CN101423450B - Method for separating carbon 5 fraction by NMP method and one-stage extraction and rectification - Google Patents
Method for separating carbon 5 fraction by NMP method and one-stage extraction and rectification Download PDFInfo
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- CN101423450B CN101423450B CN2007101765829A CN200710176582A CN101423450B CN 101423450 B CN101423450 B CN 101423450B CN 2007101765829 A CN2007101765829 A CN 2007101765829A CN 200710176582 A CN200710176582 A CN 200710176582A CN 101423450 B CN101423450 B CN 101423450B
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Abstract
The invention discloses a method for separating C5 fraction through first-stage extraction rectification by a NMP method. The method comprises the steps of dehydrogenation, dimerization reaction, deheavy, extraction rectification, steam stripping and refining, wherein isopentane is utilized to take most of acetylene hydrocarbon away from the tower top in the dehydrogenation step; and a mixed solvent of NMP and a saline solution is adopted as an extracting agent in the step of extraction rectification. The method improves the extracting agent, increases the selectivity of the extracting agent, cancels a two-stage extraction rectification unit, and reduces the using amount and the regeneration amount of the solvent, thereby reducing operating cost.
Description
Technical field
The present invention relates to a kind of separation method of C5 fraction; More particularly; The present invention relates to the method for a kind of mixed solvent with NMP (N-methyl pyrrolidone, N-Methyl pyrrolidone) and salts solution as the separating carbon 5 fraction by one-stage extraction and rectification of extraction agent.
Background technology
C5 fraction is the important co-product of ethylene producing device, and wherein isoprene, cyclopentadiene and m-pentadiene etc. all are the important source material of organic chemical industry and fine chemistry industry.Along with the development of petrochemical complex, the separation of C5 fraction and utilization are significant to the economy of making rational use of resources, improve ethylene unit.Not only boiling point is close for each component in the cracked C 5 fraction, also can form two components and three component azeotropes each other, adopts common distillatory method to be difficult to obtain high purity product.Separating technology generally adopts solvent to come separating isoprene, m-pentadiene and cyclopentadiene etc. through extracting rectifying, and solvent commonly used in the industry has acetonitrile (ACN), N (DMF), N-Methyl pyrrolidone (NMP) etc.
The acetonitrile extraction process is called for short the ACN method, is the external C that extensively adopts
5One of cut separation method.The characteristics of acetonitrile method are that the source is abundant, cheap, and are little to equipment corrosion.Because acetonitrile viscosity is low, so the plate efficiency of extraction distillation column is higher.Because boiling point is low, make system temperature lower simultaneously, can save energy consumption.The shortcoming of acetonitrile method is that solvent selectivity is lower, requires number of theoretical plate higher, and reflux ratio is bigger, though the low energy consumption that can make of boiling point is lower, also makes product carry little solvent secretly simultaneously, needs washing.The DMF method is claimed the GPI method again, is developed in 1971 by Nippon Zeon Co., Ltd. the earliest.The shortcoming of DMF method is that solvent stability is relatively poor, and very easily hydrolysis, thermal capacitance are high, boiling point is high.And the toxicity of DMF is higher relatively, and health of operators is had the potential detrimentally affect.The NMP method is succeeded in developing by German BASF AG.Compare other solvents, NMP has better choice property and to the dissolving power of diolefine, can be well isoprene and cyclopentadiene, alkynes etc. is separated; Required number of theoretical plate is few; Stability better can suppress hydrolysis preferably, thereby because boiling point height solvent-oil ratio is less than other solvents; And do not form azeotrope with water, waste water is easy to biochemical treatment.
Butadiene and isoprene from naphtha cracking for ethylene [the oil and gasjournal; 1967,65 (2): 98～104] disclose NMP method carbon five separating technologies of BASF AG, the cracking c5 cut at first gets into the prewashing tower; Wash with NMP; From cyclopentadiene, the m-pentadiene of cat head sidepiece extraction, butine etc. are difficult for dissolved constituent and get into water wash column, after washing, discharge.Prewashing top of tower material gets into extraction distillation column, and the top steams pentane, amylene, and still liquid gets into stripping tower; Stripping tower bottom solvent and water etc. send solvent recovery tower; Recycle after treatment, stripping tower steams thing and sends extractive distillation column back to, by stripping tower middle part side line extraction isoprene material; After the water wash column washing, send into the isoprene rectifying tower, obtain purity at the isoprene more than 97% by the rectifying tower top.This process using prewashing and extracting rectifying two-section extraction rectification process, flow process is longer, complicated operation.
