CN103143191A - Removal technology of cyclic solvent dipolymer in a C5 diolefin separation process by solvent method - Google Patents
Removal technology of cyclic solvent dipolymer in a C5 diolefin separation process by solvent method Download PDFInfo
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- CN103143191A CN103143191A CN2013100468801A CN201310046880A CN103143191A CN 103143191 A CN103143191 A CN 103143191A CN 2013100468801 A CN2013100468801 A CN 2013100468801A CN 201310046880 A CN201310046880 A CN 201310046880A CN 103143191 A CN103143191 A CN 103143191A
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Abstract
The invention relates to a separation technology of petroleum hydrocarbon materials, particularly to a removal technology of a cyclic solvent dipolymer in a C5 diolefin separation process by a solvent method. The technology is characterized in that: a static mixer and a solvent separation tank are disposed, the operation pressure is controlled at 300-600KPaA, and the operation temperature is at 40-60DEG C. Part of a raffinate C5 component and a cyclic solvent are mixed. By utilizing the difference of the dipolymer solubility in the raffinate C5 and the solvent, the dipolymer in the solvent can be transferred into the raffinate C5, and can be separated from a separation tank top, so that the equipment energy consumption and the difficulty of process control and operation are reduced, the control index of the dipolymer in the cyclic solvent is effectively guaranteed, and stable operation of the C5 separation process is ensured. Compared with traditional technologies of dipolymer removal by rectification, the technology reduces construction investment and equipment energy consumption. The employment of an extraction process reduces loss of the cyclic solvent and lowers the difficulty of process control and operation.
Description
Technical field
The present invention relates to a kind of petroleum hydrocarbon feed separation technique, more particularly, relate to the removing process of circulating solvent dimer in a kind of abstraction distillation separation cracking C 5 diene process.
Background technology
Cracked C 5 fraction is the accessory substance of petroleum hydrocarbon cracking process of producing ethylene, wherein contain the alkadienes composition in carbon five components such as a large amount of cyclopentadiene (CPD), isoprene (IP) and pentadiene (PD), highly purified carbon five alkadienes are the rare industrial chemicals in market.At present both at home and abroad to the separation of C5 fraction take solvent extraction rectifying as main, extractant is acetonitrile (ACN), dimethyl formamide (DMF), 1-METHYLPYRROLIDONE etc., after extracting rectifying and conventional distillation, can obtain the carbon such as the isoprene five component alkadienes products of polymer grade.
In the process of extracting distillation separation C five cuts, extractant need to be circulated in a large number, because self-polymeric reaction very easily occurs alkadienes in technical process, generate dimer, the dimer main component is dicyclopentadiene (DCPD), and dimer is accumulated in circulating solvent and will be had a strong impact on the selective of solvent.Therefore, need to the circulating solvent that the contains dimer processing of regenerating, remove the impurity such as dimer wherein.
In traditional handicraft, mostly by increasing the solvent refining tower, adopt rectifying to remove partial polymer in circulating solvent, as disclosed processes such as patent CN100999434A and CN101798255A now.CN100999434A discloses a kind of method of acetonitrile solvent method separating carbon 5 fraction, and in flow process, rectifying column 504 is DCPD depolymerization, weight-removing column, and tower reactor obtains the polymer accessory substance.CN101798255A discloses a kind of method that adopts acetonitrile separating isoprene and pentadiene, material in flow process in the still of the solvent analysis tower and side line tower enters in the middle part of the solvent refining tower, obtained by tower top that solvent acetonitrile is back to the first extractive distillation column and the second extractive distillation column recycles, in tower reactor for containing the raffinate of polymer.Above two kinds remove dimer technique, and the method that all adopts rectifying to separate removes high boiling polymer by adding thermal distillation, because the circulating solvent amount is large, causes the solvent refining energy consumption high, account for 20% left and right that carbon five separates total energy consumption.
