CN105129800A - Process and system of preparing calcium carbide and ethylene through oxygen/coal injection - Google Patents
Process and system of preparing calcium carbide and ethylene through oxygen/coal injection Download PDFInfo
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- CN105129800A CN105129800A CN201510431289.7A CN201510431289A CN105129800A CN 105129800 A CN105129800 A CN 105129800A CN 201510431289 A CN201510431289 A CN 201510431289A CN 105129800 A CN105129800 A CN 105129800A
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- Prior art keywords
- calcium carbide
- acetylene
- oxygen
- coal
- hydrogen
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- 239000005997 Calcium carbide Substances 0.000 title claims abstract description 121
- 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 121
- 238000000034 method Methods 0.000 title claims abstract description 57
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 50
- 239000001301 oxygen Substances 0.000 title claims abstract description 50
- 239000003245 coal Substances 0.000 title claims abstract description 49
- 230000008569 process Effects 0.000 title claims abstract description 35
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 239000005977 Ethylene Substances 0.000 title claims abstract description 22
- 238000002347 injection Methods 0.000 title abstract description 9
- 239000007924 injection Substances 0.000 title abstract description 9
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 claims abstract description 78
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 claims abstract description 78
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 42
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 38
- 239000001257 hydrogen Substances 0.000 claims abstract description 38
- 239000007789 gas Substances 0.000 claims abstract description 36
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 31
- 238000006243 chemical reaction Methods 0.000 claims abstract description 31
- 238000003723 Smelting Methods 0.000 claims abstract description 27
- 238000000926 separation method Methods 0.000 claims abstract description 18
- 238000005261 decarburization Methods 0.000 claims abstract description 16
- 238000004519 manufacturing process Methods 0.000 claims abstract description 14
- 239000000571 coke Substances 0.000 claims abstract description 13
- 238000002360 preparation method Methods 0.000 claims abstract description 8
- 238000002485 combustion reaction Methods 0.000 claims abstract description 6
- 239000002817 coal dust Substances 0.000 claims description 21
- 239000002893 slag Substances 0.000 claims description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 13
- 238000001816 cooling Methods 0.000 claims description 11
- 238000001035 drying Methods 0.000 claims description 10
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 9
- 230000000694 effects Effects 0.000 claims description 8
- 125000004435 hydrogen atom Chemical group [H]* 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
- 150000002431 hydrogen Chemical class 0.000 claims description 7
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 7
- 239000004571 lime Substances 0.000 claims description 7
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 6
- 238000010891 electric arc Methods 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 6
- 239000002253 acid Substances 0.000 claims description 5
- 230000004048 modification Effects 0.000 claims description 5
- 238000012986 modification Methods 0.000 claims description 5
- 239000007921 spray Substances 0.000 claims description 5
- 230000009471 action Effects 0.000 claims description 4
- 230000018044 dehydration Effects 0.000 claims description 4
- 238000006297 dehydration reaction Methods 0.000 claims description 4
- 239000003595 mist Substances 0.000 claims description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 3
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 claims description 3
- 239000004480 active ingredient 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
- 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
- 239000004332 silver Substances 0.000 claims description 3
- 229910052709 silver Inorganic materials 0.000 claims description 3
- 238000010792 warming Methods 0.000 claims description 3
- 241001062472 Stokellia anisodon Species 0.000 claims description 2
- 239000003513 alkali Substances 0.000 claims description 2
- 238000005255 carburizing Methods 0.000 claims description 2
- 239000003054 catalyst Substances 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
- 238000005272 metallurgy Methods 0.000 claims description 2
- 238000006386 neutralization reaction Methods 0.000 claims description 2
- 238000009826 distribution Methods 0.000 abstract description 5
- 239000000843 powder Substances 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 20
- 239000000243 solution Substances 0.000 description 16
- 239000007788 liquid Substances 0.000 description 11
- 238000009833 condensation Methods 0.000 description 9
- 230000005494 condensation Effects 0.000 description 9
- 230000003647 oxidation Effects 0.000 description 9
- 238000007254 oxidation reaction Methods 0.000 description 9
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 8
- 230000008676 import Effects 0.000 description 8
- 229910052725 zinc Inorganic materials 0.000 description 8
- 239000011701 zinc Substances 0.000 description 8
- 229910052799 carbon Inorganic materials 0.000 description 7
- 239000007791 liquid phase Substances 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 241000196324 Embryophyta Species 0.000 description 6
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 6
- DSMZRNNAYQIMOM-UHFFFAOYSA-N iron molybdenum Chemical compound [Fe].[Fe].[Mo] DSMZRNNAYQIMOM-UHFFFAOYSA-N 0.000 description 6
- 239000002002 slurry Substances 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 239000003518 caustics Substances 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
- 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
