CN101244970A - Apparatus and technique for producing ethylene with ethyl alcohol - Google Patents
Apparatus and technique for producing ethylene with ethyl alcohol Download PDFInfo
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- CN101244970A CN101244970A CNA2007100269198A CN200710026919A CN101244970A CN 101244970 A CN101244970 A CN 101244970A CN A2007100269198 A CNA2007100269198 A CN A2007100269198A CN 200710026919 A CN200710026919 A CN 200710026919A CN 101244970 A CN101244970 A CN 101244970A
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Abstract
The invention discloses a product device and technique of using ethanol to prepare ethylene; the raw material ethanol out of the boundary region is heated and evaporated to be ethylene steam which is divided into three stocks, and the ethylene steam of a first stock which is mixed with medium-pressure steam enters into a first heating section and then enters into a first reactor to react after being heated, the reaction products which is mixed with the ethylene steam of a second stock enters into a second heating section and then enters into a second reactor to react after being heated, the reaction products which is mixed with the ethylene steam of a third stock enters into a third heating section and then enters into a third reactor to react after being heated, the reaction product which enters into a caustic wash tower to remove carbon dioxide and acetic acid after recycling the heat by an evaporator is cooled by deep cooling after extracting water by a dryer, the liquefied rude ethylene sequentially enters into a demethanizer to remove methane, and then enters into a purifying column to remove heavy components, and the product ethylene can be obtained. The product device and technique of using ethanol to prepare ethylene of the invention has the advantages that three-step type reaction is used, conversion rate is high, the production of industrial scale can be realized, with simple technique, reliable material supply and low production cost.
Description
Technical field
The invention belongs to chemical technology field, especially relate to a kind of production equipment and technology for preparing ethene.
Background technology
Ethene is as a kind of Organic Chemicals of basis, obtained using widely in all respects of daily life, and along with the development of economy and technology, constantly widens in its use field, and usage quantity is also in continuous growth.Mostly traditionally is to be that raw material comes synthesizing ethylene with the oil, but along with constantly riseing of global oil price, also when the river rises the boat goes up for the cost of the ethene of producing, and oil is non-renewable fossil resource, the technological development of oil system ethene is very restricted, and the market competitiveness of made ethylene product is also progressively impacted.Another kind of common chemical raw materials ethanol can be converted into ethene according to following chemical reaction under 470 ℃ ~ 360 ℃ temperature under catalyst action: C
2H
5OH → C
2H
2+ H
2O sloughs the moisture in the resultant and is purified and can obtain finished product ethene.And well-known, ethanol is a kind of renewable energy source, can pass through cereal, potato class and saccharine material, by fermentation, distillation produces, can be described as a kind of inexhaustible, can not exhaustion, the capable of regeneration energy.Therefore industrial urgent need provides a kind of production equipment and the production technique that can use ethanol preparation ethene, to satisfy the growing demand to ethene at present.
Summary of the invention
The purpose of this invention is to provide a kind of can suitability for industrialized production, the production equipment of ethanol preparation ethene that cost of investment is not high.
Another purpose of the present invention provides the production technique of the simple ethanol preparation ethene of a kind of technology.
Technical solution of the present invention is: a kind of production equipment of ethanol preparation ethene, and it comprises vaporizer, soda-wash tower, moisture eliminator, demethanizing tower, purification tower, process furnace and first reactor, second reactor, the 3rd reactor and ethylene chiller, ethene deep freezer; Wherein the inlet section of vaporizer shell-side is by ethanol inlet outside the pipe connection battery limit (BL), its outlet section is first heating zone inlet of pipe connection process furnace respectively, second heating zone inlet and the 3rd heating zone inlet, medium pressure steam system pipe connection outside first heating zone inlet and the battery limit (BL), its outlet conduit connects first reactor inlet, the first reactor outlet pipe connection, second heating zone inlet, the second heating zone outlet conduit connects second reactor inlet, the second reactor outlet pipe connection the 3rd heating zone inlet, the 3rd heating zone outlet conduit connects the 3rd reactor inlet, the 3rd reactor outlet connects soda-wash tower charging layer through the evaporator tube side, the soda-wash tower top is by pipe connection moisture eliminator inlet, ethylene chiller shell-side inlet duct connects dryer export, its shell-side outlet connects demethanizing tower charging layer through the ethene deep freezer, demethanizer bottoms is by pipe connection purification tower charging layer, and the purification cat head connects the outlet of finished product ethene through ethylene chiller pipe side.