Summary of the invention
The object of the invention is to overcome the prior art deficiency, the technique that removes dimer in a kind of abstraction distillation separation cracking carbon 5-cut fraction process from circulating solvent is provided.
the removing process of circulating solvent dimer in a kind of solvent method separation of carbon 5 diene process, it is characterized in that, raffinate carbon-5 comes a supreme operation, it is the reflux pump of the first extractive distillation column of carbon five separators, the reflux pump discharging of the first extractive distillation column is No. 2 line materials, the Line 1 material is 5% of global cycle solvent, enter static mixer M-101, operating temperature is 40～60 ℃, be provided with the oblique wave card in static mixer M-101 and consist of, the weight ratio of raffinate carbon-5 and circulating solvent is 0.3～1.0, after Line 1 material and No. 2 line materials mix, No. 6 lines through pump P-101 are squeezed into separated from solvent tank V-102, the operating pressure of separated from solvent tank V-102 is 300～600KPaA, operating temperature is 40～60 ℃, separated from solvent tank V-102 is horizontal tank, the material clarification time is 0.5～1.0 hour, utilize the difference of dimer solubility in the raffinate carbon-5 solvent, lower leaf on material, the top of separated from solvent tank V-102 is the raffinate carbon-5 component that contains dimer, enter next operation raffinate carbon-5 water scrubber, circulating solvent after the bottom of separated from solvent tank V-102 is purified, turn back to abstraction distillation system.
Equipment in flow process of the present invention, static mixer and separated from solvent tank are arranged, reduced the investment of the equipment such as a tower system and attached heat exchanger, reflux pump, lime set tank, reduced simultaneously the loss of solvent, reduced the energy consumption of device, and the difficulty of technology controlling and process and operation, and effectively guaranteed the control index of dimer in the circulating solvent, guaranteed the stable operation of carbon five separating technologies.
Advantage of the present invention is as follows:
1. the employing extraction process, removed the dimer in the circulating solvent effectively.
2. remove the dimer technology with traditional rectifying and compare, reduced the energy consumption of construction investment and device.
3. the employing extraction process, reduced the loss of circulating solvent.
4. employing extraction process has reduced the difficulty of technology controlling and process and operation.
Description of drawings
Fig. 1 is schematic flow sheet of the present invention.
Static mixer M-101, pump P-101, separated from solvent tank V-102 are arranged in figure; In flow process, the Line 1 material is circulating solvent, No. 2 line materials are the raffinate carbon-5 component, No. 3 line materials are the raffinate carbon-5 component that contains dimer, No. 4 line material is the circulating solvent after purifying, and No. 5 line materials are that circulating solvent and raffinate carbon-5 component mixture, No. 6 line materials are the rear circulating solvent of pressurization and raffinate carbon-5 component mixture.
The specific embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is done further describe in detail.
Take 250,000 ton/years of devices of certain company as example, adopt the removing process of circulating solvent dimer in solvent method separation of carbon 5 diene process, circulating solvent is acetonitrile, changes the weight ratio of raffinate carbon-5 component and circulating solvent;
raffinate carbon-5 comes a supreme operation, the reflux pump of the first extractive distillation column of carbon five separators, No. 2 line materials that the reflux pump of the first extractive distillation column comes and Line 1 Matter Transfer solvent, the Line 1 material is 5% of global cycle solvent, enter static mixer M-101, operating temperature is 40～60 ℃, is provided with the oblique wave card in static mixer M-101 and consists of, and the weight ratio of raffinate carbon-5 and circulating solvent is 0.3～1, after Line 1 material and No. 2 line materials mix, No. 6 lines through pump P-101 are squeezed into separated from solvent tank V-102, the operating pressure of separated from solvent tank V-102 is 300～600KPaA, operating temperature is 40～60 ℃, separated from solvent tank V-102 is horizontal tank, the material clarification time is 0.5～1.0 hour, utilize the difference of dimer solubility in the raffinate carbon-5 solvent, lower leaf on material, the top of separated from solvent tank V-102 is the raffinate carbon-5 component that contains dimer, enter the raffinate carbon-5 water scrubber of next operation, circulating solvent after the bottom of separated from solvent tank V-102 is purified, turn back to abstraction distillation system.
Take 250,000 ton/years of devices of certain company as example, certain stream in table strand number is certain number line material number, and the data that provide are corresponding with each table by embodiment.
Embodiment 1
The weight ratio of raffinate carbon-5 component and circulating solvent is 0.3.Operating pressure is 300kPaA, 40 ℃ of operating temperatures, and charging and separated from solvent tank deck and bottom material form as table 1.
Embodiment 2
The weight ratio of raffinate carbon-5 component and circulating solvent is 1.Operating pressure is 600kPaA, 60 ℃ of operating temperatures, and charging and separated from solvent tank deck and bottom material form as table 2.
Embodiment 3
The weight ratio of raffinate carbon-5 component and circulating solvent is 0.5.Operating pressure is 400kPaA, 50 ℃ of operating temperatures, and charging and separated from solvent tank deck and bottom material form as table 3.
