CN202131248U - Production equipment used for sec-butyl acetate - Google Patents
Production equipment used for sec-butyl acetate Download PDFInfo
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- CN202131248U CN202131248U CN201120220227U CN201120220227U CN202131248U CN 202131248 U CN202131248 U CN 202131248U CN 201120220227 U CN201120220227 U CN 201120220227U CN 201120220227 U CN201120220227 U CN 201120220227U CN 202131248 U CN202131248 U CN 202131248U
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Abstract
The utility model discloses production equipment used for sec-butyl acetate, which comprises a raw material hydrogenation device, an additive reaction device, a carbon-4 separation device, an azeotropic distillation device, an acetic acid recovering device and a rectification purification device; a liquid phase outlet of the raw material hydrogenation device is communicated with a material inlet of the additive reaction device; a material outlet of the additive reaction device is communicated with a material inlet of the carbon-4 separation device; a liquid phase outlet of the carbon-4 separation device is communicated with a material inlet of the azeotropic distillation device; a liquid phase outlet and a gas phase outlet of the azeotropic distillation device are respectively communicated with a material inlet of the acetic acid covering device and a material inlet of the rectification purification device; and a gas phase outlet of the acetic acid recovering device is communicated with the material inlet of the additive reaction device. The production equipment is used for the production of the sec-butyl acetate; the conversion rate of the raw material is high; the production control is flexible; products are completely separated with byproducts so that the production purity is high; and continuous production can be realized.
Description
Technical field
The utility model relates to a kind of production unit that is used to produce 2-butyl acetate.
Background technology
2-butyl acetate is as a kind of novel dissolvent, has characteristics such as hypotoxicity, dissolving power are strong, receives people's attention gradually, and the main production equipments of 2-butyl acetate has two kinds at present, i.e. tandem tubular fixed-bed reactor and catalytic rectifying tower.
The tandem tubular fixed-bed reactor is generally taked several reactors in series, and raw material gets into from first reactor drum, gradual reaction; Discharge from last reactor drum owing to have only an opening for feed, material one by one sequential flow through each reactor drum; Practical function is equivalent to one section staged reactor, when needing more catalyst changeout, needs whole parkings just can carry out; And causing aspect the proportioning raw materials in adjustment and to regulate slowly, cause producing that load is little, feed stock conversion is low, production control is dumb.Catalytic rectifying tower is provided with conversion zone at opening for feed, because the restriction of appointed condition, its catalyst filling amount is limited, and the raw material treatment capacity is little, throughput is low, and simultaneously, the residence time of material is less relatively, and transformation efficiency is low.
And in the process of using tubular fixed-bed device fabrication 2-butyl acetate; Many side reactions can inevitably take place: the butylene in the mixed c 4 raw material can generate carbon eight, carbon 12 components by polymerization reaction take place; Hydration reaction also can take place and generate alcohol in butylene, and can generate the littler acetates of part molecular weight, the purity that has reduced 2-butyl acetate of these side reactions; Its mid-boiling point is lower than the light constituent that is called of 2-butyl acetate, is higher than the heavy constituent that are called of 2-butyl acetate.Therefore in order to improve the quality of 2-butyl acetate, in the production, must the impurity that these side reactions produce be separated.The separation equipment for purifying of the secondary butyl ester of present Dichlorodiphenyl Acetate; A kind of is to adopt flashing apparatus, azeotropy rectification column and washing still; Earlier light constituent and the carbon four common flash distillations of reaction back are come out, then adopt azeotropy rectification column and washing still separating acetic acid, 2-butyl acetate, heavy constituent; Another kind of separation equipment for purifying is flashing apparatus and two azeotropy rectification columns, after carbon four flash distillations are come out after will reacting earlier, adopts twice azeotropic distillation to isolate acetic acid earlier, separates light constituent and 2-butyl acetate again.When adopting above first kind of separating device to separate the purification 2-butyl acetate, carbon four steams with light constituent jointly, because carbon four is gas phase under normal pressure; Light constituent is a liquid phase, and boiling point differs greatly, and purposes is also too wide in the gap; All have remainingly after two kinds of separating substances mutually, quality influences each other; When adopting above second kind of device separates purification 2-butyl acetate, adopt twice azeotropic distillation to increase the difficulty of operation, and add entrainer and can introduce more impurity, influence the purity of light constituent.