Feed ethanol outside the battery limit (BL) is divided into three strands after the vaporizer heating evaporation becomes alcohol vapour, first strand of alcohol vapour with enter first heating zone after middle pressure steam mixes and further enter first reactor reaction after the heating, resultant of reaction mixes with second strand of alcohol vapour after enter second reactor reaction after the heating of second heating zone, resultant of reaction mixes with the 3rd strand of alcohol vapour after enter the 3rd reactor reaction after the heating of the 3rd heating zone, resultant of reaction enters soda-wash tower decarbonation and acetic acid after vaporizer reclaims heat, the crude ethylene gas of cat head enters the cooling of ethylene chiller shell-side deep cooling after removing moisture through moisture eliminator, crude ethylene after the liquefaction enters demethanizing tower and removes methane, the liquid ethylene of demethanizer bottoms send purification tower to take off heavy constituent, and the ethene that the purification cat head is discharged send the outlet of finished product ethene after ethylene chiller pipe side draught heat heats up.
The production technique of being produced ethene by ethanol is based on chemical reaction: C
2H
5OH → C
2H
2+ H
2O, reaction occurs in 470 ℃～360 ℃ beds, and the catalyzer major ingredient is an aluminum oxide, is thermo-negative reaction, every generation 1kg ethene and will consume the heat of 1700KJ, heat can be provided by process furnace burner fuel oil or combustion gas, carries out for guaranteeing reaction forward, and three sections reactors are set, corresponding three heating zones are set respectively, material is transformed step by step, improved whole transformation efficiency, can realize suitability for industrialized production fully.Reacted gas through conventional alkali cleaning remove carbonic acid gas and acetic acid, remove moisture after get final product after removing heavy constituent such as light constituent such as methane and ethane behind the cryogenic liquefying one by one finished product ethene, make full use of existing ripe subsequent treatment process, facility investment is little, and technology is simple.
As a kind of prioritization scheme, the weight percent that first strand of alcohol vapour, second strand of alcohol vapour, the 3rd strand of alcohol vapour account for whole alcohol vapour total amounts is respectively 32～38%, 38～50%, 18～24%, and preferred weight percent is 37%, 41%, 22%.Alcohol vapour is divided into three parts and enters the reactor internal reaction respectively, the inventory that preceding two reactors enter is bigger, can guarantee to react total amount, the inventory that the 3rd reactor enters is less, can guarantee to transform fully, the transformation efficiency that the interior ethanol synthesis of each reactor changes into ethene is inequality, and raises step by step, and staged reaction can fully improve reaction conversion ratio like this.
Described demethanizing cat head connects the burner of described process furnace by pipeline through combustion heater, and light constituents such as hydrogen of deviating from and methane can send process furnace to do fuel and use, and save cost.
Described purification cat head is through pipe connection purification cat head condenser inlet, and purification cat head condensator outlet connects the return tank top, connects described purification tower top, described methane top of tower and described ethylene chiller pipe side entrance respectively by pipeline at the bottom of the return tank.The ethene that described purification cat head is discharged is gone in the ethene return tank through purification overhead condenser cooling liquefaction is laggard, the ethene at the jar end is divided into three parts, deliver to respectively and send the outlet of finished product ethene after purification trim the top of column, the backflow of demethanizing cat head and ethylene chiller pipe side draught heat heat up, the trim the top of column that is used to purify can keep the purity of ethene, be used for the backflow of demethanizing cat head and can reclaim the ethene of discharging light constituent, conserve energy.
The temperature in of described first reactor, second reactor, the 3rd reactor is controlled to be 470 ℃, 470 ℃, 475 ℃ respectively, can fully guarantee the transformation efficiency of the producing ethylene with ethyl alcohol in each reactor.
Advantage of the present invention is: use the syllogic reaction, the transformation efficiency height of ethanol preparation ethene can be realized commercial scale production, makes full use of existing ripe purification process, saves cost of investment, and technology is simple, and raw material supply is reliable, and production cost is lower.
Description of drawings
Fig. 1 is the whole overview synoptic diagram of technology of the present invention;
Fig. 2 is a process flow diagram of the present invention.
