CN112500889A - Adsorption plant to isomerization unit feed system - Google Patents
Adsorption plant to isomerization unit feed system Download PDFInfo
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- CN112500889A CN112500889A CN202011573599.XA CN202011573599A CN112500889A CN 112500889 A CN112500889 A CN 112500889A CN 202011573599 A CN202011573599 A CN 202011573599A CN 112500889 A CN112500889 A CN 112500889A
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- heat exchanger
- deheptanizer
- isomerization
- valve
- pipeline
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- 238000006317 isomerization reaction Methods 0.000 title claims abstract description 70
- 238000001179 sorption measurement Methods 0.000 title claims abstract description 34
- 239000004927 clay Substances 0.000 claims abstract description 17
- 238000007599 discharging Methods 0.000 claims abstract description 12
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 7
- 239000000463 material Substances 0.000 claims description 24
- 238000010992 reflux Methods 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 7
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 239000008096 xylene Substances 0.000 claims description 4
- 239000007788 liquid Substances 0.000 abstract description 9
- 238000000034 method Methods 0.000 description 9
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 239000004100 Oxytetracycline Substances 0.000 description 5
- 239000004104 Oleandomycin Substances 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
- 239000004105 Penicillin G potassium Substances 0.000 description 3
- 239000004098 Tetracycline Substances 0.000 description 3
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 2
- 239000003463 adsorbent 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
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 2
- 230000009466 transformation Effects 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
- 239000013072 incoming material Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 150000003738 xylenes Chemical class 0.000 description 1
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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
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- 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 a feeding system from an adsorption device to an isomerization unit, wherein 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 hole, a deheptanizer bottom discharging pipeline is sequentially connected with a third heat exchanger and the second heat exchanger from a deheptanizer bottom discharging hole and then led to an isomerization product clay processor feeding hole, an isomerization product clay processor discharging pipeline is led to an adsorption feeding tank through an adsorption feeding pipeline, a circulating span line is arranged between the adsorption feeding pipeline and the deheptanizer feeding pipeline, and the circulating span line is connected to the deheptanizer feeding pipeline at the upstream of the first heat exchanger. The device can eliminate the liquid impact hidden trouble of the pipeline, and reduce the shutdown and accident potential safety hazard of the device, 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 refer to hydrocarbons having a benzene ring or aromatic ring structure in the molecule, and are one of closed-chain hydrocarbons having a benzene ring basic structure. The aromatic hydrocarbon comprises a benzene derivative "para-xylene", which is one of the xylene isomers, the remaining isomers including ortho-xylene and meta-xylene.
In the production process of aromatic hydrocarbon, the steps of fractionation, isomerization, adsorption, extraction, disproportionation and the like are usually required, wherein the isomerization technology adopts an Axens technology, upstream equipment for isomerization feed buffer tank incoming materials in the process is an adsorption unit raffinate tower, the materials are extracted from the side of the adsorption unit raffinate tower to a deheptanizer feed line, liquid impact is frequently generated at an interface of a tower wall of the deheptanizer when the aromatic hydrocarbon isomerization feed line is in operation and temperature rise, the liquid impact impacts a pressure gauge of a feed pipeline of the tower wall of the deheptanizer and a pipeline flange of the tower wall to cause flange leakage and even potential safety hazards of fire (the temperature of the deheptanizer is controlled at 200 ℃ and belongs to a high-temperature tower), the device cannot operate and needs to be shut down for maintenance, components in a reaction system are changed due to the shutdown of the aromatic hydrocarbon isomerization device to influence the service life of a catalyst, the operation period is longer when the aromatic hydrocarbon isomerization device is started again, 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 of the prior art, the invention provides a feeding system from an adsorption device to an isomerization unit, which can eliminate the liquid impact hidden danger of a pipeline and reduce the shutdown and accident potential of the device, thereby achieving the purpose of maintaining long-period safe operation.