Butylene in the 2-butyl acetate synthesis material is mainly derived from the mixed c 4 behind the MTBE, and the 1,3-butadiene that wherein contains has very big spinoff in the production of 2-butyl acetate.Building-up reactions can take place and generate heavy constituent in 1,3-butadiene in 2-butyl acetate synthetic, reduce 2-butyl acetate product gas purity and yield, reduces economic benefit; And oligomerisation reaction also can take place on the esterifying catalyst surface, generation colloid, blocking catalyst duct, shortening life of catalyst in divinyl; Remaining few butadiene makes the quality of n-butene not reach synthetic requirement during esterification besides, and is prone to make catalyzer to reduce because of the coking inactivation.Do not have material carbon four pretreatment units in the existing 2-butyl acetate production unit, the 1,3-butadiene that causes existing in the mixed c 4 all causes bigger influence to esterification effect, quality product.
For butylene is fully reacted, require the raw material Glacial acetic acid min. 99.5 excessive in the 2-butyl acetate production process, therefore after esterification, need the product 2-butyl acetate purified from the mixture of excessive acetic acid and 2-butyl acetate.The separating device of two kinds of materials is a common rectifying tower generally speaking, utilizes the boiling point difference of two kinds of materials, the difference of relative volatility to separate through rectifying.But; Because boiling point 117 .9 ℃ (standard atmospheric pressure) of acetic acid differ too little with the boiling point 112.3 ℃ (standard atmospheric pressures) of 2-butyl acetate, relative volatility is near 1, therefore in order to reach good separating effect; Rectifying tower needs more theoretical plate number; Cause the increase of rectifying tower height, facility investment and energy consumption cost to increase, and separating effect is undesirable, influences quality product.The method of present widely used 2-butyl acetate and acetic acid separated is an azeotropic distillation; But; In actual production, find owing to reasons such as entrainments, still have the acetic acid of trace in the 2-butyl acetate product, because 2-butyl acetate uses as solvent; The acetic acid of this content still can cause certain corrosion to follow-up production unit, container, influences all bigger to production, equipment.
Summary of the invention
The utility model technical problem to be solved is: to the deficiency of prior art existence; A kind of material purity, transformation efficiency height are provided, and production control is flexible, product purification good separating effect; Quality product, purity height can realize that quantity-produced is used for the production unit of 2-butyl acetate.
For solving the problems of the technologies described above, the technical scheme of the utility model is:
A kind of production unit that is used for 2-butyl acetate; Comprise raw material hydrogenation reaction device, addition reaction device, carbon four tripping devices, azeotropic distillation device, acetic acid retrieving arrangement and rectification and purification device; The liquid phase outlet of said raw material hydrogenation reaction device is communicated with the material inlet of said addition reaction device; The material outlet of said addition reaction device is communicated with the material inlet of said carbon four tripping devices; The liquid phase outlet of said carbon four tripping devices is communicated with the material inlet of said azeotropic distillation device; The liquid phase outlet and the gaseous phase outlet of said azeotropic distillation device are communicated with the material inlet of said acetic acid retrieving arrangement and the material inlet of said rectification and purification device respectively, and the gaseous phase outlet of said acetic acid retrieving arrangement is communicated with the material inlet of said addition reaction device.
Wherein, Said raw material hydrogenation reaction device comprises feed preheater, hydrogenator and rectifying tower; The import of said hydrogenator is communicated with the outlet of said feed preheater; The outlet of said hydrogenator is communicated with the material inlet of said rectifying tower, and the liquid phase outlet of said rectifying tower is communicated with the material inlet of said addition reaction device, and the ingress of said hydrogenator is provided with the hydrogen feed pipeline.
The gaseous phase outlet of said rectifying tower is communicated with condensing surface and return tank successively, and said return tank is respectively equipped with return line and carbon four escape routes that are communicated with the refluxing opening of said rectifying tower.