- XYFCBTPGUUZFHI-UHFFFAOYSA-N Phosphine Chemical compound P XYFCBTPGUUZFHI-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- RBFQJDQYXXHULB-UHFFFAOYSA-N arsane Chemical compound [AsH3] RBFQJDQYXXHULB-UHFFFAOYSA-N 0.000 description 4
- 238000005262 decarbonization Methods 0.000 description 4
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- -1 olefin hydrocarbon Chemical class 0.000 description 4
- 238000007670 refining Methods 0.000 description 4
- 239000000126 substance 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
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000003610 charcoal Substances 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000007701 flash-distillation Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 3
- 229910052759 nickel Inorganic materials 0.000 description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 3
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000006722 reduction reaction Methods 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-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
- 239000001569 carbon dioxide Substances 0.000 description 2
- 235000011089 carbon dioxide Nutrition 0.000 description 2
- 238000003763 carbonization Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 239000003208 petroleum 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
- 239000002699 waste material Substances 0.000 description 2
- 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
- KGWDUNBJIMUFAP-KVVVOXFISA-N Ethanolamine Oleate Chemical compound NCCO.CCCCCCCC\C=C/CCCCCCCC(O)=O KGWDUNBJIMUFAP-KVVVOXFISA-N 0.000 description 1
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 239000006227 byproduct Substances 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
- 238000004939 coking Methods 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
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 125000001741 organic sulfur group Chemical group 0.000 description 1
- GJVFBWCTGUSGDD-UHFFFAOYSA-L pentamethonium bromide Chemical compound [Br-].[Br-].C[N+](C)(C)CCCCC[N+](C)(C)C GJVFBWCTGUSGDD-UHFFFAOYSA-L 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000001737 promoting effect Effects 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
- DAJSVUQLFFJUSX-UHFFFAOYSA-M sodium;dodecane-1-sulfonate Chemical compound [Na+].CCCCCCCCCCCCS([O-])(=O)=O DAJSVUQLFFJUSX-UHFFFAOYSA-M 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 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
- 230000032258 transport Effects 0.000 description 1
Landscapes
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a process and a system of preparing calcium carbide and ethylene through oxygen/coal injection, wherein the process includes following steps: (1) preparation of calcium carbide; (2) CO conversion and decarburization and hydrogen production; (3) acetylene generation; (4) acetylene hydrogenation reaction; and (5) cryogenic separation. In the invention, oxygen and coal powder are injected during a calcium carbide smelting process. Because that heat generated from incomplete combustion of oxygen and coal can radiate to a position which is difficult to reach by arc light, the process, compared with a conventional calcium carbide furnace method, is more uniform in heat distribution in furnace, thereby reducing electric consumption in the calcium carbide furnace and calcium carbide production period. The injected coal powder can replace a part of coke, so that the process can reduce production cost of the calcium carbide. Meanwhile, the process fully utilizes calcium carbide smelting tail gas being rich in CO, which is used for preparing hydrogen through the CO conversion to prepare the hydrogen source in the acetylene hydrogenation reaction, so that not only is environment pollution reduced but also economic benefit is improved greatly.
Description
Technical field
The present invention relates to technique and system that calcium carbide and ethene are prepared in a kind of oxygen/coal winding-up, belong to technical field of coal chemical industry.
Background technology
Ethene is a kind of main raw material of petrochemical industry, and current preparation technology is the cracking alkene of petroleum naphtha and olefin hydrocarbon making by coal mainly.Within 2015, domestic ethene aggregated capacity will reach about 2,200 ten thousand t/a, the domestic ethene production capacity of the year two thousand twenty is increased to 3,250 ten thousand t/a further, expecting the domestic ethene consumption of the year two thousand twenty is 4,800 ten thousand tons, demand is greater than production capacity, and this defines serious strategy threat for China that oil reserve is not enriched.Therefore, seek another kind of new source and processing method prepares large basic organic chemical raw material-ethene, at field of industrial production petroleum replacing as raw material, the dependency of China for oil can be alleviated to a great extent.Coal olefin process produces methyl alcohol, methanol-to-olefins composition primarily of gasification preparing synthetic gas, synthetic gas.But this Technology long flow path, complex process, investment are large, carbon emission amount is high, especially cause greatly cannot carrying out in the region of lack of water for the demand of water.The invention provides one utilizes calcium carbide route to prepare acetylene and then hydrogenation reaction obtains ethene, be different from olefin hydrocarbon making by coal process, calcium carbide process of producing ethylene flow process is short, it is little to invest, carbon emission amount is low, especially selective hydrogenation of acetylene process does not need water to be reaction raw materials, water, as reactor cooling and temperature raising medium, can recycle respectively.And calcium carbide production mainly contains arc process and the hot method of oxygen.Current industrial calcium carbide is produced and is mainly adopted arc process, but in calcium carbide preparation process, electric arc cannot be applied to stove inside circumference or subregion action effect is poor, cause furnace heat skewness, cause producing power consumption high, raw coke consumption is large, and calcium carbide cost remains high.
