CN111004080A - Separation method and separation device for reaction product of propane dehydrogenation to propylene - Google Patents
Separation method and separation device for reaction product of propane dehydrogenation to propylene Download PDFInfo
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- CN111004080A CN111004080A CN201811168976.4A CN201811168976A CN111004080A CN 111004080 A CN111004080 A CN 111004080A CN 201811168976 A CN201811168976 A CN 201811168976A CN 111004080 A CN111004080 A CN 111004080A
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- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 92
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 73
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 73
- 238000000926 separation method Methods 0.000 title claims abstract description 47
- 239000001294 propane Substances 0.000 title claims abstract description 46
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 35
- 239000007795 chemical reaction product Substances 0.000 title claims abstract description 31
- 239000007789 gas Substances 0.000 claims abstract description 71
- 239000001257 hydrogen Substances 0.000 claims abstract description 30
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 30
- 239000002737 fuel gas Substances 0.000 claims abstract description 28
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000012071 phase Substances 0.000 claims abstract description 27
- 239000000047 product Substances 0.000 claims abstract description 23
- 239000007791 liquid phase Substances 0.000 claims abstract description 16
- 238000011084 recovery Methods 0.000 claims abstract description 7
- 238000003303 reheating Methods 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims abstract description 5
- 238000000605 extraction Methods 0.000 claims description 15
- 229910052799 carbon Inorganic materials 0.000 claims description 9
- 238000004781 supercooling Methods 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- 238000003795 desorption Methods 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 4
- 230000002378 acidificating effect Effects 0.000 claims description 3
- 150000002431 hydrogen Chemical class 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 230000000694 effects Effects 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract description 4
- 238000000034 method Methods 0.000 description 18
- 238000005516 engineering process Methods 0.000 description 5
- 238000001179 sorption measurement Methods 0.000 description 5
- 238000002360 preparation method Methods 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000005336 cracking Methods 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000003507 refrigerant Substances 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
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- Organic Chemistry (AREA)
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- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to the field of chemical industry, and discloses a separation method and a separation device for a reaction product of propane dehydrogenation to propylene, wherein the separation method comprises the following steps: the reaction product of propane dehydrogenation to propylene is compressed and cooled and then sent to a first-stage flash tank for gas-liquid separation; the gas phase at the top of the first-stage flash tank is reheated, pressurized and cooled again and then is sent to a PSA device; separating the hydrogen and desorbed gas in a PSA device, wherein the desorbed gas is pressurized and cooled and then sent to a second-stage flash tank, the gas phase at the top of the second-stage flash tank is reheated and then sent to a fuel gas system, and the liquid phase at the bottom of the tank is sent to a deethanizer; and (3) conveying the liquid phase at the bottom of the first-stage flash tank to a deethanizer, reheating the gas phase at the top of the deethanizer, conveying the gas phase to a fuel gas system, conveying the liquid phase at the bottom of the tower to a propylene rectifying tower, obtaining a propylene product at the top of the propylene rectifying tower, and obtaining propane at the bottom of the tower. The invention improves the separation effect of reaction products, improves the recovery effect and purity of hydrogen and can effectively reduce the energy consumption of a separation system.
Description
Technical Field
The invention belongs to the field of chemical industry, and particularly relates to a separation method and a separation device for a reaction product of propylene preparation through propane dehydrogenation.
Background
Propylene is an important basic organic chemical raw material in the chemical industry. For a long time, the source of propylene at home and abroad mainly depends on naphtha cracking co-production and FCC by-products. Statistically, the Chinese market accounts for more than 15% of the global propylene demand, and the consumption is increasing at a rate of about 5-6% per year, and the propylene demand gap is increasing in recent years. With the shortage of petroleum resources and the low price of natural gas relative to the price of crude oil, the C3 and C4 alkanes derived therefrom are receiving more and more attention, and among them, the propane catalytic dehydrogenation technology (PDH) is undoubtedly the focus of most attention in the field of C3 utilization.