Said addition reaction device comprises placed in-line three reactor drums each other at least; The said material outlet of placed in-line each reactor drum each other is communicated with the material inlet of next reactor drum; The liquid phase outlet of the rectifying tower of said raw material hydrogenation reaction device is communicated with the material inlet of the reactor drum that is positioned at series connection top; The material outlet that is positioned at the terminal reactor drum of mutual placed in-line series connection is communicated with the material inlet of said carbon four tripping devices; The ingress of said each reactor drum is provided with the pilot piping that each reactor drum is interconnected; Said pilot piping is equipped with by-pass valve control before each reactor drum, said each reactor drum is equipped with raw material from the mutual ingress of placed in-line second reactor drum and adds pipeline.
As a kind of preferred, said reactor drum is provided with placed in-line three each other.
As a kind of improvement; The material inlet place of said each reactor drum is provided with thermoswitch and mixing tank, and the liquid phase outlet of said rectifying tower or raw material are added pipeline, the material outlet of placed in-line each reactor drum is communicated with the material inlet of said mutual placed in-line next reactor drum through said thermoswitch and mixing tank each other.
As further improvement; The material outlet that is positioned at the terminal reactor drum of the series connection of mutual placed in-line reactor drum is provided with the material inlet that circulation line is communicated with the reactor drum that is positioned at series connection top; Said circulation line is provided with recycle pump, and the said material inlet place that is positioned at the reactor drum at series connection top is provided with the acetic acid feeding pipe.
Said carbon four tripping devices comprise carbon four knockout towers and the condensing surface and the return tank that are communicated with successively with the gaseous phase outlet of said carbon four knockout towers; The said material outlet that is positioned at the terminal reactor drum of mutual placed in-line series connection is communicated with the material inlet of said carbon four knockout towers; The outlet of said return tank is respectively equipped with the return line and carbon four escape routes of the refluxing opening that is communicated with said carbon four knockout towers, and the liquid phase outlet of said carbon four knockout towers is communicated with the material inlet of said azeotropic distillation device.
Said azeotropic distillation device comprises azeotropy rectification column and the condensing surface and the gun barrel that are communicated with successively with the gaseous phase outlet of said azeotropy rectification column; The liquid phase outlet of said carbon four knockout towers is communicated with the material inlet of said azeotropy rectification column; The liquid phase outlet of said azeotropy rectification column is communicated with the material inlet of said acetic acid retrieving arrangement; The oil phase outlet of said gun barrel is communicated with the material inlet of said rectification and purification device, and the water outlet and the oil phase outlet of said gun barrel are respectively equipped with the refluxing opening that return line is communicated with said azeotropy rectification column.
Said acetic acid retrieving arrangement comprises acetic acid treating tower and the condensing surface and the return tank that are communicated with successively with the gaseous phase outlet of said acetic acid treating tower; The outlet of the liquid phase of said azeotropy rectification column is communicated with the material inlet of said acetic acid treating tower, the outlet of said return tank be communicated with respectively said series connection top reactor drum material inlet and be communicated with the refluxing opening of said acetic acid treating tower through return line.
Said rectification and purification device comprises rectification and purification tower and the condensing surface and the return tank that are communicated with successively with the gaseous phase outlet of said rectification and purification tower; The oil phase outlet of said gun barrel is communicated with the material inlet of said rectification and purification tower; The sidewall of said rectification and purification tower is provided with the 2-butyl acetate outlet, and the outlet of said return tank is respectively equipped with return line and the light constituent escape route that is communicated with the refluxing opening of said rectification and purification tower.
Owing to adopted technique scheme, the beneficial effect of the utility model is:
1, the utility model is provided with raw material hydrogenation reaction device before the addition reaction device, through hydrogenation reaction, with 1 in the mixed c 4 raw material; The 3-divinyl changes into n-butene, has improved the active constituent content in the raw material, has improved conversion of raw material; The side reaction of having avoided 1,3-butadiene in synthetic, to take place has reduced the foreign matter content in the product; The purity and the yield of product 2-butyl acetate have been improved; Avoided the problem of divinyl, improved the catalytic activity of catalyzer, prolonged the work-ing life of catalyzer in the surperficial oligomerisation reaction that takes place of esterifying catalyst, generation colloid, blocking catalyst duct.