Summary of the invention
The object of this invention is to provide a kind of oxygen/coal winding-up and prepare calcium carbide and ethylene process, by controlling coal oxygen ratio, make the two incomplete combustion release amount of heat under given conditions, impel uniform heat distribution in furnace of calcium carbide, reduce power consumption, also replace part blue charcoal (coke) consumption simultaneously, and gained CO is made hydrogen, thus reduce calcium carbide production cost, greatly increase economic efficiency.
To achieve these goals, the present invention adopts following scheme:
A kind of oxygen/coal winding-up is prepared calcium carbide and ethylene process, is comprised the steps:
(1) calcium carbide preparation
Coke and lime are dropped in the furnace of calcium carbide of band aerobic/coal winding-up rifle and smelt, to injecting oxygen in stove and coal dust while the power transmission starting the arc, oxygen and coal dust firing produce heat, when in-furnace temperature reaches 2000 ~ 2200 DEG C, coke and lime react and generate calcium carbide CaC under arc heat and combustion heat effect
2with calcium carbide smelting exhaust;
(2) CO conversion, decarburization hydrogen manufacturing
CO in the calcium carbide smelting exhaust that metallurgy generates and steam generation CO transformationreation, products therefrom obtains hydrogen through decarburization, refrigerated separation;
(3) acetylene occurs
Step (1) gained calcium carbide and water carry out being obtained by reacting acetylene and carbide slag, and acetylene delivers to acetylene hydrogenation reaction process after cooling, purification, neutralization;
(4) acetylene hydrogenation reaction
In paste state bed reactor, the acetylene that step (2) gained hydrogen obtains with step (3) mixes with volume ratio 3 ~ 10:1, and selective hydrogenation of acetylene reaction occurs under catalyst action;
(5) low temperature separation process
Adopt compression and the degree of depth method of cooling acetylene hydrogenation to be reacted products therefrom to carry out low temperature separation process and obtain product ethylene.
The present invention is injecting mixed oxygen/coal in calcium carbide smelting process, and the heat produced due to oxygen coal incomplete combustion is radiation-curable to the unapproachable position of arc light, and relatively traditional furnace of calcium carbide furnace heat distribution is more even, reduces furnace of calcium carbide power consumption and calcium carbide production cycle; The coal dust sprayed into can Substitute For Partial coke, thus reduces calcium carbide production cost; Meanwhile, the present invention also makes full use of the calcium carbide smelting exhaust being rich in CO, by CO transformationreation, its obtained hydrogen is used for the hydrogen source of acetylene hydrogenation reaction, not only contributes to reducing environmental pollution, and can greatly increase economic efficiency.
In technique of the present invention, in step (1), described in be selected from long-flame coal, bottle coal, rich coal, coking coal, meager coal, lean coal one or more.
In technique of the present invention, in step (1), described coal dust intake is 130 ~ 200kg/t calcium carbide, and described oxygen intake is 70 ~ 145Nm
3/ t calcium carbide; With ton/m
3meter, the mass volume ratio of described coal dust and oxygen is 1:350-1000, is preferably 1:500-750; The two under given conditions incomplete combustion discharge a large amount of heats, be delivered to a lot of electric arc of stove inside circumference and can not act on or the place of the non-constant of action effect, thus improve the homogeneity of heat distribution in furnace of calcium carbide, reduce calcium carbide and produce power consumption; And, the part coal dust C sprayed into and calcium oxide generation reduction reaction, blue charcoal (coke) usage quantity can be reduced, reduce calcium carbide production cost, produce the flue gas being rich in CO in a large number simultaneously, and the hydrogen produced through transformationreation by the flue gas being rich in CO is as the hydrogen source of producing ethylene with acetylene hydrogenation, the CO2 that the flue gas being rich in CO produces through transformationreation and carbide slag generation carbon geochemistry react, and make nano-calcium carbonate.
In technique of the present invention, in step (2), in the calcium carbide smelting exhaust after purification, total sulfur takes off to 0.02ppm; The solution of described decarburization is selected from the mixture of N methyldiethanol amine (MDEA), diisopropanolamine (DIPA) (DIPA), N methyldiethanol amine (MDEA) and thanomin (MEA), adds the mixture of alkyl alcoholamine and boratory solution of potassium carbonate, tetramethylene sulfone and diisopropanolamine (DIPA); After decarburization in described hydrogen carbon dioxide content lower than 10ppm.
As the preferred embodiment of the present invention, in step (2), its heat recuperation, before carrying out CO transformationreation, first can be used for the intensification of acetylene hydrogenation reactor by described calcium carbide smelting exhaust.Particularly in acetylene hydrogenation reaction, establish a gas-liquid heat exchange unit, thermal oil in calcium carbide smelting exhaust and acetylene hydrogenation reactor chuck is carried out heat exchange in gas-liquid heat exchange unit, thermal oil after heat exchange is warming up to 140-220 DEG C, thus makes full use of the heat in calcium carbide smelting exhaust.
