CN111875466B - Coupling method of depropanization process before hydrocarbon steam cracking and propane dehydrogenation process - Google Patents
Coupling method of depropanization process before hydrocarbon steam cracking and propane dehydrogenation process Download PDFInfo
- Publication number
- CN111875466B CN111875466B CN202010649495.6A CN202010649495A CN111875466B CN 111875466 B CN111875466 B CN 111875466B CN 202010649495 A CN202010649495 A CN 202010649495A CN 111875466 B CN111875466 B CN 111875466B
- Authority
- CN
- China
- Prior art keywords
- propane
- tower
- cracking
- gas
- depropanization
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/04—Thermal processes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/08—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds
- C07C5/09—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds to carbon-to-carbon double bonds
-
- 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
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The invention discloses a method for coupling a depropanization process before hydrocarbon steam cracking and a propane dehydrogenation process in the technical field of petrochemical industry, which realizes the purposes of reducing equipment investment, reducing device energy consumption, reducing construction land and prolonging the service life of an alkyne hydrogenation catalyst by coupling the characteristics of cracking gas of a hydrocarbon steam cracking device and reaction gas of a propane dehydrogenation device and is beneficial to long-period stable production of the coupling device.
Description
Technical Field
The invention belongs to the field of petrochemical industry, and particularly relates to a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking.
Background
Ethylene is one of the most important basic raw materials in the petrochemical industry, and the yield of the ethylene is a mark for measuring the overall development level of the petrochemical industry in a country. The ethylene production technology comprises hydrocarbon steam cracking, methanol-to-olefin, olefin conversion and the like, wherein the hydrocarbon steam cracking is dominant. At present, the hydrocarbon steam cracking technical patenters in the world mainly have: KBR in the USA, linde in Germany, lummus in the USA and Technip in French. These techniques all employ cryogenic separation processes to obtain ethylene products. The separation process may be divided into a sequential separation process, a pre-deethanization process, and a pre-depropanization process for different cracking feedstocks.
Propylene is also one of the most important base stocks in the petrochemical industry, and conventional sources of propylene rely primarily on hydrocarbon steam cracking for co-production and refinery FCC by-products. In recent years, techniques for specifically producing propylene, such as propane dehydrogenation and methanol-to-propylene, have been greatly developed. At present, the propane dehydrogenation patent technologies in the world are as follows: camofin Process by Lummus, oleflex Process by UOP, star Process by Uhde, PDH Process by Linde, and FBD Process by Snamprogetti/Yarsintz. These processes generally employ cryogenic separation processes to separate the reaction product of propane dehydrogenation to propylene.
The hydrocarbon steam cracking and the propane dehydrogenation are both used for producing low-carbon olefin and adopt cryogenic separation process technology. The steam cracking has wide raw materials and more product types; the propane dehydrogenation has single raw material and single product. The reaction products of steam cracking and propane dehydrogenation, i.e. the cracked gas and the reaction gas, are similar in composition: mainly comprises hydrogen, methane, ethane, ethylene, propane, propylene, carbon four and aromatic hydrocarbon. The contents are obviously different: the cracking gas has high contents of methane, ethane, ethylene, acetylene and propyne, and low contents of hydrogen and carbon monoxide; the reaction gases are opposite, the contents of the former few are lower, and the contents of the latter two are higher. According to the characteristics of reaction products of the two processes, the depropanization process before hydrocarbon steam cracking and the propane dehydrogenation process are coupled, so that the purposes of reducing equipment investment, reducing device energy consumption, reducing construction land and prolonging the service life of an alkyne hydrogenation catalyst are achieved, and the long-period stable production of a coupling device is facilitated.
