CN105712814A - Improved separation method - Google Patents
Improved separation method Download PDFInfo
- Publication number
- CN105712814A CN105712814A CN201410736766.6A CN201410736766A CN105712814A CN 105712814 A CN105712814 A CN 105712814A CN 201410736766 A CN201410736766 A CN 201410736766A CN 105712814 A CN105712814 A CN 105712814A
- Authority
- CN
- China
- Prior art keywords
- gas
- liquid
- knockout drum
- pressure
- separation tank
- 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.)
- Pending
Links
Classifications
-
- 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
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to an improved separation method, which uses a high temperature gas-liquid separation tank, a low temperature gas-liquid separation tank, a low pressure gas-liquid separation tank, an air cooler, a water cooler, a circulation gas compressor, and a pressure control valve. Reaction products are cooled by the air cooler and then introduced into the high temperature gas-liquid separation tank; the gas phase material flow obtained from the top of the high temperature gas-liquid separation tank is cooled by the water cooler and then introduced into the low temperature gas-liquid separation tank; the gas phase material flow obtained from the top of the low temperature gas-liquid separation tank is returned to the reaction system by the compressor, the liquid phase material flows from the high temperature gas-liquid separation tank and the low temperature gas-liquid separation tank are mixed, then the pressure of the mixture is reduced by a pressure adjusting valve, then the mixture is fed into the low pressure gas-liquid separation tank to recover the gas phase materials, the recovered gas phase can be used as fuel gas or is returned to the reaction system by the compressor, and the liquid phase from the low pressure gas-liquid separation tank is delivered to a subsequent separation system. Compared with the conventional single-grade liquid-gas separation technology, the provided technology has the following advantages: (1) the load of air cooling is reduced; (2) the thermal energy consumption of subsequent separation system is reduced, and the energy utilization efficiency is improved; (3) the material consumption is reduced, and material utilization rate is improved.
Description
Technical field
The present invention relates to the separation method of a kind of improvement, be specially a kind of for the product containing gas phase or gas-liquid two-phase, and the liquid product after being cooled and separated need to carry out the energy-saving separation method of later separation.
Background technology
Rectification is the lock out operation unit that chemical industry is important, the separation of about 95% mutually soluble liquids mixture is all with distillation operation in the world, rectification is to utilize the operating unit that in mixture, the difference of each component volatilization degree is easily separated, and directly determines quality and the yield of final products.Rectification is again the unit operation consuming energy higher, occupies bigger proportion in production cost, and according to statistics, in chemical process, the energy consumption of 40%-70% is used for separating, and energy consumption of rectification account for therein 95%.Therefore the separating energy consumption reduced in production process is the key reducing production cost, raising competitive power of product.
Patent CN101429089B discloses a kind of for the bulkhead type rectification column containing ethylbenzene, styrene feed separation, and the method adopts divided wall column to solve the problems such as rectifying column number of units in existing styrene Production is many, investment is big, energy consumption is high.
Patent CN101830830B discloses a kind of method utilizing dividing wall rectifying column separation of extractive distillation acetonitrile-methylbenzene, and the equipment investment of the method reduces by more than 20% with energy consumption compared with conventional extraction rectificating method.
Patent CN102351634A application discloses a kind of double-effect rectification and the benzene separated energy-saving new technology being thermally integrated, and the method reduces separating energy consumption more than 70% while obtaining qualified benzaldehyde product.
Patent CN102617262A application discloses the energy-saving process method that a kind of hexamethylene-cyclohexene-benzene separates, four traditional towers, twice extraction rectification technique are become one-time extractive rectification by the method, while realizing separate targets, greatly reduce the energy consumption needed for separation process.
Patent CN101602640A discloses the energy saving separation technology of a kind of ethyl benzene/styrene, the method adopts and is divided into double tower to operate by single column ethylbenzene/styrene separating tower, mainly solves ethyl benzene/styrene separation industries device in prior art and reduces styrene polymerization loss and reduce the problem that operation energy consumption can not be taken into account.
