CN215310270U - Separation system of normal and isomeric alkane mixture - Google Patents
Separation system of normal and isomeric alkane mixture Download PDFInfo
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- CN215310270U CN215310270U CN202121087276.XU CN202121087276U CN215310270U CN 215310270 U CN215310270 U CN 215310270U CN 202121087276 U CN202121087276 U CN 202121087276U CN 215310270 U CN215310270 U CN 215310270U
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- 238000000926 separation method Methods 0.000 title claims abstract description 77
- 150000001335 aliphatic alkanes Chemical class 0.000 title claims abstract description 32
- 239000000203 mixture Substances 0.000 title claims abstract description 22
- 239000012528 membrane Substances 0.000 claims abstract description 152
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 11
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000002808 molecular sieve Substances 0.000 claims abstract description 11
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000010457 zeolite Substances 0.000 claims abstract description 11
- 239000011344 liquid material Substances 0.000 claims abstract description 6
- 239000012466 permeate Substances 0.000 claims description 40
- 230000001105 regulatory effect Effects 0.000 claims description 21
- 239000012465 retentate Substances 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 10
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000005516 engineering process Methods 0.000 abstract description 4
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 28
- 239000001282 iso-butane Substances 0.000 description 14
- IJDNQMDRQITEOD-UHFFFAOYSA-N sec-butylidene Natural products CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 14
- 238000007599 discharging Methods 0.000 description 9
- 239000012188 paraffin wax Substances 0.000 description 9
- 238000000034 method Methods 0.000 description 7
- 239000001273 butane Substances 0.000 description 6
- 238000012544 monitoring process Methods 0.000 description 6
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 5
- 239000002994 raw material Substances 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 3
- -1 small-molecule hydrocarbons Chemical class 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 2
- 238000005034 decoration Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000035699 permeability Effects 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model belongs to the field of petrochemical industry, and particularly relates to a separation system for a normal and isoparaffin mixture. The present invention provides a separation system comprising: the flash tank is provided with a mixed alkane liquid material inlet and a vaporized alkane outlet; a heater provided with an air inlet and an air outlet; the gas inlet of the heater is connected with the vaporized alkane outlet of the flash tank; the membrane component is provided with an air inlet, a permeating gas outlet and a permeating residual gas outlet, and an MFI type zeolite molecular sieve membrane is arranged in the membrane component; the air inlet of the membrane component is connected with the air outlet of the heater; and the air inlet of the vacuum pump is connected with the permeation gas outlet of the membrane module. The separation system provided by the utility model applies the membrane separation technology to the separation of the n-isoparaffin mixture, greatly reduces the separation energy consumption, and has good economic benefit and wide market prospect.
Description
Technical Field
The utility model belongs to the field of petrochemical industry, and particularly relates to a separation system for a normal and isoparaffin mixture.
Background
With the development of petrochemical industry, the application demand of small-molecule hydrocarbons is increasing, the effective utilization of the small-molecule hydrocarbons is always the focus of the attention of researchers in chemistry and chemical industry, and the separation of n-isoparaffin is the key point of the effective utilization of the small-molecule hydrocarbons. Most of the traditional n-isoparaffin separation adopts a rectification process, so that the energy consumption is high, and the stability is poor, so that the research and development of a novel high-efficiency separation technology have important strategic significance.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model aims to provide a separation system for a normal and isoparaffin mixture, which is suitable for continuous separation of the normal and isoparaffin mixture and has low separation energy consumption and high operation stability.
The utility model provides a separation system of normal isoparaffin mixture, comprising:
the flash tank is provided with a mixed alkane liquid material inlet and a vaporized alkane outlet;
a heater provided with an air inlet and an air outlet; the gas inlet of the heater is connected with the vaporized alkane outlet of the flash tank;
the membrane component is provided with an air inlet, a permeating gas outlet and a permeating residual gas outlet, and an MFI type zeolite molecular sieve membrane is arranged in the membrane component; the air inlet of the membrane component is connected with the air outlet of the heater;
and the air inlet of the vacuum pump is connected with the permeation gas outlet of the membrane module.
Preferably, the membrane component consists of a plurality of sections of membrane component units, each section of membrane component unit is provided with an air inlet, a permeating gas outlet and a permeating residual gas outlet, and an MFI type zeolite molecular sieve membrane is arranged in the membrane component unit; the gas inlet of the membrane component unit of the first section is connected with the gas outlet of the heater, the gas inlet of the membrane component unit of the next section is connected with the residual gas permeation outlet of the membrane component unit of the previous section, and the permeation gas permeation outlet of each membrane component unit is connected with the gas inlet of the vacuum pump.