In order to achieve the 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 hole, a deheptanizer bottom discharging pipeline is sequentially connected with a third heat exchanger and the second heat exchanger from a deheptanizer bottom discharging hole and then led to an isomerization product clay processor feeding hole, an isomerization product clay processor discharging pipeline is connected to an adsorption feeding tank through an adsorption feeding pipeline, a circulating span line is arranged between the adsorption feeding pipeline and the deheptanizer feeding pipeline, and the circulating span line is connected to the deheptanizer feeding pipeline on the upstream of the first heat exchanger.
Based on the technical scheme, the circulating span line is arranged, so that the 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 tower temperature, and the risk of the accident of tearing the liquid impact pipeline of the system is reduced.
Further, the output pipeline of the isomerization product clay treater is connected with the third heat exchanger and then enters the xylene reboiling furnace.
Furthermore, a first valve, a first one-way valve and a second valve are sequentially arranged on the circulating crossover.
Furthermore, a deheptanizer bottom pump is arranged on the upstream of the third heat exchanger on the discharging pipeline at the bottom of the deheptanizer.
Further, the deheptanizer feed line includes an isomerization reaction bypass line that leads from the isomerization feed surge tank to the first heat exchanger.
Furthermore, the isomerization feeding buffer tank sequentially passes through a fifth heat exchanger, a filter and a sixth heat exchanger through an isomerization feeding pipeline and enters the reaction furnace, the reaction furnace discharges materials and enters the isomerization reactor, the isomerization reactor discharges materials and enters the product separation tank through the sixth heat exchanger, and the product separation tank discharges materials and leads to the deheptanizer feeding pipeline after passing through the fifth heat exchanger.
Further, an isomerization feed pump is installed on the isomerization feed line, and the isomerization feed line downstream of the isomerization feed pump is connected to the isomerization reaction bypass line.
Furthermore, 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 overline is connected between the fourth valve and the fifth valve.
Furthermore, a sixth valve is arranged on the adsorption feeding line between the discharge line of the isomerization product clay treater and the circulating overline.
Further, the tower bottom of the deheptanizer is connected to a deheptanizer reboiler pump, and the deheptanizer reboiler pump is connected to the deheptanizer reboiler and then is introduced into the deheptanizer again for tower bottom circulation.
Furthermore, materials at the top of the deheptanizer enter an air cooler after heat exchange through a first heat exchanger, the discharged materials of the air cooler enter a reflux tank through a fourth heat exchanger, and a reflux pump guides the materials to the deheptanizer again from the reflux tank for top circulation.
The invention has the beneficial effects that: through the transformation of the pipeline, the hot materials in the deheptanizer and the feeding pipeline of the deheptanizer can effectively form circulation, so that the temperature of the feeding pipeline is raised to be consistent with the tower temperature, and the risk of the accident of tearing 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. deheptanizer feed line, 2, deheptanizer, 3, deheptanizer bottoms discharge line, 3.1, deheptanizer reboiler pump, 4, isomerate clay treater, 5, isomerate clay treater discharge line, 6, adsorbent feed line, 6.1, sixth valve, 7, adsorbent feed tank, 8, recycle crossover, 8.1, first valve, 8.2, first check valve, 8.3, second valve, 9, xylene reboiling furnace, 10, deheptanizer bottoms pump, 11, isomerate feed buffer tank, 12, isomerate feed line, 12.1, isomerate feed pump, 13, filter, 14, reactor, 15, isomerate reactor, 16, product knockout drum, 17, isomerate bypass line, 17.1, third valve, 17.2, second check valve, 17.3, fourth valve, 17.4, fifth valve, 18, deheptanizer pump, 19, reboiler, and so forth, A deheptanizer reboiler, 20, an air cooler, 21, a reflux tank, 22, a reflux pump, E703, a first heat exchanger, E704, a second heat exchanger, E707, a third heat exchanger, E705, a fourth heat exchanger, E701, a fifth heat exchanger, E702 and a sixth heat exchanger.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
An 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 hole of a deheptanizer 2, a deheptanizer tower bottom discharging pipeline 3 is sequentially connected with a third heat exchanger E707 and the second heat exchanger E704 from a deheptanizer tower bottom discharging hole and then led to a feeding hole of an isomerization product clay processor 4, an isomerization product clay processor discharging pipeline 5 is connected to an adsorption feeding tank 7 through an adsorption feeding pipeline 6, a circulating span line 8 is arranged between the adsorption feeding pipeline 6 and the deheptanizer feeding pipeline 1, and the circulating span line 8 is connected to the deheptanizer feeding pipeline 1 on the upstream of the first heat exchanger E703.