In the prior art, chinese patents CN107602323A, CN107602324A, CN109761733A and CN109761735A disclose methods for coupling depropanization process and propane dehydrogenation process before steam cracking of different hydrocarbon feedstock, respectively. The methods couple the newly-built propane dehydrogenation unit by modifying the existing steam cracking unit and increasing part of the equipment load. The cracking gas and the reaction gas are directly mixed, compressed, washed with alkali and dried, and then sent to a front propane removal system for cryogenic separation, without considering the characteristic of high hydrogen and carbon monoxide content in the propane dehydrogenation reaction gas, which can increase the cold load at the temperature of-101 ℃ and below required by hydrogen/methane separation and methane/ethylene separation. In addition, the carbon monoxide content in the mixed gas is higher, and the service life of the acetylene hydrogenation catalyst is also greatly influenced.
Chinese patent CN110914225A discloses a process and apparatus for producing propylene by combining propane dehydrogenation and steam cracking, which recycle propane back to the steam cracking process instead of propane dehydrogenation, although improving ethylene yield, also improving methane content, resulting in increased energy consumption for subsequent separation and decreased propylene yield. At the same time, the patent does not consider that the reaction gas contains a small amount of carbon dioxide, and if the reaction gas is not removed by alkaline washing, the risk of blocking the cold box exists.
None of the above patents optimizes the de-oiling tower of the propane dehydrogenation unit, which can share the low pressure depropanizer of the hydrocarbon steam cracking unit to remove heavy components, realizing further coupling.
Disclosure of Invention
The invention discloses a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking, which aims at the characteristics of cracking gas of a hydrocarbon steam cracking device and reaction gas of a propane dehydrogenation device, realizes the purposes of reducing equipment investment, reducing device energy consumption, reducing construction land and prolonging the service life of an alkyne hydrogenation catalyst by coupling the two processes, and is beneficial to long-period stable production of a coupling device.
The invention relates to a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking, which comprises the following steps:
1) Heating a hydrocarbon raw material and circulating ethane from the bottom of an ethylene rectifying tower, then feeding the heated hydrocarbon raw material and the circulating ethane into a cracking unit for steam thermal cracking reaction to generate high-temperature cracking gas, quenching the high-temperature cracking gas, compressing, alkali washing and drying the quenched high-temperature cracking gas, and then feeding the quenched high-temperature cracking gas to a front depropanization separation system;
2) The propane raw material is mixed with circulating propane from the bottom of the propylene rectifying tower, the mixture enters a propane gasification unit for gasification, and a liquid phase at the bottom of the propane gasification unit enters a low-pressure depropanizing tower; the gasified gas-phase propane enters a dehydrogenation reaction unit to perform propane dehydrogenation reaction to generate high-temperature reaction gas, the high-temperature reaction gas is condensed and flashed by a reaction gas cooling box unit after being compressed and dried, the condensed liquid phase enters a light component removal tower for separation, the non-condensed gas phase at the top of the light component removal tower enters a pyrolysis gas compression unit, and the liquid phase at the bottom of the light component removal tower enters a propylene rectifying tower;
3) After the non-condensable gas at the top of the light component removal tower from the step 2) enters a pyrolysis gas compression unit, the non-condensable gas and the pyrolysis gas in the step 1) are compressed, alkali washed and dried, then enter a high-pressure depropanizer for separation, C3 and lighter components are separated from the top of the high-pressure depropanizer, and after being treated by an acetylene hydrogenation reactor, the non-condensable gas sequentially enters a pyrolysis gas cooling box unit, a demethanizer, a deethanizer and an ethylene rectifying tower for further separation; returning the ethylene circulating in the ethylene rectifying tower to the cracking unit;
4) And (3) feeding the high-pressure depropanizing tower bottom liquid phase from the step 3) and the propane gasification unit bottom liquid phase from the step 2) into a low-pressure depropanizing tower for separation, mixing the low-pressure depropanizing tower top component with the deethanizing tower bottom component from the step 3), feeding the mixture into a propiolic hydrogenation reactor for treatment, feeding the treated component and the light component removing tower bottom liquid phase in the step 2) into a propylene rectifying tower respectively, and feeding the circulating propane in the propylene rectifying tower bottom into the propane gasification unit.
