CN117883810A - Mixed pentane precise separation device - Google Patents
Mixed pentane precise separation device Download PDFInfo
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- CN117883810A CN117883810A CN202410288509.4A CN202410288509A CN117883810A CN 117883810 A CN117883810 A CN 117883810A CN 202410288509 A CN202410288509 A CN 202410288509A CN 117883810 A CN117883810 A CN 117883810A
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- tower
- pentane
- pipeline
- reboiler
- condenser
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- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 title claims abstract description 129
- 238000000926 separation method Methods 0.000 title claims abstract description 23
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 claims abstract description 56
- 238000010992 reflux Methods 0.000 claims abstract description 30
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 claims abstract description 28
- 238000011084 recovery Methods 0.000 claims abstract description 24
- 238000003860 storage Methods 0.000 claims abstract description 21
- 238000001816 cooling Methods 0.000 claims description 16
- 239000003507 refrigerant Substances 0.000 claims description 16
- 238000005192 partition Methods 0.000 claims description 6
- 238000009826 distribution Methods 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 description 11
- 239000000203 mixture Substances 0.000 description 9
- 239000011550 stock solution Substances 0.000 description 5
- 238000001914 filtration Methods 0.000 description 4
- 238000005194 fractionation Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- 239000012530 fluid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- UHZZMRAGKVHANO-UHFFFAOYSA-M chlormequat chloride Chemical compound [Cl-].C[N+](C)(C)CCCl UHZZMRAGKVHANO-UHFFFAOYSA-M 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/04—Solvent extraction of solutions which are liquid
- B01D11/0492—Applications, solvents used
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/10—Vacuum distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to the technical field of mixed pentane separation, in particular to a mixed pentane precise separation device which comprises a premixing tank, a first preheater, a first rectifying tower, a first condenser, a first reflux tank, a first reboiler, a third preheater, a recovery tower, a third condenser, a third reflux tank, a third reboiler, a n-pentane refiner, a n-pentane storage tank, an isopentane refiner and an isopentane storage tank.
Description
Technical Field
The utility model relates to the technical field of mixed pentane separation, in particular to a mixed pentane precise separation device.
Background
Pentane is a precious light hydrocarbon resource, has the advantages of cleanness, small heat conductivity coefficient, stable chemical property and the like, and has wide application scene. The unseparated pentane mixture (containing n-pentane, isopentane and the like) is usually sold as cracking raw materials or fuel, the price is low, and the separation and purification are carried out to obtain a single pentane product with high value, so that the pentane mixture can be applied to more specific scenes, and the additional value and the resource utilization rate are higher.
The utility model provides an utility model patent document that current application number is CN202021646230.2 discloses a mixed pentane separator, including the separator tower body, the one side connection of separator tower body is provided with the inlet pipe, and is provided with the pre-heater near the position of separator tower body on the inlet pipe, the bottom of separator tower body is connected respectively and is provided with first liquid storage pot and reboiler, and the top of separator tower body is provided with heat pump unit, heat pump unit's one end is linked together with the reboiler, and heat pump unit's the other end connection is provided with branch tube head, the one end and the separator tower that divide the tube head are linked together, and the other end connection of dividing the tube head is provided with the second liquid storage pot, be provided with the filtration jar on the inlet pipe, be provided with first stock solution chamber in the first stock solution intracavity, be provided with the second stock solution chamber in the interior jar, the top of filtration jar is provided with the closing cap respectively, the bottom of filtration jar is provided with the sealing piston that is mutually nested with first stock solution chamber, the second stock solution chamber, the surface of filtration jar is provided with two semicircle hoops with corresponding position, two semicircle hoops are provided with two and are located two filter cartridge inner surface and two filter cartridge, two filter cartridge inner surface and two filter cartridge filter frame inner surface and two are provided with the filter cartridge inner surface and two filter cartridge inner surface and are located the filter cartridge inner surface and two.
In the separation device, only one-time rectification is performed, the purity of the separated product is low, and the waste heat of the reboiler is not well utilized, so that the waste of heat sources is caused.
