CN112500889B - Adsorption unit to isomerization unit feed system - Google Patents
Adsorption unit to isomerization unit feed system Download PDFInfo
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- CN112500889B CN112500889B CN202011573599.XA CN202011573599A CN112500889B CN 112500889 B CN112500889 B CN 112500889B CN 202011573599 A CN202011573599 A CN 202011573599A CN 112500889 B CN112500889 B CN 112500889B
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- Prior art keywords
- deheptanizer
- heat exchanger
- isomerization
- pipeline
- valve
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- 238000006317 isomerization reaction Methods 0.000 title claims abstract description 76
- 238000001179 sorption measurement Methods 0.000 title claims abstract description 35
- 239000004927 clay Substances 0.000 claims abstract description 18
- 238000007599 discharging Methods 0.000 claims abstract description 16
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 7
- 239000000463 material Substances 0.000 claims description 19
- 238000010992 reflux Methods 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 7
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims description 5
- 239000008096 xylene Substances 0.000 claims description 4
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 claims 2
- 238000000034 method Methods 0.000 abstract description 10
- 239000007788 liquid Substances 0.000 abstract description 9
- 230000008569 process Effects 0.000 description 6
- 239000004100 Oxytetracycline Substances 0.000 description 5
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 5
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 4
- 239000004185 Penicillin G procaine Substances 0.000 description 4
- 230000009471 action Effects 0.000 description 4
- 239000004099 Chlortetracycline Substances 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 239000004104 Oleandomycin Substances 0.000 description 2
- 239000004105 Penicillin G potassium Substances 0.000 description 2
- 239000004098 Tetracycline Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- IVSZLXZYQVIEFR-UHFFFAOYSA-N m-xylene Chemical group CC1=CC=CC(C)=C1 IVSZLXZYQVIEFR-UHFFFAOYSA-N 0.000 description 2
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 2
- 150000003738 xylenes Chemical class 0.000 description 2
- 230000004075 alteration Effects 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001555 benzenes Chemical class 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007323 disproportionation reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229940078552 o-xylene Drugs 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
-
- 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
- C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
- C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
- C07C5/31—Rearrangement of carbon atoms in the hydrocarbon skeleton changing the number of rings
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to the technical field of petrochemical industry, in particular to an adsorption device to isomerization unit feeding system, wherein a deheptanizer feeding pipeline is sequentially connected with a first heat exchanger and a second heat exchanger to exchange heat and then led to a deheptanizer feeding port, a deheptanizer bottom discharging pipeline is sequentially connected with a third heat exchanger and the second heat exchanger from a deheptanizer bottom discharging port and then led to an isomerization product clay treater feeding port, the isomerization product clay treater discharging pipeline is connected to an adsorption feeding tank through an adsorption feeding pipeline, a circulating span is arranged between the adsorption feeding pipeline and the deheptanizer feeding pipeline, and the circulating span is connected to the deheptanizer feeding pipeline at the upstream of the first heat exchanger. The method can remove the hidden trouble of liquid impact of the pipeline, reduce the shutdown of the device and the hidden trouble of accident safety, thereby achieving the purpose of maintaining long-period safe operation.
Description
Technical Field
The invention relates to the technical field of petrochemical industry, in particular to a feeding system from an adsorption device to an isomerization unit.
Background
Aromatic hydrocarbons, generally referred to as hydrocarbons having a benzene ring or aromatic ring structure in the molecule, are one of closed-chain hydrocarbons having a benzene ring basic structure. The aromatic hydrocarbon comprises a benzene derivative of 'paraxylene', wherein the paraxylene is one of xylene isomers, and the rest isomers comprise o-xylene and m-xylene.