Embodiment
Embodiment: as Fig. 1, the technological process of production of the present invention simply overview is four parts: ethanol evaporation, ethanol synthesis, alkali cleaning drying and purification.The industrial alcohol temperature of delivering to the ethylene unit within battery limit is 20 ℃, and pressure 0.1Mpa at first enters vaporized alcohol device internal heating to 300 ℃ after the pressurization through pump pressurization, sends into reaction workshop section, and is divided into three fluid streams.The middle pressure steam Wen Hehou of first fluid streams and 195 ℃ enters ethanol process furnace first heating zone 111, further is heated to 470 ℃, then enter first reactor 112, react in catalytic bed, most of ethanol conversion becomes second rare, because heat absorption, temperature out is reduced to 360 ℃.Second fluid streams then with after the resultant of reaction of first reactor 112 mixes, enters process furnace second heating zone 121, also is heated to 470 ℃, enters second reactor 122, reacts in catalytic bed, further transforms, and temperature out is reduced to 360 ℃.The 3rd fluid streams is then mixed with the resultant of reaction of second reactor 122, enters the 3rd heating zone 131 of process furnace, is heated to 475 ℃, enters the 3rd reactor 132 under 0.58Mpa pressure, and the ethanol nearly all in catalytic bed can be converted into ethene.Through three sections conversion reactions step by step.The total ethanol transformation efficiency reaches 99.4%.
Transform temperature outs through three sections and reduce to 370 ℃, the logistics of pressure 0.53Mpa, after the vaporized alcohol device reclaimed heat, water-cooled to 45 ° was sent to the alkali cleaning drying.
Come the logistics of autoreaction workshop section to enter vapor-liquid separation tank 312.Separated liquid is pending waste liquid, sends to waste water processing station outside the battery limit (BL) by waste drains pump.Isolated gas major ingredient is an ethene, and contains light hydrocarbon component and heavy constituent, and compositions such as carbonic acid gas, acetic acid are called crude ethylene.After rare and the rare mixing of circulation second of thick second, enter the rare compressor 311 of second, rise to 1.98MPa, be cooled to 45 ℃ and enter soda-wash tower 31 through water cooler 313 by 0.39MPa from purification workshop section.
The purpose of alkali cleaning is removed carbonic acid gas and acetic acid exactly, is provided with soda-wash tower 31 for this reason.Soda-wash tower 31 is the packing tower of bed more than, and most of bed of packings reduces to below the 10ppm carbon dioxide content as carbonic acid gas in the alkali liquid washing crude ethylene.The top layer bed of packings is carried alkali lye secretly and is dripped to follow-up workshop section to prevent the crude ethylene gas phase as water coolant washing soda drop.
Adsorption dry ejects the crude ethylene that takes from soda-wash tower 31 and contains the equilibrium water, must remove, and be provided with the 3A molecular sieve is the moisture eliminator 321,322 of sorbent material for this reason, after the molecular sieve adsorption water saturation, can take off and inhale the reprocessing cycle use.The rare purification workshop section that sends into of thick second after drying.
The crude ethylene that adsorption dehumifier comes out is sent to ethylene chiller 425, reduce to-14 ℃ by 35 ℃, further be as cold as-36 ℃ through ethene deep freezer 427 again, and enter demethanizing tower 41, most of ethene is liquefied under this temperature, and contained light constituent is rushed to demethanizing cat head condenser 411 through the heating of demethanizer bottoms reboiler 412, ℃ low temperature is enough to microscale ethylene liquefaction has been reduced the loss that ethene is pulled away herein-67.And containing hydrogen, the light constituent of methane is drained from demethanizing cat head condenser 411, removes fuel cartridge 61 after heating up, and finally sends to ethanol process furnace 1 and makes fuel.The working pressure 1.8Mpa of demethanizing tower 41, epimere-50 ℃, hypomere-33 ℃.
