CN103073376A - Separation process of mixed pentane - Google Patents
Separation process of mixed pentane Download PDFInfo
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- CN103073376A CN103073376A CN2013100560329A CN201310056032A CN103073376A CN 103073376 A CN103073376 A CN 103073376A CN 2013100560329 A CN2013100560329 A CN 2013100560329A CN 201310056032 A CN201310056032 A CN 201310056032A CN 103073376 A CN103073376 A CN 103073376A
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Abstract
The invention relates to a separation process of mixed pentane, and the separation process adopts a differential-pressure coupling rectifying technology for separating light components from pentane through higher pressure and for separating pentane from heavy components through lower pressure. The light components are firstly separated from the pentane through higher pressure, and then the pentane is separated from the heavy components through lower pressure; or the light components and the pentane are firstly separated from the heavy components through lower pressure, and then the light components are separated from the pentane through higher pressure. The separation process has the advantages that by pressurizing a light component removal tower, the oil-gas temperature on the top of the light component removal tower is increased, so that the oil gas can be used as the heat source of a heavy component removal tower; meanwhile, by adopting low-pressure-drop and high-efficient tower internals, the light component removal tower and the heavy component removal tower can be possibly coupled; adequate heat exchanging between raw materials and heat materials in the system can enable the recovery of majority of waste heat of the system; and compared with an ordinary two-tower sequential separation flow, the energy consumption of the entire process is reduced by 30 to 50 percent.
Description
Technical field
The present invention relates to separate in the hybrid pentane raw material processing method of hybrid pentane.
Technical background
The pentane end-use is extensive, can be used as the whipping agent of Expandable Polystyrene (EPS) and polyurethane foam system, is used for the fields such as insulation of freon-free refrigerator, refrigerator-freezer, freezer and pipeline; Can make year solvent of line low density polyethylene catalyst, the extraction agent of deasphalting industrial solvent, dewaxing by molecular sieve etc.; Also can be used as industrial chemicals, such as iso-pentane Oxidative Dehydrogenation isopentene, isoprene, pentane admixture can be produced thick amylalcohol through chlorination, rectifying, catalytic hydrolysis, obtain the l-amylalcohol after the stage trapping distillation, the research that phthalic anhydride and cis-butenedioic anhydride are produced in simultaneously Skellysolve A oxidation also obtains certain progress.
The year consumption of present China pentane, the consumption that is used for EPS (polystyrene foamed) pentane foaming agent accounts for 45% of aggregate consumption; The whipping agent consumption of urethane accounts for 50% of aggregate consumption; The linear low density polyethylene pentane carries the solvent consumption and accounts for 5% of aggregate consumption.
The method of domestic present separation hybrid pentane adopts the technique of conventional order rectifying usually, column internals adopts valve tray or corrugated plate regular packing, the technological process energy consumption is high, and the impurity in the product (alkene, pentamethylene etc.) content is wayward, and the main products yield is lower.
Chinese patent CN200910069668.0 has proposed the technique and the method that adopt double-effect rectification that hybrid pentane isomer separated, but its for raw material, product requirement and separation process and the present invention significant difference is arranged, and energy consumption is high.
Summary of the invention
The object of the invention provides a kind of less energy-consumption, hybrid pentane separating technology that product recovery rate is high.
Hybrid pentane separating technology of the present invention and device mainly comprise lightness-removing column, weight-removing column and attached corollary system, to be Skellysolve A separate the employing low-voltage with boiling point greater than the restructuring of Skellysolve A to the technological core of the method, and the light constituent that the boiling points such as iso-pentane are lower than Skellysolve A takes off the pressurized operation pattern that light process adopts elevated pressures.
