CN204981160U - System for oxygen / coal jetting preparation carbide and ethylene - Google Patents
System for oxygen / coal jetting preparation carbide and ethylene Download PDFInfo
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- CN204981160U CN204981160U CN201520531916.XU CN201520531916U CN204981160U CN 204981160 U CN204981160 U CN 204981160U CN 201520531916 U CN201520531916 U CN 201520531916U CN 204981160 U CN204981160 U CN 204981160U
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Abstract
The utility model relates to a system for oxygen / coal jetting preparation carbide and ethylene. The system is including the carbide preparation unit, acetylene generation unit, acetylene hydrogenation react unit, the cryogenic separation unit that connect gradually, the system still includes CO transform decarbonization hydrogen manufacturing unit, and its air inlet is smelted tail gas export pipeline with the carbide of carbide preparation unit and is connected its hydrogen gas outlet and acetylene hydrogenation react unit pipe connection. Adopt the system, can jet in carbide the smelting process oxygen and buggy to realize incomplete combustion through controlling its discharge rate proportion, produce a large amount of heat radiation to the position that the arc light is difficult to to reach from this, make the interior heat distribution of stove more even, showing reduction carbide stove power consumption and shortening carbide production cycle, spout into buggy fungible part coke still, and the CO that produces of incomplete combustion makes hydrogen through the transformationreation and as hydrogenation's hydrogen source, not only helps reducing environmental pollution, can improve economic benefits greatly moreover.
Description
Technical field
The utility model relates to the system that calcium carbide and ethene are prepared in a kind of oxygen/coal winding-up, belongs 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.
Utility model content
The purpose of this utility model is to provide the system that calcium carbide and ethene are prepared in a kind of oxygen/coal winding-up, when adopting this system to prepare ethene, by controlling coal-oxygen injection amount ratio, making the two incomplete combustion release amount of heat under given conditions, impelling uniform heat distribution in furnace of calcium carbide, reduce power consumption, go back the blue charcoal (coke) of Substitute For Partial simultaneously, and gained CO is made hydrogen, make whole hydrogenation process without the need to outer hydrogen source, reduce calcium carbide production cost, greatly increase economic efficiency.
To achieve these goals, the utility model adopts following scheme:
A system for calcium carbide and ethene is prepared in oxygen/coal winding-up, 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 described in the utility model, 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, 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 system described in the utility model, 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 described in the utility model, 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 described in the utility model, the reactor realizing described effect that described acetylene hydrogenation reaction member can select those skilled in the art to grasp in principle; Preferred paste state bed reactor; 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 described in the utility model, 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.
In order to make full use of the waste in preparation process, 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.
The technique adopting said system to prepare calcium carbide and ethene 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, 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.
Injecting mixed oxygen/coal in calcium carbide smelting process, 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, make 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 contribute to reducing environmental pollution, and can greatly increase economic efficiency.
Wherein, in step (1), described in be selected from long-flame coal, bottle coal, rich coal, coking coal, meager coal, lean coal one or more.
Wherein, 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.
Wherein, 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 preferred embodiment, 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.
Wherein, 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.
Wherein, 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.
Wherein, 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 system that oxygen coal injection described in the utility model prepares calcium carbide and ethene is sprayed into oxygen and coal dust by the oxygen/coal winding-up rifle be arranged in furnace of calcium carbide, is produced amount of heat and CO, improve the homogeneity of furnace heat distribution, reduce power consumption; The flue gas being simultaneously rich in CO obtains the hydrogen source of hydrogen as hydrogenation reaction through transformationreation, and the CO that transformationreation produces
2react with carbide slag generation carbon geochemistry and make nano-calcium carbonate, effectively reduce production cost, improve whole economic efficiency.Described system footprint area is few, energy consumption is low, it is little to invest and without CO
2discharge, 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, carbonic acid gas maximum discharge that the system that the winding-up of oxygen described in the utility model/coal obtains calcium carbide and ethene 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
Fig. 1 is the process flow sheet adopting oxygen described in the utility model/coal winding-up to prepare the system of calcium carbide and ethene.
Fig. 2 is the structural representation that the system of calcium carbide and ethene is prepared in oxygen described in the utility model/coal winding-up.
Embodiment
Following examples for illustration of the utility model, but are not used for limiting scope of the present utility model.
Embodiment 1
A system for calcium carbide and ethene is prepared in oxygen/coal winding-up, as shown in Figure 2, 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.
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 is paste state bed reactor; 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.
Embodiment 2
Utilize system described in embodiment 1 to prepare a method for calcium carbide and ethene, as shown in Figure 1, comprise 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, adopt system described in embodiment 1 to prepare ethene, its power consumption is reduced to 2700kwh/t calcium carbide from original 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 3
The present embodiment adopts the technique identical with embodiment 2 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.
Although above done detailed description to the utility model with a general description of the specific embodiments, on the utility model basis, can make some modifications or improvements it, this will be apparent to those skilled in the art.Therefore, these modifications or improvements on the basis of not departing from the utility model spirit, all belong to the scope that the utility model is claimed.
Claims (8)
1. a system for calcium carbide and ethene 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.
2. system according to claim 1, 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.
3. system according to claim 1, is characterized in that, 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.
4., according to the arbitrary described system of claim 1-3, it is characterized in that, 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.
5. system according to claim 4, is characterized in that, is provided with double-deck sieve plate in described carbide-feed generator, and 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.
6., according to the arbitrary described system of claim 1-3, it is characterized in that, described acetylene hydrogenation reaction member is paste state bed reactor; 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.
7., according to the arbitrary described system of claim 1-3, it is characterized in that, 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.
8. according to the arbitrary described system of claim 1-3, it is characterized in that, it 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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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520531916.XU CN204981160U (en) | 2015-07-21 | 2015-07-21 | System for oxygen / coal jetting preparation carbide and ethylene |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105129800A (en) * | 2015-07-21 | 2015-12-09 | 北京神雾环境能源科技集团股份有限公司 | Process and system of preparing calcium carbide and ethylene through oxygen/coal injection |
| CN105948049A (en) * | 2016-04-29 | 2016-09-21 | 神雾环保技术股份有限公司 | System and method for producing calcium carbide by utilizing carbide slag |
| CN106006554A (en) * | 2016-07-25 | 2016-10-12 | 神雾环保技术股份有限公司 | System and method for preparing hydrogen-rich gas and calcium carbide by calcium carbide residue |
| CN106241735A (en) * | 2016-07-25 | 2016-12-21 | 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 carbide |
| 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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2015
- 2015-07-21 CN CN201520531916.XU patent/CN204981160U/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105129800A (en) * | 2015-07-21 | 2015-12-09 | 北京神雾环境能源科技集团股份有限公司 | Process and system of preparing calcium carbide and ethylene through oxygen/coal injection |
| CN105129800B (en) * | 2015-07-21 | 2017-11-03 | 神雾科技集团股份有限公司 | A kind of oxygen/coal injection prepares the technique and system of calcium carbide and ethene |
| CN105948049A (en) * | 2016-04-29 | 2016-09-21 | 神雾环保技术股份有限公司 | System and method for producing calcium carbide by utilizing carbide slag |
| 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 |
| CN106006554A (en) * | 2016-07-25 | 2016-10-12 | 神雾环保技术股份有限公司 | System and method for preparing hydrogen-rich gas and calcium carbide by calcium carbide residue |
| CN106241735A (en) * | 2016-07-25 | 2016-12-21 | 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 carbide |
| 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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