Further, the isomerized product clay treater outlet line 5 is connected to the third heat exchanger E707 and then to a xylene reboiling furnace 9.
Furthermore, a first valve 8.1, a first one-way valve 8.2 and a second valve 8.3 are sequentially arranged on the circulating crossover 8.
Further, a deheptanizer bottom pump 10 is arranged on the bottom discharge line 3 of the deheptanizer at the upstream of the third heat exchanger E707.
Further, the deheptanizer feed line 1 includes an isomerization reaction bypass line 17 leading from the isomerization feed buffer tank 11 to the first heat exchanger E703.
Further, the isomerization feed buffer tank 11 sequentially passes through a fifth heat exchanger E701, a filter 13 and a sixth heat exchanger E702 through an isomerization feed pipeline 12 and enters a reaction furnace 14, the reaction furnace 14 discharges materials and enters an isomerization reactor 15, the isomerization reactor 15 discharges materials and enters a product separation tank 16 through the sixth heat exchanger E702, and the product separation tank 16 discharges materials and leads to the deheptanizer feed pipeline 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 check valve 17.2, a fourth valve 17.3, and a fifth valve 17.4 are sequentially provided in the isomerization reaction bypass line 17, and a circulation crossover 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 feeding line between the discharging line 5 of the isomerization product clay treater and the cross line 8 for circulation.
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 introduced into the deheptanizer 2 again for bottom circulation.
Further, the material at the top of the deheptanizer 2 enters an air cooler 20 after heat exchange through a first heat exchanger, the material discharged from the air cooler enters a reflux tank 21 through a fourth heat exchanger E705, and the material is introduced to the deheptanizer 2 again from the reflux tank 21 by a reflux pump 22 for top circulation.
In the modification process of the embodiment, a tee joint is added to a pipeline from the isomerized product clay processor 4 to the adsorption feed tank 7, and the pipeline is added to a pipeline behind an isomerization reaction bypass valve (a fourth valve 17.3), wherein the specification of the pipeline is DN200 and 5TB, the length of the pipeline is 10 meters, and the specification of the tee joint is DN200 and 5 TB.
1 first check valve 8.2 is added, the specifications of the check valves are DN200 and 5TB, and two gate valves (the first valve 8.1 and the second valve 8.3) DN200 and 5TB are adopted, so that hot materials in the isomerization tower and the feeding pipeline can effectively form circulation, the temperature rise of the feeding pipeline is consistent with the temperature of the tower, and the risk of accidents of tearing the pipeline due to liquid impact of the system is reduced.
To further illustrate this embodiment, after the retrofit is completed, when the plant is shut down or in operation, the recycling jumper 8 is applied, as shown in fig. 1, and the first valve 8.1, the first one-way valve 8.2 and the second valve 8.3 are opened.
The deheptanizer self-circulation temperature rise during normal start-up period comprises tower bottom circulation and tower top circulation. Wherein, the tower bottom circulates: the bottom material of the deheptanizer 2 enters a deheptanizer bottom pump 18 and is heated to return to the deheptanizer 2 through a deheptanizer reboiling furnace 19. Tower top circulation: the material at the top of the deheptanizer 2 enters an air cooler 20, passes through a deheptanizer top water cooler (a fourth heat exchanger E705) to a deheptanizer reflux tank 21, and returns to the deheptanizer 2 under the action of a reflux pump 22.