Summary of the invention
The technical problem to be solved in the present invention is the high energy in product separation process and loss of material problem.The present invention relates to the separation method of a kind of improvement, including high temperature knockout drum, low temperature knockout drum, low-pressure gas-liquid knockout drum, air cooler, water cooler, recycle gas compressor, pressure-control valve etc..Product enters High Temperature Gas liquid knockout drum after air cooling cools down, low temperature knockout drum is entered after the water cooled device cooling of gaseous stream that tank deck obtains, the tank deck gaseous stream obtained is returned response system by compressor cycle, reduce pressure through pressure-regulating valve after the liquid phase stream mixing that high temperature and low temperature knockout drum obtain, it is re-fed into low-pressure gas-liquid knockout drum and reclaims wherein gaseous phase materials, the gas phase reclaimed can as fuel gas or through compressor Returning reacting system, the liquid phase feeding subsequent separation system that low-pressure gas-liquid knockout drum obtains.Compared to traditional single stage gas-liquid separation technique, present invention process has following advantage: (1) reduces air cooling load；(2) decrease the heat consumption of subsequent separation system, improve the utilization ratio of energy；(3) decrease supplies consumption, improve the utilization ratio of material.
As follows in the technical solution used in the present invention: the separation method of a kind of improvement, said method comprising the steps of:
I) product (S.1) obtained by response system (I) enters air cooling (1) cooling, and logistics after cooling (S.2) enters high temperature knockout drum (2) and carries out one-level gas-liquid separation；
Ii) enter low temperature knockout drum (3) after the cooling further of the above-mentioned tank deck gaseous stream (S.3) water cooled (5) obtained after high temperature knockout drum (2) separates and carry out two grades of gas-liquid separations；
Iii) the tank deck gaseous stream (S.5) that above-mentioned low temperature knockout drum (3) obtains after separating returns response system (I) through recycle gas compressor (6) compression Posterior circle；
Iv) above-mentioned high temperature enters low-pressure gas-liquid knockout drum (4) separate tank bottoms liquid phase stream (the S.6 and S.7) mixing obtained with low temperature knockout drum after after pressure-regulating valve reduces pressure；
V) gaseous stream (S.10) obtained by above-mentioned low-pressure gas-liquid knockout drum (4) enters fuel system (III) or by Returning reacting system (I) after compressor (6) supercharging as fuel gas；
Vi) liquid phase stream feeding subsequent separation system (II) that above-mentioned low-pressure gas-liquid knockout drum (4) obtains is easily separated and obtains target product.
Preferably, the reaction that described product participates in from gas phase；
It is highly preferred that described product is from hydrogenation reaction；
Preferably, described product is gas phase or gas-liquid two-phase；
It is highly preferred that the separated rear gas phase of described product loops back response system；
Preferably, described product temperature is more than 150 DEG C；
It is highly preferred that described product temperature is more than 200 DEG C；
Preferably, described air cooler process-stream outlet temperature is more than 50 DEG C；
It is highly preferred that described air cooler process-stream outlet temperature is more than 100 DEG C；
Preferably, described water cooler process-stream outlet temperature is more than 5 DEG C；
It is highly preferred that described water cooler process-stream outlet temperature is more than 30 DEG C；
Preferably, described low-pressure gas-liquid knockout drum top gaseous phase can be sent to fuel gas system, and its pressure need to be higher than the pressure of fuel gas system；
Preferably, described low-pressure gas-liquid knockout drum gas recovery can be back to response system after compressor supercharging；
Preferably, the liquid product that described product obtains after gas-liquid separation enters subsequent separation system；
Preferably, described subsequent separation system includes the separation method of calorific requirement supply；
It is highly preferred that described subsequent separation system includes the separation methods such as rectification separation.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the inventive method.
In Fig. 1, I is response system, and II is subsequent separation system, and III is fuel system.