In the method for the invention, in step (3), described calcium carbide being crushed to granularity is 200 ~ 400mm, sends in carbide-feed generator and reacts with water, the acetylene gas generated through cooling, purify the phosphuret-(t)ed hydrogen, the hydrogen sulfide that remove wherein, then in alkali and the acid mist removed wherein; In acetylene gas after described purification Phosphine content lower than 0.1ppm, hydrogen sulfide content lower than 0.1ppm, hydrogen arsenide content lower than the content of 0.1ppm and water lower than 80ppm.
In the method for the invention, in step (4), described catalyzer adopts particle diameter to be 20 ~ 100 μm, and palladium is main active ingredient, silver and ruthenium is auxiliary agent, aluminium sesquioxide is the catalyzer of carrier; Described hydrogenation conditions is: reaction pressure is 0.2 ~ 1.5MPa, and temperature of reaction is 140 ~ 220 DEG C.
In the method for the invention, in step (1), it is electric arc furnace of calcium carbide that described calcium carbide prepares unit, comprises the outlet of body of heater, bell, opening for feed and calcium carbide furnace gas; Wherein, the roof of described body of heater and/or sidewall embed branched can oxygen/coal winding-up rifle of height up and down, multiple oxygen spray pipes that described oxygen/coal winding-up rifle comprises coal dust jet pipe and distributes along the circumference of described coal dust jet pipe, described oxygen/coal winding-up rifle rifle body is copper material, built-in snakelike water-cooled tube.Due to described winding-up rifle adjustable length in described furnace of calcium carbide, in smelting process, bottom oxygen coal injection rifle, be placed in top, molten bath, non-molten bath zone, fractureing of fuel nozzle, oxygen spray pipe and calcium carbide draft tube can be avoided, and the oxidation of fuel injection process electrode base, reduce export license.
In order to make full use of the waste in preparation process, by the CO that step (2) produces
2pass into and carry out carburizing reagent in the carbide slag that step (3) obtains and obtain calcium carbonate, then obtain fusoid nano-calcium carbonate of 50 ~ 100nm through surface modification, dehydration, drying.
The present invention also provides the system realizing above-mentioned oxygen/coal mixed injection and prepare calcium carbide and ethylene process, comprises the calcium carbide connected successively and prepares unit, acetylene generating unit, acetylene hydrogenation reaction member, low temperature separation process unit;
Wherein, also comprise CO conversion decarburization Hydrogen Unit, the calcium carbide smelting exhaust outlet conduit that its inlet mouth and calcium carbide prepare unit is connected, and its hydrogen air outlet is connected with acetylene hydrogenation reaction member pipeline.
In system of the present invention, it is electric arc furnace of calcium carbide that described calcium carbide prepares unit, comprise the outlet of body of heater, bell, opening for feed and calcium carbide furnace gas, wherein, the roof of described body of heater and/or sidewall embed branched can oxygen/coal winding-up rifle of height up and down, multiple oxygen spray pipes that described oxygen/coal winding-up rifle comprises coal dust jet pipe and distributes along the circumference of described coal dust jet pipe, also arrange snakelike water-cooled tube in described oxygen/coal winding-up rifle.By arranging winding-up rifle at furnace of calcium carbide sidewall or furnace roof, existing furnace of calcium carbide electrode can be avoided easy to break, and in fuel injection process, electrode base is oxidizable, the situation that export license is large.
In order to make full use of the waste in preparation process, system of the present invention also comprises carbide slag carbonation unit, and it exports with the carbide slag of acetylene generating unit and the CO of CO conversion decarburization Hydrogen Unit respectively
2outlet connects.
In system of the present invention, described CO conversion decarburization Hydrogen Unit comprises calcium carbide smelting exhaust refining plant, CO changing device, decarbonization device; Wherein, described calcium carbide smelting exhaust refining plant comprise be linked in sequence adsorption filter, ferric oxide desulfurizer, radial compressor, heating furnace, pre-iron molybdenum hydrogenator, one-level iron molybdenum hydrogenator, stair oxidation zinc desulfurizer, nickel Co-Mo hydrogenation reactor and secondary oxidation zinc desulfurizer; Described decarbonization device comprises decarbonizing tower and regenerator column, described secondary oxidation zinc desulfurizer connects the bottom of described decarbonizing tower by pipeline, described decarbonizing tower top is provided with alkanolamine solution import, alkanolamine solution outlet is provided with bottom decarbonizing tower, described alkanolamine solution outlet connects regenerator column by pipeline, the alkanolamine solution outlet of regenerator column is connected with the alkanolamine solution import of decarbonizing tower, the CO that regenerator column top is arranged
2outlet connects described carbide slag carbonation unit.
In system of the present invention, described acetylene generating unit comprises carbide-feed generator, peace and quiet tower, caustic neutralizer column and condensation drying device; Wherein, be provided with air outlet bottom carbide-feed generator, it is connected with peace and quiet tower, caustic neutralizer column, condensation drying device in turn by pipeline, and the acetylene gas outlet of described condensation drying device connects ethylene making unit by pipeline.Preferably, be provided with double-deck sieve plate in described carbide-feed generator, 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.