In the future domestic market, with the continuous operation of Methanol To Olefin (MTO) devices, the impact on the traditional FCC and ethylene cracking olefin production line is bound to be generated. The production of propylene and isobutylene as by-products of FCC and ethylene cracking will be less and less. Therefore, the technology for preparing propylene by propane dehydrogenation faces a very good development opportunity and has huge market potential.
At present, the patent technologies for preparing propylene by propane dehydrogenation in the world are as follows: the Oleflex process from UOP, the Catofin process from LUMMUS, the Star process from Uhde, the FBD-4 process from Snamprogetti/Yarsintz, and the PDH process from Linde/Pasteur. These processes generally employ cryogenic processes to separate the reaction product of propane dehydrogenation to propylene. The cryogenic separation process is a main method for separating naphtha steam cracking products, has mature technology and wide application, and almost all three carbon in reaction products are condensed due to low temperature of refrigerant, so that the yield of propylene is high, but the requirement on equipment materials is high, and the energy consumption is high.
CN102795956B discloses a recovery method of a reaction product of propane dehydrogenation to propylene, which adopts a mode of combining membrane separation and cryogenic separation to separate the reaction product of propane dehydrogenation to propylene. However, the recovery rate of the hydrogen-rich gas in the membrane separation is low, and if the hydrogen-rich gas is required to be sent out as a product and needs to be compressed separately, the total energy consumption is not reduced.
Basfoggin discloses a series of patents CN100567230C, CN101087740B, CN101137605A, CN101415661A, which include the whole process from propane dehydrogenation to product separation. Because the reaction product contains H2O、CO2、CO、N2CN100567230C discloses the use of washing processes to remove part of the impurities, and CN101087740B, CN101137605A disclose the use of inert absorbents to separate the part of the impurities. CN101415661A discloses a method for separating propylene products by adopting pressure swing adsorption. However, the hydrogen-rich gas obtained by the methods has low hydrogen content and high hydrocarbon content and can only be used as fuel gas to be burnt.
CN102040445 discloses a process flow for dehydrogenating a low-carbon hydrocarbon rich in propane to prepare propylene, which adopts gasoline as an absorbent to separate light components and carbon III in a propane dehydrogenation product. However, the propane dehydrogenation product has high hydrogen content, the required circulating amount of the absorbent is very large, and the energy consumption is high.
Disclosure of Invention
In order to overcome the defects, the invention aims to provide the method and the device for separating the reaction product of the dehydrogenation of propane to propylene, which have the advantages of good separation effect, simple operation, low energy consumption and high added value of byproducts.
The invention provides a separation method of a reaction product for preparing propylene by propane dehydrogenation, which comprises the following steps:
the reaction product of propane dehydrogenation to propylene is compressed and cooled and then sent to a first-stage flash tank for gas-liquid separation;
the gas phase at the top of the first-stage flash tank is reheated, pressurized and cooled again and then is sent to a PSA device; separating the hydrogen and desorbed gas in a PSA device, wherein the desorbed gas is pressurized and cooled and then sent to a second-stage flash tank, the gas phase at the top of the second-stage flash tank is reheated and then sent to a fuel gas system, and the liquid phase at the bottom of the tank is sent to a deethanizer;
and (3) conveying the liquid phase at the bottom of the first-stage flash tank to a deethanizer, reheating the gas phase at the top of the deethanizer, conveying the gas phase to a fuel gas system, conveying the liquid phase at the bottom of the tower to a propylene rectifying tower, obtaining a propylene product at the top of the propylene rectifying tower, and obtaining propane at the bottom of the tower.
According to the invention, preferably, the gas phase at the top of the deethanizer can also be sent to a tail gas supercooling tower for carbon three recovery, and then sent to a fuel gas system after reheating.