The addition reactor of the addition reaction device of the utility model is provided with placed in-line three each other, and the ingress of each reactor drum is provided with the pilot piping that each reactor drum is interconnected, and is equipped with raw material from the ingress of placed in-line second reactor drum each other and adds pipeline; According to the production needs; Such as catalyst changeout more or according to the transformation efficiency situation, through pilot piping can control wherein one participate in reaction to several reactor drums, production control is flexible; Can in each reactor drum of participating in reacting, add raw material through adding pipeline; Guarantee that every section reactor drum can both running at full capacity, improved output, and guaranteed feed stock conversion, product purity and yield.
The utility model is provided with carbon four tripping devices, azeotropic distillation device, acetic acid retrieving arrangement and rectification and purification device, earlier low-boiling carbon four components are come out through carbon four knockout tower rectifying separation after the addition reaction, and then the liquid phase that carbon four knockout towers are separated is through the azeotropy rectification column azeotropic distillation; The acetic acid of azeotropy rectification column liquid phase outlet goes to participate in addition reaction again after the refining purification of acetic acid treating tower, avoided the high problem that influences reaction conversion ratio and product purity of water-content in the acetic acid, and 2-butyl acetate, light constituent and part heavy constituent are gone rectification and purification tower rectification and purification after being steamed by the azeotropic distillation cat head; Light constituent is from the extraction of rectification and purification cat head; The product 2-butyl acetate obtains heavy constituent from the extraction of rectification and purification tower side wall at the bottom of the rectification and purification tower, can obtain four kinds of value products simultaneously; Separate thoroughly; And the carbon four-component heat enthalpy value of separating is high, can be used as the abrasive energy, and light constituent can be used as compound lard and is used as solvent etc.; Heavy constituent have gasoline, the similar component of diesel oil; Can be used as the oil product blender, the product 2-butyl acetate purity that obtains is high, and content can reach 99.5wt%.
2, the addition reaction device of the utility model is equipped with thermoswitch in the ingress of each reactor drum; The temperature of charge that guarantees every section reactor drum of entering is a desired reaction temperature; Help controlling proper reaction conditions, guaranteed reaction effect, and be communicated with the import of the reactor drum at the top that is positioned at said mutual placed in-line reactor drum through circulation line in the outlet of the terminal reactor drum of the series connection of mutual placed in-line reactor drum; On circulation line, be provided with recycle pump; According to the reaction conversion ratio situation, can control material and carry out circulating reaction, further improved feed stock conversion, product purity and yield.
3, the utility model is equipped with return line at the gun barrel of the return tank of rectifying tower, acetic acid treating tower, carbon four knockout towers and the rectification and purification tower of raw material hydrogenation reaction device, azeotropy rectification column and is communicated with the refluxing opening of said rectifying tower, acetic acid treating tower, carbon four knockout towers, azeotropy rectification column and rectification and purification tower; Through the gas-liquid two-phase mass-and heat-transfer, gas phase temperature and rectification effect have been regulated.
Description of drawings
Below in conjunction with accompanying drawing and embodiment the utility model is further specified.
Accompanying drawing is the structural representation of the utility model embodiment.
Among the figure, 1. raw material hydrogenation reaction device; 11. feed preheater; 12. hydrogenator; 13. rectifying tower; 14. hydrogen feed pipeline; 15. hydrogenation condensing surface; 16. hydrogenation return tank; 17. hydrogenating carbon four escape routes; 2. addition reaction device; 21. reactor drum; 22. pilot piping; 23. by-pass valve control; 24. raw material is added pipeline; 25. thermoswitch; 26. mixing tank; 27. circulation line; 28. recycle pump; 29. acetic acid feeding pipe; 3. carbon four tripping devices; 31. carbon four knockout towers; 32. carbon four separation condensers; 33. carbon four separates return tank; 34. carbon four separates carbon four escape routes; 4. azeotropic distillation device; 41. azeotropy rectification column; 42. azeotropic distillation condensing surface; 43. gun barrel; 5. acetic acid retrieving arrangement; 51. acetic acid treating tower; 52. acetic acid is made with extra care condensing surface; 53. acetic acid is made with extra care return tank; 6. rectification and purification device; 61. rectification and purification tower; 62. rectification and purification condensing surface; 63. rectification and purification return tank; 64. 2-butyl acetate outlet; 65. light constituent escape route.