Disclosure of Invention
The utility model aims to provide a precise separation device for mixed pentane, which can improve the purity of a separation product and reduce energy consumption.
In order to achieve the above object, the technical scheme of the present utility model is as follows: the utility model provides a mixed pentane precision separation device, includes the pre-mix jar that establishes side by side, first rectifying column, recovery tower, normal pentane refiner and isopentane refiner, one side of normal pentane refiner is provided with the normal pentane storage tank through the pipe connection, one side of isopentane refiner is provided with the isopentane storage tank through the pipe connection, the top of a tower one side of first rectifying column is provided with the first condenser through the pipe connection, the below of first condenser is provided with the first reflux drum through the pipe connection, the first reflux drum passes through the pipe connection respectively and connects isopentane refiner and first rectifying column, one side of the bottom of a tower of first rectifying column is provided with the first pre-heater through the pipe connection, the first pre-heater is provided with the first reboiler through the pipe connection in the bottom of a tower of first rectifying column, one side of a tower of recovery column is provided with the third condenser through the pipe connection, the below of third condenser is provided with the third reflux drum through the pipe connection, the third reflux drum passes through the pre-heater through the pipe connection in the bottom of a tower and the first rectifying column, the bottom of a tower is provided with the first feed inlet through the first feed inlet and the recovery tower respectively, the bottom of a tower is provided with the first feed inlet through the first feed inlet respectively.
Further, the precise pentane mixing and separating device further comprises a second rectifying tower, a second condenser connected through a pipeline is arranged on one side of the top of the second rectifying tower, a second reflux tank connected through a pipeline is arranged below the second condenser, the second reflux tank is respectively connected with an isopentane refiner and the second rectifying tower through pipelines, a second preheater connected through a pipeline is arranged on one side of the bottom of the second rectifying tower, a second reboiler connected through a pipeline is arranged on the other side of the bottom of the second rectifying tower, a feed inlet of the first reboiler and a feed inlet of the second preheater are respectively connected through a pipeline through a bottom discharge outlet of the first rectifying tower, and a feed inlet of the second reboiler and a feed inlet of the third preheater are respectively connected through pipelines.
Further, the first condenser, the second condenser and the third condenser are sleeve type condensers, each sleeve type condenser comprises a shell with openings at two ends and a plurality of groups of cooling sleeves arranged in the shell, refrigerant inlets of all the cooling sleeves are converged into a main inlet at one side of the shell through a distribution pipe, and refrigerant outlets of all the cooling sleeves are converged into a main outlet at the other side of the shell through another distribution pipe.
Further, the cooling jacket comprises an inner pipe and an outer pipe sleeved outside the inner pipe, the inner pipe is connected with the inner wall of the outer pipe through a spiral partition plate arranged on the outer wall, a cavity between the outer pipe and the inner pipe is divided into spiral cavities by the spiral partition plate, flanges connected with the inner pipe are arranged at two ends of the outer pipe, the spiral cavities are sealed by the flanges, medium guide pipes which run the same as the spiral cavities are arranged in the spiral cavities, one end of each medium guide pipe penetrates out of the outer pipe and is located at one end of the outer pipe, the other end of each medium guide pipe penetrates out of the outer pipe and is located at the other end of the outer pipe, the refrigerant inlet is communicated with the spiral cavities and is arranged at one end of the outer pipe, and the refrigerant outlet is communicated with the spiral cavities and is arranged at the other end of the outer pipe.
Further, the first rectifying tower, the second rectifying tower and the recovery tower are all connected with a vacuum pump set.
Furthermore, air coolers are connected to the pipeline between the isopentane refiner and the isopentane storage tank and the pipeline between the n-pentane refiner and the n-pentane storage tank.
Further, the first reboiler, the second reboiler and the third reboiler are thermosiphon type reboilers.
