CN105712815A - Energy saving separation method - Google Patents
Energy saving separation method Download PDFInfo
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- CN105712815A CN105712815A CN201410736769.XA CN201410736769A CN105712815A CN 105712815 A CN105712815 A CN 105712815A CN 201410736769 A CN201410736769 A CN 201410736769A CN 105712815 A CN105712815 A CN 105712815A
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- knockout drum
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- 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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
The invention relates to an energy saving separation method, which uses a high temperature gas-liquid separation tank, a low temperature gas-liquid separation tank, an air cooler, a water cooler, and a circulation gas compressor. 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; and the liquid phase material flows from the high temperature gas-liquid separation tank and the low temperature gas-liquid separation tank are mixed and then delivered to a subsequent separation system. The provided method has the advantages that the air cooling load is reduced, the thermal energy consumption of subsequent separation system is reduced, and the utilization rate of energy of reaction product is improved.
Description
Technical field
The present invention relates to a kind of energy-conservation separation method, 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 present invention proposes a kind of energy-conservation separation method, including high temperature knockout drum, low temperature knockout drum, air cooler, water cooler, recycle gas compressor 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 sends into subsequent separation system after being returned, by compressor cycle, the liquid phase stream mixing that response system, high temperature and low temperature knockout drum obtain.Present invention process reduces air cooling load, decreases the heat consumption of subsequent separation system, improves the utilization ratio of product energy.
As follows in the technical solution used in the present invention: a kind of energy-conservation separation method, 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 (4) 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 (5) compression Posterior circle；
Iv) above-mentioned high temperature enters subsequent separation system (II) separate tank bottoms liquid phase stream (the S.6 and S.7) mixing obtained with low temperature knockout drum after.
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, the liquid product that described product obtains after gas-liquid separation obtains target product after subsequent separation system separates；
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.
1 is product air cooler, and 2 is product high temperature knockout drum, and 3 is product low temperature knockout drum, and 4 is product water cooler, and 5 is recycle gas compressor.
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, is S.7 low temperature knockout drum liquid phase stream, be S.8 high/low temperature knockout drum liquid phase mixture diffluence piece-rate system.
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 100t/h, after air cooling cools down, temperature is 140 DEG C, obtaining gaseous stream after high temperature knockout drum separates and be about 40t/h, after water cooled cooling, temperature is 40 DEG C, obtains recycle hydrogen logistics and be about 7.5t/h after separating then through low temperature knockout drum, the liquid-phase mixing logistics temperature obtained by high temperature and low temperature knockout drum is 120 DEG C, enters subsequent separation system and is easily separated.
Through adjusting, this technological process air cooling load is about 36MW, 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 6MW.
[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 100t/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 7.5t/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 48MW, and water-cooled load is about 3MW, and subsequent separation system energy consumption (does not include the separation that clay tower is follow-up) and is about 15MW.
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 25% can be saved after adopting the inventive method, can save later separation energy consumption about 60%.
[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 100t/h, after air cooling cools down, temperature is 100 DEG C, obtaining gaseous stream after high temperature knockout drum separates and be about 45t/h, after water cooled cooling, temperature is 20 DEG C, obtains recycle hydrogen logistics and be about 10t/h after separating then through low temperature knockout drum, the liquid-phase mixing logistics temperature obtained by high temperature and low temperature knockout drum is 85 DEG C, enters subsequent separation system and is easily separated.
Through adjusting, this technological process air cooling load is about 27MW, 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 53MW.
[comparative example 2]
Below in conjunction with Fig. 2, comparative example 1 is described.
Same for acetate hydrogenation plant, some processes flow process is as shown in Figure 2, hydrogenation reaction product mass flow is 100t/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 10t/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 32MW, and water-cooled load is about 3MW, and subsequent separation system energy consumption (includes methanol/ethanol separation, methanol purification and ethyl alcohol purification) and is about 56MW.
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 5%.
[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, obtains gaseous stream and be about 83t/h after high temperature knockout drum separates, and 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, and pressure is 2.9MPag, 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%.
Claims (7)
1. an energy-conservation separation method, 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 (4) 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 (5) compression Posterior circle；
Iv) above-mentioned high temperature enters subsequent separation system (II) separate tank bottoms liquid phase stream (the S.6 and S.7) mixing obtained with low temperature knockout drum after.
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 (4) outlet temperature is more than 5 DEG C.
6. method according to claim 1, it is characterised in that it is characterized in that S11 enters subsequent separation system (II).
7. method according to claim 1, it is characterised in that subsequent separation system (II) includes the separation method of calorific requirement supply.
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| CN201410736769.XA CN105712815A (en) | 2014-12-05 | 2014-12-05 | Energy saving separation method |
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| CN201410736769.XA CN105712815A (en) | 2014-12-05 | 2014-12-05 | Energy saving separation method |
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Citations (6)
| 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 |
| 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 CN201410736769.XA patent/CN105712815A/en active Pending
Patent Citations (6)
| 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 |
| 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 |
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Application publication date: 20160629 |