Embodiment
As shown in the figure; A kind of production unit that is used for 2-butyl acetate; Comprise raw material hydrogenation reaction device 1, addition reaction device 2, carbon four tripping devices 3, azeotropic distillation device 4, acetic acid retrieving arrangement 5 and rectification and purification device 6; Said raw material hydrogenation reaction device 1 comprises feed preheater 11, hydrogenator 12 and rectifying tower 13; The import of said hydrogenator 12 is communicated with the outlet of said feed preheater 11, and the outlet of said hydrogenator 12 is communicated with the material inlet of said rectifying tower 13, and the ingress of said hydrogenator 12 is provided with hydrogen feed pipeline 14; The gaseous phase outlet of said rectifying tower 13 is communicated with hydrogenation condensing surface 15 and hydrogenation return tank 16 successively, and said hydrogenation return tank 16 is respectively equipped with return line and hydrogenating carbon four escape routes 17 that are communicated with the refluxing opening of said rectifying tower 13; Said addition reaction device 2 comprises placed in-line three reactor drums 21 each other; The said material outlet of placed in-line each reactor drum 21 each other is communicated with the material inlet of next reactor drum 21; The liquid phase outlet of said rectifying tower 13 is communicated with the material inlet of the reactor drum 21 that is positioned at series connection top; The ingress of said each reactor drum 21 is provided with the pilot piping 22 that each reactor drum 21 is interconnected; Said pilot piping 22 is equipped with by-pass valve control 23 before each reactor drum 21; Said each reactor drum 21 is equipped with raw material from the mutual ingress of placed in-line second reactor drum 21 and adds pipeline 24; The material inlet place that is positioned at the reactor drum 21 at series connection top is provided with acetic acid feeding pipe 29; The material inlet place of said each reactor drum 21 is provided with thermoswitch 25 and mixing tank 26; The liquid phase outlet that is positioned at acetic acid feeding pipe 29, the rectifying tower 13 at series connection top is communicated with the reactor drum 21 that is positioned at series connection top through mixing tank 26 and thermoswitch 25; Said raw material add pipeline 24, each other placed in-line second or the outlet of the material outlet of the 3rd reactor drum 21, said thermoswitch 25 be communicated with the material inlet of said mutual placed in-line next reactor drum 21 through mixing tank 26, the material outlet that is positioned at the terminal reactor drum 21 of the series connection of mutual placed in-line reactor drum 21 is provided with the material inlet that circulation line 27 is communicated with the reactor drum 21 that is positioned at series connection top, said circulation line 27 is provided with recycle pump 28; Said carbon four tripping devices 3 comprise that carbon four separation condensers 32 that carbon four knockout towers 31 and gaseous phase outlet with said carbon four knockout towers 31 are communicated with successively separate return tank 33 with carbon four; The material outlet that is positioned at the terminal reactor drum 21 of mutual placed in-line series connection is communicated with the material inlet of said carbon four knockout towers 31, and the return line that the outlet of said carbon four return tanks 33 is respectively equipped with the refluxing opening that is communicated with said carbon four knockout towers 31 separates carbon four escape routes 34 with carbon four; Said azeotropic distillation device 4 comprises azeotropy rectification column 41 and the azeotropic distillation condensing surface 42 and gun barrel 43 that are communicated with successively with the gaseous phase outlet of said azeotropy rectification column 41; The liquid phase outlet of said carbon four knockout towers 31 is communicated with the material inlet of said azeotropy rectification column 41, and the water outlet and the oil phase outlet of said gun barrel 43 are respectively equipped with the refluxing opening that return line is communicated with said azeotropy rectification column 41; Said acetic acid retrieving arrangement 5 comprises acetic acid treating tower 51 and the refining condensing surface 52 of acetic acid and the refining return tank 53 of acetic acid that are communicated with successively with the gaseous phase outlet of said acetic acid treating tower 51; The outlet of the liquid phase of said azeotropy rectification column 41 is communicated with the material inlet of said acetic acid treating tower 51, and the outlet of the refining return tank 53 of said acetic acid is communicated with the material inlet of reactor drum 21 at refluxing opening and the said series connection top of said acetic acid treating tower 51 respectively through return line; Said rectification and purification device 6 comprises rectification and purification tower 61 and the rectification and purification condensing surface 62 and rectification and purification return tank 63 that are communicated with successively with the gaseous phase outlet of said rectification and purification tower 61; The oil phase outlet of said gun barrel 43 is communicated with the material inlet of said rectification and purification tower 61; The sidewall of said rectification and purification tower 61 is provided with 2-butyl acetate outlet 64, and the outlet of the refining return tank 63 of said acetic acid is respectively equipped with return line and the light constituent escape route 65 that is communicated with the refluxing opening of said rectification and purification tower 61.
