239000000047 product Substances 0.000 claims description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 20
- 239000002893 slag Substances 0.000 claims description 17
- 239000005977 Ethylene Substances 0.000 claims description 16
- -1 calcium carbides Chemical class 0.000 claims description 13
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 12
- 239000011575 calcium Substances 0.000 claims description 11
- 229910052791 calcium Inorganic materials 0.000 claims description 11
- 238000001816 cooling Methods 0.000 claims description 11
- 239000003054 catalyst Substances 0.000 claims description 9
- XYFCBTPGUUZFHI-UHFFFAOYSA-N Phosphine Chemical compound P XYFCBTPGUUZFHI-UHFFFAOYSA-N 0.000 claims description 8
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 7
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 7
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 7
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 7
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 7
- 239000004571 lime Substances 0.000 claims description 7
- 238000000746 purification Methods 0.000 claims description 7
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 6
- 239000007795 chemical reaction product Substances 0.000 claims description 5
- 239000002253 acid Substances 0.000 claims description 4
- 230000009471 action Effects 0.000 claims description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 claims description 3
- 239000003513 alkali Substances 0.000 claims description 3
- 239000012752 auxiliary agent Substances 0.000 claims description 3
- 230000005540 biological transmission Effects 0.000 claims description 3
- 238000010304 firing Methods 0.000 claims description 3
- 239000003595 mist Substances 0.000 claims description 3
- 229910052763 palladium Inorganic materials 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 229910052707 ruthenium Inorganic materials 0.000 claims description 3
- 229910052709 silver Inorganic materials 0.000 claims description 3
- 239000004332 silver Substances 0.000 claims description 3
- 238000010792 warming Methods 0.000 claims description 3
- 238000005255 carburizing Methods 0.000 claims description 2
- 239000003153 chemical reaction reagent Substances 0.000 claims description 2
- 230000006835 compression Effects 0.000 claims description 2
- 238000007906 compression Methods 0.000 claims description 2
- 229910052593 corundum Inorganic materials 0.000 claims description 2
- 238000005272 metallurgy Methods 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 2
- 150000001345 alkine derivatives Chemical class 0.000 claims 1
- 238000009826 distribution Methods 0.000 abstract description 6
- 230000009467 reduction Effects 0.000 abstract description 6
- 238000002485 combustion reaction Methods 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- 150000002431 hydrogen Chemical class 0.000 abstract description 3
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- 230000000149 penetrating effect Effects 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 14
- 238000002360 preparation method Methods 0.000 description 13
- 239000007788 liquid Substances 0.000 description 12
- 229910052799 carbon Inorganic materials 0.000 description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 10
- 230000003647 oxidation Effects 0.000 description 9
- 238000007254 oxidation reaction Methods 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 230000005611 electricity Effects 0.000 description 8
- 239000002002 slurry Substances 0.000 description 8
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 7
- 238000009833 condensation Methods 0.000 description 7
- 230000005494 condensation Effects 0.000 description 7
- 238000001035 drying Methods 0.000 description 7
- 230000008676 import Effects 0.000 description 7
- 239000007791 liquid phase Substances 0.000 description 7
- 238000006722 reduction reaction Methods 0.000 description 7
- 229910052725 zinc Inorganic materials 0.000 description 7
- 239000011701 zinc Substances 0.000 description 7
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 6
- DSMZRNNAYQIMOM-UHFFFAOYSA-N iron molybdenum Chemical compound [Fe].[Fe].[Mo] DSMZRNNAYQIMOM-UHFFFAOYSA-N 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- LVTYICIALWPMFW-UHFFFAOYSA-N diisopropanolamine Chemical compound CC(O)CNCC(C)O LVTYICIALWPMFW-UHFFFAOYSA-N 0.000 description 5
- 229940043276 diisopropanolamine Drugs 0.000 description 5
- 239000003546 flue gas Substances 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 5
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 5
- 239000004575 stone Substances 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 239000003518 caustics Substances 0.000 description 4
- 238000005262 decarbonization Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000010891 electric arc Methods 0.000 description 4
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 4
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- RBFQJDQYXXHULB-UHFFFAOYSA-N arsane Chemical compound [AsH3] RBFQJDQYXXHULB-UHFFFAOYSA-N 0.000 description 3
- 229910000070 arsenic hydride Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- ZZVUWRFHKOJYTH-UHFFFAOYSA-N diphenhydramine Chemical compound C=1C=CC=CC=1C(OCCN(C)C)C1=CC=CC=C1 ZZVUWRFHKOJYTH-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 238000003780 insertion Methods 0.000 description 3