Preferably, a mixed alkane feed regulating valve is arranged at a mixed alkane liquid feed inlet of the flash tank.
Preferably, a feeding flow meter is arranged on a connecting pipeline between the vaporized alkane outlet of the flash tank and the air inlet of the heater.
Preferably, a membrane module air inlet thermometer and a membrane module air inlet pressure gauge are installed on a connecting pipeline between the air outlet of the heater and the air inlet of the membrane module.
Preferably, a residual gas seepage outlet of the membrane component is provided with a residual gas seepage discharge flowmeter and a residual gas seepage discharge regulating valve.
Preferably, a permeate gas outlet of the membrane module is provided with a permeate gas discharging thermometer and a permeate gas discharging regulating valve.
Preferably, a permeate gas discharge pressure gauge is installed on a connecting pipeline between a permeate gas outlet of the membrane module and a gas inlet of the vacuum pump.
Preferably, a permeate gas discharge flowmeter is mounted on a connecting pipeline between a permeate gas outlet of the membrane module and a gas inlet of the vacuum pump.
Compared with the prior art, the utility model provides the n-isoparaffin mixture separation system with low energy consumption. The present invention provides a separation system comprising: the flash tank is provided with a mixed alkane liquid material inlet and a vaporized alkane outlet; a heater provided with an air inlet and an air outlet; the gas inlet of the heater is connected with the vaporized alkane outlet of the flash tank; the membrane component is provided with an air inlet, a permeating gas outlet and a permeating residual gas outlet, and an MFI type zeolite molecular sieve membrane is arranged in the membrane component; the air inlet of the membrane component is connected with the air outlet of the heater; and the air inlet of the vacuum pump is connected with the permeation gas outlet of the membrane module. When the separation system operates, normal-isoparaffin mixed liquid materials are firstly vaporized into gas in a flash tank, then the gas enters a heater for heating, the heated mixed paraffin gas enters a membrane component for separation, normal paraffin in the mixed paraffin gas permeates through a separation membrane and is pumped out from a permeation gas outlet of the membrane component by a vacuum pump, isoparaffin in the mixed paraffin gas is intercepted by the separation membrane, and finally the gas is discharged from a residual permeation gas outlet of the membrane component to form a high-purity isoparaffin product. The separation system provided by the utility model applies the membrane separation technology to the separation of the normal and isoparaffin mixture, and the MFI type zeolite molecular sieve membrane adopted can permeate normal paraffins and retain isoparaffins, and has the characteristics of high permeability, good repeatability and high stability. The separation system does not adopt the traditional rectification separation, greatly reduces the separation energy consumption, and has good economic benefit and wide market prospect.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a schematic diagram of a normal isoparaffin mixture separation system provided by an embodiment of the present invention;
FIG. 2 is a flow chart of a multistage membrane separation system for n-isoparaffin mixture provided by the embodiment of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The utility model provides a separation system of normal isoparaffin mixture, comprising:
the flash tank is provided with a mixed alkane liquid material inlet and a vaporized alkane outlet;
a heater provided with an air inlet and an air outlet; the gas inlet of the heater is connected with the vaporized alkane outlet of the flash tank;
the membrane component is provided with an air inlet, a permeating gas outlet and a permeating residual gas outlet, and an MFI type zeolite molecular sieve membrane is arranged in the membrane component; the air inlet of the membrane component is connected with the air outlet of the heater;
and the air inlet of the vacuum pump is connected with the permeation gas outlet of the membrane module.
Referring to fig. 1 and fig. 2, fig. 1 is a schematic diagram of an n-isoparaffin mixture separation system according to an embodiment of the present invention, and fig. 2 is a flowchart of a multi-stage n-isoparaffin mixture membrane separation system according to an embodiment of the present invention, in which 1 is a mixed paraffin feed regulating valve, 2 is a flash tank, 3 is a feed flow meter, 4 is a heater, 5 is a membrane module inlet thermometer, 6 is a membrane module inlet pressure gauge, 7 is a membrane module, 7-1 is a first stage membrane module unit, 7-2 is a second stage membrane module unit, 7-3 is a third stage membrane module unit, 7-4 is a fourth stage membrane module unit, 7-5 is a fifth stage membrane module unit, 7-6 is a sixth stage membrane module unit, 7-7 is a seventh stage membrane module unit, 8 is an excess gas discharge flow meter, 9 is an excess gas discharge regulating valve, and 10 is an excess gas discharge thermometer, 11 is a permeable gas discharging regulating valve, 12 is a permeable gas discharging pressure gauge, 13 is a permeable gas discharging flowmeter, and 14 is a vacuum pump.