The method power consumption of adopting traditional component sequentially to cut is high, the relative volatility minimizing amplitude of dividing with restructuring in pressure process because of Skellysolve A is larger, it is not obvious that Skellysolve A and restructuring separate the differential pressure coupling process energy-saving effect that adopt to pressurize, the present invention adopts the differential pressure coupling technique, adopt the light constituent higher pressure to separate extraction from the lightness-removing column top, Skellysolve A enters weight-removing column with recombinating to divide at the bottom of the tower, and Skellysolve A separates extraction from the weight-removing column top, and the weight-removing column employing is than the differential pressure coupling rectification technology of low pressure separation.Can adopt first light constituent to separate with the Skellysolve A higher pressure, rear Skellysolve A divides the method for separating than low pressure with restructuring, such as flow process 1; Perhaps first Skellysolve A minute separates than low pressure with restructuring, and the method that rear light constituent separates with the Skellysolve A higher pressure is as follows such as flow process 2. technical schemes of the present invention:
A kind of separating technology of hybrid pentane, it may further comprise the steps:
The hybrid pentane raw material after pump boosts with system in thermal material after a series of heat exchange, enter lightness-removing column 1 near bubble point temperature and carry out rectifying, the working pressure of lightness-removing column 1 is 0.4～1.4MPa (a), the cat head oil gas analysis of lightness-removing column 1 cuts to the part iso-pentane, comprise that light constituent that boiling point is lower than it enters after reboiler 3 carries out heat exchange at the bottom of the weight-removing column, all enter lightness-removing column top return tank 5 after the condensation, part is returned cat head as backflow, part is as light constituent product (comprising the part iso-pentane), carrying device after further cooling off, being provided with reboiler 4 at the bottom of the lightness-removing column at the bottom of the lightness-removing column provides lightness-removing column 1 required heat, thermal source can adopt steam or the common heating medium of heat conduction wet goods industry, product introduction weight-removing column 2 at the bottom of the tower of lightness-removing column 1, the working pressure of weight-removing column 2 is 0.15～0.45MPa (a), weight-removing column 2 cat head oil gas (part iso-pentane and Skellysolve A component) enter weight-removing column top return tank 8 after weight-removing column top condenser 7 complete coagulating, part is returned cat head as backflow, part is as hybrid pentane product or Skellysolve A, carrying device after cooling, be provided with reboiler 3 at the bottom of the weight-removing column that 2 heat requirements of weight-removing column are provided at the bottom of weight-removing column 2 towers, thermal source adopts the oil gas on lightness-removing column top, the bottom product component of attaching most importance to.
Flow process 2:
A kind of separating technology of hybrid pentane, it may further comprise the steps:
The hybrid pentane raw material after pump boosts with system in thermal material after a series of heat exchange, enter weight-removing column 2 near bubble point temperature and carry out rectifying, the working pressure of weight-removing column 2 is 0.15～0.45MPa (a), be provided with reboiler 3 at the bottom of the weight-removing column that 2 heat requirements of weight-removing column are provided at the bottom of the weight-removing column, thermal source adopts the oil gas on lightness-removing column top, oil oil heat exchanger 10 at the bottom of raw material/weight-removing column goes out device at the bottom of the weight-removing column, weight-removing column 2 cat head oil gas enter weight-removing column top return tank 8 after condenser 7 condensations of weight-removing column top, part is returned cat head as backflow, part is through entering lightness-removing column 1 after interchanger 6 heat exchange at the bottom of lightness-removing column top interchanger 11 and the tower, carry out rectifying, the working pressure of lightness-removing column 1 is 0.4～1.4MPa (a), after lightness-removing column 1 overhead oil aerial root cuts according to boiling range, enter at the bottom of the weight-removing column and enter lightness-removing column top return tank 5 after reboiler 3 whole condensations, part is returned cat head as backflow, part is as light constituent product (comprising the part iso-pentane), carrying device after cooling, being provided with reboiler 4 at the bottom of the lightness-removing column at the bottom of the lightness-removing column provides lightness-removing column 1 required heat, thermal source can adopt steam or the common heating medium of heat conduction wet goods industry, and the product of at the bottom of the lightness-removing column or tower bottom side line is as Skellysolve A or hybrid pentane product.
Lightness-removing column operational condition of the present invention is: cat head working pressure 0.4～1.4MPa (a), 75～165 ℃ of tower top temperatures, reflux ratio 5～20,70～150 of number of theoretical plates; The weight-removing column operational condition is: cat head working pressure 0.15～0.45MPa (a), 33～89 ℃ of tower top temperatures, reflux ratio 3～20,50～120 of number of theoretical plates.
Lightness-removing column among the present invention all loads high efficiency low pressure drop with weight-removing column and separates structured packing UT-SW and snappiness sparger.