- 230000037431 insertion Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 239000000292 calcium oxide Substances 0.000 description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000002105 nanoparticle Substances 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 125000001741 organic sulfur group Chemical group 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 229910000073 phosphorus hydride Inorganic materials 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- BTBUEUYNUDRHOZ-UHFFFAOYSA-N Borate Chemical compound [O-]B([O-])[O-] BTBUEUYNUDRHOZ-UHFFFAOYSA-N 0.000 description 1
- 241001391944 Commicarpus scandens Species 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical group [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- DBMJMQXJHONAFJ-UHFFFAOYSA-M Sodium laurylsulphate Chemical compound [Na+].CCCCCCCCCCCCOS([O-])(=O)=O DBMJMQXJHONAFJ-UHFFFAOYSA-M 0.000 description 1
- 241001062472 Stokellia anisodon Species 0.000 description 1
- QZYDAIMOJUSSFT-UHFFFAOYSA-N [Co].[Ni].[Mo] Chemical compound [Co].[Ni].[Mo] QZYDAIMOJUSSFT-UHFFFAOYSA-N 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
Landscapes
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to the technique and system that a kind of oxygen/coal injection prepares calcium carbide and ethene.The technique comprises the following steps：(1) prepared by calcium carbide；(2) CO conversion, decarburization hydrogen manufacturing；(3) acetylene occurs；(4) acetylene hydrogenation reacts；(5) cryogenic separation.The present invention injecting oxygen and coal dust in calcium carbide smelting process, the unapproachable position of arc light is arrived because the heat of oxygen coal imperfect combustion generation is radiation-curable, and relatively conventional furnace of calcium carbide furnace heat distribution is more uniform, reduction furnace of calcium carbide power consumption and calcium carbide production cycle；The coal dust of penetrating can substitute part of coke, so as to reduce calcium carbide production cost；Meanwhile, the present invention also makes full use of the calcium carbide smelting exhaust rich in CO, and hydrogen, which is made, by CO transformationreations is used for the hydrogen source that acetylene hydrogenation reacts, and not only facilitates reduction environmental pollution, and can greatly improve economic benefit.
Description
Technical field
The present invention relates to the technique and system that a kind of oxygen/coal injection prepares calcium carbide and ethene, belong to technical field of coal chemical industry.
Background technology
Ethene is a kind of primary raw material of petro chemical industry, and current preparation technology is mainly the cracking alkene of naphtha
And coal-to-olefin.Domestic ethene aggregated capacity in 2015 is up to 22,000,000 t/a or so, and the year two thousand twenty country ethene production capacity further increases
It is added to 32,500,000 t/a, it is contemplated that to the domestic ethene consumption figure of the year two thousand twenty be 48,000,000 tons, demand is more than production capacity, and this is stored up for oil
Serious strategy threat is formd for standby not abundant China.Therefore, another new source and process system are sought
Standby large basic organic chemical raw material-ethene, substitutes oil as raw material in field of industrial production, can largely alleviate
Dependence of the China for oil.Coal olefin process mainly produces methanol, methanol-to-olefins by coal gasification preparing synthetic gas, synthesis gas
Composition.But the technology long flow path, complex process, investment are greatly, carbon emission amount is high, demand especially for water causes greatly
It can not be carried out in the region of water shortage.Present invention offer one kind prepares acetylene using carbide and then hydrogenation reaction obtains ethene, no
Coal-to-olefin process is same as, calcium carbide process of producing ethylene flow is short, it is low to invest small, carbon emission amount, especially selective hydrogenation of acetylene
Process does not need water to be reaction raw materials, and water is cooled down and temperature raising medium as reactor, can recycled respectively.And calcium carbide production master
There are arc process and the hot method of oxygen.The production of industry calcium carbide mainly uses arc process, but in calcium carbide preparation process, electric arc can not at present
It is applied to stove inner rim or subregion action effect is poor, cause furnace heat skewness, causes production power consumption high, raw material
Coke consumption is big, and calcium carbide cost remains high.
The content of the invention
Calcium carbide and ethylene process are prepared it is an object of the invention to provide a kind of oxygen/coal injection, by controlling coal oxygen ratio, is made
The two imperfect combustion release amount of heat under given conditions, promotes uniform heat distribution in furnace of calcium carbide, reduces power consumption, simultaneously
Also replace part semi-coke (coke) consumption, and hydrogen is made in gained CO, so as to reduce calcium carbide production cost, greatly improve economy
Benefit.