The liquid ethylene that demethanizer bottoms reboiler 412 is discharged is sent into purification tower 42 at-31 ℃, with heavy constituent such as rejecting ethanes.Purification tower 42 is provided with five sections filling batch, service temperature-34 ℃, pressure 1.64Mpa.The heavy constituent such as ethane that discharge purification tower 42 bottoms drain into fuel cartridge 61 through tower bottom reboiler 422 heating, finally send to ethanol process furnace 1 and make fuel.And the liquid ethylene that purification tower 42 cats head are discharged is sent into ethene return tank 422 through purification overhead condenser 421.Ethene is except that the most of purity 99.8% of quantity of reflux with maintenance ethene as purification tower 42 in the return tank 422, a small amount of cold as demethanizing cat head condenser 411, remaining liquid ethylene is pressurized to 2Mpa through supercharger 426 after cold recovery, be qualified ethene finished product.
Be example with the production equipment of producing 1.5 ten thousand tons of ethene every year below, further describe the present invention, wherein raw material is an industrial alcohol product ethene purity 99.8%, and its technological process of production is seen Fig. 2.
The industrial alcohol temperature of delivering to the ethylene unit within battery limit is 20 ℃, pressure 0.1Mpa enters with the flow of 3732kg/h, at first enters ethanol well heater 21 through the pump pressurization and is heated to 159 ℃ of its boiling points, pass through ethanol evaporation device 22 again, be divided into three parts after further being heated to 300 ℃ to enter process furnace 1.
First gang of alcohol vapour flow 1381kg/h, after adding 2395kg/h middle pressure steam (195 ℃) mixing, temperature rises to 233 ℃, enters first heating zone 111 of ethanol process furnace 1 under 1.01Mda pressure, temperature is risen to 470 ℃ enter first reactor 112 and carry out catalyzed reaction.
Second gang of alcohol vapour flow 1530kg/h, then the reaction effluent with first reactor 112 mixes, and 339 ℃ of temperature, enters second heating zone 121 of ethanol process furnace 1 during pressure 0.86Mpa, also temperature is risen to 470 ℃, enter second reactor 122 at 0.73Mpa pressure and carry out catalyzed reaction.
The 3rd gang of alcohol vapour flow 821kg/h, then mix,, enter the 3rd heating zone 131 of ethanol process furnace 1 under the 0.66Mpa pressure at 349 ℃ with second reactor, 122 reaction effluents, temperature is risen to 475 °, under 0.58mpa pressure, enter the 3rd reactor 132.
What be worth particularly pointing out is: the weight percent that first strand of alcohol vapour, second strand of alcohol vapour, the 3rd strand of alcohol vapour account for whole alcohol vapour total amounts is respectively 32～38%, 38～50%, 18～24%, and preferred weight percent is 37%, 41%, 22%.The operation of ethanol process furnace, very crucial to the control of each section temperature of charge, the act of the success or failure of relevant this technology.The realization that interlocking system guarantees operation index must be set, as for adopting three-stage heating furnace, also be key point for this reason certainly.
It is inequality that three partial material enter the transformation efficiency that reactor reaction changes into ethene, and raises step by step.Press the reactor sequencing, transformation efficiency is followed successively by 75%, 82% and 99.4%, and ethanol conversion becomes the 3rd section outlet of purity of ethene to reach 40%, the purity 96.5% after being equivalent to dewater.
The about 6127kg/h of material by 132 generations of the 3rd reactor, under 375 ℃ and 0.53Mpa, pass through ethanol evaporation device 22, ethanol evaporation device 23,21 heat exchange of ethanol well heater one by one, temperature drops to 288 ℃, 174 ℃ and 138 ℃ one by one, generate condenser 14 through reaction again and reduce to 45 ℃ at last, and under 0.39Mpa, enter knockout drum 312.
The about 3982kg/h of vapor-liquid separation tank 312 isolated liquid, the liquid waste disposal station outside waste drains pump is delivered to the battery limit (BL).The gas phase major ingredient that vapor-liquid separation tank 312 is told is an ethene, also have heavy constituent such as light constituent such as carbonic acid gas, hydrogen, methane and ethane, by product one acetic acid that contains catalyzed reaction simultaneously, to the follow-up equipment pipeline be brought corrosion as not removing, need add caustic lye of soda for this reason and neutralize acetic acid.