Advantage of the present invention is:
1. by to the lightness-removing column pressurized operation, improve the oil gas temperature on lightness-removing column top, enabled the thermal source as weight-removing column.
2. adopt simultaneously low pressure drop, High Efficient Column Internals, make the two tower-coupled possibilities that become.
3. the waste heat of system's overwhelming majority has been reclaimed in the abundant heat exchange of thermal material in raw material and the system.
4. the energy consumption of whole process is compared with conventional two towers order separation process and is reduced by 30～50%.
5. pentane content can be greater than 99% in iso-pentane, Skellysolve A, the hybrid pentane product, can form by adjusting two column overhead extraction ratios, cooperating and regulate two tower working pressures, reflux and recently adjust the ratio of iso-pentane and Skellysolve A in the product according to raw material according to customer requirement; The separating high-purity iso-pentane can switch to the order differential pressure coupling of above-mentioned flow process 1, flexible operation.
6. the hybrid pentane rate of recovery is greater than 90%.
Description of drawings
Fig. 1 is the schematic diagram of the flow process 1 of the inventive method;
Fig. 2 is the schematic diagram of the flow process 2 of the inventive method.
Wherein: 1 is lightness-removing column; 2 is weight-removing column; 3 is reboiler at the bottom of the weight-removing column; 4 is reboiler at the bottom of the lightness-removing column; 5 is lightness-removing column top return tank; 6 is interchanger at the bottom of the lightness-removing column; 7 is weight-removing column top condenser; 8 is weight-removing column top return tank; 9 is reboiler at the bottom of the weight-removing column; 10 is interchanger at the bottom of the weight-removing column; 11 is lightness-removing column top condenser.
Embodiment
Adopt flow process 1(Fig. 1) the pentane separation process: utilize hybrid pentane raw material production pentane foaming agent, main products is iso-pentane: Skellysolve A=(30 ± 3): the whipping agent hybrid pentane of (70 ± 3), adopt the differential pressure coupling rectification flow process, install 210～220 ℃ the thermal oil that outer supplying heat source is provided by system, raw material warp and interchanger at the bottom of the weight-removing column [10], enter lightness-removing column [1] behind interchanger at the bottom of the lightness-removing column [6] and thermal material heat exchange to 90～100 ℃, lightness-removing column top oil gas enters lightness-removing column return tank [5] after reboiler at the bottom of the weight-removing column [3] is entirely solidifying, part is returned cat head as trim the top of column, part is as light constituent product carrying device after cooling, lightness-removing column working pressure 1.1～1.3MPa(a), 110～120 ℃ of overhead oil temperature degree, temperature is 94～98 ℃ behind reboiler, overhead product goes out 38～44 ℃ in device, and reboiler at the bottom of the lightness-removing column [4] adopts system's heat-conducting oil heating.Product introduction weight-removing column [2] at the bottom of the lightness-removing column, cat head oil gas enters weight-removing column top return tank [8] after weight-removing column top condenser [7] condensation, part is returned cat head as trim the top of column, part is as hybrid pentane product carrying device after cooling, weight-removing column working pressure 0.15～0.35 MPa(a), 51～56 ℃ of tower top temperatures, 38～44 ℃ of hybrid pentane product temperatures.
Adopt flow process 2(Fig. 2) the pentane separation process: utilize hybrid pentane raw material production high purity iso-pentane, main products is iso-pentane 〉=96 ℅, adopt conventional order differential pressure coupling rectification flow process, install 170～185 ℃ the steam that outer supplying heat source is provided by system, raw material through with interchanger at the bottom of the weight-removing column [10] and thermal material heat exchange to 50～60 ℃ after enter weight-removing column [2], weight-removing column top oil gas enters weight-removing column top return tank [8] after weight-removing column top condenser [7] condensation, part is returned cat head as trim the top of column, part is as light constituent product carrying device after cooling, and oil is through pushing up with lightness-removing column at the bottom of the weight-removing column, end interchanger [11], [6] enter lightness-removing column [1] behind heat exchange to 90～105 ℃; Lightness-removing column top oil gas enters lightness-removing column top return tank [5] after reboiler at the bottom of the weight-removing column [3] heat exchange is entirely solidifying, part is returned cat head as trim the top of column, the part through the cooling after as iso-pentane product carrying device, lightness-removing column working pressure 1.0～1.4MPa(a), 100～115 ℃ of overhead oil temperature degree, overhead product goes out 38～44 ℃ in device, product interchanger [2] heat exchange and further be cooled to 35-45 ℃ and go out device at the bottom of lightness-removing column at the bottom of the lightness-removing column.Reboiler [9] adopts system's steam heating, weight-removing column working pressure 0.33～45MPa(a), 45～51 ℃ of tower top temperatures, 25～35 ℃ of iso-pentane product temperatures at the bottom of reboiler at the bottom of the lightness-removing column [4], the weight-removing column.