In the invention, the reaction product of propylene preparation by propane dehydrogenation preferably further comprises a pretreatment step before entering the first flash tank, wherein the pretreatment step comprises acidic component removal and drying. The cooled reaction product of propylene preparation by propane dehydrogenation enters a first-stage flash tank for gas-liquid separation after the pretreatment of compressing to 0.5-3.05MPaG, removing acid components, drying and the like.
According to the invention, the first-stage flash tank preferably operates at a temperature of-40 ℃ to 18 ℃ and a pressure of 0.5MPaG to 3.0 MPaG. The liquid phase separated by the first-stage flash tank is discharged through the bottom of the tank and is pressurized by a pump and then enters a deethanizer. And the gas phase separated by the first-stage flash tank is discharged from the top of the tank, and is sent to a PSA device after being reheated by a heat exchanger, increased by a compressor and recooled by the heat exchanger in sequence.
According to the present invention, preferably, the PSA apparatus inlet temperature is 20 ℃ to 40 ℃ and the inlet pressure is 2.0-3.0 MPaG. The gas phase flow is divided into qualified high-purity hydrogen product and desorbed gas through a PSA device, preferably, the outlet hydrogen pressure of the PSA device is 2.3-2.5MPaG, the desorbed gas pressure is 0.01-0.05MPaG, and the concentration of the hydrogen separated by the PSA device is 92.5-99.999 mol%. Wherein, the obtained high-purity hydrogen product is sent to a hydrogen pipe network or circulated back to the propane dehydrogenation reactor as diluent gas according to the reaction requirement; the stripping gas is pressurized and cooled and then sent to a second-stage flash tank, the working temperature of the second-stage flash tank is preferably-100 ℃ to-35 ℃, and the pressure of the second-stage flash tank is preferably 0.2MPaG to 0.6 MPaG. According to the invention, preferably, the gas phase at the top of the second-stage flash tank is reheated to 30-40 ℃ and then sent to a fuel gas system, and the liquid phase at the bottom of the tank is sent to a deethanizer.
In the invention, preferably, the gas phase at the top of the deethanizer is reheated to 30-40 ℃ and then sent to a fuel gas system, and further preferably, the gas phase at the top of the deethanizer is sent to a tail gas supercooling tower to recover carbon III, and then reheated and sent to the fuel gas system. And (3) sending the liquid phase at the bottom of the deethanizer to a propylene rectifying tower, obtaining a qualified propylene product at the top of the propylene rectifying tower, and returning propane at the bottom of the propylene rectifying tower as circulating propane to the depropanizer to participate in the propane dehydrogenation reaction.
Another aspect of the present invention provides a separation apparatus for producing a reaction product of propylene by propane dehydrogenation, the separation apparatus comprising: the system comprises a feed compressor, a first heat exchanger, a first-stage flash tank, a second heat exchanger, a PSA feed compressor, a third heat exchanger, a PSA device, a PSA tail gas compressor, a fourth heat exchanger, a second-stage flash tank, a fifth heat exchanger, a deethanizer, a sixth heat exchanger and a propylene rectifying tower;
wherein, a feed pipeline of a reaction product for preparing propylene by propane dehydrogenation is sequentially connected with a feed compressor, a first heat exchanger and a first-stage flash tank;
the tank top of the first-stage flash tank is sequentially connected with a second heat exchanger, a PSA feeding compressor, a third heat exchanger and a PSA device, and the tank bottom is connected with a deethanizer;
the PSA device is respectively provided with a hydrogen extraction pipeline and a desorption gas extraction pipeline;
the desorbed gas extraction pipeline is sequentially connected with the PSA tail gas compressor, the fourth heat exchanger and the second-stage flash tank;
the top of the second-stage flash tank is sequentially connected with a fifth heat exchanger and a fuel gas system, and the bottom of the tank is connected with a deethanizer;
the top of the deethanizer is sequentially connected with a sixth heat exchanger and a fuel gas system, and the bottom of the deethanizer is connected with a propylene rectifying tower;
the top of the propylene rectifying tower is provided with a propylene product extraction pipeline, and the bottom of the propylene rectifying tower is provided with a propane extraction pipeline.