In system of the present invention, the reactor realizing effect of the present invention that described acetylene hydrogenation reaction member can select those skilled in the art to grasp in principle; Preferred paste state bed reactor in the present invention; Described paste state bed reactor is 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 hydrogen inlet and the hydrogen of paste state bed reactor merge pipeline and is connected, and the product gas outlet of paste state bed reactor is connected with low temperature separation process unit.Wherein, described paste state bed reactor is the reactor having chuck, top in reactor is provided with gas-liquid separator, reactor bottom is provided with gas distributor, dactylethrae interchanger is positioned at above gas distributor, and condenser is between gas-liquid separator and dactylethrae interchanger.
In system of the present invention, described low temperature separation process unit comprises the flash distillation plant, deethanizing column, ethylene rectification tower, depropanizing tower, propylene rectification tower, debutanizing tower, the anti-butylene rectifying tower that connect successively.
The present invention adopts oxygen/coal mixed injection mode to improve the homogeneity of heat distribution in furnace of calcium carbide in furnace of calcium carbide, reduce power consumption, blue charcoal (coke) usage quantity, produce the flue gas being rich in CO in a large number, and the flue gas being rich in CO is obtained the hydrogen source of hydrogen as producing ethylene with acetylene hydrogenation through transformationreation, the CO that transformationreation produces
2react with carbide slag generation carbon geochemistry and make nano-calcium carbonate; Technique of the present invention and system have that flow process is short, floor space is few, energy consumption is low, less investment and without CO
2the advantages such as discharge, in the gaseous products of generation, ethene accounts for 75 ~ 85%, and 1-butylene accounts for 2 ~ 5%, and anti-butylene accounts for 15 ~ 20%, and all the other are ethane, propylene and C
5 +deng by product, after reaction, gas is after low temperature separation process, and hydrogen is recycled.
Generally speaking, the winding-up of oxygen of the present invention/coal obtains carbonic acid gas maximum discharge that calcium carbide and ethylene process can avoid other Coal Chemical Industry process problem and the problem to water resources heavy dependence, be typical low-carbon (LC), clean coal conversion process, Green Sustainable, the energy-saving and emission-reduction promoting China's coal resource clean utilization and acetylene chemical industry are had great importance.
Accompanying drawing explanation
Calcium carbide and ethylene process schematic flow sheet are prepared in Fig. 1 oxygen of the present invention/coal winding-up.
Calcium carbide and ethylene system structural representation are prepared in Fig. 2 oxygen of the present invention/coal winding-up.
Embodiment
Following examples for illustration of the present invention, but are not used for limiting the scope of the invention.
Embodiment 1
A kind of oxygen/coal winding-up is prepared calcium carbide and ethylene process, as shown in Figure 1, is comprised the steps:
(1) calcium carbide preparation
The coke of release mesh and lime are transported to calcium carbide factory, enter in furnace of calcium carbide through charging machine and furnace charge hopper, the winding-up rifle injecting oxygen/coal dust intermixture in stove being arranged on furnace of calcium carbide sidewall or furnace roof is utilized while the power transmission starting the arc, oxygen and coal dust firing produce a large amount of heats, and the straying quatity of wherein said oxygen is 95Nm
3/ t calcium carbide, the intake of pulverized anthracite is 130kg/t calcium carbide; When bath temperature is heated to 2000-2200 DEG C, coke and lime are reduced at furnace of calcium carbide, are melted into calcium carbide under the effect of arc heat, resistance heat and reaction heat, calcium carbide is flowed in 1t pot bag by fire door, transports between building and cools, deliver to acetylene generation operation afterwards; Carbon simultaneously in part coal dust and lime generation reduction reaction generate calcium carbide, reduce coke usage quantity.
(2) CO conversion, decarburization hydrogen manufacturing
Purification: first the calcium carbide smelting exhaust being rich in CO is compressed to after 0.8MPaG through spiral-lobe compressor and enters adsorption filter, removing naphthalene wherein, enter ferric oxide desulfurizer after the impurity such as tar and remove most of inorganic sulfur and part organosulfur, be compressed to 3.5MPaG through radial compressor afterwards and enter heating furnace, pre-iron molybdenum, one-level iron molybdenum hydrogenator, most of organic sulfur conversion in calcium carbide smelting exhaust is made to be inorganic sulfur, enter stair oxidation zinc desulfurizer afterwards, remove hydrogen sulfide wherein, finally enter nickel Co-Mo hydrogenation reactor and secondary oxidation zinc desulfurizer, the total sulfur in gas is made to take off to 0.02ppm,
Calcium carbide smelting exhaust after purification utilizes steam preheating to 250 DEG C, form hydrogen through CO transformationreation and reclaim steam generation by reaction heat wherein, gained hydrogen removes through separator the bottom entering decarbonizing tower after free liquid and entrained solid impurity, with the alkanolamine solution counter current contact flowed from top to bottom by tower top, remove acid gas composition wherein, the solution droplets may carried in discharge knockout drum removing hydrogen, go out carbon dioxide content in decarbonizing tower hydrogen and, lower than 10ppm, be sent to the paste state bed reactor of acetylene hydrogenation reaction workshop section; Alkanolamine solution bottom decarbonizing tower enters regenerator column and regenerates, and the alkanolamine solution after regeneration enters decarbonizing tower internal recycle and uses after heat exchange, cooling.
