CN217139234U - Multistage pentane distillation combined system - Google Patents
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- CN217139234U CN217139234U CN202220311461.0U CN202220311461U CN217139234U CN 217139234 U CN217139234 U CN 217139234U CN 202220311461 U CN202220311461 U CN 202220311461U CN 217139234 U CN217139234 U CN 217139234U
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Abstract
The application discloses multistage pentane distillation combined system includes: the multistage distillation tower, the multistage distillation tower is provided with one-level distillation plant, one-level distillation plant is provided with the one-level heater, one-level distillation plant is connected with the cyclopentane outlet pipe, one-level distillation plant below is provided with the second grade distillation plant, the second grade distillation plant is provided with the second grade heater, the second grade distillation plant below is provided with tertiary distillation plant, tertiary distillation plant is provided with tertiary heater, tertiary distillation plant below is provided with the lightness-removing tower, the lightness-removing tower is connected with the condensation pre-heater, the condensation pre-heater is connected with thick pentane import pipe. The method has the advantages that the cyclopentane, the n-pentane and the isopentane are separated, the first-stage distillation device extracts the cyclopentane, the second-stage distillation device extracts the n-pentane, the third-stage distillation device extracts the isopentane, the extraction principle is that distillation extraction is carried out according to the boiling point difference among all the components, and the multi-stage distillation separation of the crude pentane can be effectively carried out.
Description
Technical Field
The present application relates to the field of pentane separation, and in particular to a distillation combination for multistage pentane.
Background
The main purpose of distillation is to separate volatile and semi-volatile impurities from chemical reagents containing the impurities or to evaporate volatile and semi-volatile bulk, leaving behind non-volatile and non-volatile impurities, the change in the saturated vapor pressure of a substance at different temperatures being the basis of the separation by distillation, in general, if there is a large difference in the vapor pressure of two components in a liquid mixture, more volatile and semi-volatile components can be enriched in the vapor phase, two phases-the liquid and the vapor phase-can be recovered separately, volatile and semi-volatile components are enriched in the vapor phase and non-volatile components are enriched in the liquid phase, distillation is the process of separating components or substances from a liquid mixture by selective boiling and condensation, distillation can result in essentially complete separation (almost pure components), or partial separation effects increase the concentration of selected components in the mixture, in either case, the process takes advantage of the differences in volatility of the mixture components. In industrial chemistry, distillation is a unit operation of virtually universal importance, but it is a physical separation process rather than a chemical reaction.
The pentane product has wide application, can be used as a foaming agent of expandable polystyrene and a polyurethane foam system, and is used in the fields of heat preservation of fluorine-free refrigerators, freezers, refrigeration houses, pipelines and the like; can be used as a carrier solvent of a linear low density polyethylene catalyst, an industrial solvent for removing Zheqing, an extractant for dewaxing a molecular sieve and the like; it can also be used as chemical raw material, such as isopentene and isoprene prepared by dehydrogenation of isopentane, the crude pentanol can be produced by chlorination, rectification and catalytic hydrolysis of pentane mixture, the 1-pentanol can be obtained by multi-stage separation and distillation, and the research of producing phthalic anhydride and maleic anhydride by oxidation of n-pentane also makes a certain progress. At present, the annual consumption of pentane in China is about 45 percent of the total consumption of EPS (expanded polystyrene) pentane foaming agent; the consumption of the foaming agent of the polyurethane accounts for about 50 percent of the total consumption; the linear low density polyethylene pentane-based solvent consumption accounted for about 5% of the total consumption. The prior domestic method for separating mixed pentane usually adopts a conventional sequential rectification process, the internal parts of the tower adopt a float valve tray or corrugated plate regular packing, the energy consumption of the process is high, the content of impurities (olefin, cyclopentane and the like) in the product is difficult to control, and the yield of main products is low. Chinese patent CN200910069668.0 proposes a process and a method for separating mixed pentane isomer by double-effect rectification, but the requirements of raw materials and products and the separation flow are obviously different from the invention, and the energy consumption is high.