To achieve these goals, the present invention uses following scheme：
A kind of oxygen/coal injection prepares calcium carbide and ethylene process, comprises the following steps：
(1) prepared by calcium carbide
It will smelt, sprayed while the power transmission starting the arc into stove in the furnace of calcium carbide of coke and lime input with aerobic/coal injection rifle
Oxygen blast gas and coal dust, oxygen produce heat with coal dust firing, and when in-furnace temperature is up to 2000~2200 DEG C, coke and lime are in electricity
Reaction generation calcium carbide CaC under arc heat and burning heat effect2With calcium carbide smelting exhaust；
(2) CO conversion, decarburization hydrogen manufacturing
CO and steam generation CO transformationreations in the calcium carbide smelting exhaust of metallurgy generation, products therefrom through decarburization,
Refrigerated separation obtains hydrogen；
(3) acetylene occurs
Calcium carbide obtained by step (1) with water react obtaining acetylene and carbide slag, and acetylene is sent after cooling down, purifying, neutralize
To acetylene hydrogenation reaction process；
(4) acetylene hydrogenation reacts
In paste state bed reactor, hydrogen obtained by step (2) is with acetylene made from step (3) with volume ratio 3~10:1 mixes
Close, selective hydrogenation of acetylene reaction occurs under catalyst action；
(5) cryogenic separation
Acetylene hydrogenation reaction products therefrom is carried out by cryogenic separation using compression and depth cooling means and obtains product ethylene.
Present invention injecting mixed oxygen/coal in calcium carbide smelting process, because the heat that oxygen coal imperfect combustion is produced can spoke
The unapproachable position of arc light is mapped to, relatively conventional furnace of calcium carbide furnace heat distribution is more uniform, reduction furnace of calcium carbide power consumption and electricity
The stone production cycle；The coal dust of penetrating can substitute part of coke, so as to reduce calcium carbide production cost；Meanwhile, the present invention also fills
Divide using the calcium carbide smelting exhaust rich in CO, hydrogen, which is made, by CO transformationreations is used for the hydrogen source that acetylene hydrogenation reacts,
Reduction environmental pollution is not only facilitated, and economic benefit can be greatly improved.
It is described in jet coal, bottle coal, rich coal, coking coal, meager coal, lean coal in step (1) in technique of the present invention
One or more.
In technique of the present invention, in step (1), the coal dust intake is 130~200kg/t calcium carbides, the oxygen
Intake is 70~145Nm3/ t calcium carbides；With ton/m3Meter, the mass volume ratio of the coal dust and oxygen is 1:350-1000, preferably
For 1:500-750；The two under given conditions imperfect combustion discharge substantial amounts of heat, be delivered to many electric arcs of stove inner rim not
It can act on or the excessively poor place of action effect, so that the uniformity of calcium carbide furnace heat distribution is improved, reduction calcium carbide production
Power consumption；Moreover, with calcium oxide reduction reaction occurs for the part coal dust C sprayed into, semi-coke (coke) usage amount, reduction electricity can be reduced
Stone production cost, while producing a large amount of hydrogen conducts for being rich in CO flue gas, and will be enriched in the transformed reaction generation of CO flue gas
With carbide slag carbon geochemistry reaction, system occur for the hydrogen source of producing ethylene with acetylene hydrogenation, the CO2 that the transformed reaction of the flue gas rich in CO is produced
Into nano-calcium carbonate.
In technique of the present invention, in step (2), total sulfur is taken off to 0.02ppm in the calcium carbide smelting exhaust after purification；It is described
The solution of decarburization is selected from N methyldiethanol amine (MDEA), diisopropanolamine (DIPA) (DIPA), N methyldiethanol amine (MDEA) and second
The mixture of hydramine (MEA), add alkyl alcoholamine and borate solution of potassium carbonate, sulfolane and diisopropanolamine (DIPA) mixing
Thing；Carbon dioxide content is less than 10ppm in the hydrogen after decarburization.
As the preferred embodiment of the present invention, in step (2), the calcium carbide smelting exhaust is carrying out CO transformationreations
Before, its heat recovery first can be used for the heating of acetylene hydrogenation reactor.Particularly a gas is set in acetylene hydrogenation reaction
Liquid heat exchange unit, calcium carbide smelting exhaust is changed with the conduction oil in acetylene hydrogenation reactor chuck in gas-liquid heat exchange unit
Heat, the conduction oil after heat exchange is warming up to 140-220 DEG C, so as to make full use of the heat in calcium carbide smelting exhaust.
In the method for the invention, in step (3), the calcium carbide is crushed to granularity for 200~400mm, acetylene is sent into
Reacted in generator with water, the acetylene gas of generation removes hydrogen phosphide therein, hydrogen sulfide through cooling, purification, then through in alkali
With removal acid mist therein；Phosphine content is less than less than 0.1ppm, hydrogen sulfide content in acetylene gas after the purification
0.1ppm, arsenic hydride content are less than 80ppm less than the content of 0.1ppm and water.
In the method for the invention, in step (4), the catalyst uses particle diameter for 20~100 μm, and palladium is main activearm
Point, silver and ruthenium is auxiliary agent, alundum (Al2O3) is carrier catalyst；The hydrogenation conditions are：Reaction pressure be 0.2~
1.5MPa, reaction temperature is 140~220 DEG C.