1 is product air cooler, and 2 is product separating at high temperature tank, and 3 is product cryogenic separation tank, and 4 is product low pressure separation pot, and 5 is product water cooler, and 6 is recycle gas compressor, and 7 is pressure-control valve.
S.1 it is product autoreaction system, S.2 it is air cooler outlet streams, S.3 it is high temperature knockout drum gaseous stream, S.4 it is water cooler outlet streams, S.5 it is low temperature knockout drum gaseous stream, S.6 it is high temperature knockout drum liquid phase stream, S.7 it is low temperature knockout drum liquid phase stream, S.8 it is compressor outlet logistics, S.9 for removing low-pressure gas-liquid knockout drum after high/low temperature knockout drum liquid-phase mixing logistics decompression, S.10 remove fuel gas system or recycle compressor entrance for low-pressure gas-liquid knockout drum vapour phase, be S.11 low-pressure gas-liquid knockout drum liquid phase.
Fig. 2 is conventional product separation process scheme sketch.
In Fig. 2, I is response system, and II is subsequent separation system.
1 is product knockout drum, and 2 is product air cooler, and 3 is product water cooler, and 4 is recycle gas compressor.
S.1 it is product autoreaction system, is S.2 air cooler outlet streams, be S.3 water cooler outlet streams, be S.4 knockout drum gaseous stream, be S.5 compressor outlet logistics, be S.6 knockout drum liquid phase stream.
The invention will be further elaborated by the examples below.
Detailed description of the invention
[embodiment 1]
Below in conjunction with Fig. 1, embodiment 1 is described.
For Aromatic Hydrocarbon United Plant disproportionation unit, technological process is as shown in Figure 1, dismutation reaction product quality flow is 200t/h, after air cooling cools down, temperature is 140 DEG C, after high temperature knockout drum separates, obtain gaseous stream be about 80t/h, after water cooled cooling, temperature is 40 DEG C, obtain recycle hydrogen logistics after separating then through low temperature knockout drum and be about 15t/h, the liquid-phase mixing logistics temperature obtained by high temperature and low temperature knockout drum is 120 DEG C, pressure is 0.9MPag, be decompressed to after 0.4MPag reclaiming fuel tolerance through pressure-control valve is 200kg/h, key component is the hydrogen in product, methane, ethane etc., fuel gas pipe network can be entered as fuel gas.The liquid phase that low-pressure gas-liquid knockout drum obtains enters subsequent separation system and is easily separated.
Through adjusting, this technological process air cooling load is about 70MW, and water-cooled load is about 10MW, and subsequent separation system energy consumption (does not include the separation that clay tower is follow-up) and is about 11MW.
[comparative example 1]
Below in conjunction with Fig. 2, comparative example 1 is described.
Same for Aromatic Hydrocarbon United Plant disproportionation unit, some processes flow process is as shown in Figure 2, dismutation reaction product quality flow is 200t/h, after air cooling cools down, temperature is 55 DEG C, it it is 40 DEG C then through temperature after cooling by water, obtain recycle hydrogen logistics after being separated by knockout drum and be about 15t/h, knockout drum the liquid phase stream temperature obtained is 40 DEG C, enters subsequent separation system and is easily separated.
Through adjusting, this technological process air cooling load is about 98MW, and water-cooled load is about 6MW, and subsequent separation system energy consumption (does not include the separation that clay tower is follow-up) and is about 35MW.
Compared with comparative example by above-described embodiment it can be seen that compared with single-stage gas liquid separation method, air cooling load about 29% can be saved after adopting the inventive method, can save later separation energy consumption about 69% the recyclable gaseous phase materials of about 1.5%.
[embodiment 2]
Below in conjunction with Fig. 1, embodiment 2 is described.