After the technical scheme is adopted, the utility model has the beneficial effects that:
1. the mixed pentane is mixed with the extractant in the premixing tank, and then the mixture is preheated, so that the thermal movement speed of molecules can be increased, the mixed pentane and the extractant are better and uniformly mixed, the extractant can selectively interact with one component in the mixed pentane, so that the solubility of the component in the extractant is far higher than that of other components, the selectivity enables the separation process to be more accurate, single components with higher purity can be obtained, the occurrence of side reactions is reduced, and the purity and quality of the product are improved;
2. the mixed pentane is separated twice by the first rectifying tower and the second rectifying tower, the concentration of the product is higher, and the recovery tower can recover the extractant to realize cyclic utilization;
3. the waste heat of the reboiler is reused by the preheater, so that the use of high-quality energy sources is reduced, and the production cost is reduced.
Drawings
In order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the utility model, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic illustration of the present utility model;
fig. 2 is a schematic structural view of the cooling jacket.
In the figure: 1-premix tank, 2-first preheater, 3-first rectifying tower, 4-first condenser, 5-first reflux tank, 6-second preheater, 7-second rectifying tower, 8-second condenser, 9-third preheater, 10-recovery tower, 11-third condenser, 12-third reflux tank, 13-n-pentane refiner, 14-isopentane refiner, 15-isopentane storage tank, 16-n-pentane storage tank, 17-third reboiler, 18-second reflux tank, 19-second reboiler, 20-first reboiler, 21-inner tube, 22-outer tube, 23-spiral baffle, 24-spiral cavity, 25-medium conduit, 26-refrigerant outlet, 27-refrigerant inlet.
Detailed Description
Features and exemplary embodiments of various aspects of the present utility model will be described in detail below, and in order to make the objects, technical solutions and advantages of the present utility model more apparent, the present utility model will be described in further detail below with reference to the accompanying drawings and the detailed embodiments. It should be understood that the specific embodiments described herein are merely configured to illustrate the utility model and are not configured to limit the utility model. It will be apparent to one skilled in the art that the present utility model may be practiced without some of these specific details. The following description of the embodiments is merely intended to provide a better understanding of the utility model by showing examples of the utility model.
The directional terms appearing in the following description are those directions shown in the drawings and do not limit the specific structure of the utility model. In the description of the present utility model, it should also be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be directly connected or indirectly connected. The specific meaning of the above terms in the present utility model can be understood as appropriate by those of ordinary skill in the art.
As shown in fig. 1 to 2, the embodiment provides a mixed pentane precise separation device, which comprises a tower, a premixing tank 1, a first rectifying tower 3, a second rectifying tower 7, a recovery tower 10, a normal pentane refiner 13 and an isopentane refiner 14, wherein the tower is arranged side by side.
An n-pentane storage tank 16 connected by a pipeline is arranged on one side of the n-pentane refiner 13, an isopentane storage tank 15 connected by a pipeline is arranged on one side of the isopentane refiner 14, and air coolers are connected on a pipeline between the isopentane refiner 14 and the isopentane storage tank 15 and a pipeline between the n-pentane refiner 13 and the n-pentane storage tank 16. The air cooler can cool the separated pentane component to a lower temperature, so that the volatility of the pentane component is effectively reduced, and the pentane component is easier to carry out subsequent storage operation in a liquid state.
A first condenser 4 connected by a pipeline is arranged on one side of the top of the first rectifying tower 3, and a first reflux tank 5 connected by a pipeline is arranged below the first condenser 4. The bottom side of the first rectifying tower 3 is provided with a first preheater 2 connected through a pipeline, the first preheater 2 is connected with the premixing tank 1 through a pipeline, and the other side of the bottom of the first rectifying tower 3 is provided with a first reboiler 20 connected through a pipeline.
The top of the second rectifying tower 7 is provided with a second condenser 8 connected by a pipeline, a second reflux tank 18 connected by a pipeline is arranged below the second condenser 8, and the second reflux tank 18 is respectively connected with the isopentane rectifying device 14 and the second rectifying tower 7 by pipelines. The bottom side of the second rectifying tower 7 is provided with a second preheater 6 connected by a pipeline, and the other side of the bottom of the second rectifying tower 7 is provided with a second reboiler 19 connected by a pipeline.