The invention relates to a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking, which is further characterized in that: the front-end depropanization separation system comprises a high-pressure depropanization tower and a low-pressure depropanization tower.
The invention relates to a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking, which is further characterized in that: obtaining propylene and propane products from the propylene rectifying tower, recycling the propane to the propane gasification unit, and sending the propylene products out of the battery limits;
the invention relates to a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking, which is further characterized in that: and the liquid phase of the low-pressure depropanizing tower enters a debutanizing tower to obtain C4, C5 and heavier products, and the products are respectively sent out of the battery limits.
The invention relates to a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking, which is further characterized in that: the nominal capacity of the hydrocarbon steam cracking device is 30-150 ten thousand tons per year. The nominal capacity of the propane dehydrogenation device is 15-90 ten thousand tons/year.
The invention relates to a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking, which is further characterized in that: the operation conditions of the cracking furnace in the hydrocarbon steam cracking unit are that the reaction pressure is 0.10-0.25 MPaA and the reaction temperature is 780-870 ℃.
The invention relates to a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking, which is further characterized in that: the operation conditions of the reactor in the propane dehydrogenation reaction unit are that the reaction pressure is 0.10-0.35 MPaA and the reaction temperature is 450-700 ℃.
The invention relates to a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking, which is further characterized in that: the operation pressure of the cold box unit is 0.50-4.0 MPaA, and the operation temperature is-165-30 ℃.
The invention relates to a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking, which is further characterized in that: the operating pressure of the cracking gas cooling box unit is 0.50-4.0 MPaA, and the operating temperature is-165-30 ℃.
The invention relates to a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking, which is further characterized in that: the operating pressure of the reaction gas cooling box unit is 0.50-1.3 MPaA, and the operating temperature is-101-30 ℃.
The invention relates to a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking, which is further characterized in that: the raw materials of the hydrocarbon steam cracking device comprise light hydrocarbon, naphtha, diesel oil and hydrogenated tail oil.
The invention relates to a method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking. The coupling device shares a set of alkaline washing tower, a propylene rectifying tower, a low-pressure depropanizer, an ethylene refrigeration compressor and a propylene refrigeration compressor. The separated ethane returns to the cracking unit of the hydrocarbon steam cracking device, and the separated propane returns to the propane gasification unit of the propane dehydrogenation device.
The coupling method provided by the invention has the following beneficial effects:
1) The pyrolysis gas and the reaction gas are respectively compressed and dried, which is beneficial to the long-period stable production of the coupling device. The steam cracking and the propane dehydrogenation are high-temperature reactions, the conditions are harsh, coking is easy to occur, and the steam cracking and the propane dehydrogenation are respectively compressed to avoid mutual interference.
2) The reaction gas is subjected to cryogenic removal to remove most of hydrogen and carbon monoxide, so that the cold load of the coupling device at the temperature of-101 ℃ and below for hydrogen/methane separation and methane/ethylene separation is reduced; the content of carbon monoxide is reduced, and the service life of the acetylene hydrogenation catalyst is prolonged.
3) The separated propane is circularly returned to the propane dehydrogenation device, so that the yield of the propylene is improved, the methane content is reduced, the economic benefit of the coupling device is better, and the energy consumption is lower.
4) The coupling device recovers the ethylene in the propane dehydrogenation reaction gas, and the economic benefit of the device is improved.
5) The coupling device shares a set of alkaline washing tower, a propylene rectifying tower, a low-pressure depropanizer, an ethylene refrigeration compressor and a propylene refrigeration compressor, so that the equipment investment is reduced, and the construction land is reduced.
Drawings
FIG. 1 is a schematic flow diagram of a depropanization process before hydrocarbon steam cracking and a propane dehydrogenation process coupled according to the present invention.