In the method for the invention, in step (1), the calcium carbide preparation unit is electric arc furnace of calcium carbide, including body of heater, stove
Lid, charging aperture and calcium carbide furnace gas outlet；Wherein, the roof of the body of heater and/or wall insertion in side is branched can height up and down
Oxygen/coal injection rifle, the oxygen/coal injection rifle includes coal dust jet pipe and sprayed along circumferentially distributed multiple oxygen of the coal dust jet pipe
Pipe, the oxygen/coal injection rifle gun body is copper material, built-in snakelike cooling water pipe.Because the injection rifle is in the furnace of calcium carbide
Adjustable length, in smelting process, oxygen coal injection rifle bottom is placed in molten bath top, non-molten bath zone, can avoid fuel nozzle,
Oxygen spray pipe and calcium carbide draft tube fracture, and fuel injection process electrode base oxidation, reduce export license.
In order to make full use of the discarded object in preparation process, the CO that step (2) is produced2It is passed through the electricity that step (3) is obtained
Carburizing reagent is carried out in rock ballast and obtains calcium carbonate, then it is surface-modified, be dehydrated, be dried to obtain the fusoid of 50~100nm and receive
Rice calcium carbonate.
The present invention also provides and realizes the system that above-mentioned oxygen/coal mixed injection prepares calcium carbide and ethylene process, including connects successively
The calcium carbide preparation unit that connects, acetylene generating unit, acetylene hydrogenation reaction member, cryogenic separation unit；
Wherein, in addition to CO conversion decarburization Hydrogen Units, its air inlet and the calcium carbide smelting exhaust of calcium carbide preparation unit go out
Mouth pipeline connection, its hydrogen gas outlet is connected with acetylene hydrogenation reaction member pipeline.
In system of the present invention, the calcium carbide preparation unit is electric arc furnace of calcium carbide, including body of heater, bell, charging aperture
With calcium carbide furnace gas outlet, wherein, the insertion of the roof and/or side wall of the body of heater it is branched can height up and down oxygen/coal injection
Rifle, the oxygen/coal injection rifle includes coal dust jet pipe and circumferentially distributed multiple oxygen spray pipes along the coal dust jet pipe, described
Snakelike cooling water pipe is also arranged in oxygen/coal injection rifle.By setting injection rifle in calcium carbide furnace sidewall or furnace roof, existing electricity can be avoided
Stone stove electrode is easy to break, and electrode base is oxidizable during fuel injection, the big situation of export license.
In order to make full use of the discarded object in preparation process, system of the present invention also includes carbide slag carbonation unit, its
Respectively with the outlet of the carbide slag of acetylene generating unit and the CO of CO conversion decarburization Hydrogen Units2Outlet connection.
In system of the present invention, the CO conversion decarburizations Hydrogen Unit includes calcium carbide smelting exhaust purifier, CO and become
Changing device, decarbonization device；Wherein, the calcium carbide smelting exhaust purifier includes adsorption filter, the iron oxide being linked in sequence
Desulfurizer, centrifugal compressor, heating furnace, pre- iron molybdenum hydrogenation reactor, one-level iron molybdenum hydrogenation reactor, stair oxidation zinc desulfurization
Groove, nickel Co-Mo hydrogenation reactor and secondary oxidation zinc desulfurizer；The decarbonization device includes decarbonizing tower and regenerator, described two grades
Zinc oxide desulfurization groove is connected by pipeline and is provided with alkanolamine solution import at the top of the bottom of the decarbonizing tower, the decarbonizing tower, is taken off
Carbon tower bottom is provided with alkanolamine solution outlet, and the alkanolamine solution outlet connects regenerator by pipeline, and the hydramine of regenerator is molten
Liquid outlet is connected with the alkanolamine solution import of decarbonizing tower, the CO set at the top of regenerator2The connection carbide slag carbonization in outlet is single
Member.
In system of the present invention, the acetylene generating unit includes acetylene generator, peace and quiet tower, caustic neutralizer column and cold
Solidifying drying device；Wherein, acetylene generator bottom is provided with gas outlet, and it has been sequentially connected with peace and quiet tower, alkali by pipeline and neutralized
Tower, condensation drying device, the acetylene gas outlet of the condensation drying device connect ethene preparation unit by pipeline.It is preferred that
Provided with double-deck sieve plate in ground, the acetylene generator, the spacing of the lath of upper strata sieve plate is 300mm, the lath of lower floor's sieve plate
Spacing is 80mm.
In system of the present invention, the acetylene hydrogenation reaction member may be selected those skilled in the art and grasped in principle
Achievable effect of the present invention reactor；Preferred paste state bed reactor in the present invention；The paste state bed reactor is set
It is equipped with acetylene import, hydrogen inlet, product gas outlet；Wherein, the acetylene import of paste state bed reactor and acetylene generating unit
It is connected, hydrogen inlet and the hydrogen of paste state bed reactor merge pipeline and is connected, the product gas outlet and depth of paste state bed reactor
Cold separative element is connected.Wherein, the paste state bed reactor is top in the reactor for having chuck, reactor provided with gas-liquid point
It is located at from device, reactor bottom provided with gas distributor, finger-type heat exchange of heat pipe above gas distributor, condenser is between gas-liquid point
From between device and finger-type heat exchange of heat pipe.