For acetate hydrogenation plant, some processes flow process is as shown in Figure 1, hydrogenation reaction product mass flow is 200t/h, after air cooling cools down, temperature is 100 DEG C, after high temperature knockout drum separates, obtain gaseous stream be about 90t/h, after water cooled cooling, temperature is 20 DEG C, obtain recycle hydrogen logistics after separating then through low temperature knockout drum and be about 20t/h, the liquid-phase mixing logistics temperature obtained by high temperature and low temperature knockout drum is 85 DEG C, pressure is 2.9MPag, be decompressed to after 0.8MPag reclaiming fuel tolerance through pressure-control valve is 50kg/h, key component is the lighter hydrocarbons such as the acetaldehyde in product, fuel gas pipe network can be entered as fuel gas.The liquid phase that low-pressure gas-liquid knockout drum obtains enters subsequent separation system and is easily separated.
Through adjusting, this technological process air cooling load is about 50MW, and water-cooled load is about 8MW, and subsequent separation system energy consumption (includes methanol/ethanol separation, methanol purification and ethyl alcohol purification) and is about 103MW.
[comparative example 2]
Below in conjunction with Fig. 2, comparative example 2 is described.
Same for acetate hydrogenation plant, some processes flow process is as shown in Figure 2, hydrogenation reaction product mass flow is 200t/h, after air cooling cools down, temperature is 55 DEG C, it it is 20 DEG C then through temperature after cooling by water, obtain recycle hydrogen logistics after being separated by knockout drum and be about 20t/h, knockout drum the liquid phase stream temperature obtained is 20 DEG C, enters subsequent separation system and is easily separated.
Through adjusting, this technological process air cooling load is about 60MW, and water-cooled load is about 5MW, and subsequent separation system energy consumption (includes methanol/ethanol separation, methanol purification and ethyl alcohol purification) and is about 110MW.
Compared with comparative example by above-described embodiment it can be seen that compared with single-stage gas liquid separation method, air cooling load about 17% can be saved after adopting the inventive method, can save later separation energy consumption about 6% the recyclable gaseous phase materials of about 0.4%.
[embodiment 3]
Below in conjunction with Fig. 1, embodiment 3 is described.
For oxalate hydrogenation plant, some processes flow process is as shown in Figure 1, hydrogenation reaction product mass flow is 200t/h, after air cooling cools down, temperature is 130 DEG C, after high temperature knockout drum separates, obtain gaseous stream be about 83t/h, after water cooled cooling, temperature is 15 DEG C, obtain recycle hydrogen logistics after separating then through low temperature knockout drum and be about 25t/h, the liquid-phase mixing logistics temperature obtained by high temperature and low temperature knockout drum is 87 DEG C, pressure is 2.9MPag, be decompressed to after 0.5MPag reclaiming fuel tolerance through pressure-control valve is 60kg/h, key component is the hydrogen in product, lighter hydrocarbons, fuel gas pipe network can be entered as fuel gas.The liquid phase that low-pressure gas-liquid knockout drum obtains enters subsequent separation system and is easily separated.
Through adjusting, this technological process air cooling load is about 46MW, and water-cooled load is about 12MW, and subsequent separation system energy consumption is about 85MW.
[comparative example 3]
Below in conjunction with Fig. 2, comparative example 3 is described.
Same for oxalate hydrogenation plant, some processes flow process is as shown in Figure 2, hydrogenation reaction product mass flow is 200t/h, after air cooling cools down, temperature is 55 DEG C, it it is 15 DEG C then through temperature after cooling by water, obtain recycle hydrogen logistics after being separated by knockout drum and be about 24t/h, knockout drum the liquid phase stream temperature obtained is 15 DEG C, enters subsequent separation system and is easily separated.
Through adjusting, this technological process air cooling load is about 55MW, and water-cooled load is about 8MW, and subsequent separation system energy consumption (includes methanol/ethanol separation, methanol purification and ethyl alcohol purification) and is about 92MW.
Compared with comparative example by above-described embodiment it can be seen that compared with single-stage gas liquid separation method, air cooling load about 16% can be saved after adopting the inventive method, can save later separation energy consumption about 8% the recyclable gaseous phase materials of about 0.5%.