In the production process of aromatic hydrocarbon, the steps of fractionation, isomerization, adsorption, extraction, disproportionation and the like are usually needed, wherein the isomerization technology adopts the Axens technology, upstream equipment of the feed of an isomerization feed buffer tank is an adsorption unit raffinate tower in the process, the feed is laterally extracted from the adsorption unit raffinate tower to a deheptanizer feed line, liquid impact is usually generated at an interface of a wall of the deheptanizer when the aromatic hydrocarbon isomerization feed line is started to operate and heat oil, the liquid impact impacts a pressure gauge of a feed line of the wall of the deheptanizer and a flange of the wall of the tower, flange leakage is caused, even potential safety hazards of fire occur (the temperature of the deheptanizer is controlled at 200 ℃, the deheptanizer belongs to a high-temperature tower), the device cannot operate and needs to be overhauled, the components in a reaction system are transformed due to the shutdown of the aromatic hydrocarbon isomerization device, the service life of the catalyst is influenced, the operation period is long when the product is difficult to reach the qualified standard, and the energy consumption of the device is very large.
Disclosure of Invention
In view of the defects in the prior art, the invention provides an adsorption device-isomerization unit feeding system which can eliminate the hidden trouble of liquid impact of a pipeline and reduce the shutdown of the device and the hidden trouble of accident safety, thereby achieving the purpose of maintaining long-period safe operation.
In order to achieve the above purpose, the technical scheme provided by the invention is that an adsorption device is connected to an isomerization unit feeding system, a deheptanizer feeding pipeline is sequentially connected with a first heat exchanger and a second heat exchanger for heat exchange and then led to a deheptanizer feeding port, a deheptanizer bottom discharging pipeline is sequentially connected with a third heat exchanger and the second heat exchanger through a deheptanizer bottom discharging port and then led to an isomerization product clay treater feeding port, the isomerization product clay treater discharging pipeline is connected to an adsorption feeding tank through an adsorption feeding pipeline, a circulating span is arranged between the adsorption feeding pipeline and the deheptanizer feeding pipeline, and the circulating span is connected to the deheptanizer feeding pipeline at the upstream of the first heat exchanger.
Based on the technical scheme, the circulating jumper is arranged, so that hot materials in the deheptanizer and the feeding pipeline of the deheptanizer can be effectively circulated, the temperature of the feeding pipeline is increased to be consistent with the temperature of the tower, and the risk of tearing accidents of the liquid impact pipeline of the system is reduced.
Further, the isomerization product clay treater discharge line is connected to the third heat exchanger before the xylene reboiler.
Further, a first valve, a first one-way valve and a second valve are sequentially arranged on the circulating jumper.
Further, a deheptanizer bottom pump is arranged on the upper stream of the third heat exchanger on the deheptanizer bottom discharging pipeline.
Further, the deheptanizer feed line includes an isomerization reaction bypass line leading to the first heat exchanger from the isomerization feed buffer tank.
Further, the isomerization feed buffer tank sequentially passes through the fifth heat exchanger, the filter and the sixth heat exchanger through the isomerization feed pipeline to enter a reaction furnace, the discharge of the reaction furnace enters an isomerization reactor, the discharge of the isomerization reactor enters a product separation tank through the sixth heat exchanger, and the discharge of the product separation tank is led to the feed pipeline of the deheptanizer after passing through the fifth heat exchanger.
Further, an isomerization feed pump is arranged on the isomerization feed line, and an isomerization feed line downstream of the isomerization feed pump is connected into the isomerization reaction bypass line.
Further, a third valve, a second one-way valve, a fourth valve and a fifth valve are sequentially arranged on the isomerization reaction bypass pipeline, and a circulating jumper is connected between the fourth valve and the fifth valve.
Further, a sixth valve is arranged on an adsorption feed line between a discharging line of the isomerisation product clay treater and a circulating span line.
Further, the bottom of the deheptanizer is connected to a deheptanizer reboiler pump, and the deheptanizer reboiler pump is connected to a deheptanizer reboiler and then reintroduced into the deheptanizer for bottom circulation.
Further, the tower top material of the deheptanizer enters an air cooler after heat exchange of the first heat exchanger, the discharged material of the air cooler enters a reflux tank through a fourth heat exchanger, and a reflux pump leads the material to the deheptanizer again from the reflux tank for tower top circulation.