It is the two-section extraction rectification process of extraction agent that existing C5 fraction separating technology is mainly with DMF, and every section comprises extracting rectifying and stripping.C5 fraction is introduced into pretreatment unit, and pretreatment unit comprises and takes off light, dimerization reaction in advance, takes off heavy three parts in advance.C5 fraction removes most of low boiling component in the raw material in taking off with light packs putting in advance; Get into dipolymer reactor then; In this most of cyclopentadiene dimerization is NSC 7352, dimerisation products get into again taking off in advance the refitting put, isoprene and m-pentadiene, NSC 7352 are carried out initial gross separation.Weight-removing column cat head material gets into first extractive distillation column in advance; The extracting rectifying column overhead is isolated alkane and monoolefine as raffinate; Isoprene and solvent get into first stripping tower; The C5 fraction that stripping goes out gets into weight-removing column, further separates with m-pentadiene, NSC 7352 at this isoprene.Thick isoprene gets into the second extracting rectifying unit; Remove wherein a spot of cyclopentadiene and alkynes; The isoprene of the second extracting rectifying cat head gets into the further refining qualified polymerization grade isoprene product that obtains of lightness-removing column; The solvent of extractive distillation column still gets into second stripping tower and the vacuum stripper of back and carries out stripping, isolated solvent recycled utilization.Material from preparatory weight-removing column and weight-removing column still is sent to m-pentadiene and NSC 7352 refined unit.Existing C5 fraction separation process is longer, and the table of equipment number is many, complicated operation.
In order to improve existing C5 fraction separation process, each research unit has carried out a large amount of research, has obtained certain progress.
CNl412165 discloses and has a kind ofly removed alkynes, C 5 diene in the five fractions of petroleum cracked carbon and other component are carried out isolating one-section abstraction rectification technique for the choice of Solvent catalytic hydrogenation process with DMF.Its characteristics are, before carbon five materials carry out extracting and separating, remove alkynes wherein through selective catalytic hydrogenation technology earlier, remove micro-cyclopentadiene through reactive distillation again.This technology has been saved second section extracting rectifying, has been simplified solvent recovery unit, has reduced investment cost, process cost and energy consumption, has reduced production cost.But because the selectivity of solvent DMF is limited, when recycle ratio is bigger for the unitary solvent of catalytic distillation, and process cost is higher.And owing in technology, adopted catalyzed reaction, quality product can receive Effect on Performance such as catalyst activity, selectivity, and the production cycle also can receive the restriction of catalyst life.
It is the employing reactive distillation of solvent and the method that the selective catalytic hydrogenation process integration comes separating cracked carbon-5 fraction with DMF that CN1490286 discloses a kind of.Pass through reactive distillation process; Saved the hot dipolymer reactor of common employing, removed alkynes, alkynes has been removed before extracting rectifying through selective catalytic hydrogenation technology; Saved the common second section extracting rectifying that adopts; Shorten whole process flow, reduced facility investment and process cost, reduced production cost.Though the separation process of C5 fraction is simplified in this invention, owing to adopted catalytic hydrogenation reaction, there is the problem that operational cycle of quality product and device limits by catalyst performance equally.
In sum, existing technology exists problems such as solvent selectivity is relatively poor, flow process is complicated, operational difficulty.
Summary of the invention
The present invention is complicated for the flow process that solves existing C5 fraction separating process existence, the problem of operational difficulty; In order to improve extraction agent, to improve selection of Extractant property, proposed to do the C5 fraction one-section abstraction rectifying separation technology of extraction agent with the mixed solvent that contains NMP.