Claims (9)
1. the separation method improved, said method comprising the steps of:
I) product (S.1) obtained by response system (I) enters air cooling (1) cooling, and logistics after cooling (S.2) enters high temperature knockout drum (2) and carries out one-level gas-liquid separation；
Ii) enter low temperature knockout drum (3) after the cooling further of the above-mentioned tank deck gaseous stream (S.3) water cooled (5) obtained after high temperature knockout drum (2) separates and carry out two grades of gas-liquid separations；
Iii) the tank deck gaseous stream (S.5) that above-mentioned low temperature knockout drum (3) obtains after separating returns response system (I) through recycle gas compressor (6) compression Posterior circle；
Iv) above-mentioned high temperature enters low-pressure gas-liquid knockout drum (4) separate tank bottoms liquid phase stream (the S.6 and S.7) mixing obtained with low temperature knockout drum after after pressure-regulating valve reduces pressure；
V) gaseous stream (S.10) obtained by above-mentioned low-pressure gas-liquid knockout drum (4) enters fuel system (III) or by Returning reacting system (I) after compressor (6) supercharging as fuel gas；
Vi) liquid phase stream feeding subsequent separation system (II) that above-mentioned low-pressure gas-liquid knockout drum (4) obtains is easily separated and obtains target product.
2. method according to claim 1, it is characterised in that described reaction is the reaction having gas phase to participate in, and product is gas phase or gas-liquid two-phase.
3. method according to claim 1, it is characterised in that the product temperature obtained by response system is more than 150 DEG C.
4. method according to claim 1, it is characterised in that air cooling (1) outlet temperature is more than 50 DEG C.
5. method according to claim 1, it is characterised in that water-cooled (5) outlet temperature is more than 5 DEG C.
6. method according to claim 1, it is characterised in that low-pressure gas-liquid knockout drum gas recovery can enter fuel gas system, its pressure is higher than the pressure of fuel gas system.
7. method according to claim 1, it is characterised in that low-pressure gas-liquid knockout drum gas recovery can be back to response system (I) after compressor (6) supercharging.
8. method according to claim 1, it is characterised in that S11 enters subsequent separation system (II).
9. method according to claim 1, it is characterised in that subsequent separation system (II) includes the separation method of calorific requirement supply.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410736766.6A CN105712814A (en) | 2014-12-05 | 2014-12-05 | Improved separation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410736766.6A CN105712814A (en) | 2014-12-05 | 2014-12-05 | Improved separation method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105712814A true CN105712814A (en) | 2016-06-29 |
Family
ID=56143817
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410736766.6A Pending CN105712814A (en) | 2014-12-05 | 2014-12-05 | Improved separation method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105712814A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108504383A (en) * | 2017-02-24 | 2018-09-07 | 何巨堂 | The deceleration split-phase guidance system that the choke zone gas-liquid injection stream of reducing transformer uses |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1407304A (en) * | 2001-09-11 | 2003-04-02 | 中国石油化工股份有限公司 | Improved light hydrocarbon deep cooling separating method |
| CN1690030A (en) * | 2004-04-29 | 2005-11-02 | 中国石油化工股份有限公司 | Improved toluene disproportionation process |
| CN1884236A (en) * | 2005-06-22 | 2006-12-27 | 中国石油化工股份有限公司 | Method for producing aromatic hydrocarbon |
| CN101348235A (en) * | 2007-07-19 | 2009-01-21 | 中国石油化工集团公司 | Hydrogen recovery method for hydrogenation plant |
| CN101717656A (en) * | 2008-10-09 | 2010-06-02 | 中科合成油技术有限公司 | Grading liquefaction method for solid fuel containing carbon and three-phase suspension bed reactor for same |
| CN103725313A (en) * | 2012-10-10 | 2014-04-16 | 中国石油化工集团公司 | Method and device for secondary condensation and separation of catalytic reforming prehydrogenation reaction products |