In system of the present invention, the cryogenic separation unit includes flash distillation plant, dethanizer, the ethene being sequentially connected
Rectifying column, depropanizing tower, propylene rectification tower, debutanizing tower, anti-butylene rectifying column.
The present invention improves the uniformity of calcium carbide furnace heat distribution, drop in furnace of calcium carbide using oxygen/coal mixed injection mode
Low power consumption, semi-coke (coke) usage amount, produce a large amount of flue gases rich in CO, and will be enriched in the obtained hydrogen of the transformed reaction of CO flue gas
Gas is as the hydrogen source of producing ethylene with acetylene hydrogenation, the CO that transformationreation is produced2Occur carbon geochemistry reaction with carbide slag and nano-sized carbon is made
Sour calcium；Technique and system of the present invention have that flow is short, floor space is few, energy consumption is low, small investment and without CO2Discharge etc. is excellent
Ethene accounts for 75~85%, 1- butylene and accounts for 2~5% in point, the gaseous products of generation, and anti-butylene accounts for 15~20%, remaining be ethane,
Propylene and C5 +Deng accessory substance, gas is after cryogenic separation after reaction, and hydrogen is recycled.
Sum it up, oxygen of the present invention/coal injection acquisition calcium carbide and ethylene process can avoid other coal chemical industry processes
The carbon dioxide maximum discharge of presence and the problem of to water resource heavy dependence, is typical low-carbon, clean coal conversion process, to pushing away
The Green Sustainable of dynamic China's coal resource clean utilization and acetylene chemical industry, energy-saving and emission-reduction have great importance.
Brief description of the drawings
Fig. 1 oxygen of the present invention/coal injection prepares calcium carbide and ethylene process schematic flow sheet.
Fig. 2 oxygen of the present invention/coal injection prepares calcium carbide and ethylene system structural representation.
Embodiment
Following examples are used to illustrate the present invention, but are not limited to the scope of the present invention.
Embodiment 1
A kind of oxygen/coal injection prepares calcium carbide and ethylene process, as shown in figure 1, comprising the following steps：
(1) prepared by calcium carbide
The coke and lime of release mesh are transported to calcium carbide factory, enter furnace of calcium carbide through charger and furnace charge hopper
In, while the power transmission starting the arc using the injection rifle installed in calcium carbide furnace sidewall or furnace roof into stove injecting oxygen/coal dust intermixture,
Oxygen produces substantial amounts of heat with coal dust firing, wherein the straying quatity of the oxygen is 95Nm3/ t calcium carbides, anchracite duff is passed through
Measure as 130kg/t calcium carbides；When bath temperature is heated to 2000-2200 DEG C, coke and lime are in arc heat, resistance heat and reaction
Be reduced in the presence of heat in furnace of calcium carbide, be melted into calcium carbide, it is interior that calcium carbide flows into 1t pot bags by fire door, transport between pouring carry out it is cold
But, acetylene is delivered to afterwards occurs process；With lime reduction reaction generation calcium carbide occurs for the carbon in the coal dust of part simultaneously, reduces coke
Usage amount.
(2) CO conversion, decarburization hydrogen manufacturing
Purification：Calcium carbide smelting exhaust rich in CO first pass around helical-lobe compressor be compressed to after 0.8MPaG enter adsorbed
Filter, removes and enters the most of inorganic sulfur of iron oxide desulfurizer removing and part organic sulfur after the impurity such as naphthalene therein, tar, it
3.5MPaG is compressed into heating furnace, pre- iron molybdenum, one-level iron molybdenum hydrogenation reactor by centrifugal compressor afterwards, makes calcium carbide smelting
It is inorganic sulfur to refine most of organic sulfur conversion in tail gas, afterwards into stair oxidation zinc desulfurizer, removes hydrogen sulfide therein, most
Enter nickel cobalt molybdenum hydrogenation reactor and secondary oxidation zinc desulfurizer afterwards, the total sulfur in gas is taken off to 0.02ppm；
Calcium carbide smelting exhaust after purification, to 250 DEG C, is formed hydrogen through CO transformationreations and returned using steam preheating
Steam generation by reaction heat therein is received, gained hydrogen enters de- after removing the liquid dissociated and entrained solid impurity through separator
The bottom of carbon tower, with the alkanolamine solution counter current contacting flowed from top to bottom by tower top, removes acid gas composition therein, through outlet point
The solution droplets that may be carried in hydrogen are removed from device, goes out carbon dioxide content in decarbonizing tower hydrogen and is less than 10ppm, be sent to acetylene
The paste state bed reactor of hydrogenation reaction workshop section；The alkanolamine solution of decarburization tower bottom enters regenerator and regenerated, the hydramine after regeneration
Solution is used after heat exchange, cooling into decarbonizing tower interior circulation.