Concrete technical scheme is following:
The separation method of mixing C5 fraction one-section abstraction of the present invention rectifying may further comprise the steps:
(1) take off gently: will mix C5 fraction and send into lightness-removing column, the light constituent that will comprise carbon four components, iso-pentane and most of alkynes is from the cat head extraction; The material that comprises isoprene, cyclopentadiene and m-pentadiene is drawn from the tower still;
(2) dimerization reaction: described lightness-removing column tower still material is sent into dipolymer reactor carry out dimerization reaction, make cyclopentadiene generation dimerization reaction wherein generate NSC 7352, the transformation efficiency of cyclopentadiene reaches more than 85%;
(3) take off heavily: described material through the dipolymer reactor reaction is sent into weight-removing column, and the light constituent that comprises isoprene, pentane, amylene is from the cat head extraction; The heavy constituent that mainly comprise m-pentadiene, cyclopentadiene and NSC 7352 are sent to m-pentadiene and NSC 7352 refined unit from the extraction of tower still;
(4) extracting rectifying: the weight-removing column overhead fraction that will comprise isoprene, pentane, amylene is introduced extractive distillation column; In the presence of the solvent that contains N-Methyl pyrrolidone (NMP), carry out extracting rectifying; The component that comprises pentane, amylene is from the cat head extraction; The solvent material that is rich in isoprene is sent into stripping tower from the extraction of tower still; The solvent of the described NMP of containing is the mixed solvent of NMP and salts solution, and the volume ratio of NMP and salts solution is (100～1000): 1; Described solvent gets into described extractive distillation column from cat head;
(5) stripping: the solvent material that is rich in isoprene that obtains from extracting rectifying Tata still carries out the stripping separation stripping tower; The material that comprises isoprene and a small amount of cyclopentadiene, m-pentadiene is from the cat head extraction; Solvent loops back extractive distillation column from the extraction of tower still; The preferred little solvent regeneration unit that desolvates of extracting out, most of solvent directly recycles after reclaiming heat;
(6) refining: as will to introduce the isoprene treating tower by the material that comprises isoprene that described stripping tower cat head obtains; Isoprene is thoroughly separated with wherein a small amount of m-pentadiene, cyclopentadiene, NSC 7352; From the qualified polymerization grade isoprene of cat head extraction, tower still material is sent to m-pentadiene and NSC 7352 refined unit.
In the lightness-removing column of the step (1) of method of the present invention; Lower boiling carbon four components and iso-pentane are from the cat head extraction; Utilize iso-pentane and alkynes to form the principle of azeotrope, the most alkynes in the C5 fraction also will be with iso-pentane from the cat head extraction, and the recovery of cat head alkynes is more than 99%.
In the method for the invention, described solvent is the mixed solvent of NMP (N-Methyl pyrrolidone) and salts solution; Preferred described salts solution is the aqueous solution of an alkali metal salt, and salt proportion in solution is 0.1～30% (mass percent).Wherein, described an alkali metal salt can be NaCl, KCl, NaSCN, KSCN, CH
3COOK etc.
Preferably in described step (2), described dipolymer reactor is a tubular reactor, in baffle is housed.In this reactor drum, the cyclopentadiene dimerization is a NSC 7352, and dimerization reaction is thermopositive reaction, and more preferably reaction conditions is: pressure 0.8～1.6MPa, 60～120 ℃ of temperature.
Preferably in described step (3), described weight-removing column is a reaction fractionating tower, and cyclopentadiene dimerization reaction takes place in tower generates NSC 7352, and the total conversion rate of cyclopentadiene reaches more than 98%.
The number of theoretical plate of preferred described weight-removing column is 100～150, and working pressure is 0.3～0.4MPa, and tower top temperature is 65～75 ℃, and tower still temperature is 95～105 ℃, and reflux ratio is 10～20.
Preferably in described step (4), the number of theoretical plate of described extractive distillation column is 70～120.
Preferably in described step (4), described solvent gets into described extractive distillation column from cat head, and described solvent is 1～8 with the mass ratio of the material that gets into extractive distillation column.
Preferably in described step (6); Described isoprene treating tower is a reaction fractionating tower; There is not the cyclopentadiene of complete reaction to continue to take place dimerization reaction generation NSC 7352; The NSC 7352 that the cyclopentadiene dimerization reaction generates is from the extraction of tower still, and cyclopentadiene concentration is reduced to below the 1ppm in the isoprene product that cat head obtains.