The principle of work of the utility model is: after feed preheater 11 preheatings of the at first incoming stock hydrogenation reaction device 1 of mixed c 4 raw material; Mix back entering hydrogenator 12 with hydrogen from hydrogen feed pipeline 14; In hydrogenator 12, carry out hydrogenation reaction; In the mixed c 4 raw material 1; The 3-divinyl changes into n-butene, and carbon four raw materials behind hydrogenation get into rectifying tower 13 and carry out rectifying, carbon four light constituents from the gaseous phase outlet extraction at rectifying tower 13 tops after get into hydrogenation return tank 16 after 15 condensations of hydrogenation condensing surface; Discharge through the outlet of return tank 16 bottoms then; Wherein most of gas phase temperature of in return line refluxes back rectifying tower 13, regulating in the rectifying tower 13, few part extraction is discharged as carbon fourth officer product from hydrogenating carbon four escape routes 17, and the n-butene after the rectification and purification discharges addition reaction device 2 from the outlet of rectifying tower 13 bottom liquid phases.
Raw material butylene after the hydrogenation reaction and the acetic acid that comes from acetic acid retrieving arrangement 5 or from the raw material acetic acid of acetic acid feeding pipe 29 at first after mixing tank 26 mixes; Be adjusted to the temperature of reaction that needs through thermoswitch 25; The import of the reactor drum of the series connection head end of certainly mutual placed in-line three reactor drums 21 gets into reactor drum 21 then; Under the effect of catalyst in reactor, carry out first order reaction; Material after the first order reaction is discharged from the reactor outlet 21 of the head end of connecting; Earlier through thermoswitch 25 be adjusted to reaction temperature required after, with add the adding the raw material butylene and get into mixing tank 26 jointly and mix of pipeline 24 from raw material after, get into each other and carry out second order reaction in placed in-line second reactor drum 21; Then the material after the second order reaction earlier through thermoswitch 25 be adjusted to reaction temperature required after; With add the adding the raw material butylene and get into mixing tank 26 jointly and mix of pipeline 24 from raw material after, get into and be positioned at the terminal reactor drum 21 of series connection and carry out third order reaction, the product after the third order reaction is discharged carbon elimination four tripping devices 3 from the material outlet that is positioned at the terminal reactor drum 21 of series connection; According to reaction conversion ratio situation ON cycle pump 28, the terminal reactor outlet 21 of the series connection material of the discharging reactor drum 21 that can self-circulation pipeline 27 be circulated back to the series connection head end participates in reacting once more certainly.According to reaction conversion ratio situation or reactor drum 21 inner catalyst catalytic capability situation or produce can not running at full capacity the time; Close the charging valve before any reactor drum 21; Open the by-pass valve control 23 on the pilot piping 22 before this reactor drum 21 then, make material get into next reactor drum 21 and react, do not participate in the more catalyst changeout or the maintenance of reactor drum 21 of reacting; Therefore under the situation of more catalyst changeout or maintenance; Can not stop each reactor drum 21 is carried out in turn, can not full production the time, also can select one of them or two reactor drums 21 reactions.