A third condenser 11 connected by a pipeline is arranged on one side of the top of the recovery tower 10, a third reflux tank 12 connected by a pipeline is arranged below the third condenser 11, and the third reflux tank 12 is respectively connected with a n-pentane refiner 13 and the recovery tower 10 by a pipeline. The third preheater 9 connected by a pipeline is arranged at one side of the bottom of the recovery tower 10, and the third reboiler 17 connected by a pipeline is arranged at the other side of the bottom of the recovery tower 10.
The bottom discharge port of the first rectifying tower 3 is respectively connected with the feed port of the first reboiler 20 and the feed port of the second preheater 6 through pipelines, the bottom discharge port of the second rectifying tower 7 is respectively connected with the feed port of the second reboiler 19 and the feed port of the third preheater 9 through pipelines, and the bottom discharge port of the recovery tower 10 is respectively connected with the feed port of the third reboiler 17 and the feed port of the premixing tank 1 through pipelines.
The first rectifying tower 3, the second rectifying tower 7 and the recovery tower 10 are all connected with vacuum pump sets, and the vacuum pump sets can provide low pressure or vacuum environment for the first rectifying tower 3, the second rectifying tower 7 and the recovery tower 10, so that the boiling point of mixed pentane is reduced, the separation of pentane components can be realized at a lower temperature, and the separation efficiency is improved. Under the condition of low pressure or vacuum, the heat required in the rectification process is reduced, the operation temperature is reduced, and the energy consumption can be reduced. The first reboiler 20, the second reboiler 19 and the third reboiler 17 are all thermosiphon type reboilers, and the generated vapor-liquid mixture automatically returns to the tower by heating the tower bottom fluid to partially vaporize the tower bottom fluid, so that the stable performance of the rectification operation is maintained.
The mixed pentane and the extractant are fully mixed in the premixing tank 1, then the mixture is pumped to the first preheater 2 for preheating, the preheated pentane mixture is sent to the first rectifying tower 3 for fractionation, the first reboiler 20 heats and gasifies the pentane mixture at the bottom of the tower, light components (mostly isopentane) are distilled out from the top of the tower, the light components are condensed into liquid phases by the first condenser 4 and then flow into the first reflux tank 5, a part of the liquid phases in the first reflux tank 5 are reintroduced into the first rectifying tower 3 for fractionation, the other part of the liquid phases in the first reflux tank 5 are sent to the second rectifying tower 7 for further rectification after being preheated by the second preheater 6, and heavy components (mostly n-pentane and the extractant) are guided out from the bottom of the tower, preheated by the second preheater 6 and then sent to the second rectifying tower 7. The second reboiler 19 heats and vaporizes the mixture at the bottom of the tower again, light component (isopentane) is distilled out from the top of the tower, condensed into liquid phase by the second condenser 8 and flows into the second reflux tank 18, a part of liquid phase in the second reflux tank 18 is sent to the isopentane refiner 14 as product for purification, the purified isopentane is further cooled by the air cooler and then stored in the isopentane storage tank 15, another part of liquid phase in the second reflux tank 18 is led into the second rectifying tower 7 again for fractionation, and heavy component (n-pentane and extractant) is led out from the bottom of the tower, preheated by the third preheater 9 and then sent to the recovery tower 10. The recovery tower 10 heats and vaporizes the mixture at the bottom of the tower again, light component (n-pentane) is distilled out from the top of the tower, condensed into liquid phase by the third condenser 11 and flows into the third reflux tank 12, a part of liquid phase in the third reflux tank 12 is used as a product to be sent to the n-pentane refiner 13 for refining, the refined n-pentane is further cooled by an air cooler and then is stored in the n-pentane storage tank 16, the other part of liquid phase in the third reflux tank 12 is reintroduced into the recovery tower 10 for fractionation again, and heavy component (extractant) is exported from the bottom of the tower and then sent to the premixing tank 1 for recycling.