The method of the separating carbon 5 fraction by one-stage extraction and rectification that the present invention proposes has following characteristics:
(1) in the prior art to adopt DMF be extraction agent more, and DMF meets water and is prone to take place hydrolysis and generates acid, and the mixed solvent that adopts NMP and salts solution among the present invention is as extraction agent, thereby avoided because of problems such as equipment corrosion that the solvent hydrolysis produces, obstructions;
(2) mixed solvent that adopts NMP and salt solvent among the present invention is as extraction agent; After adding salts solution; The relative volatility of carbon five each components in NMP further increases; The selectivity of mixed solvent strengthens, thereby can reduce the unitary solvent of the extracting rectifying consumption of circulating solvent when greatly, reduces process cost;
(3) boiling point of NMP is high, and solvent-oil ratio is little, and does not form azeotrope with water, and waste water is easy to biochemical treatment;
(4) utilize iso-pentane and alkynes to form the principle of azeotrope; Before extracting rectifying, just the alkynes in the C5 fraction is removed, thereby cancelled the two-stage extraction rectifying in the existing procedure, reduced number of devices; Therefore simplify flow process greatly, reduced facility investment;
(5) owing to cancelled the two-stage extraction rectification cell among the present invention, reduced solvent usage quantity and regeneration amount, thereby reduced process cost;
(6) in carbon five tripping devices in order to ensure safety, need the concentration of alkynes in the gear, alkynes promptly is removed taking off light unit among the present invention, thereby has strengthened the security and the stability of device operation greatly;
(7) do not need catalyzer in the one-section abstraction rectification process of the present invention, thereby make the quality of operation and the product of device can avoid the influence and the restriction of catalyst performance;
(8) in the one-section abstraction rectification process of the present invention; M-pentadiene, cyclopentadiene and the NSC 7352 of the overwhelming majority are sent to m-pentadiene and NSC 7352 refined unit from the extraction of tower still; Thereby reduced the load of extracting rectifying unit and isoprene refined unit, reduced facility investment and process cost.
Description of drawings
Fig. 1 is the schematic flow sheet of NMP method separating carbon 5 fraction by one-stage extraction and rectification method of the present invention.
1 lightness-removing column; 2 dipolymer reactors; 3 weight-removing columns; 4 extractive distillation columns; 5 stripping towers; 6 isoprene treating towers; The 7C5 raw material; 8 light constituents; 9 heavy constituent; 10 raffinates; 11 solvents; 12 isoprene products; 13 heavy constituent.
Embodiment
Further explain method of the present invention with reference to figure 1 below, but the present invention is not limited to this.
Separating carbon 5 fraction by one-stage extraction and rectification method of the present invention may further comprise the steps:
(1) takes off gently: mix C5 fraction raw material 7 and (mainly consist of carbon 4 8.4%, pentane 11.6%, amylene 19.2; Alkynes 0.2%, isoprene 21.4%, cyclopentadiene 17.2%; M-pentadiene 13.9%, carbon 6 8.1%) get into lightness-removing column 1, light constituents 8 such as most alkynes, carbon four and iso-pentane are from the cat head extraction; Alkynes is 99.7% in the recovery of cat head, and lightness-removing column still material is sent to dipolymer reactor 2.The number of theoretical plate of lightness-removing column is 120, and operating reflux ratio is 16, and the content of control lightness-removing column cat head isoprene is 1%, and iso-pentane is 95% in the recovery of cat head.
(2) dimerization reaction: the material from the lightness-removing column still is sent to dipolymer reactor 2; At this cyclopentadiene generation dimerization reaction; Reaction conditions is: 90 ℃ of temperature of reaction, pressure 1.2MPa, and the transformation efficiency of cyclopentadiene is 85%, the concentration of cyclopentadiene is 3% in the reaction product.