Soda-wash tower 31 is one to have the packing tower of five sections beds, and the alkali lye of concentration 8% enters from soda-wash tower 31 middle parts (second and third section bed), washing crude ethylene gas from bottom to top.The about 2300kg/h crude ethylene of flow, the cyclic ethylene 190kg/h that sends here with purification workshop section demethanizing cat head condenser 411 mixes, boost to 1.93Mpa through ethylene compressor 311, be cooled to 95 ℃ through water cooler 313 and enter soda-wash tower 31 bottoms, through-, behind two, three, four sections fillers, carbon dioxide content is reduced to below the 10ppm in the gas.Alkali lye recycles by recycle pump 332 with the flow of 1840Kg/h, and constantly washing gas for replenishing the loss of alkali lye, replenishes 8% alkali lye 42kg/h to alkali lye storage tank 331 from the external world, and mends in the soda-wash tower 31 by alkali lye volume pump 33.Bring follow-up workshop section into for preventing that crude ethylene from dripping the alkali lye of carrying secretly, at the 5th bed filler place of soda-wash tower, add the process water of inbound traffics 1200Kg/h by technology water pump 34, washing is through the crude ethylene of alkali cleaning, and is cooled to 30 ℃.
Obviously the crude ethylene after washing is entrained with moisture, for preventing to freeze under the low temperature just must remove these moisture content, the moisture eliminator 321,322 that two 3A molecular sieves that use in parallel are made sorbent material is set again for this reason.Regeneration system rapidly can be set respectively,, will not give unnecessary details once more because of it is a common technology in the prior art.From the effusive crude ethylene 2300Kg/h of soda-wash tower cat head, enter the moisture eliminator dehydration.
Through the secondary cooling of ethylene chiller 425 and ethene deep freezer 427, temperature is reduced to-14 ℃ and-36 ℃ by 35 ℃ to dehydration crude ethylene 2300kg/h successively, and sends into demethanizing tower 41 again, to remove light constituent such as methane.Gas drops to-36 and spends time overwhelming majority ethene and be liquefied and can rely on gravity to flow into demethanizing tower 41, contained light constituent is evaporated at demethanizer bottoms reboiler 412 and rises to cat head, and low-87 degree that reach of demethanizing cat head condenser 411 temperature, this temperature is enough to most ethene condensations are not taken away by gas.Light constituent such as hydrogen, methane is then discharged from demethanizing cat head condenser 411, delivers to fuel cartridge 61 after combustion heater 62 reclaims cold, as the fuel use of ethanol process furnace 1.The liquid that remains at the bottom of the tower then rises to-31 ℃ and enter purification tower 42 from reboiler 412.
The effect of purification tower is that ethene is made last purification processing.After the operations such as crude ethylene process alkali cleaning, drying and demethanizing, remaining impurity is heavy constituent.Remove heavy constituent, the purity of ethene can reach the requirement of qualified finished product.Purification tower 42 also is provided with the filler of five sections beds, and at-34 ℃ to-17 ℃, 1.64Mpa pressure is operation down, and final rectifying goes out purity and reaches 99.8% ethene.And heavy constituent such as ethane sink to tower bottom, finally-17 ℃ of discharges, send to the fuel that fuel cartridge 61 is made process furnace 1 through intensification, and flow can reach 39.3Kg/h.Distilled product about 6320Kg/h in purification tower top flows into ethene return tank 423 through purification overhead condenser 421.The liquid ethylene one 4107Kg/h of portion is used for the backflow of purification tower 42 to improve the purity of ethene in the return tank 423, (190Kg/h) for the cold of demethanizing tower condenser 411 on a small quantity, and the residual current amount 2023Kg/h of institute liquid ethene reclaims colds and supercharger 426 through ethylene chiller 425 and is pressurized to 2.0Mpa and is final finished ethene.
In purification workshop section, use the refrigeration system of propylene as heat-eliminating medium.In the propylene tank 55 42 ℃, the propylene of 1.62Mp are cooled to-6 ℃ through 59 decompressions of one-level pressure reducer, 0.39Mpa flow is 10800Kg/h, after entering the air-breathing jar 60 of propylene secondary compression, part 7398Kg/h sends into second depressurized device 63, and another part 3402Kg/h directly enters propylene compressor 51 inlets.A propylene liquid part that enters second depressurized device 63 is used as purification overhead condenser 421 colds, propylene after the vaporization returns in the propylene holding tank 53, another part uses as the cold of ethene deep freezer 427, and the propylene after the vaporization directly enters propylene compressor 51 inlets behind propylene one-level air supply tank 52.The propylene of propylene compressor 51 outlets divides three parts to use, first part is as demethanizer bottoms reboiler 412 thermals source, enter propylene collector 54 after the liquefaction, return propylene tank 55, second section is as the thermal source of purification tower bottom reboiler 422, enter after the liquefaction in the propylene holding tank 57, return propylene tank 55; Third part directly enters in third rare storage tank 55 after third rare condenser 56 condensations.