The mixed pentane and the extractant are mixed in the premixing tank 1 and then preheated, so that the thermal movement speed of molecules can be increased, the mixed pentane and the extractant are better and uniformly mixed, the extractant can selectively interact with one component in the mixed pentane, the solubility of the component in the extractant is far higher than that of other components, the selectivity enables the separation process to be more accurate, single components with higher purity can be obtained, the occurrence of side reactions is reduced, and the purity and quality of products are improved. The mixed pentane is separated twice by the first rectifying tower 3 and the second rectifying tower 7, the concentration of the product is higher, and the recovery tower 10 can recover the extractant, thereby realizing the recycling. The waste heat of the first reboiler 20, the second reboiler 19 and the third reboiler 17 is reused by the first preheater 2, the second preheater 6 and the third preheater 9 respectively, so that the use of high-quality energy sources is reduced, and the production cost is reduced.
The first condenser 4, the second condenser 8 and the third condenser 11 are all sleeve condensers, each sleeve condenser comprises a shell with openings at two ends and a plurality of groups of cooling sleeves arranged in the shell, refrigerant inlets 27 of all the cooling sleeves are converged into a main inlet on one side of the shell through a distributing pipe, and refrigerant outlets 26 of all the cooling sleeves are converged into a main outlet on the other side of the shell through another distributing pipe. The gaseous pentane enters the double pipe condenser from the main inlet, is split to the cooling double pipe through the distributing pipe, and the condensed liquid phase flows to the main outlet after being collected through the other distributing pipe.
The cooling jacket comprises an inner tube 21 and an outer tube 22 sleeved outside the inner tube 21, wherein the inner tube 21 is connected with the inner wall of the outer tube 22 through a spiral partition plate 23 arranged on the outer wall, and a cavity between the outer tube 22 and the inner tube 21 is separated into a spiral cavity 24 by the spiral partition plate 23. Flanges are arranged at both ends of the outer tube 22 for connecting the inner tube 21, and the flanges seal the spiral cavity 24. A medium conduit 25 with the same trend as the spiral cavity 24 is arranged in the spiral cavity 24, one end of the medium conduit 25 penetrates out of the outer tube 22 and is positioned at one end of the outer tube 22, and the other end of the medium conduit 25 penetrates out of the outer tube 22 and is positioned at the other end of the outer tube 22. The refrigerant inlet 27 is connected to the spiral chamber 24 and is disposed at one end of the outer tube 22, and the refrigerant outlet 26 is connected to the spiral chamber 24 and is disposed at the other end of the outer tube 22.
The gaseous pentane moves forward along the medium conduit 25, the refrigerant enters the spiral cavity 24 from the refrigerant inlet 27 to exchange heat with the medium conduit 25, and the gaseous pentane is condensed into liquid phase pentane, so that the heat exchange area is increased under the condition that the volume of the condenser is unchanged due to the spiral cavity 24 and the medium conduit 25. Because the two ends of the cooling sleeve are hollow, the temperature of the inner cavity of the inner tube 21 is increased, the density of gas is reduced, and external cold air can flow into the inner cavity of the inner tube 21 in the heat exchange process, so that the cooling efficiency is further improved, and the energy consumption is reduced.
In accordance with the above embodiments of the utility model, these embodiments are not exhaustive of all details, nor are they intended to limit the utility model to the precise embodiments disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the utility model and the practical application, to thereby enable others skilled in the art to best utilize the utility model and various modifications as are suited to the particular use contemplated. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model should be included in the protection scope of the present utility model.