The cyclopentane produced by the cyclopentane device of the fine chemical plant has low purity, and the market price of the product is severely restricted. The key component affecting the purity of the cyclopentane product is 2, 2 dimethylbutane. Cyclopentane (CP) and 2, 2-dimethylbutane (22MB) have atmospheric boiling points of 49.25 and 49.74 ℃ respectively, and have a difference of 0.49 ℃, belong to a near-boiling system, and form an azeotrope due to the linear relationship between the saturated vapor pressure and the temperature of the Cyclopentane (CP) and the 2, 2-dimethylbutane (22MB) at a temperature of 49.4 ℃ and a composition of 5 or so. In the industry, the extraction method is commonly used for separating azeotropic systems, and the extraction method needs to experimentally screen an extracting agent to improve the dissolving capacity of a certain component in the system, and the dissolving capacity of other components is as low as possible. Extraction techniques are separation processes that utilize a balance of solubility. The solvent selection itself is not very difficult, it is very difficult to find a high performance extractant because the polarity and molecular size of the cyclopentane/2, 2_ dimethylbutane system are very similar, and the loss of cyclopentane product is also large because the cyclopentane composition of the system is already as high as 95.88%. Meanwhile, from the operation aspects of equipment efficiency, production experience and the like, the production performance of extraction equipment is very low, and a tower cannot be built too high, so that the separation of the cyclopentane/2, 2_ dimethylbutane system is not suitable.
The crude pentane needs to be subjected to multi-step distillation, and the crude pentane is separated and subjected to extraction of various components, including: the separation of cyclopentane, n-pentane, isopentane, the one-level distillation plant is drawed cyclopentane, the second grade distillation plant is drawed of n-pentane, the tertiary distillation plant is drawed isopentane, the principle of drawing is to carry out the distillation extraction according to the boiling point difference between each component, can effectively carry out the multistage distillation separation of crude pentane.
SUMMERY OF THE UTILITY MODEL
The application provides a multistage pentane distillation combined system separates cyclopentane, n-pentane, isopentane, and one-level distillation plant extracts the cyclopentane, and two-level distillation plant carries out the extraction of n-pentane, and tertiary distillation plant extracts the isopentane, and the principle of extracting distills according to the boiling point difference between each component and extracts, can effectively carry out the multistage distillation separation of crude pentane.
The application provides a multistage pentane distillation integrated system, includes: the multistage distillation tower, the multistage distillation tower is provided with one-level distillation plant, one-level distillation plant is provided with the one-level heater, one-level distillation plant is connected with the cyclopentane outlet pipe, one-level distillation plant below is provided with the second grade distillation plant, the second grade distillation plant is provided with the second grade heater, the second grade distillation plant below is provided with tertiary distillation plant, tertiary distillation plant is provided with tertiary heater, tertiary distillation plant below is provided with the lightness-removing tower, the lightness-removing tower is connected with the condensation pre-heater, the condensation pre-heater is connected with thick pentane import pipe.
Further, the primary distillation device is connected with a primary condenser, the primary distillation device is connected with a primary reflux tank, and the primary distillation device is connected with a primary reboiler.
Further, the second-stage distillation device is connected with a second-stage condenser, the second-stage distillation device is connected with a second-stage reflux tank, and the second-stage distillation device is connected with a second-stage reboiler.
Further, tertiary distillation plant is connected with tertiary condenser, and tertiary distillation plant is connected with tertiary reflux drum, and tertiary distillation plant is connected with tertiary reboiler.
Further, the secondary distillation device is connected with a n-pentane outlet pipe.
Further, the third-stage distillation device is connected with an isopentane outlet pipe.