(3) take off heavily: reaction product step 2) is sent to weight-removing column 3; At this; Heavy constituent such as m-pentadiene, NSC 7352 separate with isoprene; Be sent to m-pentadiene and NSC 7352 refined unit from the extraction of tower still, m-pentadiene and cyclopentadiene reach more than 99.5% in the recovery of tower still, and light constituents such as isoprene are sent to extractive distillation column 4 from the cat head extraction.The number of theoretical plate of weight-removing column is 100, and operating reflux ratio is 20, and the control weight-removing column cat head isoprene recovery is 99.5%, and m-pentadiene and cyclopentadiene, NSC 7352 are 99% in the recovery of tower still.
(4) extracting rectifying: solvent for use is the mixed solvent of the NMP and the NaSCN aqueous solution, and the volume ratio of NMP and salts solution is 500: 1, and the concentration of salt is 15% (mass percent) in the salts solution; Mixed solvent injects from the extracting rectifying top of tower, and C5 fraction is sprayed, and the number of theoretical plate of extractive distillation column is 100; Operational condition is: solvent ratio 5; 49.6 ℃ of tower top temperatures, tower top pressure 0.19MPa, reflux ratio 4; From the cat head extraction, the solvent material that is rich in isoprene is from the extraction of tower still as raffinate 10 for indissoluble such as pentane, amylene component.
(5) stripping: the tower still solvent material that step 4) obtains is sent to stripping tower 5, and hydro carbons such as isoprene are sent to isoprene treating tower 6 from the cat head extraction, and solvent 11 is sent to the extractive distillation column recycle from the extraction of tower still.The number of theoretical plate of stripping tower is 25, and operating reflux ratio is 2,40 ℃ of tower top temperatures.
(6) refining: at this; NSC 7352 continues that dimerization reaction all takes place and generates NSC 7352; Isoprene thoroughly separates with m-pentadiene, cyclopentadiene and NSC 7352 etc.; Obtain the polymerization grade isoprene product at cat head, the heavy constituent of tower still are sent to m-pentadiene and NSC 7352 refined unit.The number of theoretical plate of treating tower is 130, and operating reflux ratio is 10; The product of polymerization grade isoprene is formed as shown in table 1.
Table 1 polymerization grade isoprene product is formed
| Component | Content (wt) |
| Isoprene alkane and the total alkynes m-pentadiene of monoolefine isoprene dipolymer cyclopentadiene thiocarbonyl group compound | ≥99.3％ ＜0.6％ ＜0.1％ ＜50ppm ＜80ppm 1ppm ＜5ppm ＜10ppm |
Claims (9)
1. separation method that mixes the rectifying of C5 fraction one-section abstraction, it may further comprise the steps:
(1) take off gently: will mix C5 fraction and send into lightness-removing column, the light constituent that will comprise carbon four components, iso-pentane and most of alkynes is from the cat head extraction; The material that comprises isoprene, cyclopentadiene and m-pentadiene is drawn from the tower still;
(2) dimerization reaction: described lightness-removing column tower still material is sent into dipolymer reactor carry out dimerization reaction, make cyclopentadiene generation dimerization reaction wherein generate NSC 7352, the transformation efficiency of cyclopentadiene reaches more than 85%;
(3) take off heavily: described material through the dipolymer reactor reaction is sent into weight-removing column, and the light constituent that comprises isoprene, pentane, amylene is from the cat head extraction; The heavy constituent that comprise m-pentadiene, cyclopentadiene and NSC 7352 are sent to m-pentadiene and NSC 7352 refined unit from the extraction of tower still;
(4) extracting rectifying: the weight-removing column overhead fraction that will comprise isoprene, pentane, amylene is introduced extractive distillation column; In the presence of the solvent that contains N-Methyl pyrrolidone (NMP), carry out extracting rectifying; The component that comprises pentane, amylene is from the cat head extraction; The solvent material that is rich in isoprene is sent into stripping tower from the extraction of tower still; The solvent of the described NMP of containing is the mixed solvent of NMP and salts solution, and the volume ratio of NMP and salts solution is (100～1000): 1;
(5) stripping: the solvent material that is rich in isoprene that obtains from extracting rectifying Tata still separates stripping tower, and the material that comprises isoprene and a small amount of cyclopentadiene, m-pentadiene is from the cat head extraction, and solvent loops back extractive distillation column from the extraction of tower still;
(6) refining: as will to introduce the isoprene treating tower by the material that comprises isoprene that described stripping tower cat head obtains; Isoprene is thoroughly separated with wherein a small amount of m-pentadiene, cyclopentadiene, NSC 7352; From the qualified polymerization grade isoprene of cat head extraction, tower still material is sent to m-pentadiene and NSC 7352 refined unit.