(3) acetylene occurs
The calcium carbide of generation is broken for 200~400mm of granularity feeding acetylene generators through calcium carbide crusher and reacted with water,
The spacing of lath provided with double-deck sieve plate upper sieve plate inside acetylene generator is 300mm, and grand calcium carbide and water in 300mm is anti-
Should, the spacing of the lath of lower floor's sieve plate is 80mm, and the grand calcium carbide in 80mm reacts with water, calcium carbide or powder meeting less than 80mm
Overflow in secondary generator secondary response again.The operating efficiency of acetylene generator is greatly improved by the structure sieve plate, electricity is improved
Stone utilization rate；In order that calcium carbide can be evenly distributed on sieve plate, umbrella distribution cone, increase electricity are set in the upper sieve plate of generator
The surface area of Shi Yushui contacts, to improve the operating efficiency of generator.Calcium carbide produces acetylene gas after hydrolysis is contacted with water, through pair hair
After efficient washing cooling tower washing on raw device, into positive water seal, and carbide slag is discharged, carbide slag discharges into slurry by generator
Stirring pool, plate and frame type filter-press extruding is extracted into by slush pump, makes to be used as life in slag, water separation, the current Huis pond after separation
Fisheries water；React hydrogen phosphide, hydrogen sulfide and the arsenic entered after the scrubbed cooling of acetylene gas of generation in peace and quiet tower removing acetylene gas
Change hydrogen, go out Phosphine content in the acetylene gas of peace and quiet tower and be less than 0.1ppm and arsenic hydride content less than 0.1ppm, hydrogen sulfide content
Less than 0.1ppm, the acid mist that removing hydrogen phosphide, hydrogen sulfide and arsenic hydride and acetylene gas enter in caustic neutralizer column removing acetylene gas takes off
Acetylene gas after acid-mist-removing removes the moisture in acetylene gas after supercharging and condensation, and the content of the acetylene gas reclaimed water after dehydration is less than
80ppm, sends into acetylene hydrogenation reaction process.
(4) acetylene hydrogenation reacts
Hydrogen obtained by step (2) is with acetylene made from step (3) with volume ratio 3~10:1 is mixed into acetylene hydrogenation reaction
The paste state bed reactor of process, carries out selective hydrogenation of acetylene reaction in the presence of catalyst, generates the products such as ethene；
Acetylene hydrogenation reaction process, which is used, carries chuck, gas distributor, finger-type heat exchange of heat pipe, condenser and gas-liquid separation
The slurry bed system of device is as reactor, and catalyst uses 20~100 μm of palladium to be auxiliary agent, three oxidations for main active component, silver and ruthenium
Two aluminium are the catalyst of carrier, and reaction pressure is 0.2~1.5MPa, and reaction temperature is 140~220 DEG C；Pass through in course of reaction
The flow of the cooling medium of dactylethrae in the circular flow and slurry bed system of conduction oil in chuck is controlled, the temperature control of reaction is existed
140~220 DEG C, the condenser on slurry bed system top condenses the liquid phase solvent of evaporation, and the liquid phase solvent of condensation is back to slurry bed system
Interior, the gas-liquid separator at the top of paste state bed reactor divides carried secretly in reaction product 99% liquid phase solvent and reaction product
From dropping back into slurry bed system, reaction product goes out paste state bed reactor from reactor head gas vent, into cryogenic separation process.
(5) cryogenic separation
The product of acetylene hydrogenation is compressed to 3.4~3.9MPa, then gas phase is cooled down and flashed step by step, be finally cooled to-
163~-169 DEG C, sub-argument goes out hydrogen in hydrogen gas tank, and the liquid phase of each flash tank is entered dethanizer, dethanizer gaseous products
Ethylene product is obtained into ethylene rectifying column, liquid-phase product enters depropanizing tower, and depropanizing tower gaseous products enter propylene rectifying
Tower obtains propylene product, and liquid-phase product enters debutanizing tower, and debutanizing tower gaseous products enter anti-butylene rectifying column, and tower top is obtained
Anti- butylene product, the C that liquid-phase product is and mixed5Deng product.
(6) carbide slag is carbonized
By step (3) produce carbide slag is scrubbed, scalping, remove filtering after mechanical admixture, dry be sized to 125 μm with
In 1050 DEG C of calcinings after lower, water is added after burnt carbide slag cooling, the mass ratio of water and calcium oxide is 20~40:1, obtain
To calcium hydroxide slurry, the CO of step (2) generation is passed through in aqua calcis afterwards2Progress is carbonized, and to obtain calcium carbonate molten
Liquid, calcium carbonate soln obtains the nano-sized carbon that particle diameter is 50~100nm after the modification of dodecyl sodium sulfate surface, dehydration, drying
Sour calcium.
It is computed, 2700kwh/t electricity is reduced to from existing 3100kwh/t calcium carbides using power consumption after mixed injection technique
Stone, production cost is reduced to 175 yuan/t calcium carbides, rich in CO exhaust gas volumns increase about 200Nm3/ t calcium carbides, total exhaust gas volumn about 600Nm3/
t。
Embodiment 2
The present embodiment prepares ethene using technique same as Example 1, and difference is, the calcium carbide smelting exhaust is entering
Before row CO transformationreations, its heat recovery can be first used for the heating of acetylene hydrogenation reactor.Particularly in acetylene hydrogenation
A gas-liquid heat exchange unit is set in reaction, by the conduction oil in calcium carbide smelting exhaust and acetylene hydrogenation reactor chuck in gas-liquid heat exchange
Exchanged heat in unit, the conduction oil after heat exchange is warming up to 140-220 DEG C, so as to make full use of the heat in calcium carbide smelting exhaust
Amount.
Embodiment 3
It is a kind of to realize the system that oxygen described in embodiment 1/coal mixed injection prepares calcium carbide and ethylene process, as shown in Fig. 2 bag
Include the calcium carbide preparation unit being sequentially connected, acetylene generating unit, acetylene hydrogenation reaction member, cryogenic separation unit；
Wherein, in addition to CO conversion decarburization Hydrogen Units, its air inlet and the calcium carbide smelting exhaust of calcium carbide preparation unit go out
Mouth pipeline connection, its hydrogen gas outlet is connected with acetylene hydrogenation reaction member pipeline.
Wherein, the calcium carbide preparation unit be electric arc furnace of calcium carbide, including body of heater, bell, charging aperture and calcium carbide furnace gas outlet,
Wherein, the roof of the body of heater and/or the insertion of side wall it is branched can height up and down oxygen/coal injection rifle, the oxygen/coal injection
Rifle includes going back cloth in coal dust jet pipe and circumferentially distributed multiple oxygen spray pipes along the coal dust jet pipe, the oxygen/coal injection rifle
Put snakelike cooling water pipe.
The system also includes carbide slag carbonation unit, and it is exported respectively with the carbide slag of acetylene generating unit and CO is converted
The CO of decarburization Hydrogen Unit2Outlet connection.Wherein, the CO conversion decarburizations Hydrogen Unit includes calcium carbide smelting exhaust purification dress
Put, CO converting means, decarbonization device；Wherein, the calcium carbide smelting exhaust purifier include be linked in sequence adsorption filter,
Iron oxide desulfurizer, centrifugal compressor, heating furnace, pre- iron molybdenum hydrogenation reactor, one-level iron molybdenum hydrogenation reactor, stair oxidation
Zinc desulfurizer, nickel Co-Mo hydrogenation reactor and secondary oxidation zinc desulfurizer；The decarbonization device includes decarbonizing tower and regenerator, institute
The bottom that secondary oxidation zinc desulfurizer connects the decarbonizing tower by pipeline is stated, the decarbonizing tower top is provided with alkanolamine solution and entered
Mouthful, decarburization tower bottom is provided with alkanolamine solution outlet, and the alkanolamine solution outlet connects regenerator, the alcohol of regenerator by pipeline
Amine aqueous solution outlet is connected with the alkanolamine solution import of decarbonizing tower, the CO set at the top of regenerator2The outlet connection carbide slag carbon
Change unit.
Wherein, the acetylene generating unit includes acetylene generator, peace and quiet tower, caustic neutralizer column and condensation drying device；
Wherein, acetylene generator bottom is provided with gas outlet, and it has been sequentially connected with peace and quiet tower, caustic neutralizer column, condensation drying by pipeline
Device, the acetylene gas outlet of the condensation drying device connects ethene preparation unit by pipeline.Preferably, the acetylene hair
Provided with double-deck sieve plate in raw device, the spacing of the lath of upper strata sieve plate is 300mm, and the spacing of the lath of lower floor's sieve plate is 80mm.
Wherein, this achievable hair that those skilled in the art are grasped may be selected in the acetylene hydrogenation reaction member in principle
The reactor of the bright effect；Preferred paste state bed reactor in the present invention；The paste state bed reactor be provided with acetylene import,
Hydrogen inlet, product gas outlet；Wherein, the acetylene import of paste state bed reactor is connected with acetylene generating unit, and slurry bed system is anti-
The hydrogen inlet and hydrogen for answering device merge pipeline and are connected, product gas outlet and the cryogenic separation unit phase of paste state bed reactor
Even.Wherein, the paste state bed reactor is that top in the reactor for having chuck, reactor is provided with gas-liquid separator, reactor
Bottom is located above gas distributor provided with gas distributor, finger-type heat exchange of heat pipe, and condenser is between gas-liquid separator and finger-type
Between heat exchange of heat pipe.