The separation system provided by the utility model comprises a flash tank 2, a heater 4, a membrane module 7 and a vacuum pump 14. The flash tank 2 is used for vaporizing raw material liquid (n-isoparaffin mixed liquid) into gas, and is provided with a mixed paraffin liquid inlet and a vaporized paraffin outlet.
In the separation system provided by the utility model, a heater 4 is used for heating vaporized alkane to meet the requirement of inlet air temperature of a membrane component, and is provided with an air inlet and an air outlet; the air inlet of the heater 4 is connected with the vaporized alkane outlet of the flash tank 2.
In the separation system provided by the utility model, a membrane component 7 is used for separating normal paraffin and isoparaffin contained in vaporized paraffin, is provided with an air inlet, a permeate gas outlet and a retentate gas outlet, and is internally provided with an MFI type zeolite molecular sieve membrane; the air inlet of the membrane component 7 is connected with the air outlet of the heater 4. When the membrane module 7 is in operation, the vaporized alkane is divided into two parts, namely permeate gas and retentate gas, in the membrane module 7, the main component of the permeate gas is normal alkane, and the main component of the retentate gas is isoparaffin.
In the separation system provided by the utility model, the vacuum pump 14 is used for vacuumizing a permeation gas outlet of the membrane module 7 and providing a negative pressure driving force for the membrane module 7; the inlet of the vacuum pump 14 is connected to the permeate outlet of the membrane module 7.
In the separation system provided by the present invention, the membrane module 7 is preferably composed of a plurality of sections of membrane module units, each section of membrane module unit is provided with an air inlet, a permeate gas outlet and a retentate gas outlet, and an MFI type zeolite molecular sieve membrane is installed inside. In the utility model, the connection mode of the membrane module units can be parallel connection or series connection; when the treatment capacity needs to be increased, the multi-stage membrane module units are preferably connected in parallel, and when the concentration of isoparaffin needs to be increased, the multi-stage membrane module units are preferably connected in series. In one embodiment provided by the utility model, the gas inlet of the membrane module unit in the first section is connected with the gas outlet of the heater 4, the gas inlet of the membrane module unit in the next section is connected with the residual gas outlet of the membrane module unit in the previous section, and the permeate gas outlet of each membrane module unit is connected with the gas inlet of the vacuum pump 14. In one embodiment provided by the utility model, the membrane module 7 is composed of seven sections of membrane module units, and specifically comprises a first section of membrane module unit 7-1, a second section of membrane module unit 7-2, a third section of membrane module unit 7-3, a fourth section of membrane module unit 7-4, a fifth section of membrane module unit 7-5, a sixth section of membrane module unit 7-6 and a seventh section of membrane module unit 7-7, as shown in fig. 2.
In the separation system provided by the utility model, a mixed alkane liquid inlet of the flash tank 2 is preferably provided with a mixed alkane feeding regulating valve 1, and a connecting pipeline between a vaporized alkane outlet of the flash tank 2 and an air inlet of the heater 4 is preferably provided with a feed flowmeter 3. In the utility model, the feeding flow of the system is accurately controlled by regulating the opening degree of the mixed alkane feeding regulating valve 1 and observing the reading of the feeding flowmeter 3.
In the separation system provided by the utility model, a membrane module air inlet thermometer 5 is preferably arranged on a connecting pipeline between the air outlet of the heater 4 and the air inlet of the membrane module 7, and is used for accurately monitoring the air inlet temperature of the membrane module 7.
In the separation system provided by the utility model, a membrane module air inlet pressure gauge 6 is preferably arranged on a connecting pipeline between an air outlet of a heater 4 and an air inlet of a membrane module 7 and is used for accurately monitoring the air inlet pressure of the membrane module 7.
In the separation system provided by the utility model, the residual gas seepage outlet of the membrane module 7 is preferably provided with a residual gas seepage discharge flowmeter 8 for accurately monitoring the residual gas seepage discharge flow.
In the separation system provided by the utility model, the residual gas permeation outlet of the membrane module 7 is preferably provided with a residual gas permeation discharge regulating valve 9 for regulating and controlling the discharge flow of the residual gas permeation, so as to regulate and control the air inlet pressure of the membrane module 7.