The invention has the beneficial effects that: through the transformation of the pipeline, hot materials in the deheptanizer and a feed pipeline of the deheptanizer can be effectively circulated, so that the temperature of the feed pipeline is increased to be consistent with the temperature of the tower, and the risk of tearing accidents of the liquid impact pipeline of the system is reduced.
Drawings
FIG. 1 is a process flow diagram of the present invention;
in the figure: 1. the deheptanizer feed line, 2, deheptanizer, 3, deheptanizer bottoms take-off line, 3.1, deheptanizer reboiler pump, 4, isomerisation product clay treater, 5, isomerisation product clay treater take-off line, 6, adsorption feed line, 6.1, sixth valve, 7, adsorption feed tank, 8, recycle cross line, 8.1, first valve, 8.2, first check valve, 8.3, second valve, 9, xylenes reboiler, 10, deheptanizer bottoms pump, 11, isomerisation feed buffer tank, 12, isomerisation feed line, 12.1, isomerisation feed pump, 13, filter, 14, reaction furnace, 15, isomerisation reactor, 16, product separation tank, 17, isomerisation reaction bypass line, 17.1, third valve, 17.2, second check valve, 17.3, fourth valve, 17.4, fifth valve, 18, deheptanizer pump, 19, deheptanizer, 20, reboiler, 21, reflux tank, 22, E703, second heat exchanger, E702, third heat exchanger E, f-exchanger E707, heat exchanger E-exchanger-702, fourth heat exchanger-f-exchanger-707.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
The adsorption device is connected to an isomerization unit feeding system, a deheptanizer feeding pipeline 1 is sequentially connected with a first heat exchanger E703 and a second heat exchanger E704 for heat exchange and then led to a feeding port of a deheptanizer 2, a deheptanizer bottom discharging pipeline 3 is sequentially connected to a third heat exchanger E707 and a feeding port of an isomerization product clay treater 4 from the deheptanizer bottom discharging port of the deheptanizer, an isomerization product clay treater discharging pipeline 5 is connected to an adsorption feeding tank 7 through an adsorption feeding pipeline 6, a circulating span 8 is arranged between the adsorption feeding pipeline 6 and the deheptanizer feeding pipeline 1, and the circulating span 8 is connected to the deheptanizer feeding pipeline 1 upstream of the first heat exchanger E703.
Further, the isomerisation product clay treater discharge line 5 is connected to the third heat exchanger E707 before to the xylene reboiler 9.
Further, a first valve 8.1, a first one-way valve 8.2 and a second valve 8.3 are sequentially installed on the circulating jumper 8.
Further, a deheptanizer bottom pump 10 is arranged on the discharge line 3 at the bottom of the deheptanizer, upstream of the third heat exchanger E707.
Further, the deheptanizer feed line 1 includes an isomerization reaction bypass line 17 leading to the first heat exchanger E703 from the isomerization feed buffer tank 11.
Further, the isomerization feed buffer tank 11 sequentially passes through the fifth heat exchanger E701, the filter 13 and the sixth heat exchanger E702 through the isomerization feed line 12, and enters the reaction furnace 14, the discharged material of the reaction furnace 14 enters the isomerization reactor 15, the discharged material of the isomerization reactor 15 enters the product separation tank 16 through the sixth heat exchanger E702, and the discharged material of the product separation tank 16 is led to the deheptanizer feed line 1 after passing through the fifth heat exchanger E701.
Further, an isomerization feed pump 12.1 is installed on the isomerization feed line 12, and the isomerization feed line 12 downstream of the isomerization feed pump 12.1 is connected to the isomerization reaction bypass line 17.
Further, a third valve 17.1, a second one-way valve 17.2, a fourth valve 17.3 and a fifth valve 17.4 are sequentially arranged on the isomerization reaction bypass pipeline 17, and a circulation jumper 8 is connected between the fourth valve 17.3 and the fifth valve 17.4.
Further, a sixth valve 6.1 is arranged on the adsorption feed line between the isomerization product clay treater discharging line 5 and the circulating span line 8.