Material after the addition reaction gets into carbon four knockout towers 31, and vaporization separates in carbon four knockout towers 31, and lower boiling carbon four components are from the cat head extraction; After 32 condensations of carbon four separation condensers, get into carbon four and separate return tanks 33, part is separated carbon four escape routes 34 as carbon fourth officer product through carbon four and is discharged, and part is through return line carbon four knockout towers 31 that reflux back; Liquid phase discharges azeotropic distillation device 4 from the liquid phase outlet at the bottom of the tower; Material inlet from azeotropy rectification column 41 gets into, and separates through vaporization, and the liquid phase acetic acid that obtains at the bottom of the tower removes acetic acid retrieving arrangement 5; 2-butyl acetate, light constituent and part heavy constituent by azeotropy rectification column 41 top extraction after; The water separation tank 43 that after 42 condensations of azeotropic distillation condensing surface, deoils, through oily water separation, entrainer is discharged the azeotropy rectification column 41 that refluxes back from the water outlet of gun barrel 43; The oil phase partial reflux returns azeotropy rectification column 41, and remaining oil phase removes rectification and purification device 6.
After liquid phase acetic acid gets into acetic acid treating tower 51; Through refining rectifying; Acetic acid is discharged from gaseous phase outlet and after refining condensing surface 52 condensations of acetic acid, is got into the refining return tank 53 of acetic acid; Partial reflux returns acetic acid treating tower 51, and part goes addition reaction device 2 to participate in addition reaction, and useless acetic acid is discharged at the bottom of acetic acid treating tower 51 towers.
Oil phase from gun barrel 43 gets into from the material inlet of rectification and purification tower 61; Further rectification and purification; Light constituent gets into rectification and purification return tank 63 from the cat head extraction of rectification and purification tower 61 after 62 condensations of rectification and purification condensing surface, part is discharged through light constituent escape route 65 as the light constituent sub product; The product 2-butyl acetate is discharged through the 2-butyl acetate outlet 64 of rectification and purification tower 61 sidewalls, and heavy constituent were discharged from 61 ends of rectification and purification tower.
Claims (10)
1. production unit that is used for 2-butyl acetate; It is characterized in that: comprise raw material hydrogenation reaction device, addition reaction device, carbon four tripping devices, azeotropic distillation device, acetic acid retrieving arrangement and rectification and purification device; The liquid phase outlet of said raw material hydrogenation reaction device is communicated with the material inlet of said addition reaction device; The material outlet of said addition reaction device is communicated with the material inlet of said carbon four tripping devices; The liquid phase outlet of said carbon four tripping devices is communicated with the material inlet of said azeotropic distillation device; The liquid phase outlet and the gaseous phase outlet of said azeotropic distillation device are communicated with the material inlet of said acetic acid retrieving arrangement and the material inlet of said rectification and purification device respectively, and the gaseous phase outlet of said acetic acid retrieving arrangement is communicated with the material inlet of said addition reaction device.
2. the production unit that is used for 2-butyl acetate as claimed in claim 1; It is characterized in that: said raw material hydrogenation reaction device comprises feed preheater, hydrogenator and rectifying tower; The import of said hydrogenator is communicated with the outlet of said feed preheater; The outlet of said hydrogenator is communicated with the material inlet of said rectifying tower, and the liquid phase outlet of said rectifying tower is communicated with the material inlet of said addition reaction device, and the ingress of said hydrogenator is provided with the hydrogen feed pipeline.
3. the production unit that is used for 2-butyl acetate as claimed in claim 2; It is characterized in that: the gaseous phase outlet of said rectifying tower is communicated with condensing surface and return tank successively, and said return tank is respectively equipped with return line and carbon four escape routes that are communicated with the refluxing opening of said rectifying tower.
4. the production unit that is used for 2-butyl acetate as claimed in claim 2; It is characterized in that: said addition reaction device comprises placed in-line three reactor drums each other at least; The said material outlet of placed in-line each reactor drum each other is communicated with the material inlet of next reactor drum; The liquid phase outlet of the rectifying tower of said raw material hydrogenation reaction device is communicated with the material inlet of the reactor drum that is positioned at series connection top; The material outlet that is positioned at the terminal reactor drum of mutual placed in-line series connection is communicated with the material inlet of said carbon four tripping devices; The ingress of said each reactor drum is provided with the pilot piping that each reactor drum is interconnected, and said pilot piping is equipped with by-pass valve control before each reactor drum, and said each reactor drum is equipped with raw material from the mutual ingress of placed in-line second reactor drum and adds pipeline.