Embodiment 4
The weight ratio of raffinate carbon-5 component and circulating solvent is 0.6.Operating pressure is 350kPaA, 45 ℃ of operating temperatures, and charging and separated from solvent tank deck and bottom material form as table 4.
Embodiment 5
The weight ratio of raffinate carbon-5 component and circulating solvent is 0.8.Operating pressure is 500kPaA, 55 ℃ of operating temperatures, and charging and separated from solvent tank deck and bottom material form as table 5.
Table 1
Table 2
Table 3
Table 4
Table 5
Claims (1)
1. the removing process of circulating solvent dimer in a solvent method separation of carbon 5 diene process, it is characterized in that, raffinate carbon-5 comes a supreme operation, it is the reflux pump of the first extractive distillation column of carbon five separators, the reflux pump discharging of the first extractive distillation column is (2) number line material, mix with (1) number line material circulating solvent, (1) number line material is 5% of global cycle solvent, enter static mixer (M-101), operating temperature is 40～60 ℃, being provided with the oblique wave card in static mixer (M-101) consists of, the weight ratio of raffinate carbon-5 and circulating solvent is 0.3～1.0, (1) after number line material and (2) number line material mixes, number line is squeezed into separated from solvent tank (V-102) through (6) of pump (P-101), the operating pressure of separated from solvent tank (V-102) is 300～600KPaA, operating temperature is 40～60 ℃, separated from solvent tank (V-102) is horizontal tank, the material clarification time is 0.5～1.0 hour, utilize the difference of dimer solubility in the raffinate carbon-5 solvent, lower leaf on material, the top of separated from solvent tank (V-102) is the raffinate carbon-5 component that contains dimer, enter next operation raffinate carbon-5 water scrubber, circulating solvent after the bottom of separated from solvent tank (V-102) is purified, turn back to abstraction distillation system.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201310046880.1A CN103143191B (en) | 2013-01-25 | 2013-01-25 | Removal technology of cyclic solvent dipolymer in a C5 diolefin separation process by solvent method |
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| CN201310046880.1A CN103143191B (en) | 2013-01-25 | 2013-01-25 | Removal technology of cyclic solvent dipolymer in a C5 diolefin separation process by solvent method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103709066A (en) * | 2013-12-25 | 2014-04-09 | 天津大学 | System and method for separating out acetonitrile in acetonitrile-water-dicyclopentadiene system |
| CN103724227A (en) * | 2013-12-25 | 2014-04-16 | 天津大学 | System and method for refining recycle solvent through extracting isoprene by acetonitrile |
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| CN1253130A (en) * | 1998-11-09 | 2000-05-17 | 化学工业部北京化工研究院 | Method for separating diolefin from carbon five fraction |
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| CN102040456A (en) * | 2009-10-20 | 2011-05-04 | 中国石油化工股份有限公司 | Method for preparing dicyclopentadiene and emulsifying packed tower used thereby |
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| SU1068413A1 (en) * | 1981-09-21 | 1984-01-23 | Предприятие П/Я В-8585 | Process for recovering c4-c5 diolefins |
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| CN1160034A (en) * | 1996-03-20 | 1997-09-24 | 中国石油化工总公司 | Method for separation of cracking C5 fraction |
| CN1253130A (en) * | 1998-11-09 | 2000-05-17 | 化学工业部北京化工研究院 | Method for separating diolefin from carbon five fraction |
| 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 |
| CN1876608A (en) * | 2006-06-29 | 2006-12-13 | 山东玉皇化工有限公司 | Polymerization grade isoprene production method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103709066A (en) * | 2013-12-25 | 2014-04-09 | 天津大学 | System and method for separating out acetonitrile in acetonitrile-water-dicyclopentadiene system |
| CN103724227A (en) * | 2013-12-25 | 2014-04-16 | 天津大学 | System and method for refining recycle solvent through extracting isoprene by acetonitrile |
| CN103724227B (en) * | 2013-12-25 | 2016-03-30 | 天津大学 | Acetonitrile method isoprene extraction circulating solvent refining system and method |
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Effective date of registration: 20200928 Address after: 132002 3-6 and 9-13 floors of Block A, Jihua Economic and Trade Center, Tongtan Road, Changyi District, Jilin Province Patentee after: PetroChina Jilin Chemical Engineering Co.,Ltd. Address before: Changyi District of Jilin city in Jilin province 132002 Tong Tan Road Jihua Trade Center building A Patentee before: JILIN DESIGNING INSTITUTE OF CNPC NORTHEAST REFINING & CHEMICAL ENGINEERING Co.,Ltd. |