Above-listed detailed description is specifying at one of the utility model possible embodiments, this embodiment is not in order to limit claim of the present utility model, allly do not break away from the equivalence that the utility model does and implement or change, all should be contained in the claim of this case.
Claims (10)
1. the production equipment of an ethanol preparation ethene, comprise vaporizer, soda-wash tower, moisture eliminator, demethanizing tower and purification tower, it is characterized in that: it also is provided with process furnace and first reactor, second reactor, the 3rd reactor and ethylene chiller, ethene deep freezer; Wherein the inlet section of vaporizer shell-side is by ethanol inlet outside the pipe connection battery limit (BL), its outlet section is first heating zone inlet of pipe connection process furnace respectively, second heating zone inlet and the 3rd heating zone inlet, medium pressure steam system pipe connection outside first heating zone inlet and the battery limit (BL), its outlet conduit connects first reactor inlet, the first reactor outlet pipe connection, second heating zone inlet, the second heating zone outlet conduit connects second reactor inlet, the second reactor outlet pipe connection the 3rd heating zone inlet, the 3rd heating zone outlet conduit connects the 3rd reactor inlet, the 3rd reactor outlet connects soda-wash tower charging layer through the evaporator tube side, the soda-wash tower top is by pipe connection moisture eliminator inlet, ethylene chiller shell-side inlet duct connects dryer export, its shell-side outlet connects demethanizing tower charging layer through the ethene deep freezer, demethanizer bottoms is by pipe connection purification tower charging layer, and the purification cat head connects the outlet of finished product ethene through ethylene chiller pipe side.
2. the production equipment of ethanol preparation ethene according to claim 1 is characterized in that: described demethanizing cat head connects the burner of described process furnace through combustion heater by pipeline.
3. the production equipment of ethanol preparation ethene according to claim 1, it is characterized in that: described purification tower push pipe road connects purification cat head condenser inlet, purification cat head condensator outlet connects the return tank top, connects described purification tower top, described methane top of tower and described ethylene chiller pipe side entrance respectively by pipeline at the bottom of the return tank.
4. the production equipment of ethanol preparation ethene according to claim 1 is characterized in that: described moisture eliminator is the mole sieve drier that uses in parallel.
5. the production technique of an ethanol preparation ethene, it is characterized in that: the feed ethanol outside the battery limit (BL) is divided into three strands after the vaporizer heating evaporation becomes alcohol vapour, first strand of alcohol vapour with enter first heating zone after middle pressure steam mixes and further enter first reactor reaction after the heating, resultant of reaction mixes with second strand of alcohol vapour after enter second reactor reaction after the heating of second heating zone, resultant of reaction mixes with the 3rd strand of alcohol vapour after enter the 3rd reactor reaction after the heating of the 3rd heating zone, resultant of reaction enters soda-wash tower decarbonation and acetic acid after vaporizer reclaims heat, the crude ethylene gas of cat head enters the cooling of ethylene chiller shell-side deep cooling after removing moisture through moisture eliminator, crude ethylene after the liquefaction enters demethanizing tower and removes methane, the liquid ethylene of demethanizer bottoms send purification tower to take off heavy constituent, and the ethene that the purification cat head is discharged send the outlet of finished product ethene after ethylene chiller pipe side draught heat heats up.
6. the production technique of ethanol preparation ethene according to claim 5 is characterized in that: the weight percent that first strand of alcohol vapour, second strand of alcohol vapour, the 3rd strand of alcohol vapour account for whole alcohol vapour total amounts is respectively 32～38%, 38～50%, 18～24%.
7. the production technique of ethanol preparation ethene according to claim 6 is characterized in that: the weight percent that first strand of alcohol vapour, second strand of alcohol vapour, the 3rd strand of alcohol vapour account for whole alcohol vapour total amounts is respectively 37%, 41%, 22%.
8. according to the production technique of claim 5,6 or 7 described ethanol preparation ethene, it is characterized in that: the light constituent that described demethanizing cat head is deviate from send process furnace to do fuel and uses.