Adopt flow process 2(Fig. 2) the pentane separation process: utilize hybrid pentane raw material production high purity Skellysolve A, main products is Skellysolve A 〉=96 ℅, adopt the differential pressure coupling rectification flow process, install 210～220 ℃ the thermal oil that outer supplying heat source is provided by system, raw material through with interchanger at the bottom of the weight-removing column [10] and thermal material heat exchange to 70～80 ℃ after enter weight-removing column [2], be provided with reboiler [3] at the bottom of the weight-removing column that rectifying institute heat requirement is provided at the bottom of the weight-removing column, thermal source adopts the oil gas on lightness-removing column top, weight-removing column working pressure 0.15～0.35 MPa(a), 48～53 ℃ of tower top temperatures, oil interchanger [10] and be cooled to 38～44 ℃ and go out device at the bottom of weight-removing column at the bottom of the weight-removing column, weight-removing column top oil gas enters weight-removing column top return tank [8] after weight-removing column top condenser [7] condensation, part is returned cat head as backflow, part is through pushing up with lightness-removing column, end interchanger [11], [6] enter lightness-removing column [1] behind heat exchange to 90～105 ℃, lightness-removing column top oil gas enters weight-removing column top reboiler [3] and all enters lightness-removing column top return tank [5] after the condensation, part is returned cat head as backflow, part is as light constituent product carrying device through lightness-removing column top interchanger [11] and after being cooled to 38～44 ℃, lightness-removing column working pressure 1.1～1.4MPa(a), 110～120 ℃ of overhead oil temperature degree, temperature is 96～100 ℃ behind reboiler, overhead product goes out 38～44 ℃ in device, the Skellysolve A product is cooled to 38～44 ℃ through heat exchange and goes out device at the bottom of the tower, and reboiler at the bottom of the lightness-removing column [4] adopts system's heat-conducting oil heating.
Claims (4)
1. the separating technology of a hybrid pentane is characterized in that it may further comprise the steps:
The hybrid pentane raw material after pump boosts with system in thermal material after a series of heat exchange, enter lightness-removing column (1) near bubble point temperature and carry out rectifying, the working pressure of lightness-removing column (1) is 0.4～1.4MPa (a), the cat head oil gas analysis of lightness-removing column 1 cuts to the part iso-pentane and comprises that light constituent that boiling point is lower than it enters after reboiler (3) carries out heat exchange at the bottom of the weight-removing column, all enter lightness-removing column top return tank (5) after the condensation, part is returned cat head as backflow, part is as the light constituent product, comprise the part iso-pentane, carrying device after further cooling off, reboiler (4) provides lightness-removing column (1) required heat at the bottom of being provided with lightness-removing column at the bottom of the lightness-removing column, thermal source can adopt steam or the common heating medium of heat conduction wet goods industry, product introduction weight-removing column (2) at the bottom of the tower of lightness-removing column (1), the working pressure of weight-removing column (2) is 0.15～0.45MPa (a), the part iso-pentane of weight-removing column (2) cat head oil gas and Skellysolve A component enter weight-removing column top return tank (8) after weight-removing column top condenser (7) is entirely solidifying, part is returned cat head as backflow, part is as hybrid pentane product or Skellysolve A, carrying device after cooling, be provided with reboiler (3) at the bottom of the weight-removing column that weight-removing column (2) institute heat requirement is provided at the bottom of weight-removing column (2) tower, thermal source adopts the oil gas on lightness-removing column top, the bottom product component of attaching most importance to.