(3) acetylene occurs
The calcium carbide generated is broken for granularity 200 ~ 400mm feeding carbide-feed generator through calcium carbide crusher and water reacts, the spacing that carbide-feed generator inside is provided with the lath of double-deck sieve plate upper sieve plate is 300mm, the grand calcium carbide in 300mm and water react, the spacing of the lath of lower floor's sieve plate is 80mm, the grand calcium carbide in 80mm and water react, and are less than the calcium carbide of 80mm or powder and overflow in secondary producer secondary response again.Greatly can be improved the working efficiency of carbide-feed generator by this structure sieve plate, improve calcium carbide utilization ratio; In order to enable calcium carbide be evenly distributed on sieve plate, establishing umbrella to distribute cone at the upper sieve plate of producer, increasing the surface-area that calcium carbide contacts with water, to improve the working efficiency of producer.Calcium carbide produces acetylene gas after contacting with water and being hydrolyzed, after the efficient washing cooling tower washing on secondary producer, enter positive water seal, and discharge carbide slag, carbide slag discharges into slag by producer and starches agitated pool, be extracted into plate and frame(type)filter press by slush pump to extrude, slag, water be separated, as water of productive use in the current Huis pond after separation; The acetylene gas that reaction generates enters peace and quiet tower and removes phosphuret-(t)ed hydrogen, hydrogen sulfide and hydrogen arsenide in acetylene gas after wash cooling, to go out in the acetylene gas of peace and quiet tower Phosphine content lower than 0.1ppm, hydrogen sulfide content lower than 0.1ppm and hydrogen arsenide content lower than 0.1ppm, remove phosphuret-(t)ed hydrogen, hydrogen sulfide and hydrogen arsenide and acetylene gas and enter acid mist in caustic neutralizer column removing acetylene gas, remove the acetylene gas after acid mist after supercharging and condensation, remove moisture in acetylene gas, in acetylene gas after dehydration, the content of water is lower than 80ppm, sends into acetylene hydrogenation reaction process.
(4) acetylene hydrogenation reaction
The acetylene that step (2) gained hydrogen and step (3) obtain is mixed into the paste state bed reactor of acetylene hydrogenation reaction process with volume ratio 3 ~ 10:1, under the effect of catalyzer, carry out selective hydrogenation of acetylene reaction, generate the products such as ethene;
Acetylene hydrogenation reaction process adopts with the slurry bed system of chuck, gas distributor, dactylethrae interchanger, condenser and gas-liquid separator as reactor, it is auxiliary agent that catalyzer adopts the palladium of 20 ~ 100 μm to be main active ingredient, silver and ruthenium, aluminium sesquioxide is the catalyzer of carrier, reaction pressure is 0.2 ~ 1.5MPa, and temperature of reaction is 140 ~ 220 DEG C; By the flow of the heat-eliminating medium of dactylethrae in the circular flow of thermal oil in control chuck and slurry bed system in reaction process, the temperature of reaction is made to control at 140 ~ 220 DEG C, the condenser on slurry bed system top, by the liquid phase solvent condensation of evaporation, the liquid phase solvent of condensation is back in slurry bed system, the liquid phase solvent of carry secretly in reaction product 99% is separated with reaction product by the gas-liquid separator at the top of paste state bed reactor, fall back in slurry bed system, reaction product goes out paste state bed reactor from reactor head pneumatic outlet, enters low temperature separation process operation.
(5) low temperature separation process
The product of acetylene hydrogenation is compressed to 3.4 ~ 3.9MPa, then gas phase cools and flash distillation step by step, finally be cooled to-163 ~-169 DEG C, in hydrogen gas tank, sub-argument goes out hydrogen, the liquid phase of each flash tank is entered deethanizing column, deethanizing column gaseous products enters ethylene rectification tower and obtains ethylene product, liquid-phase product enters depropanizing tower, depropanizing tower gaseous products enters propylene rectification tower and obtains propylene product, liquid-phase product enters debutanizing tower, debutanizing tower gaseous products enters anti-butylene rectifying tower, and tower top obtains anti-butylene product, the C that liquid-phase product is and mixes
5deng product.
(6) carbide slag carbonization
Carbide slag step (3) produced filters after washing, scalping, removing mechanical impurity, drying is sized to less than 125 μm afterwards 1050 DEG C of calcinings, water is added after burnt carbide slag cooling, the mass ratio of water and calcium oxide is 20 ~ 40:1, obtain calcium hydroxide slurry, in aqua calcis, pass into the CO that step (2) produces afterwards
2carry out carbonization and obtain calcium carbonate soln, calcium carbonate soln obtains the nano-calcium carbonate that particle diameter is 50 ~ 100nm after sodium laurylsulfonate surface modification, dehydration, drying.