The reference symbols shown in the figures are:
1-hydrocarbon cracking raw material, 2-cracking product, 3-cracking gas, 4-mixed gas, 5-refined gas, 6-mixed hydrocarbon, 7-C3 and lighter components, 8-acetylene hydrogenation feed, 9-acetylene hydrogenation product, 10-hydrogen, 11-demethanizer feed, 12-methane, 13-C2/C3 components, 14-C2 components, 15-C3 components I, 16-ethylene product, 17-recycled ethane, 18-C3 and heavier components, 19-C3 components II, 20-propyne hydrogenation product, 21-propylene product, 22-recycled propane, 23-C4 and heavier components, 24-C4 components, 25-C5 and heavier components, 26-propane raw material, 27-gas phase propane, 28-reaction gas, 29-compressed gas, 30-dehydrogenation product, 31-hydrogen-containing tail gas, 32-light component stripping feed, 33-noncondensable gas, 34-C3 components, 13-3-cracking gas, 101-mixed gas, 103-refined gas, 103-acetylene dehydrogenation unit, 103-hydrogenation unit, 103-dehydrogenation unit, 103-propylene dehydrogenation unit, 103-rectification unit, 103-dehydrogenation unit, high-pressure-rectification unit, high pressure-rectification unit, and high pressure-rectification unit; 201-propane gasification unit, 202-dehydrogenation reaction unit, 203-reaction gas compression unit, 204-reaction gas drying unit, 205-reaction gas cooling box unit and 206-light component removal tower.
Detailed Description
The present invention is described in further detail below with reference to fig. 1 and the specific examples, which do not limit the scope of the claimed invention.
As shown in fig. 1, a hydrocarbon cracking raw material 1 and circulating ethane 17 from the bottom of an ethylene rectifying tower 111 are heated and then enter a cracking unit 101 for steam thermal cracking reaction, a generated cracking product 2 is sent to a quenching unit 102, and heavy hydrocarbon is separated by oil cooling and water cooling to obtain a cracking gas 3. The cracked gas 3 is mixed with the non-condensable gas 33 from the top of the light component removal tower 206 and then enters the cracked gas compression unit 103, the acid gas of the boosted mixed gas 4 is removed by the alkali washing unit 104 to form refined gas 5, and the water is removed by the cracked gas drying unit 105 to form mixed hydrocarbon 6. The mixed hydrocarbon 6 enters a high-pressure depropanizing tower 106, C3 and lighter components 7 are separated from the top of the high-pressure depropanizing tower, the pressure of the mixed hydrocarbon is increased by a cracked gas compression unit 103, the increased acetylene hydrogenation feed 8 enters an acetylene hydrogenation reactor 107, an acetylene hydrogenation product 9 at the outlet of the reactor is sent to a cracked gas cold box unit 108, and hydrogen 10 is obtained by cryogenic separation. The condensed multiple demethanizer feeds 11 enter a demethanizer 109 respectively, the top of the demethanizer is methane 12, and the bottom of the demethanizer is a C2/C3 component 13. The C2/C3 components 13 enter a deethanizer 110 to separate C2 and C3, the top of the deethanizer is C2 component 14, and the bottom of the deethanizer is C3 component I15. C2 components 14 enter an ethylene rectifying tower 111 to separate ethylene and ethane, an ethylene product 16 is arranged at the top of the ethylene rectifying tower, and circulating ethane 17 in the bottom of the ethylene rectifying tower returns to the cracking unit 101. The C3 and heavier components 18 in the tower bottom of the high-pressure depropanizing tower 106 are sent to a low-pressure depropanizing tower 112 to separate C3, C4 and heavier components, the C3 component II 19 is arranged at the top of the low-pressure depropanizing tower, and the C4 and heavier components 23 are arranged at the tower bottom of the low-pressure depropanizing tower. The C3 component II 19 and the C3 component I15 from the bottom of the deethanizer 110 are mixed and enter a propyne hydrogenation reactor 113, a propyne hydrogenation product 20 at the outlet of the reactor is sent to a propylene rectifying tower 114 to separate propylene and propane, a propylene product 21 is at the top of the propylene rectifying tower, and circulating propane 22 at the bottom of the propylene rectifying tower returns to a propane gasification unit 201. The C4 and heavier components 23 at the bottom of the low pressure depropanizer 112 are sent to a debutanizer 115 for separation of C4 and C5 and heavier components, the top of the debutanizer is the C4 component 24, and the bottom of the debutanizer is the C5 and heavier components 25.