In the separation system provided by the utility model, a permeate gas outlet of the membrane module 7 is preferably provided with a permeate gas outlet thermometer 10 for accurately monitoring the permeate gas outlet temperature of the membrane module 7.
In the separation system provided by the utility model, a permeate gas outlet of the membrane module 7 is preferably provided with a permeate gas discharging regulating valve 11 for regulating and controlling the flow of permeate gas discharging.
In the separation system provided by the utility model, a connecting pipeline between a permeate gas outlet of the membrane module 7 and a gas inlet of a vacuum pump 14 is preferably provided with a permeate gas discharge pressure gauge 12 for accurately monitoring the vacuum degree of the permeate side of the membrane module 7.
In the separation system provided by the utility model, a connecting pipeline between a permeate gas outlet of the membrane module 7 and an air inlet of the vacuum pump 14 is preferably provided with a permeate gas discharge flow meter 13 for accurately monitoring the permeate gas discharge flow.
In the separation system provided by the present invention, the driving force for membrane separation is pressure driven, including positive and negative pressure. Wherein, the positive pressure is controlled by the residual gas discharge regulating valve 9, and the negative pressure is realized by the vacuum pumping of the vacuum pump 14.
The separation system provided by the utility model applies the membrane separation technology to the separation of the normal and isoparaffin mixture, and the MFI type zeolite molecular sieve membrane adopted can permeate normal paraffins and retain isoparaffins, and has the characteristics of high permeability, good repeatability and high stability. The system does not adopt the traditional rectification separation, greatly reduces the separation energy consumption, and has good economic benefit and wide market prospect.
For the sake of clarity, the separation of normal isobutane is taken as an example and is explained in detail by the following examples.
Example 1
The separation of the normal butane and the isobutane mixture is carried out in the separation system shown in fig. 2, and the specific process is as follows:
fully opening a valve switch on an outlet path of a permeation gas pipe, opening a vacuum pump 14 for tightness test until the vacuum degree reaches-0.1 MPa, displaying the reading of a permeation gas discharging flowmeter 13 as 0, testing the tightness degree of each joint of the device if the vacuum degree cannot be reached, then opening a flash tank 2 and a heater 4 for heating, paying attention to prevent temperature runaway, slowly heating the heater 4, opening a mixed alkane feeding regulating valve 1 to start to introduce raw material liquid (normal/isobutane mixed liquid) when the flash tank is heated to more than 100 ℃, and regulating the feeding pressure of a membrane module by regulating a residual gas discharging regulating valve 9.
The mixed butane raw material liquid is vaporized into gas through a flash tank 2, the feeding flow is controlled through a feeding flow meter 3, and then the mixed butane raw material liquid enters a heater 4 for heating. And the heated mixed butane gas enters the first stage membrane module unit 7-1 from the feed inlet of the membrane module for separation, the mixed butane gas completes the separation process while flowing on the surface of the membrane, wherein most of the permeated mixed butane gas is normal butane, and most of isobutane is trapped. After the first-stage membrane separation, the gas is divided into two parts, namely residual gas and permeation gas, the residual gas is discharged from a residual gas permeation outlet of the first-stage membrane module unit 7-1 and then sequentially enters a second-stage membrane module unit 7-2, a third-stage membrane module unit 7-3, a fourth-stage membrane module unit 7-4, a fifth-stage membrane module unit 7-5, a sixth-stage membrane module unit 7-6 and a seventh-stage membrane module unit 7-7 to be continuously separated, and the permeation gas is pumped out from a permeation gas outlet of each stage of membrane module unit by a vacuum pump 14. In this way, n-butane in the mixed butane gas gradually permeates through the membrane in the process of flowing through each section of membrane module unit to become permeate gas, and the permeate gas is pumped out from a permeate gas outlet by the vacuum pump 14; and the residual gas is continuously separated and concentrated by each subsequent membrane module unit, and is discharged from a residual gas outlet of the last membrane module unit, so that a high-purity isobutane product is obtained.
In the present example, when the feed flow rate was set to 3L/min, the flash tank temperature was 100 ℃, the heater was 110 ℃, the membrane module unit temperature in each stage was 70 ℃, and the membrane module inlet gauge pressure was 0.1MPaG, the concentration of isobutane in the retentate gas was 98.23%.