Further, the bottom of the deheptanizer 2 is connected to a deheptanizer reboiler pump 18, and the deheptanizer reboiler pump 18 is connected to a deheptanizer reboiler 19, and then the deheptanizer is reintroduced into the deheptanizer 2 for bottom circulation.
Further, the tower top material of the deheptanizer 2 enters an air cooler 20 after heat exchange by the first heat exchanger, the discharged material of the air cooler enters a reflux tank 21 by a fourth heat exchanger E705, and a reflux pump 22 leads the material from the reflux tank 21 to the deheptanizer 2 again for tower top circulation.
The modification process of this embodiment is to add a tee on the line from the isomerization product clay treater 4 to the adsorption feed tank 7, and add a line to the line after the isomerization bypass valve (fourth valve 17.3), the line specification is DN200, 5TB, the length is 10 meters, and the tee specification is DN200, 5TB.
1 first check valve 8.2 is added, the specifications of the check valves are DN200 and 5TB, and two gate valves (a first valve 8.1 and a second valve 8.3) are DN200 and 5TB, so that hot materials in the isomerization tower and a feeding pipeline can be effectively circulated, the temperature of the feeding pipeline is increased to be consistent with the temperature of the tower, and the tearing accident risk of a liquid impact pipeline of the system is reduced.
Further describing this embodiment, when the device is shut down or started up after the modification is completed, the cycle jumper 8 is put into operation, and the first valve 8.1, the first check valve 8.2 and the second valve 8.3 of the valve are opened as shown in fig. 1.
The self-circulation temperature rise of the deheptanizer during normal operation comprises bottom circulation and top circulation. Wherein, the bottom of the tower circulates: the deheptanizer bottoms from deheptanizer column 2 is fed to deheptanizer bottoms pump 18 and warmed back to deheptanizer column 2 via deheptanizer reboiler 19. Overhead circulation: the overhead material from deheptanizer 2 is passed to air cooler 20, through deheptanizer overhead water cooler (fourth heat exchanger E705) to deheptanizer reflux drum 21, and back to deheptanizer 2 under the action of reflux pump 22.
After the temperature of the deheptanizer is increased to 150 ℃, the deheptanizer is pumped to a deheptanizer heat exchanger (a third heat exchanger), sequentially flows to a sixth valve 6.1, a first valve 8.1, a first check valve 8.2 and a second valve 8.3 through an isomerisation product clay treater, flows to a deheptanizer feeding heat exchanger (a first heat exchanger E703) through an isomerisation reaction bypass pipeline 17, flows to a deheptanizer feeding heat exchanger (a second heat exchanger E704) through a deheptanizer heat exchanger, and finally returns to the deheptanizer 2.
When the pipeline is started, the liquid impact alleviation degree of the pipeline, which is close to the tower wall of the deheptanizer 2, is monitored during temperature rising, and through the improvement of the embodiment, the liquid impact phenomenon of the tower wall of the deheptanizer 2 is obviously alleviated.
It is noted that relational terms such as first and second, and the like are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Moreover, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising one … …" does not exclude the presence of other like elements in a process, method, article, or apparatus that comprises the element.
Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. Adsorption unit to isomerization unit feed system, characterized by: the feeding pipeline of the deheptanizer is sequentially connected with the first heat exchanger and the second heat exchanger for heat exchange and then led to the feeding port of the deheptanizer, the discharging pipeline of the bottom of the deheptanizer is sequentially connected with the third heat exchanger and the second heat exchanger through the discharging port of the bottom of the deheptanizer and then led to the feeding port of the clay treater of the isomerization product, the discharging pipeline of the clay treater of the isomerization product is connected to an adsorption feeding tank through an adsorption feeding pipeline, a circulating span is arranged between the adsorption feeding pipeline and a feeding pipeline of the deheptanizer, and the circulating span is connected to the feeding pipeline of the deheptanizer at the upstream of the first heat exchanger; the first valve, the first one-way valve and the second valve are sequentially arranged on the circulating jumper;
the bottom of the deheptanizer is connected to a deheptanizer reboiler pump, and the deheptanizer reboiler pump is connected to a deheptanizer reboiler and then is reintroduced into the deheptanizer for bottom circulation;
the tower top material of the deheptanizer enters an air cooler after heat exchange of the first heat exchanger, the discharged material of the air cooler enters a reflux tank through a fourth heat exchanger, and a reflux pump leads the material to the deheptanizer again from the reflux tank for tower top circulation.