The propane raw material 26 and the circulating propane 22 from the bottom of the propylene rectifying tower 114 are mixed and then enter a propane gasification unit 201 for gasification, the gas-phase propane 27 is heated and then enters a dehydrogenation reaction unit 202 for propane dehydrogenation reaction, the reaction gas 28 after the reaction is cooled and then enters a reaction gas compression unit 203, the compressed gas 29 after the pressure increase enters a reaction gas drying unit 204 for moisture removal, the dehydrogenation product 30 after the drying is sent to a reaction gas cooling box unit 205, and the hydrogen-containing tail gas 31 is obtained through cryogenic separation. The condensed multi-strand light component removal tower feeding 32 respectively enters a light component removal tower 206, the light component removal tower top non-condensable gas 33 is sent to a cracking gas compression unit 103, and the light component removal tower bottom C3 component III 34 is sent to a propylene rectifying tower 114 for separating propylene and propane. The dehydrogenation heavy component 35 at the bottom of the propane gasification unit 201 is sent to a low-pressure depropanizer 112 to separate the heavy component.
Claims (9)
1. A method for coupling a depropanization process and a propane dehydrogenation process before hydrocarbon steam cracking is characterized by comprising the following steps:
1) Heating a hydrocarbon raw material and circulating ethane from the bottom of an ethylene rectifying tower, then feeding the heated hydrocarbon raw material and the circulating ethane into a cracking unit for steam thermal cracking reaction to generate high-temperature cracking gas, quenching the high-temperature cracking gas, compressing, carrying out alkali washing and drying, and then feeding the high-temperature cracking gas to a front depropanization separation system;
2) The propane raw material is mixed with circulating propane from the bottom of the propylene rectifying tower, the mixture enters a propane gasification unit for gasification, and a liquid phase at the bottom of the propane gasification unit enters a low-pressure depropanizing tower; the gasified gas-phase propane enters a dehydrogenation reaction unit to perform propane dehydrogenation reaction to generate high-temperature reaction gas, the high-temperature reaction gas is condensed and flashed by a reaction gas cooling box unit after being compressed and dried, the condensed liquid phase enters a light component removal tower for separation, the non-condensed gas phase at the top of the light component removal tower enters a pyrolysis gas compression unit, and the liquid phase at the bottom of the light component removal tower enters a propylene rectifying tower;
3) After the non-condensable gas at the top of the light component removal tower from the step 2) enters a cracking gas compression unit, the non-condensable gas and the high-temperature cracking gas in the step 1) are compressed, alkali washed and dried, then enter a high-pressure depropanizing tower for separation, C3 and lighter components are separated from the top of the high-pressure depropanizing tower, and after being treated by an acetylene hydrogenation reactor, the components sequentially enter a cracking gas cold box unit, a demethanizer, a deethanizer and an ethylene rectifying tower for further separation; returning the ethylene circulating in the ethylene rectifying tower to the cracking unit;
4) And (3) feeding the high-pressure depropanizing tower bottom liquid phase from the step 3) and the propane gasification unit bottom liquid phase from the step 2) into a low-pressure depropanizing tower for separation, mixing the low-pressure depropanizing tower top component with the deethanizing tower bottom component from the step 3), feeding the mixture into a propiolic hydrogenation reactor for treatment, feeding the treated component and the light component removing tower bottom liquid phase in the step 2) into a propylene rectifying tower respectively, and returning the circulating propane in the propylene rectifying tower bottom to the propane gasification unit.