According to the technical scheme, the application provides a multistage pentane distillation combination system, which comprises: the multistage distillation tower, the multistage distillation tower is whole system's main part distillation plant, the multistage distillation tower is provided with one-level distillation plant, one-level distillation plant distills the collection to cyclopentane, the cyclopentane boiling point 49.3 degrees centigrade, one-level distillation plant is provided with one-level heater, one-level heater heats one-level distillation plant, make one-level distillation plant temperature be higher than 49.3 degrees centigrade, one-level distillation plant is connected with the cyclopentane outlet pipe, make cyclopentane discharge the collection in the steam form, reach the separation effect, be provided with second distillation plant below one-level distillation plant, second distillation plant distills the collection to pentane, normal pentane boiling point 36.1 degrees centigrade, second distillation plant is provided with the second grade heater, second grade heater heats second distillation plant, make second distillation plant temperature be higher than 36.1 degrees centigrade, make normal pentane discharge the collection in the steam form, the separation effect is achieved, a third-level distillation device is arranged below the second-level distillation device, the third-level distillation device distills and collects isopentane, the boiling point of the isopentane is 27.8 ℃, the third-level distillation device is provided with a third-level heater, the third-level heater heats the third-level distillation device, the temperature of the third-level distillation device is higher than 27.8 ℃, the cyclopentane is discharged and collected in a steam shape, the separation effect is achieved, a lightness removing tower is arranged below the third-level distillation device and removes alkane and olefin below C5, the lightness removing tower is connected with a condensation preheater, the condensation preheater can preliminarily preheat the crude pentane, the condensation preheater is connected with a crude pentane inlet pipe, the crude pentane inlet pipe inputs the crude pentane into the multistage distillation tower, the multistage separation is carried out, the first-level condenser condenses the gaseous cyclopentane, the purity is higher after the distillation, the gaseous cyclopentane is liquefied by the condensation, collecting, the first-stage reflux tank can reflux the distilled cyclopentane, redistilling and purifying, the first-stage reboiler can redistilling in a heating mode to obtain high-purity cyclopentane, the second-stage condenser condenses the gaseous n-pentane, the purity is higher after distillation, the condensed liquefied gaseous n-pentane is collected, the second-stage reflux tank can reflux the distilled n-pentane, redistilling and purifying, the second-stage reboiler can redistilling in a heating mode to obtain high-purity n-pentane, the third-stage condenser condenses the gaseous isopentane, the purity is higher after distillation, the condensed liquefied gaseous isopentane is collected, the third-stage reflux tank can reflux the distilled isopentane, redistilling and purifying, the third-stage reboiler redistilling in a heating mode to obtain high-purity isopentane, and the n-pentane outlet pipe is used for discharging and collecting liquid n-pentane, and the isopentane outlet pipe is used for discharging and collecting liquid isopentane.
In summary, the above case has the following beneficial effects:
1. the multistage pentane distillation combined system related to the application has the advantages of simple structure and small occupied area.
2. The multistage pentane distillation combined system has a good distillation and separation effect, and the obtained components have high purity, so that the requirement of multistage pentane separation on purity is met.
Drawings
In order to more clearly illustrate the technical solution of the present application, the drawings needed to be used in the embodiments will be briefly described below, and it is obvious to those skilled in the art that other drawings can be obtained according to the drawings without any creative effort.
Fig. 1 is a schematic structural diagram of the present application.
FIG. 2 is a schematic structural diagram of a primary distillation device, a secondary distillation device and a tertiary distillation device.
Illustration of the drawings:
the system comprises a 1-multistage distillation tower, a 2-first-stage distillation device, a 3-first-stage heater, a 4-second-stage distillation device, a 5-second-stage heater, a 6-third-stage distillation device, a 7-third-stage heater, an 8-lightness removing tower, a 9-condensation preheater, a 10-cyclopentane outlet pipe, a 11-crude pentane inlet pipe, a 1-first-stage reflux tank, a 2-second-stage reflux tank, a 3-third-stage reflux tank, b 1-first-stage condenser, b 2-second-stage condenser, b 3-third-stage condenser, c 1-first-stage reboiler, c 2-second-stage reboiler and c 3-third-stage reboiler.
Detailed Description
In order to make those skilled in the art better understand the technical solutions in the present application, the technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the accompanying drawings.
Other embodiments of the present application will be apparent to those skilled in the art from consideration of the specification and practice of the application disclosed herein. This application is intended to cover any variations, uses, or adaptations of the invention following, in general, the principles of the application and including such departures from the present disclosure as come within known or customary practice within the art to which the invention pertains. It is intended that the specification and examples be considered as exemplary only, with a true scope of the disclosure being indicated by the following claims.
See fig. 1 for a solution known from the above.