After the temperature of the deheptanizer is raised to 150 ℃, a deheptanizer bottom pump is put into a deheptanizer bottom heat exchanger (a third heat exchanger), and the mixture passes through an isomerization product clay treater, sequentially passes through a sixth valve 6.1, a first valve 8.1, a first check valve 8.2 and a second valve 8.3, passes through an isomerization reaction bypass pipeline 17 to a deheptanizer feeding heat exchanger (a first heat exchanger E703), passes through a deheptanizer bottom feeding heat exchanger (a second heat exchanger E704) and finally returns to the deheptanizer 2.
When the pipeline is put into operation, the liquid impact relieving degree of the pipeline close to the tower wall of the deheptanizer 2 is monitored during temperature rise, and through the transformation of the embodiment, the liquid impact phenomenon at the tower wall of the deheptanizer 2 is obviously relieved.
It is noted that, herein, relational terms such as first and second, and the like may be 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. Also, 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 an … …" does not exclude the presence of other identical 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 appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (10)
1. Adsorption equipment to isomerization unit charge-in system, its characterized in that: the device comprises a deheptanizer, a first heat exchanger, a second heat exchanger, an isomerization product clay treater, an adsorption feed tank, a circulating span line, a first heat exchanger, a second heat exchanger, a third heat exchanger, a fourth heat exchanger, a fifth heat exchanger, a sixth heat exchanger, a fifth heat exchanger, a sixth.
2. The adsorption unit to isomerization unit feed system of claim 1, wherein: and the outlet pipeline of the isomerization product clay treater is connected to the third heat exchanger and then enters the xylene reboiling furnace.
3. The adsorption unit to isomerization unit feed system of claim 1, wherein: and a first valve, a first one-way valve and a second valve are sequentially arranged on the circulating crossover wire.
4. The adsorption unit to isomerization unit feed system of claim 1, wherein: and a deheptanizer bottom pump is arranged on the upstream of the third heat exchanger on the discharging pipe line at the bottom of the deheptanizer.
5. The adsorption unit to isomerization unit feed system of claim 1, wherein: the deheptanizer feed line includes an isomerization reaction bypass line leading from the isomerization feed surge tank to the first heat exchanger.
6. The adsorption unit to isomerization unit feed system of claim 5, wherein: the isomerization feeding buffer tank sequentially passes through a fifth heat exchanger, a filter and a sixth heat exchanger through an isomerization feeding pipeline and enters a reaction furnace, the reaction furnace discharges materials and enters an isomerization reactor, the isomerization reactor discharges materials and enters a product separation tank through the sixth heat exchanger, and the product separation tank discharges materials and is led to the deheptanizer feeding pipeline after passing through the fifth heat exchanger.
7. The adsorption unit to isomerization unit feed system of claim 5, 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 overline is connected between the fourth valve and the fifth valve.
8. The adsorption unit to isomerization unit feed system of claim 1, wherein: and a sixth valve is arranged on the adsorption feeding pipeline between the discharge pipeline of the isomerization product clay treater and the circulating overline.
9. The adsorption unit to isomerization unit feed system of claim 1, wherein: the bottom of the deheptanizer is connected to a reboiler pump of the deheptanizer, and the reboiler pump of the deheptanizer is connected to the reboiler of the deheptanizer and then is introduced into the deheptanizer again for bottom circulation.
10. The adsorption unit to isomerization unit feed system of claim 1, wherein: and materials at the top of the deheptanizer enter an air cooler after heat exchange through a first heat exchanger, the discharged materials of the air cooler enter a reflux tank through a fourth heat exchanger, and a reflux pump guides the materials to the deheptanizer again from the reflux tank for tower top circulation.
Priority Applications (1)
| 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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| 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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| CN112500889A true CN112500889A (en) | 2021-03-16 |
| CN112500889B 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)
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|---|---|---|---|---|
| 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 |
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| 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, vol. 46, no. 7, pages 63 - 66 * |
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