2. the separating technology of a hybrid pentane is characterized in that it may further comprise the steps:
The hybrid pentane raw material after pump boosts with system in thermal material after a series of heat exchange, enter weight-removing column (2) near bubble point temperature and carry out rectifying, the working pressure of weight-removing column (2) is 0.15～0.45MPa (a), be provided with reboiler (3) at the bottom of the weight-removing column that weight-removing column (2) institute heat requirement is provided at the bottom of the weight-removing column, thermal source adopts the oil gas on lightness-removing column top, oil oil heat exchanger (10) at the bottom of raw material/weight-removing column goes out device at the bottom of the weight-removing column, weight-removing column (2) cat head oil gas enters weight-removing column top return tank (8) after weight-removing column top condenser (7) condensation, part is returned cat head as backflow, part is through entering lightness-removing column (1) after interchanger (6) heat exchange at the bottom of lightness-removing column top interchanger (11) and the tower, carry out rectifying, the working pressure of lightness-removing column (1) is 0.4～1.4MPa (a), reboiler (3) all entered lightness-removing column top return tank (5) after the condensation at the bottom of lightness-removing column (1) cat head oil gas entered weight-removing column, part is returned cat head as backflow, part is as the light constituent product, comprise the part iso-pentane, carrying device after cooling, reboiler (4) provides lightness-removing column (1) required heat at the bottom of being provided with lightness-removing column at the bottom of the lightness-removing column, thermal source can adopt steam or the common heating medium of heat conduction wet goods industry, and the product of at the bottom of the lightness-removing column or tower bottom side line is as pentane or hybrid pentane product.
3. separating technology according to claim 1 and 2 is characterized in that: 75～165 ℃ of the tower top temperatures of described lightness-removing column (1), reflux ratio 5～20,70～150 of number of theoretical plates; 33～89 ℃ of the tower top temperatures of described weight-removing column (2), reflux ratio 3～20,50～120 of number of theoretical plates.
4. separating technology according to claim 1 and 2, it is characterized in that: described lightness-removing column all loads high efficiency low pressure drop with weight-removing column and separates structured packing UT-SW and snappiness sparger.
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Cited By (8)
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| CN104211553A (en) * | 2014-08-08 | 2014-12-17 | 宁波海越新材料有限公司 | Method for purification of isooctane |
| CN104710262A (en) * | 2015-02-12 | 2015-06-17 | 新疆独山子天利实业总公司 | Method for producing pentane foaming agent with a difference ratio of isopentane to n-pentane being 5:5 |
| CN105949026A (en) * | 2016-06-27 | 2016-09-21 | 河南中托力合化学有限公司 | Mixed pentane precise separation device |
| CN107285978A (en) * | 2017-07-03 | 2017-10-24 | 无锡南理工科技发展有限公司 | The preparation method of normal butane |
| CN107285977A (en) * | 2017-07-03 | 2017-10-24 | 无锡南理工科技发展有限公司 | A kind of system and device that normal butane is prepared by the positive structure of iso-butane |
| CN108329235A (en) * | 2018-03-02 | 2018-07-27 | 天津赛普泰克科技有限公司 | A kind of process producing high-purity Bravo |
| CN108698957A (en) * | 2015-08-29 | 2018-10-23 | 环球油品公司 | Multistage pressure for butadiene reactor is to improve energy regenerating |
| CN114653319A (en) * | 2022-03-31 | 2022-06-24 | 濮阳市联众兴业化工有限公司 | Device for producing pentane foaming agent and using method |
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| CN108329235A (en) * | 2018-03-02 | 2018-07-27 | 天津赛普泰克科技有限公司 | A kind of process producing high-purity Bravo |
| CN108329235B (en) * | 2018-03-02 | 2020-10-02 | 天津赛普泰克科技有限公司 | Process for producing high-purity chlorothalonil |
| CN114653319A (en) * | 2022-03-31 | 2022-06-24 | 濮阳市联众兴业化工有限公司 | Device for producing pentane foaming agent and using method |
| CN114653319B (en) * | 2022-03-31 | 2023-12-22 | 濮阳市联众兴业化工有限公司 | Device for producing pentane foaming agent and use method |
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Application publication date: 20130501 |