2. method according to claim 1 is characterized in that: said salts solution is the aqueous solution of an alkali metal salt, and described salt shared mass percent in solution is 0.1～30%.
3. method according to claim 1 is characterized in that: in described step (2), described dipolymer reactor is a tubular reactor, in baffle is housed.
4. method according to claim 3 is characterized in that: in described dipolymer reactor, the cyclopentadiene dimerization is a NSC 7352, and reaction conditions is: pressure 0.8～1.6MPa, 60～120 ℃ of temperature.
5. method according to claim 1 is characterized in that:
Described weight-removing column is a reaction fractionating tower, and cyclopentadiene dimerization reaction takes place in tower generates NSC 7352, and the total conversion rate of cyclopentadiene reaches more than 98%.
6. method according to claim 1; It is characterized in that: in described step (3), described weight-removing column is a reaction fractionating tower, and its number of theoretical plate is 100～150; Working pressure is 0.3～0.4MPa; Tower top temperature is 65～75 ℃, and tower still temperature is 95～105 ℃, and reflux ratio is 10～20.
7. method according to claim 1 is characterized in that: in described step (4), the number of theoretical plate of described extractive distillation column is 70～120.
8. method according to claim 1 is characterized in that: in described step (4), described solvent gets into described extractive distillation column from cat head, and described solvent is 1～8 with the mass ratio of the material that gets into extractive distillation column.
9. method according to claim 1; It is characterized in that; In described step (6), described isoprene treating tower is a reaction fractionating tower, does not have the cyclopentadiene of complete reaction to continue to take place dimerization reaction generation NSC 7352; The NSC 7352 that the cyclopentadiene dimerization reaction generates is from the extraction of tower still, and the concentration of cyclopentadiene is less than 1ppm in the isoprene product that cat head obtains.
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| CN102336625A (en) * | 2010-07-28 | 2012-02-01 | 中国石油化工股份有限公司 | NMP mixed solvent extraction method of butadiene |
| CN102850158B (en) * | 2011-06-29 | 2014-12-31 | 中国石油化工股份有限公司 | Mixed solvent for C5 separation |
| CN107001187A (en) | 2014-12-18 | 2017-08-01 | 沙特基础工业全球技术有限公司 | Extracted using the isoprene of the C5 raw materials of reservation |
| CN111099951B (en) * | 2018-10-25 | 2024-01-23 | 中国石油化工股份有限公司 | Method for comprehensively utilizing light carbon five |
| CN111320520B (en) * | 2018-12-14 | 2024-01-23 | 中国石油化工股份有限公司 | Extractive distillation tower for butadiene separation and separation method |
| CN114853573B (en) * | 2022-05-27 | 2023-06-13 | 辽宁石油化工大学 | Separation and purification method and system for 1, 4-butanediol |
| CN114853571B (en) * | 2022-05-27 | 2023-06-13 | 辽宁石油化工大学 | Production process and system of 1, 4-butanediol |
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| SU653244A1 (en) * | 1974-05-13 | 1979-03-25 | Предприятие П/Я В-8585 | Method of separating mixtures of c5 hydrocarbons of different saturation degree |
| CN1412165A (en) * | 2001-10-12 | 2003-04-23 | 中国石油化工股份有限公司 | Separation method of cracked C5 fraction |
| CN1490286A (en) * | 2002-10-16 | 2004-04-21 | 中国石油化工股份有限公司 | Separating method for cracking C5-fraction |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU653244A1 (en) * | 1974-05-13 | 1979-03-25 | Предприятие П/Я В-8585 | Method of separating mixtures of c5 hydrocarbons of different saturation degree |
| CN1412165A (en) * | 2001-10-12 | 2003-04-23 | 中国石油化工股份有限公司 | Separation method of cracked C5 fraction |
| CN1490286A (en) * | 2002-10-16 | 2004-04-21 | 中国石油化工股份有限公司 | Separating method for cracking C5-fraction |
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