9. according to the production technique of claim 5,6 or 7 described ethanol preparation ethene, it is characterized in that: the ethene that described purification cat head is discharged is gone in the ethene return tank through purification overhead condenser cooling liquefaction is laggard, the ethene at the jar end is divided into three parts, delivers to respectively and send the outlet of finished product ethene after purification trim the top of column, the backflow of demethanizing cat head and ethylene chiller pipe side draught heat heat up.
10. according to the production technique of claim 5,6 or 7 described ethanol preparation ethene, it is characterized in that: the temperature in of described first reactor, second reactor, the 3rd reactor is controlled to be 470 ℃, 470 ℃, 475 ℃ respectively.
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Cited By (8)
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| CN103121898A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Separating and recycling method of products containing ethylene |
| WO2013170752A1 (en) * | 2012-05-16 | 2013-11-21 | 中国石油化工股份有限公司 | Device and method for producing ethylene |
| CN113045372A (en) * | 2021-03-16 | 2021-06-29 | 天津大学 | Production process and device for preparing ethylene by ethanol dehydration |
| CN113429252A (en) * | 2021-06-15 | 2021-09-24 | 杭州制氧机集团股份有限公司 | Low-temperature purification device for ethylene |
| CN115055132A (en) * | 2022-06-15 | 2022-09-16 | 天津大学 | Production process and device for preparing ethylene by ethanol dehydration |
| CN115322068A (en) * | 2022-08-30 | 2022-11-11 | 天津大学 | Thermal coupling method and device for preparing ethylene by ethanol dehydration |
| CN115364821A (en) * | 2022-08-22 | 2022-11-22 | 和远潜江电子特种气体有限公司 | Preparation method of modified adsorbent and application of modified adsorbent in synthesis and purification of high-purity ethylene |
| WO2024050412A1 (en) * | 2022-08-28 | 2024-03-07 | Uop Llc | High temperature final dehydration reactor in dehydration process to prevent diethyl ether production |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103121898A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Separating and recycling method of products containing ethylene |
| CN103121898B (en) * | 2011-11-18 | 2015-04-08 | 中国石油化工股份有限公司 | Separating and recycling method of products containing ethylene |
| WO2013170752A1 (en) * | 2012-05-16 | 2013-11-21 | 中国石油化工股份有限公司 | Device and method for producing ethylene |
| US9738575B2 (en) | 2012-05-16 | 2017-08-22 | China Petroleum & Chemical Corporation | Apparatus for producing ethylene and a producing method thereof |
| CN113045372B (en) * | 2021-03-16 | 2022-01-28 | 天津大学 | Production process and device for preparing ethylene by ethanol dehydration |
| CN113045372A (en) * | 2021-03-16 | 2021-06-29 | 天津大学 | Production process and device for preparing ethylene by ethanol dehydration |
| CN113429252A (en) * | 2021-06-15 | 2021-09-24 | 杭州制氧机集团股份有限公司 | Low-temperature purification device for ethylene |
| CN113429252B (en) * | 2021-06-15 | 2024-09-27 | 杭氧集团股份有限公司 | Low-temperature purifying device for ethylene |
| CN115055132A (en) * | 2022-06-15 | 2022-09-16 | 天津大学 | Production process and device for preparing ethylene by ethanol dehydration |
| EP4293003A1 (en) * | 2022-06-15 | 2023-12-20 | Tianjin University | Preparation of ethylene by ethanol dehydration and device thereof |
| CN115364821A (en) * | 2022-08-22 | 2022-11-22 | 和远潜江电子特种气体有限公司 | Preparation method of modified adsorbent and application of modified adsorbent in synthesis and purification of high-purity ethylene |
| CN115364821B (en) * | 2022-08-22 | 2024-10-18 | 和远潜江电子特种气体有限公司 | Preparation method of modified adsorbent and application of modified adsorbent in synthesis and purification of high-purity ethylene |
| WO2024050412A1 (en) * | 2022-08-28 | 2024-03-07 | Uop Llc | High temperature final dehydration reactor in dehydration process to prevent diethyl ether production |
| CN115322068A (en) * | 2022-08-30 | 2022-11-11 | 天津大学 | Thermal coupling method and device for preparing ethylene by ethanol dehydration |
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