5. the production unit that is used for 2-butyl acetate as claimed in claim 4; It is characterized in that: the material inlet place of said each reactor drum is provided with thermoswitch and mixing tank, and the liquid phase outlet of said rectifying tower or raw material are added pipeline, the material outlet of placed in-line each reactor drum is communicated with the material inlet of said mutual placed in-line next reactor drum through said thermoswitch and mixing tank each other.
6. the production unit that is used for 2-butyl acetate as claimed in claim 4; It is characterized in that: the material outlet that is positioned at the terminal reactor drum of the series connection of mutual placed in-line reactor drum is provided with the material inlet that circulation line is communicated with the reactor drum that is positioned at series connection top; Said circulation line is provided with recycle pump, and the said material inlet place that is positioned at the reactor drum at series connection top is provided with the acetic acid feeding pipe.
7. the production unit that is used for 2-butyl acetate as claimed in claim 4; It is characterized in that: said carbon four tripping devices comprise carbon four knockout towers and the condensing surface and the return tank that are communicated with successively with the gaseous phase outlet of said carbon four knockout towers; The said material outlet that is positioned at the terminal reactor drum of mutual placed in-line series connection is communicated with the material inlet of said carbon four knockout towers; The outlet of said return tank is respectively equipped with the return line and carbon four escape routes of the refluxing opening that is communicated with said carbon four knockout towers, and the liquid phase outlet of said carbon four knockout towers is communicated with the material inlet of said azeotropic distillation device.
8. the production unit that is used for 2-butyl acetate as claimed in claim 7; It is characterized in that: said azeotropic distillation device comprises azeotropy rectification column and the condensing surface and the gun barrel that are communicated with successively with the gaseous phase outlet of said azeotropy rectification column; The liquid phase outlet of said carbon four knockout towers is communicated with the material inlet of said azeotropy rectification column; The liquid phase outlet of said azeotropy rectification column is communicated with the material inlet of said acetic acid retrieving arrangement; The oil phase outlet of said gun barrel is communicated with the material inlet of said rectification and purification device, and the water outlet and the oil phase outlet of said gun barrel are respectively equipped with the refluxing opening that return line is communicated with said azeotropy rectification column.
9. the production unit that is used for 2-butyl acetate as claimed in claim 8; It is characterized in that: said acetic acid retrieving arrangement comprises acetic acid treating tower and the condensing surface and the return tank that are communicated with successively with the gaseous phase outlet of said acetic acid treating tower; The outlet of the liquid phase of said azeotropy rectification column is communicated with the material inlet of said acetic acid treating tower, the outlet of said return tank be communicated with respectively said series connection top reactor drum material inlet and be communicated with the refluxing opening of said acetic acid treating tower through return line.
10. the production unit that is used for 2-butyl acetate as claimed in claim 8; It is characterized in that: said rectification and purification device comprises rectification and purification tower and the condensing surface and the return tank that are communicated with successively with the gaseous phase outlet of said rectification and purification tower; The oil phase outlet of said gun barrel is communicated with the material inlet of said rectification and purification tower; The sidewall of said rectification and purification tower is provided with the 2-butyl acetate outlet, and the outlet of said return tank is respectively equipped with return line and the light constituent escape route that is communicated with the refluxing opening of said rectification and purification tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120220227U CN202131248U (en) | 2011-06-27 | 2011-06-27 | Production equipment used for sec-butyl acetate |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120220227U CN202131248U (en) | 2011-06-27 | 2011-06-27 | Production equipment used for sec-butyl acetate |
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| CN202131248U true CN202131248U (en) | 2012-02-01 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201120220227U Expired - Fee Related CN202131248U (en) | 2011-06-27 | 2011-06-27 | Production equipment used for sec-butyl acetate |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102276452A (en) * | 2011-06-27 | 2011-12-14 | 潍坊亿兴化工科技有限公司 | Production equipment for sec-butyl acetate |
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2011
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102276452A (en) * | 2011-06-27 | 2011-12-14 | 潍坊亿兴化工科技有限公司 | Production equipment for sec-butyl acetate |
| CN102276452B (en) * | 2011-06-27 | 2013-09-04 | 潍坊亿兴化工科技有限公司 | Production equipment for sec-butyl acetate |
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