| CN103725306A (en) * | 2012-10-10 | 2014-04-16 | 中国石油化工集团公司 | Separation method and separation device for reform reaction product |
-
2014
- 2014-12-05 CN CN201410736766.6A patent/CN105712814A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1407304A (en) * | 2001-09-11 | 2003-04-02 | 中国石油化工股份有限公司 | Improved light hydrocarbon deep cooling separating method |
| CN1690030A (en) * | 2004-04-29 | 2005-11-02 | 中国石油化工股份有限公司 | Improved toluene disproportionation process |
| CN1884236A (en) * | 2005-06-22 | 2006-12-27 | 中国石油化工股份有限公司 | Method for producing aromatic hydrocarbon |
| CN101348235A (en) * | 2007-07-19 | 2009-01-21 | 中国石油化工集团公司 | Hydrogen recovery method for hydrogenation plant |
| CN101717656A (en) * | 2008-10-09 | 2010-06-02 | 中科合成油技术有限公司 | Grading liquefaction method for solid fuel containing carbon and three-phase suspension bed reactor for same |
| CN103725313A (en) * | 2012-10-10 | 2014-04-16 | 中国石油化工集团公司 | Method and device for secondary condensation and separation of catalytic reforming prehydrogenation reaction products |
| CN103725306A (en) * | 2012-10-10 | 2014-04-16 | 中国石油化工集团公司 | Separation method and separation device for reform reaction product |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108504383A (en) * | 2017-02-24 | 2018-09-07 | 何巨堂 | The deceleration split-phase guidance system that the choke zone gas-liquid injection stream of reducing transformer uses |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN204162631U (en) | A kind of xylene production system | |
| CN103467248B (en) | A kind of energy-saving ester through hydrogenation technique | |
| CN101602641B (en) | Double-effect rectification method and system thereof for finely separating hybrid pentane isomer | |
| CN103073376A (en) | Separation process of mixed pentane | |
| CN106336337A (en) | Method for separating toluene and n-propanol azeotrope through heat-integrated pressure-swing distillation | |
| JP2017534603A (en) | Distillation equipment | |
| CN102675029A (en) | Method for separating methylcyclohexane and toluene through differential pressure thermal coupling extractive rectification | |
| CN112358375B (en) | Two-tower double-heat-pump integrated 1-butene refining energy-saving process and device | |
| CN105712814A (en) | Improved separation method | |
| CN105964007B (en) | A kind of equipment and technique for separating n-butanol isobutanol mixtures | |
| CN105566030A (en) | Method for separating BTX | |
| CN208414288U (en) | A kind of differential pressure thermocouple propylene refining separation system in production of propylene oxide | |
| CN108586185A (en) | A kind of differential pressure thermocouple propylene refining piece-rate system and separation method | |
| CN101966397A (en) | Energy-saving rectifying device for integrating energy in rectifying tower sequence and method | |
| CN105330504B (en) | Reclaim the device of refined propylene | |
| CN105016972A (en) | Method used for separating methyl propionate and methyl alcohol azeotrope via differential pressure rectification, and device used for realizing method | |
| CN106380403B (en) | The method for efficiently separating dimethyl oxalate and dimethyl carbonate | |
| CN213760551U (en) | 1-butene refining energy-saving device with heat pump heat integration | |
| CN213760550U (en) | Two-tower double-heat-pump integrated 1-butene refining energy-saving device | |
| CN201670808U (en) | Energy saving device using low-temperature waste water to vaporize propylene depolymerized oil column feedstock in a step way | |
| CN204265660U (en) | A kind of device of the hydrogen circulation amount reduced in hydrogenation process | |
| CN101792679B (en) | Energy-saving method for vaporizing feed of propylene depolymerization oil tower by stepped utilization of low-temperature wastewater and device thereof | |
| CN108059581B (en) | Method for preparing tetrahydronaphthalene by naphthalene hydrogenation | |
| CN105712815A (en) | Energy saving separation method | |
| CN105498264A (en) | Paraxylene disproportionated product fractionation system and processing method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160629 |
|
| RJ01 | Rejection of invention patent application after publication |