2. The adsorption unit to isomerization unit feed system of claim 1, wherein: the isomerization product clay treater discharge line is connected to the third heat exchanger back to the xylene reboiler.
3. The adsorption unit to isomerization unit feed system of claim 1, wherein: and a deheptanizer bottom pump is arranged at the upstream of the third heat exchanger on the deheptanizer bottom discharge pipeline.
4. The adsorption unit to isomerization unit feed system of claim 1, wherein: the deheptanizer feed line includes an isomerization reaction bypass line leading to the first heat exchanger from the isomerization feed buffer tank.
5. The adsorption unit to isomerization unit feed system of claim 4, wherein: the isomerization feed buffer tank sequentially passes through the fifth heat exchanger, the filter and the sixth heat exchanger through the isomerization feed pipeline to enter the reaction furnace, the discharged material of the reaction furnace enters the isomerization reactor, the discharged material of the isomerization reactor enters the product separation tank through the sixth heat exchanger, and the discharged material of the product separation tank is led to the feed pipeline of the heptane removing tower after passing through the fifth heat exchanger.
6. The adsorption unit to isomerization unit feed system of claim 4, wherein: and a third valve, a second one-way valve, a fourth valve and a fifth valve are sequentially arranged on the isomerization reaction bypass pipeline, and a circulating jumper is connected between the fourth valve and the fifth valve.
7. The adsorption unit to isomerization unit feed system of claim 1, wherein: and a sixth valve is arranged on an adsorption feed pipe line between a discharging pipeline of the isomerisation product clay treater and a circulating span line.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202011573599.XA CN112500889B (en) | 2020-12-28 | 2020-12-28 | Adsorption unit to isomerization unit feed system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011573599.XA CN112500889B (en) | 2020-12-28 | 2020-12-28 | Adsorption unit to isomerization unit feed system |
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| CN112500889A CN112500889A (en) | 2021-03-16 |
| CN112500889B true CN112500889B (en) | 2024-02-20 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109370636A (en) * | 2018-12-08 | 2019-02-22 | 大连福佳·大化石油化工有限公司 | Aromatics isomerization process system |
| CN209368154U (en) * | 2018-12-24 | 2019-09-10 | 中化弘润石油化工有限公司 | A kind of aromatics seperation heat integration goes into operation optimization system |
| CN110937969A (en) * | 2018-09-25 | 2020-03-31 | 中国石油化工股份有限公司 | Device and process for producing paraxylene |
| CN214654683U (en) * | 2020-12-28 | 2021-11-09 | 大连福佳·大化石油化工有限公司 | Adsorption equipment to isomerization unit feed system |
-
2020
- 2020-12-28 CN CN202011573599.XA patent/CN112500889B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110937969A (en) * | 2018-09-25 | 2020-03-31 | 中国石油化工股份有限公司 | Device and process for producing paraxylene |
| CN109370636A (en) * | 2018-12-08 | 2019-02-22 | 大连福佳·大化石油化工有限公司 | Aromatics isomerization process system |
| CN209368154U (en) * | 2018-12-24 | 2019-09-10 | 中化弘润石油化工有限公司 | A kind of aromatics seperation heat integration goes into operation optimization system |
| CN214654683U (en) * | 2020-12-28 | 2021-11-09 | 大连福佳·大化石油化工有限公司 | Adsorption equipment to isomerization unit feed system |
Non-Patent Citations (2)
| Title |
|---|
| 秦文戈.RIC-200型C8芳烃异构化催化剂在国产化芳烃装置的工业应用.石油炼制与化工.2015,第46卷(第7期),63-66. * |
| 黄翔云 ; .金陵石化PX抽余液塔改造.河南化工.2010,(14),48-50. * |
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