As calculated, after adopting mixed injection technique, power consumption is reduced to 2700kwh/t calcium carbide from existing 3100kwh/t calcium carbide, and production cost is reduced to 175 yuan/t calcium carbide, is rich in CO exhaust gas volumn increase about 200Nm
3/ t calcium carbide, total exhaust gas volumn is about 600Nm
3/ t.
Embodiment 2
The present embodiment adopts the technique identical with embodiment 1 to prepare ethene, and difference is, its heat recuperation, before carrying out CO transformationreation, first can be used for the intensification of acetylene hydrogenation reactor by described calcium carbide smelting exhaust.Particularly in acetylene hydrogenation reaction, establish a gas-liquid heat exchange unit, thermal oil in calcium carbide smelting exhaust and acetylene hydrogenation reactor chuck is carried out heat exchange in gas-liquid heat exchange unit, thermal oil after heat exchange is warming up to 140-220 DEG C, thus makes full use of the heat in calcium carbide smelting exhaust.
Embodiment 3
Realize the system that oxygen described in embodiment 1/coal mixed injection prepares calcium carbide and ethylene process, as shown in Figure 2, comprise the calcium carbide connected successively and prepare unit, acetylene generating unit, acetylene hydrogenation reaction member, low temperature separation process unit;
Wherein, also comprise CO conversion decarburization Hydrogen Unit, the calcium carbide smelting exhaust outlet conduit that its inlet mouth and calcium carbide prepare unit is connected, and its hydrogen air outlet is connected with acetylene hydrogenation reaction member pipeline.
Wherein, it is electric arc furnace of calcium carbide that described calcium carbide prepares unit, comprise the outlet of body of heater, bell, opening for feed and calcium carbide furnace gas, wherein, the roof of described body of heater and/or sidewall embed branched can oxygen/coal winding-up rifle of height up and down, multiple oxygen spray pipes that described oxygen/coal winding-up rifle comprises coal dust jet pipe and distributes along the circumference of described coal dust jet pipe, also arrange snakelike water-cooled tube in described oxygen/coal winding-up rifle.
Described system also comprises carbide slag carbonation unit, and it exports with the carbide slag of acetylene generating unit and the CO of CO conversion decarburization Hydrogen Unit respectively
2outlet connects.Wherein, described CO conversion decarburization Hydrogen Unit comprises calcium carbide smelting exhaust refining plant, CO changing device, decarbonization device; Wherein, described calcium carbide smelting exhaust refining plant comprise be linked in sequence adsorption filter, ferric oxide desulfurizer, radial compressor, heating furnace, pre-iron molybdenum hydrogenator, one-level iron molybdenum hydrogenator, stair oxidation zinc desulfurizer, nickel Co-Mo hydrogenation reactor and secondary oxidation zinc desulfurizer; Described decarbonization device comprises decarbonizing tower and regenerator column, described secondary oxidation zinc desulfurizer connects the bottom of described decarbonizing tower by pipeline, described decarbonizing tower top is provided with alkanolamine solution import, alkanolamine solution outlet is provided with bottom decarbonizing tower, described alkanolamine solution outlet connects regenerator column by pipeline, the alkanolamine solution outlet of regenerator column is connected with the alkanolamine solution import of decarbonizing tower, the CO that regenerator column top is arranged
2outlet connects described carbide slag carbonation unit.
Wherein, described acetylene generating unit comprises carbide-feed generator, peace and quiet tower, caustic neutralizer column and condensation drying device; Wherein, be provided with air outlet bottom carbide-feed generator, it is connected with peace and quiet tower, caustic neutralizer column, condensation drying device in turn by pipeline, and the acetylene gas outlet of described condensation drying device connects ethylene making unit by pipeline.Preferably, be provided with double-deck sieve plate in described carbide-feed generator, 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, described acetylene hydrogenation reaction member can select the reactor realizing effect of the present invention that those skilled in the art grasp in principle; Preferred paste state bed reactor in the present invention; Described paste state bed reactor is 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 hydrogen inlet and the hydrogen of paste state bed reactor merge pipeline and is connected, and the product gas outlet of paste state bed reactor is connected with low temperature separation process unit.Wherein, described paste state bed reactor is the reactor having chuck, top in reactor is provided with gas-liquid separator, reactor bottom is provided with gas distributor, dactylethrae interchanger is positioned at above gas distributor, and condenser is between gas-liquid separator and dactylethrae interchanger.
Wherein, described low temperature separation process unit comprises the flash distillation plant, deethanizing column, ethylene rectification tower, depropanizing tower, propylene rectification tower, debutanizing tower, the anti-butylene rectifying tower that connect successively.
Although above the present invention is described in detail with a general description of the specific embodiments, on basis of the present invention, can make some modifications or improvements it, this will be apparent to those skilled in the art.Therefore, these modifications or improvements without departing from theon the basis of the spirit of the present invention, all belong to the scope of protection of present invention.
Claims (10)
1. a technique for calcium carbide and ethene is prepared in oxygen/coal winding-up, it is characterized in that, comprises the steps:
(1) calcium carbide preparation
Coke and lime are dropped in the furnace of calcium carbide of band aerobic/coal winding-up rifle and smelt, to injecting oxygen in stove and coal dust while the power transmission starting the arc, oxygen and coal dust firing produce heat, and when in-furnace temperature reaches 2000 ~ 2200 DEG C, coke and lime react and generates calcium carbide CaC under arc heat and combustion heat effect
2with calcium carbide smelting exhaust;
(2) CO conversion, decarburization hydrogen manufacturing
CO in the calcium carbide smelting exhaust that metallurgy generates and steam generation CO transformationreation, products therefrom obtains hydrogen through decarburization, refrigerated separation;
(3) acetylene occurs
Step (1) gained calcium carbide and water carry out being obtained by reacting acetylene and carbide slag, and acetylene delivers to acetylene hydrogenation reaction process after cooling, purification, neutralization;
(4) acetylene hydrogenation reaction
In paste state bed reactor, the acetylene that step (2) gained hydrogen obtains with step (3) mixes with volume ratio 3 ~ 10:1, and selective hydrogenation of acetylene reaction occurs under catalyst action;
(5) low temperature separation process
Adopt compression and the degree of depth method of cooling acetylene hydrogenation to be reacted products therefrom to carry out low temperature separation process and obtain product ethylene.
2. technique according to claim 1, is characterized in that, in step (1), described coal dust intake is 130 ~ 200kg/t calcium carbide, and described oxygen intake is 70 ~ 145Nm
3/ t calcium carbide.
3. technique according to claim 1, is characterized in that, in step (1), with ton/m
3meter, the mass volume ratio of described coal dust and oxygen is 1:350-1000.
4. technique according to claim 1, it is characterized in that, in step (3), described calcium carbide being crushed to granularity is 200 ~ 400mm, send in carbide-feed generator and react with water, the acetylene gas generated through cooling, purify the phosphuret-(t)ed hydrogen, the hydrogen sulfide that remove wherein, then in alkali and the acid mist removed wherein.
5. technique according to claim 1, is characterized in that, in step (4), described catalyzer adopts particle diameter to be 20 ~ 100 μm, and palladium is main active ingredient, silver and ruthenium is auxiliary agent, aluminium sesquioxide is the catalyzer of carrier; Described hydrogenation conditions is: reaction pressure is 0.2 ~ 1.5MPa, and temperature of reaction is 140 ~ 220 DEG C.
6. technique according to claim 1, it is characterized in that, in step (2), described calcium carbide smelting exhaust is before carrying out CO transformationreation, first carry out heat exchange by the thermal oil in pipeline and acetylene hydrogenation reactor chuck, make thermal oil be warming up to 140 ~ 220 DEG C.
7., according to the arbitrary described technique of claim 1-6, it is characterized in that, by the CO that step (2) produces
2pass into and carry out carburizing reagent in the carbide slag that step (3) obtains and obtain calcium carbonate, then obtain fusoid nano-calcium carbonate of 50 ~ 100nm through surface modification, dehydration, drying.
8. a system for calcium carbide and ethylene process is prepared in oxygen/coal winding-up, it is characterized in that, comprises the calcium carbide connected successively and prepare unit, acetylene generating unit, acetylene hydrogenation reaction member, low temperature separation process unit;
Described system also comprises CO conversion decarburization Hydrogen Unit, and the calcium carbide smelting exhaust outlet conduit that its inlet mouth and calcium carbide prepare unit is connected, and its hydrogen air outlet is connected with acetylene hydrogenation reaction member pipeline.
9. system according to claim 8, it is characterized in that, it is electric arc furnace of calcium carbide that described calcium carbide prepares unit, comprise the outlet of body of heater, bell, opening for feed and calcium carbide furnace gas, wherein, the roof of described body of heater and/or sidewall embed branched can oxygen/coal winding-up rifle of height up and down, multiple oxygen spray pipes that described oxygen/coal winding-up rifle comprises coal dust jet pipe and distribute along the circumference of described coal dust jet pipe, described oxygen/coal is jetted in rifle and is also arranged snakelike water-cooled tube.
10. system according to claim 8, is characterized in that, described system also comprises carbide slag carbonation unit, and it exports with the carbide slag of acetylene generating unit and the CO of CO conversion decarburization Hydrogen Unit respectively
2outlet connects.
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Address after: 102200 Beijing city Changping District Machi Town cow Road No. 18 Applicant after: Shenwu Technology Group Co.,Ltd. Address before: 102200 Beijing city Changping District Machi Town cow Road No. 18 Applicant before: BEIJING SHENWU ENVIRONMENT AND ENERGY TECHNOLOGY Co.,Ltd. |
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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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