Claims (7)
1. The utility model provides a mix accurate separator of pentane which characterized in that: including premixing jar (1), first rectifying column (3), recovery tower (10), normal pentane refiner (13) and isopentane refiner (14) of setting up side by side, one side of normal pentane refiner (13) is provided with normal pentane storage tank (16) through the pipeline connection, one side of isopentane refiner (14) is provided with isopentane storage tank (15) through the pipeline connection, the top of a tower side of first rectifying column (3) is provided with first condenser (4) through the pipeline connection, the below of first condenser (4) is provided with first reflux drum (5) through the pipeline connection, first reflux drum (5) are connected isopentane refiner (14) and first rectifying column (3) respectively through the pipeline, one side of the bottom of a tower of first rectifying column (3) is provided with first preheater (2) through the pipeline connection, the bottom of a tower opposite side of first rectifying column (3) is provided with first condenser (20) through the pipeline connection, the top of a tower (10) is provided with through pipeline connection, reflux drum (12) are connected with each other through pipeline (12), the tower bottom one side of recovery tower (10) is provided with third pre-heater (9) through pipe connection, the tower bottom opposite side of recovery tower (10) is provided with third reboiler (17) through pipe connection, the tower bottom discharge gate of recovery tower (10) is connected the feed inlet of third reboiler (17) and the feed inlet of premix jar (1) respectively through the pipeline, the tower bottom discharge gate of first rectifying column (3) is connected the feed inlet of first reboiler (20) and the feed inlet of third pre-heater (9) respectively through the pipeline.
2. The mixed pentane precise separation device of claim 1, wherein: the mixed pentane precise separation device further comprises a second rectifying tower (7), a second condenser (8) connected through a pipeline is arranged on one side of the top of the second rectifying tower (7), a second reflux tank (18) connected through a pipeline is arranged below the second condenser (8), the second reflux tank (18) is respectively connected with an isopentane refiner (14) and the second rectifying tower (7) through pipelines, a second preheater (6) connected through a pipeline is arranged on one side of the bottom of the second rectifying tower (7), a second reboiler (19) connected through a pipeline is arranged on the other side of the bottom of the second rectifying tower (7), a bottom discharge port of the first rectifying tower (3) is respectively connected with a feed port of the first reboiler (20) and a feed port of the second preheater (6) through pipelines, and a bottom discharge port of the second rectifying tower (7) is respectively connected with a feed port of the second reboiler (19) and a feed port of the third preheater (9) through pipelines.
3. The mixed pentane precise separation device of claim 2, wherein: the first condenser (4), the second condenser (8) and the third condenser (11) are sleeve type condensers, each sleeve type condenser comprises a shell with openings at two ends and a plurality of groups of cooling sleeves arranged in the shell, refrigerant inlets (27) of all the cooling sleeves are converged into a main inlet at one side of the shell through distribution pipes, and refrigerant outlets (26) of all the cooling sleeves are converged into a main outlet at the other side of the shell through another distribution pipe.
4. A mixed pentane precision separation apparatus according to claim 3, wherein: the cooling jacket comprises an inner tube (21) and an outer tube (22) sleeved outside the inner tube (21), the inner tube (21) is connected with the inner wall of the outer tube (22) through a spiral partition plate (23) arranged on the outer wall, a cavity between the outer tube (22) and the inner tube (21) is partitioned into a spiral cavity (24) by the spiral partition plate (23), flanges connected with the inner tube (21) are arranged at two ends of the outer tube (22), the spiral cavity (24) is sealed by the flanges, a medium conduit (25) with the same trend as that of the spiral cavity (24) is arranged in the spiral cavity (24), one end of the medium conduit (25) penetrates out of the outer tube (22) and is located at one end of the outer tube (22), the other end of the medium conduit (25) penetrates out of the outer tube (22) and is located at the other end of the outer tube (22), a refrigerant inlet (27) is communicated with the spiral cavity (24) and is arranged at one end of the outer tube (22), and a refrigerant outlet (26) is communicated with the spiral cavity (24) and is arranged at the other end of the outer tube (22).
5. The mixed pentane precise separation device of claim 2, wherein: the first rectifying tower (3), the second rectifying tower (7) and the recovery tower (10) are all connected with a vacuum pump set.
6. The mixed pentane precise separation device of claim 1, wherein: air coolers are connected to the pipeline between the isopentane refiner (14) and the isopentane storage tank (15) and the pipeline between the n-pentane refiner (13) and the n-pentane storage tank (16).
7. The mixed pentane precise separation device of claim 1, wherein: the first reboiler (20), the second reboiler (19) and the third reboiler (17) are thermosyphon type reboilers.
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