According to the invention, preferably, a tail gas supercooling tower is further arranged at the top of the deethanizer, and the top of the deethanizer is sequentially connected with the tail gas supercooling tower, the sixth heat exchanger and a fuel gas system.
Compared with the prior art, the invention has the following advantages:
(1) according to the invention, at least 70 mol% of hydrogen in the reactant for preparing propylene by propane dehydrogenation is separated by the pressure swing adsorption PSA device, so that the feeding treatment capacity of the subsequent separation unit is reduced, namely the equipment size of the subsequent separation unit is reduced, the equipment cost in the cryogenic process is saved, the total refrigeration load of the cryogenic separation is reduced, and the power consumption of the compressor is reduced.
(2) The invention removes partial hydrogen through pressure swing adsorption, so that the concentration of carbon three in the hydrocarbon-rich material flow is relatively high, the backward movement of cold energy is avoided, the distribution of the required refrigeration load is deviated to a high-temperature refrigerant with lower grade, and the energy consumption is further reduced.
(3) In the invention, the high-purity hydrogen of the pressure swing adsorption PSA device and the carbon content in the gas phase at the top of the second-stage flash tank for cryogenic separation are lower, the propylene loss is less, and the high recovery rate of the propylene is ensured.
(4) The invention adopts the mode of combining pressure swing adsorption PSA and cryogenic separation technology to remove light components in the reaction product for preparing propylene by propane dehydrogenation, separates to obtain gas-phase hydrogen-rich product and fuel gas, and refines the liquid-phase product to obtain propylene, thereby improving the separation effect of the reaction product, improving the recovery effect and purity of hydrogen, and effectively reducing the energy consumption of a separation system.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in more detail exemplary embodiments thereof with reference to the attached drawings, in which like reference numerals generally represent like parts throughout.
FIG. 1 shows a flow diagram of a process for the separation of reaction products of propane dehydrogenation to propylene according to example 1 of the present invention.
Fig. 2 shows a flow diagram of a method for separating a reaction product from the dehydrogenation of propane to propylene according to an embodiment of the present invention.
Description of reference numerals:
1. a feed compressor; 2. a first heat exchanger; 3. a first-stage flash tank; 4. a second heat exchanger; 5. a PSA feed compressor; 6. a third heat exchanger; 7. a PSA unit; 8. a PSA tail gas compressor; 9. a fourth heat exchanger; 10. a second-stage flash tank; 11. a fifth heat exchanger; 12. a deethanizer; 13. a sixth heat exchanger; 14. a propylene rectification column; 15. and (5) tail gas supercooling.
100. Dehydrogenating propane to prepare propylene reaction product; 200. a high purity hydrogen product; 300. desorbing gas; 400. a fuel gas; 500. a propylene product; 600. the propane is recycled.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the following describes preferred embodiments of the present invention, it should be understood that the present invention may be embodied in various forms and should not be limited by the embodiments set forth herein.
Example 1
Taking a 66 ten thousand tons of propylene dehydrogenation reaction product recovery device as an example, the separation method shown in fig. 1 is adopted to obtain the results shown in the following table 1 through flow simulation.
A separation device:
a feed pipeline of a reaction product for preparing propylene by propane dehydrogenation is sequentially connected with a feed compressor 1, a first heat exchanger 2 and a first-stage flash tank 3; the top of the first-stage flash tank 3 is sequentially connected with a second heat exchanger 4, a PSA feeding compressor 5, a third heat exchanger 6 and a PSA device 7, and the bottom of the tank is connected with a deethanizer 12; the PSA device 7 is respectively provided with a hydrogen extraction pipeline and a desorption gas extraction pipeline; the desorbed gas extraction pipeline is sequentially connected with a PSA tail gas compressor 8, a fourth heat exchanger 9 and a second-stage flash tank 10; the top of the second-stage flash tank 10 is sequentially connected with a fifth heat exchanger 11 and a fuel gas system, and the bottom of the tank is connected with a deethanizer 12; the top of the deethanizer 12 is sequentially connected with a tail gas supercooling tower 15, a sixth heat exchanger 13 and a fuel gas system, and the bottom of the deethanizer is connected with a propylene rectifying tower 14; a propylene product extraction pipeline is arranged at the top of the propylene rectifying tower 14, and a propane extraction pipeline is arranged at the bottom of the tower.