Wherein, the cryogenic separation unit includes the flash distillation plant being sequentially connected, dethanizer, ethylene rectifying column, de- third
Alkane tower, propylene rectification tower, debutanizing tower, anti-butylene rectifying column.
Although above the present invention is described in detail with a general description of the specific embodiments,
On the basis of the present invention, it can be made some modifications or improvements, this will be apparent to those skilled in the art.Cause
This, these modifications or improvements, belong to the scope of protection of present invention without departing from theon the basis of the spirit of the present invention.
Claims (6)
1. the technique that a kind of oxygen/coal injection prepares calcium carbide and ethene, it is characterised in that comprise the following steps：
(1) prepared by calcium carbide
It will be smelted in the furnace of calcium carbide of coke and lime input with aerobic/coal injection rifle, oxygen be blown into stove while the power transmission starting the arc
Gas and coal dust, oxygen produce heat with coal dust firing, and when in-furnace temperature is up to 2000~2200 DEG C, coke and lime are in arc heat
With reaction generation calcium carbide CaC under burning heat effect2With calcium carbide smelting exhaust；
Wherein, with ton/m3Meter, the mass volume ratio of the coal dust and oxygen is 1:350-1000；
(2) CO conversion, decarburization hydrogen manufacturing
CO and steam generation CO transformationreations in the calcium carbide smelting exhaust of metallurgy generation, products therefrom is through decarburization, cooling
Isolated hydrogen；
(3) acetylene occurs
Calcium carbide obtained by step (1) with water react obtaining acetylene and carbide slag, and acetylene delivers to second after cooling down, purifying, neutralize
Alkynes hydrogenation reaction process；
(4) acetylene hydrogenation reacts
In paste state bed reactor, hydrogen obtained by step (2) is with acetylene made from step (3) with volume ratio 3~10:1 mixing,
Selective hydrogenation of acetylene reaction occurs under catalyst action；
(5) cryogenic separation
Acetylene hydrogenation reaction products therefrom is carried out by cryogenic separation using compression and depth cooling means and obtains product ethylene.
2. technique according to claim 1, it is characterised in that in step (1), the coal dust intake is 130~
200kg/t calcium carbides, the oxygen intake is 70~145Nm3/ t calcium carbides.
3. technique according to claim 1, it is characterised in that in step (3), it is 200 that the calcium carbide is crushed into granularity
Reacted in~400mm, feeding acetylene generator with water, the acetylene gas of generation through cooling, purification removing hydrogen phosphide therein,
Hydrogen sulfide, then through in alkali and removing acid mist therein.
4. technique according to claim 1, it is characterised in that in step (4), the catalyst use particle diameter for 20~
100 μm, palladium is the catalyst that main active component, silver and ruthenium are auxiliary agent, alundum (Al2O3) is carrier；The condition of the hydrogenation reaction
For：0.2~1.5MPa of reaction pressure, 140~220 DEG C of reaction temperature.
5. technique according to claim 1, it is characterised in that in step (2), the calcium carbide smelting exhaust is carrying out CO
Before transformationreation, first pass through pipeline and exchanged heat with the conduction oil in acetylene hydrogenation reactor chuck, be warming up to conduction oil
140~220 DEG C.
6. according to any described techniques of claim 1-6, it is characterised in that the CO for producing step (2)2Step (3) is passed through to obtain
To carbide slag in carry out carburizing reagent obtain calcium carbonate, then spindle that is surface-modified, being dehydrated, be dried to obtain 50~100nm
The nano-calcium carbonate of shape.
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| CN105948049B (en) * | 2016-04-29 | 2018-01-19 | 神雾环保技术股份有限公司 | A kind of system and method for production of calcium carbide from its residue |
| CN106006554B (en) * | 2016-07-25 | 2018-05-08 | 神雾环保技术股份有限公司 | A kind of carbide slag prepares the system and method for hydrogen-rich gas and calcium carbide |
| CN106241735B (en) * | 2016-07-25 | 2018-05-08 | 神雾环保技术股份有限公司 | A kind of carbide slag prepares the system and method for hydrogen-rich gas and calcium carbide |
| KR102570212B1 (en) * | 2016-08-09 | 2023-08-23 | 유니챰 가부시키가이샤 | absorbent article |
| CN107676627A (en) * | 2017-10-26 | 2018-02-09 | 北京华福工程有限公司 | The method of controlling security of producing ethylene with acetylene hydrogenation device |
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Denomination of invention: Process and system of preparing calcium carbide and ethylene through oxygen/coal injection Effective date of registration: 20180327 Granted publication date: 20171103 Pledgee: Tianfeng Securities Co.,Ltd. Pledgor: Shenwu Technology Group Co.,Ltd. Registration number: 2018990000230 |
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