Example 1:
a multistage pentane distillation combination system comprising: the multistage distillation tower 1 is a main distillation device of the whole system, the multistage distillation tower 1 is provided with a first-stage distillation device 2, the first-stage distillation device 2 distills and collects cyclopentane with a boiling point of 49.3 ℃, the first-stage distillation device 2 is provided with a first-stage heating device 3, the first-stage heating device 3 is butted with a cyclopentane outlet pipe 10 to heat the first-stage distillation device 2, the temperature of the first-stage distillation device 2 is higher than 49.3 ℃, the first-stage distillation device 2 and the pentane are in a steam state and are discharged and collected to achieve the separation effect, a second-stage distillation device 4 is arranged below the first-stage distillation device 2, the second-stage distillation device 4 distills and collects the normal pentane with a boiling point of 36.1 ℃, the second-stage distillation device 4 is provided with a second-stage heating device 5, the second-stage heating device 5 heats the second-stage distillation device 4, and the temperature of the second-stage distillation device 4 is higher than 36.1 ℃, the normal pentane is discharged and collected in a steam state to achieve the separation effect, a tertiary distillation device 6 is arranged below a secondary distillation device 4, the tertiary distillation device 6 is used for distilling and collecting isopentane, the boiling point of the isopentane is 27.8 ℃, the tertiary distillation device 6 is provided with a tertiary heater 7, the tertiary heater 7 is used for heating the tertiary distillation device 6 to ensure that the temperature of the tertiary distillation device 6 is higher than 27.8 ℃, the cyclopentane is discharged and collected in a steam state to achieve the separation effect, a light component removal tower is arranged below the tertiary distillation device 6, and the light component removal tower 8 is used for removing alkanes below C5, olefin is got rid of, and lightness-removing tower 8 is connected with condensation pre-heater 9, and condensation pre-heater 9 can carry out preliminary preheating with thick pentane, and condensation pre-heater 9 is connected with thick pentane import pipe 11, and thick pentane import pipe 11 carries out thick pentane to the inside input of multistage distillation tower 1, carries out the multi-stage separation.
Preferably, the primary distillation apparatus 2 is connected with a primary condenser 3, the primary distillation apparatus 2 is connected with a primary reflux drum a1, and the primary distillation apparatus 2 is connected with a primary reboiler c 1.
First-order condenser 3 condenses gaseous cyclopentane, and the purity is higher after the distillation, and the condensation liquefies gaseous cyclopentane, collects, and first-order backward flow jar a1 can flow back the cyclopentane after the distillation, and the redistillation purifies, and first-order reboiler c1 distills once more through the mode that heaies up, obtains high-purity cyclopentane.
Preferably, the secondary distillation apparatus 4 is connected with a secondary condenser b2, the secondary distillation apparatus 4 is connected with a secondary reflux drum a2, and the secondary distillation apparatus 4 is connected with a secondary reboiler c 2.
The secondary condenser b2 condenses the gaseous n-pentane, the purity is higher after distillation, the condensed gaseous n-pentane is liquefied and collected, the distilled n-pentane can be refluxed by the secondary reflux tank a2 and purified after redistillation, and the secondary reboiler c2 redistilles in a heating mode to obtain the high-purity n-pentane.
Preferably, the third distillation device 6 is connected with a third condenser b3, the third distillation device 6 is connected with a third reflux drum a3, and the third distillation device 6 is connected with a third reboiler c 3.
Tertiary condenser b3 condenses gaseous isopentane, and the purity is higher after the distillation, and the condensation liquefies gaseous isopentane, collects, and tertiary reflux drum a3 can flow back the isopentane after the distillation, and the redistillation purifies, and tertiary reboiler c3 distills once more through the mode of intensification, obtains high-purity isopentane.
Preferably, the secondary distillation unit 4 is connected to a n-pentane outlet.
The n-pentane outlet pipe is used for discharging and collecting liquid n-pentane.
Preferably, the tertiary distillation device 6 is connected with an isopentane outlet pipe.
And the isopentane outlet pipe is used for discharging and collecting liquid isopentane.