The process flow comprises the following steps:
the reaction product 100 of the propane dehydrogenation propylene preparation is compressed to 1.3MPaG by a feed compressor 1, and is subjected to heat exchange with a propylene refrigerant in a first heat exchanger 2, temperature reduction to-35 ℃, removal of acidic substances, drying and then sent to a first-stage flash tank 3 for gas-liquid separation; the working pressure in the first-stage flash tank 3 is 1.3MPaG, and the temperature is-35 ℃.
The gas phase at the top of the first-stage flash tank 3 is reheated by a second heat exchanger 4, pressurized to 2.6MPaG by a PSA feeding compressor 5, cooled to 40 ℃ by a third heat exchanger 6 and then sent to a PSA device 7; high-purity hydrogen product 200 with the purity of 99.999 percent and desorbed gas 300 are obtained by separation in a PSA device 7, wherein the gas pressure at the inlet of the PSA device 7 is 2.5MPaG, the pressure of the high-purity hydrogen product 200 is 2.4MPaG, and the pressure of the desorbed gas 300 is 0.2 MPaG. The desorbed gas 300 is pressurized to 0.5MPaG by a PSA tail gas compressor 8, cooled to-97 ℃ by a fourth heat exchanger 9 and then sent to a second-stage flash tank 10, the gas phase at the top of the second-stage flash tank 10 is reheated to 35 ℃ by a fifth heat exchanger 11 and then sent to a fuel gas system as fuel gas 400, and the liquid phase at the bottom of the tank is sent to a deethanizer 12.
The liquid phase at the bottom of the first-stage flash tank 3 is sent to a deethanizer 12.
And (3) sending the gas phase at the top of the deethanizer 12 to tail gas through a cooling tower 15 to recover carbon III, reheating the gas phase to 35 ℃ through a sixth heat exchanger 13, sending the reheated gas to a fuel gas system as fuel gas 400, sending the liquid phase at the bottom of the deethanizer to a propylene rectifying tower 14, obtaining a propylene product 500 at the top of the propylene rectifying tower 14, and obtaining the circulating propane 600 at the bottom of the tower.
TABLE 1
Wherein, a large amount of hydrogen is used as the circulating gas in the separation process and is respectively used for the regeneration system and the reactor system, so that the mass flow of the hydrogen between the product gas and the pure hydrogen has deviation.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (10)
1. A separation method of a reaction product for preparing propylene by propane dehydrogenation is characterized by comprising the following steps:
the reaction product of propane dehydrogenation to propylene is compressed and cooled and then sent to a first-stage flash tank for gas-liquid separation;
the gas phase at the top of the first-stage flash tank is reheated, pressurized and cooled again and then is sent to a PSA device; separating the hydrogen and desorbed gas in a PSA device, wherein the desorbed gas is pressurized and cooled and then sent to a second-stage flash tank, the gas phase at the top of the second-stage flash tank is reheated and then sent to a fuel gas system, and the liquid phase at the bottom of the tank is sent to a deethanizer;
and (3) conveying the liquid phase at the bottom of the first-stage flash tank to a deethanizer, reheating the gas phase at the top of the deethanizer, conveying the gas phase to a fuel gas system, conveying the liquid phase at the bottom of the tower to a propylene rectifying tower, obtaining a propylene product at the top of the propylene rectifying tower, and obtaining propane at the bottom of the tower.
2. The separation method according to claim 1, wherein the overhead gas phase of the deethanizer can be sent to a tail gas supercooling tower for carbon recovery, and then sent to a fuel gas system after reheating.