Example 2
The separation of the n-butane and the isobutane mixture was carried out in the separation system shown in fig. 2, in a specific process see example 1; in this example, when the feed flow rate was set to 3.5L/min, the flash tank temperature was 120 ℃, the heater was 140 ℃, the membrane module unit temperature in each stage was 90 ℃, and the membrane module inlet gauge pressure was 0.1MPaG, the isobutane concentration in the retentate gas was 98.18%.
Example 3
The separation of the n-butane and the isobutane mixture was carried out in the separation system shown in fig. 2, in a specific process see example 1; in the present example, when the feed flow rate was set to 5L/min, the flash tank temperature was 120 ℃, the heater was 140 ℃, the membrane module unit temperature in each stage was 82 ℃, and the membrane module inlet gauge pressure was 0.2MPaG, the concentration of isobutane in the retentate gas was 96.42%.
Example 4
The separation of the n-butane and the isobutane mixture was carried out in the separation system shown in fig. 2, in a specific process see example 1; in the present example, when the feed flow rate was set to 4L/min, the flash tank temperature was 140 ℃, the heater was 130 ℃, the membrane module unit temperature in each stage was 86 ℃, and the membrane module inlet gauge pressure was 0.1MPaG, the isobutane concentration in the retentate gas was 97.20%.
Example 5
The separation of the n-butane and the isobutane mixture was carried out in the separation system shown in fig. 2, in a specific process see example 1; in this example, when the feed flow rate was set to 6.5L/min, the flash tank temperature was 110 ℃, the heater was 120 ℃, the membrane module unit temperature in each stage was 80 ℃, and the membrane module inlet gauge pressure was 0.2MPaG, the isobutane concentration in the retentate gas was 96.56%.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (9)
1. A separation system for a n-isoparaffin mixture, comprising:
the flash tank is provided with a mixed alkane liquid material inlet and a vaporized alkane outlet;
a heater provided with an air inlet and an air outlet; the gas inlet of the heater is connected with the vaporized alkane outlet of the flash tank;
the membrane component is provided with an air inlet, a permeating gas outlet and a permeating residual gas outlet, and an MFI type zeolite molecular sieve membrane is arranged in the membrane component; the air inlet of the membrane component is connected with the air outlet of the heater;
and the air inlet of the vacuum pump is connected with the permeation gas outlet of the membrane module.
2. The separation system according to claim 1, wherein the membrane module is composed of a plurality of sections of membrane module units, each section of membrane module unit is provided with a gas inlet, a permeate gas outlet and a retentate gas outlet, and an MFI type zeolite molecular sieve membrane is arranged in each section of membrane module unit; the gas inlet of the membrane component unit of the first section is connected with the gas outlet of the heater, the gas inlet of the membrane component unit of the next section is connected with the residual gas permeation outlet of the membrane component unit of the previous section, and the permeation gas permeation outlet of each membrane component unit is connected with the gas inlet of the vacuum pump.
3. The separation system of claim 1 wherein the mixed alkane liquid feed inlet of the flash tank is fitted with a mixed alkane feed regulating valve.
4. The separation system of claim 1, wherein a feed flow meter is installed in a connection line between the vaporized alkane outlet of the flash tank and the gas inlet of the heater.
5. The separation system according to claim 1, wherein a membrane module inlet air thermometer and a membrane module inlet air pressure gauge are installed on a connecting pipeline between the outlet of the heater and the inlet of the membrane module.
6. The separation system of claim 1, wherein the retentate outlet of the membrane module is fitted with a retentate discharge flow meter and a retentate discharge regulating valve.
7. The separation system of claim 1, wherein the permeate gas outlet of the membrane module is fitted with a permeate gas outlet thermometer and a permeate gas outlet regulating valve.
8. The separation system of claim 1, wherein a permeate gas discharge pressure gauge is installed on a connecting pipeline between a permeate gas outlet of the membrane module and an air inlet of the vacuum pump.
9. The separation system according to claim 1, wherein a permeate gas discharge flow meter is installed on a connecting pipeline between a permeate gas outlet of the membrane module and an air inlet of the vacuum pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121087276.XU CN215310270U (en) | 2021-05-20 | 2021-05-20 | Separation system of normal and isomeric alkane mixture |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121087276.XU CN215310270U (en) | 2021-05-20 | 2021-05-20 | Separation system of normal and isomeric alkane mixture |
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| CN215310270U true CN215310270U (en) | 2021-12-28 |
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| CN202121087276.XU Active CN215310270U (en) | 2021-05-20 | 2021-05-20 | Separation system of normal and isomeric alkane mixture |
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