Example 2, see figure 2:
in the figure, a is a reflux tank, a first-stage reflux tank a1, a second-stage reflux tank a2, a third-stage reflux tank a3, b is a condenser, a first-stage condenser b1, a second-stage condenser b2, a third-stage condenser b3, c is a reboiler, a first-stage reboiler c1, a second-stage reboiler c2, a third-stage reboiler c3, a first-stage condenser 3 condenses gaseous cyclopentane, the purity is higher after distillation, the gaseous cyclopentane is liquefied by condensation and collected, the first-stage reflux tank a1 can reflux the distilled cyclopentane, the secondary distillation is carried out for purification, the first-stage reboiler c1 carries out secondary distillation by heating to obtain high-purity cyclopentane, the second-stage condenser b2 condenses gaseous n-pentane, the purity is higher after distillation, the gaseous n-pentane is liquefied by condensation and is collected, the second-stage reflux tank a2 can reflux the distilled n-pentane and carry out the secondary distillation for purification, redistilling in a second-stage reboiler c2 by heating to obtain high-purity n-pentane, condensing in a third-stage condenser b3 to obtain isopentane with higher purity, liquefying and collecting the isopentane, refluxing in a third-stage reflux tank a3 to purify the distilled isopentane, redistilling in a third-stage reboiler c3 by heating to obtain high-purity isopentane, and separating raw material crude pentane in each stage by the connection and combined action of a first-stage reflux tank a1, a second-stage reflux tank a2, a third-stage reflux tank a3, a first-stage condenser b1, a second-stage condenser b2, a third-stage condenser b3, a first-stage c1, a second-stage reboiler c2 and a third-stage reboiler c3, wherein the crude pentane is distilled and separated into cyclopentane, and the cyclopentane is separated into cyclopentane in each stage by the separation action of each stage, The high-purity components are obtained from n-pentane and isopentane, the three components are collected and utilized, the reflux tank is used for refluxing liquid converted from the components of gas after being cooled by the condenser, and each liquid component is reboiled by the reboiler, so that the purity of the components obtained by separation of the whole device is improved.
It will be understood that the present application is not limited to the precise arrangements described above and shown in the drawings and that various modifications and changes may be made without departing from the scope thereof. The above-described embodiments of the present application do not limit the scope of the present application.
Claims (6)
1. A multistage pentane distillation combination system, comprising: multistage distillation tower (1), multistage distillation tower (1) is provided with one-level distillation plant (2), one-level distillation plant (2) are provided with one-level heater (3), one-level distillation plant (2) are connected with cyclopentane outlet pipe (10), one-level distillation plant (2) below is provided with second grade distillation plant (4), second grade distillation plant (4) are provided with second grade heater (5), second grade distillation plant (4) below is provided with tertiary distillation plant (6), tertiary distillation plant (6) are provided with tertiary heater (7), tertiary distillation plant (6) below is provided with lightness-removing column (8), lightness-removing column (8) are connected with condensation preheater (9), condensation preheater (9) are connected with crude pentane import pipe (11).
2. A multistage pentane distillation combination system according to claim 1, wherein a primary condenser (b1) is connected to the primary distillation unit (2), a primary reflux drum (a1) is connected to the primary distillation unit (2), and a primary reboiler (c1) is connected to the primary distillation unit (2).
3. A multistage pentane distillation combination according to claim 1, wherein a secondary condenser (b2) is connected to the secondary distillation unit (4), a secondary reflux drum (a2) is connected to the secondary distillation unit (4), and a secondary reboiler (c2) is connected to the secondary distillation unit (4).
4. A multistage pentane distillation combination according to claim 1, wherein a tertiary condenser (b3) is connected to the tertiary distillation unit (6), a tertiary reflux drum (a3) is connected to the tertiary distillation unit (6), and a tertiary reboiler (c3) is connected to the tertiary distillation unit (6).
5. A multistage pentane distillation combination system according to claim 1, wherein said secondary distillation unit is connected to a n-pentane outlet line.
6. A multistage pentane distillation combination system according to claim 1, wherein an isopentane exit tube is connected to said tertiary distillation unit.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116082113A (en) * | 2023-03-13 | 2023-05-09 | 新疆天利石化股份有限公司 | Method for producing high-purity cyclopentane and methylcyclopentane by hydrogenating nine light components of carbon |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116082113A (en) * | 2023-03-13 | 2023-05-09 | 新疆天利石化股份有限公司 | Method for producing high-purity cyclopentane and methylcyclopentane by hydrogenating nine light components of carbon |
| CN116082113B (en) * | 2023-03-13 | 2023-08-01 | 新疆天利石化股份有限公司 | Method for producing high-purity cyclopentane and methylcyclopentane by hydrogenating nine light components of carbon |
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