3. The separation method according to claim 1, wherein the reaction product of propane dehydrogenation to propylene further comprises a pretreatment step before entering the first flash tank, and the pretreatment step comprises removal of acidic components and drying.
4. The separation process according to claim 1, wherein the first stage flash tank is operated at a temperature of-40 ℃ to 18 ℃ and a pressure of 0.5MPaG to 3.0 MPaG.
5. The separation process according to claim 1, wherein the second stage flash tank is operated at a temperature of-100 ℃ to-35 ℃ and a pressure of 0.2MPaG to 0.6 MPaG.
6. The separation process of claim 1, wherein the concentration of hydrogen separated by the PSA apparatus is from 92.5 to 99.999 mol%.
7. The separation process according to claim 1, wherein the PSA unit inlet temperature is from 20 ℃ to 40 ℃ and the inlet pressure is from 2.0 to 3.0 MPaG; the outlet hydrogen pressure of the PSA device is 2.3-2.5MPaG, and the desorption gas pressure is 0.01-0.05 MPaG.
8. The separation process of claim 1, wherein the overhead gas phase of the deethanizer is reheated to 30 ℃ to 40 ℃ and then fed to a fuel gas system, and the overhead gas phase of the second-stage flash drum is reheated to 30 ℃ to 40 ℃ and then fed to the fuel gas system.
9. A separation device for preparing propylene reaction products by propane dehydrogenation is characterized by comprising: the system comprises a feed compressor, a first heat exchanger, a first-stage flash tank, a second heat exchanger, a PSA feed compressor, a third heat exchanger, a PSA device, a PSA tail gas compressor, a fourth heat exchanger, a second-stage flash tank, a fifth heat exchanger, a deethanizer, a sixth heat exchanger and a propylene rectifying tower;
wherein, a feed pipeline of a reaction product for preparing propylene by propane dehydrogenation is sequentially connected with a feed compressor, a first heat exchanger and a first-stage flash tank;
the tank top of the first-stage flash tank is sequentially connected with a second heat exchanger, a PSA feeding compressor, a third heat exchanger and a PSA device, and the tank bottom is connected with a deethanizer;
the PSA device is respectively provided with a hydrogen extraction pipeline and a desorption gas extraction pipeline;
the desorbed gas extraction pipeline is sequentially connected with the PSA tail gas compressor, the fourth heat exchanger and the second-stage flash tank;
the top of the second-stage flash tank is sequentially connected with a fifth heat exchanger and a fuel gas system, and the bottom of the tank is connected with a deethanizer;
the top of the deethanizer is sequentially connected with a sixth heat exchanger and a fuel gas system, and the bottom of the deethanizer is connected with a propylene rectifying tower;
the top of the propylene rectifying tower is provided with a propylene product extraction pipeline, and the bottom of the propylene rectifying tower is provided with a propane extraction pipeline.
10. The separation device according to claim 9, wherein a tail gas supercooling tower is further arranged at the top of the deethanizer, and the top of the deethanizer is sequentially connected with the tail gas supercooling tower, the sixth heat exchanger and a fuel gas system.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113717023A (en) * | 2020-05-26 | 2021-11-30 | 中国石油天然气集团有限公司 | Method and device for separating propane dehydrogenation product |
| CN113856571A (en) * | 2021-11-08 | 2021-12-31 | 万华化学集团股份有限公司 | Electric heating plate type reactor and application thereof |
| CN114163291A (en) * | 2020-09-10 | 2022-03-11 | 惠生工程（中国）有限公司 | Propane dehydrogenation reaction product separation system and method |
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| CN114804148A (en) * | 2022-02-16 | 2022-07-29 | 天津大学 | Propane dehydrogenation and chemical looping combustion and synthetic ammonia coupling system and process |
| CN114804148B (en) * | 2022-02-16 | 2024-04-19 | 天津大学 | Propane dehydrogenation and chemical looping combustion coupling system and process for synthesizing ammonia |
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