2. The method of claim 1 for coupling a depropanization process with a propane dehydrogenation process prior to steam cracking, wherein: the front-end depropanization separation system comprises a high-pressure depropanization tower and a low-pressure depropanization tower.
3. The method of claim 1 for coupling a depropanization process with a propane dehydrogenation process prior to steam cracking, wherein: the operation conditions of the cracking furnace in the hydrocarbon steam cracking unit are that the reaction pressure is 0.10-0.25 MPaA and the reaction temperature is 780-870 ℃.
4. The method of claim 1 for coupling a depropanization process with a propane dehydrogenation process prior to steam cracking, wherein: the operation conditions of the reactor in the propane dehydrogenation reaction unit are that the reaction pressure is 0.10-0.35 MPaA and the reaction temperature is 450-700 ℃.
5. The method of claim 1 for coupling a depropanization process with a propane dehydrogenation process prior to steam cracking, wherein: the operating pressure of the pyrolysis gas cooling box unit is 0.50-1.3 MPaA, and the operating temperature is-101-30 ℃.
6. The method of claim 1 for coupling a depropanization process with a propane dehydrogenation process prior to steam cracking, wherein: the operating pressure of the reaction gas cooling box unit is 0.50-4.0 MPaA, and the operating temperature is-165-30 ℃.
7. The method of claim 1 for coupling a depropanization process with a propane dehydrogenation process prior to steam cracking, wherein: the raw materials of the cracking unit comprise light hydrocarbon, naphtha, diesel oil and hydrogenation tail oil.
8. The method of claim 1 for coupling a depropanization process with a propane dehydrogenation process prior to steam cracking, wherein: and obtaining propylene and propane products from the propylene rectifying tower, recycling the propane to the propane gasification unit, and sending the propylene products out of the battery limits.
9. The method of claim 1 for coupling a depropanization process with a propane dehydrogenation process prior to steam cracking, wherein: and the liquid phase of the low-pressure depropanizing tower enters a debutanizing tower to obtain C4, C5 and heavier products, and the products are respectively sent out of the battery limits.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010649495.6A CN111875466B (en) | 2020-07-08 | 2020-07-08 | Coupling method of depropanization process before hydrocarbon steam cracking and propane dehydrogenation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010649495.6A CN111875466B (en) | 2020-07-08 | 2020-07-08 | Coupling method of depropanization process before hydrocarbon steam cracking and propane dehydrogenation process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN111875466A CN111875466A (en) | 2020-11-03 |
| CN111875466B true CN111875466B (en) | 2022-10-14 |
Family
ID=73150341
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010649495.6A Active CN111875466B (en) | 2020-07-08 | 2020-07-08 | Coupling method of depropanization process before hydrocarbon steam cracking and propane dehydrogenation process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111875466B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107602324A (en) * | 2017-10-11 | 2018-01-19 | 中石化上海工程有限公司 | The method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique |
| CN107602323A (en) * | 2017-10-11 | 2018-01-19 | 中石化上海工程有限公司 | The method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique |
| CN108645119A (en) * | 2018-06-14 | 2018-10-12 | 北京恒泰洁能科技有限公司 | Dehydrogenating propane product gas cryogenic separation device and method |
| CN109761735A (en) * | 2019-01-21 | 2019-05-17 | 中石化上海工程有限公司 | The method that naphtha and Deposition During Propane Pyrolysis predepropanization are coupled with PDH |
| CN109761733A (en) * | 2019-01-21 | 2019-05-17 | 中石化上海工程有限公司 | The method that naphtha and ethane cracking predepropanization are coupled with PDH |
| CN109809958A (en) * | 2019-01-21 | 2019-05-28 | 中石化上海工程有限公司 | The method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique |
-
2020
- 2020-07-08 CN CN202010649495.6A patent/CN111875466B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107602324A (en) * | 2017-10-11 | 2018-01-19 | 中石化上海工程有限公司 | The method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique |
| CN107602323A (en) * | 2017-10-11 | 2018-01-19 | 中石化上海工程有限公司 | The method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique |
| CN108645119A (en) * | 2018-06-14 | 2018-10-12 | 北京恒泰洁能科技有限公司 | Dehydrogenating propane product gas cryogenic separation device and method |
| CN109761735A (en) * | 2019-01-21 | 2019-05-17 | 中石化上海工程有限公司 | The method that naphtha and Deposition During Propane Pyrolysis predepropanization are coupled with PDH |
| CN109761733A (en) * | 2019-01-21 | 2019-05-17 | 中石化上海工程有限公司 | The method that naphtha and ethane cracking predepropanization are coupled with PDH |
| CN109809958A (en) * | 2019-01-21 | 2019-05-28 | 中石化上海工程有限公司 | The method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique |
Also Published As
| Publication number | Publication date |
|---|---|
| CN111875466A (en) | 2020-11-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7939702B2 (en) | Process for increasing production of light olefins from hydrocarbon feedstock in catalytic cracking | |
| US11649406B2 (en) | Method and system for separating light hydrocarbons | |
| CN104230617B (en) | The method that MTO technique couples with Petroleum and Deposition During Propane Pyrolysis order separating technology | |
| CN108276236B (en) | Cryogenic separation and recovery method for Fischer-Tropsch synthesis tail gas for increasing olefin yield | |
| CN110092701B (en) | Light hydrocarbon separation method for MTO product mixed gas | |
| CN110388790B (en) | Ethane cracking cryogenic separation process method | |
| CN101092570B (en) | Method of catalytic cracking reaction for separating oil and gas rich in light hydrocarbon | |
| CN111807921B (en) | Coupling method of deethanization process before hydrocarbon steam cracking and propane dehydrogenation process | |
| CN111747814B (en) | Method for coupling deethanization process and propane dehydrogenation process before hydrocarbon steam cracking | |
| RU2767522C2 (en) | Method and apparatus for converting ethylene present in head stream from fcc plant in order to increase propylene production | |
| CN111875466B (en) | Coupling method of depropanization process before hydrocarbon steam cracking and propane dehydrogenation process | |
| CN111747813B (en) | Method for coupling hydrocarbon steam cracking sequential separation process and propane dehydrogenation process | |
| CN111848327B (en) | Method for coupling depropanization process and propane dehydrogenation process before hydrocarbon steam cracking | |
| CN111875467A (en) | Coupling method of hydrocarbon steam cracking sequential separation process and propane dehydrogenation process | |
| CN109734549A (en) | Naphtha and Deposition During Propane Pyrolysis sequentially separate the method coupled with PDH | |
| CN114644540A (en) | Device and method for preparing low-carbon olefin from alcohol | |
| CN110937970B (en) | Method and system for preparing propylene | |
| CN116694359B (en) | DCC integrated system and method for increasing yield of olefin | |
| CN110937975A (en) | Method and system for preparing propylene | |
| CN112920008B (en) | Method and device for separating hydrocarbon pyrolysis gas and producing ethylbenzene by using hydrocarbon pyrolysis gas | |
| CN216614470U (en) | Light oil catalytic cracking reaction system | |
| CN115710152A (en) | System and method for preparing polymerization-grade olefin through DCC (DCC) integration with comprehensive utilization of carbon four | |
| CN110950733A (en) | Separation device and method for methanol-to-olefin gas | |
| CN114436732A (en) | Method and system for preparing ethylbenzene and hydrogen by using refinery dry gas | |
| CN110218140B (en) | Method for producing high-quality ethylbenzene by cracking light hydrocarbon |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |