CN1059851A - Method for recovering solvents in the hydro carbons process - Google Patents
Method for recovering solvents in the hydro carbons process Download PDFInfo
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- CN1059851A CN1059851A CN91110451A CN91110451A CN1059851A CN 1059851 A CN1059851 A CN 1059851A CN 91110451 A CN91110451 A CN 91110451A CN 91110451 A CN91110451 A CN 91110451A CN 1059851 A CN1059851 A CN 1059851A
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- solvent
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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Abstract
The invention provides the method for recovering solvents in a kind of hydro carbons process, is to draw after the heat exchanging network theory is studied.In the variable hot and cold streaming system of multiple-effect evaporation, when reaching at how narrow, the heat of recovery is maximum, and heat transfer area also is rational economically.After the lube oil furfural refining unit of 320,000 tons/year of commercial plants adopts the present invention, reclaim the furfural method with double tower and compare, can save 20～35% energy consumption, amount to 1,180,000 yuan/year.Transform for existing three tower recovery technologies, can save 10～20% energy consumption and 10～30% heat transfer area.
Description
The invention relates to the method for recovering solvents in the solvent processing petroleum hydrocarbon process, relate to the solvent refined oil process, the improvement of method for recovering solvents in the solvent dewaxing process.
Handling lubricating oil with solvent is a kind of petroleum refining process, and this process generates the mixed liquor that contains solvent and oil after solvent is handled lubricating oil, need from then on to reclaim solvent in the mixture.Solvent recovery adopts the multitower recovery system, also claims multi-effect evaporation system, and each pressure tower difference can fully recover energy energy efficient.
In prior art, as US4,214,975 and US4,422,923.This technology reclaims each evaporating column pressure of solvent and is followed successively by low pressure, high and medium voltage.
Another technology is US4,390,418, and US4,419,227 and EP98,359.Each evaporating column pressure that this technology reclaims solvent raises successively.
More than all do not adopt in 5 technology medium pressure column top steam be used to heat medium pressure column self charging, also not to the first evaporating column charging in appropriate position shunting and different hot-fluid heat exchange, promptly do not have appropriate parallel heat exchanging.
Another technology is J58-122,002, and this technology adopts the heat exchange process of three tower parallel connections, is about to the first tower charging and is divided into three strands, respectively with the hot-fluid heat exchange, and enters the evaporating column of three same pressure respectively.This technology does not consider with the first single evaporating column do not have to consider at appropriate position parallel heat exchanging yet.Medium pressure column equally also of no use top solvent vapo(u)r heating self charging.
Another technology is US4,830,711, and this technology is considered to improve the recovery heat with compressor.Its pressure sequence adopts first high pressure and back low pressure.This technology is inapplicable for the solvent of easy condensation or easy coking.
The objective of the invention is to overcome the shortcoming of prior art, propose a kind of according to the variable hot and cold stream principle of multiple-effect evaporation, improve the heat exchange process of solvent recovery multitower system and the method for operating condition, to reduce heating furnace fuel oil consumption and to make the heat exchanger heat transfer area the most reasonable.
Draw after the theory of heat exchanging network of the present invention is studied, in the variable hot and cold streaming system of multiple-effect evaporation, when reaching how narrow some when (also claiming narrow point, folder point, pinch point), the heat of recovery is maximum, and heat transfer area also is rational economically.Under the situation of how narrow point, have only the parallel heat exchanging of employing just can overcome the difficulty that heat-exchange network has a narrow range of temperature, also show that solvent vapo(u)r heating medium pressure column self charging of pushing up with medium pressure column can obtain good effect simultaneously.Therefore, the present invention heats second evaporating column self charging with the solvent vapo(u)r of second evaporating column (being medium pressure column) cat head.And adopt the first evaporating column charging heat exchange to be in proper order simultaneously: divide equally earlier be three stocks not with first, second and the 3rd condensate liquid parallel heat exchanging that evaporates the recovered overhead solvent; Again with the first evaporation cat head steam heat-exchanging; Dividing equally is two strands again, with the condensate liquid parallel heat exchanging of the second and the 3rd evaporating column recovery solvent; Again with the steam heat-exchanging of the second evaporating column recovered solvent partial condensation.This flow process be not experience and arbitrarily, be to carry out in strict accordance with the theory that the inventor proposes.For three towers evaporations at the ratio of the 3rd evaporating column charging and this tower evaporation capacity greater than 60 to 80%, it is uneconomic adopting the 3rd evaporation cat head Steam Heating the 3rd evaporating column self charging.For reclaiming dissolving agent process more than three towers, which tower will adopt the charging of evaporation cat head Steam Heating self, how much decide according to this tower charging oil content.
Therefore, feature of the present invention is to adopt three evaporating columns to reclaim solvent at least, the pressure of three towers is low pressure in turn, medium and high pressure, adopt second evaporating column (medium pressure column) top solvent vapo(u)r to heat second evaporating column self charging in the present invention, and in the first evaporating column feeding preheating process, earlier solvent-laden material being divided equally is other and first evaporating columns of three stocks, second evaporating column and the 3rd evaporation cat head recovered solvent condensate liquid parallel heat exchanging, again with the first evaporation cat head solvent vapo(u)r heat exchange, divide equally is that two stocks are not with second again, the 3rd evaporating column reclaims the condensate liquid parallel heat exchanging of solvent, evaporates the steam heat-exchanging of solvent overhead partial condensation with second again.
Accompanying drawing 1 is a method for recovering solvents flow chart of the present invention, among the figure:
1-solvent and oil mixture
The 32 cold flow chargings of 2-heat exchanger
The 33 cold flow chargings of 3-heat exchanger
The 34 cold flow chargings of 4-heat exchanger
The 32 cold flow dischargings of 5-heat exchanger
The 33 cold flow dischargings of 6-heat exchanger
The 34 cold flow dischargings of 7-heat exchanger
8-heat exchanger 32,33,34 discharging concetrated pipes
The 35 cold flow dischargings of 9-heat exchanger
The 36 cold flow chargings of 10-heat exchanger
The 37 cold flow chargings of 11-heat exchanger
The 36 cold flow dischargings of 12-heat exchanger
The 37 cold flow dischargings of 13-heat exchanger
14-heat exchanger 36,37 discharging concetrated pipes
The 38 cold flow dischargings of 15-condenser
The 39 cold flow chargings of 16-condenser
17-first evaporating column 43 overhead vapours
The 35 hot-fluid dischargings of 18-condenser
The 34 hot-fluid discharging throttlings of 19-heat exchanger are cut down
The 39 cold flow dischargings of 20-condenser
The 40 cold flow dischargings of 21-condenser
22-second evaporating column 44 overhead vapours
The 39 hot-fluid dischargings of 23-condenser
The 38 hot-fluid dischargings of 24-condenser
The 36 hot-fluid dischargings of 25-heat exchanger
The 41 cold flow chargings of 26-heating furnace
The 41 cold flow dischargings of 27-heating furnace
28-the 3rd evaporating column 45 overhead vapours
The 40 hot-fluid dischargings of 29-condenser
The 37 hot-fluid dischargings of 30-heat exchanger
The 32 hot-fluid discharging throttlings of 31-heat exchanger are cut down
32,33, the 34-heat exchanger
The 35-condenser
36, the 37-heat exchanger
38,39, the 40-condenser
The 41-heating furnace
45 dischargings of 42-the 3rd evaporating column
43-first evaporating column
44-second evaporating column
45-the 3rd evaporating column
46-condenser 38 cross-lines
47-condenser 39 cross-lines
48-heat exchanger 33 hot-fluid outlet throttlings cut down
The solvent recovery flow chart that is used for containing furfural and extraction oil below in conjunction with accompanying drawing 1 concrete explanation the present invention. It is three strand 2,3,4 that solvent and extraction oil mixing rear (solvent accounts for 90～95% matter) are divided equally by 1, enters respectively heat exchanger 32,33 and 34. The outlet be respectively 5,6,7, merge into one 8, enter condenser 35, outlet is 9, dividing equally is two strand 10,11. Enter respectively heat exchanger 36,37, outlet is 12,13, merges into 14, enters condenser 38, and outlet is 15, and cross-line 43 is arranged herein, is used for the control temperature, enters first evaporating column 43. First evaporating column, 43 pressure are 0.1 to 0.18MPa(absolute pressure), 165～180 ℃ of temperature. First evaporating column, 43 bottoms are for containing solvent liquid, enter condenser 39 through 16, and outlet is 20, and cross-line 44 is arranged herein, is used for the control temperature. Enter condenser 40, outlet is 21, enters second evaporating column 44. The second evaporating column pressure is 0.15 to 0.21MPa(absolute pressure), 175～190 ℃ of temperature.
Second evaporating column, 44 bottoms are for containing solvent liquid, enter heating furnace 41 through 26, and outlet is 27, enters the 3rd evaporating column 45. The pressure of the 3rd evaporating column 45 is 0.2 to 0.25MPa(absolute pressure), 195～220 ℃ of temperature. The 3rd evaporating column 45 bottoms are for containing solvent 10～35%(matter) liquid.
The first evaporation solvent overhead steam enters condenser 35 by 17, all is condensed into liquid, and outlet is 18, enters heat exchanger 34, and outlet is 19. The temperature of heat exchanger 34 drops to 155～160 ℃ from 165～175 ℃.
Second evaporating column 44, solvent overhead steam enter condenser 39 from 22, after the partial condensation, enter condenser 38 by 23, all be condensed into liquid, outlet is 24, enters heat exchanger 36, and outlet is 25, enter heat exchanger 33, outlet is 48, and the pressure of the gate control cut down the 3rd evaporating column 44 is arranged.The temperature of heat exchanger 36 is reduced to 165～175 ℃ from 175～190 ℃, and the temperature of heat exchanger 33 is reduced to 155～160 ℃ from 165～175 ℃.
The 3rd evaporating column 45, solvent overhead steam enter condenser 40 from 28, all are condensed into liquid, and outlet is 29, enters heat exchanger 37, and outlet is 30, enters heat exchanger 32, and outlet is 31, and the pressure of the gate control cut down the 3rd evaporating column 45 is arranged.The temperature of heat exchanger 37 is reduced to 165～175 ℃ from 175～190 ℃, and the temperature of heat exchanger 32 is reduced to 155～160 ℃ from 165～175 ℃.
The above solvent recovering system that proposes is also applicable to furfural, the recovery of other solvents such as N-methyl pyrrolidone.Or the butanone-toluene in the solvent dewaxing process, butanone-toluol-benzene, first isobutyl ketone-toluene, the solvent recovery of first isobutyl ketone-toluol-benzene.
To the lube oil furfural refining of 320,000 tons/year of commercial plants, behind employing the present invention, reclaim furfural with double tower and compare, can save 20 to 35% energy consumption, amount to 1,180,000 yuan/year.For three towers evaporations prior art, adopt the present invention after, can save 10 to 30% heat transfer area and 10 to 20% energy consumption.
Further demonstrate characteristics of the present invention below.
Embodiment 1
What produce during matter lubricating oil in processing contains furfural 93.64%(matter) 99.1 tons of Extracts/time, heat exchange to 168 ℃ is evaporated in first evaporating column, pressure is the 0.155MPa(absolute pressure); Heat exchange to 188 ℃ is again evaporated in second evaporating column, and pressure is the 0.187MPa(absolute pressure); Be heated to 214 ℃ at last, evaporate in the 3rd evaporating column, pressure is the 0.218MPa(absolute pressure).Extract oil out at the bottom of the last tower and contain furfural 25%(matter).Imitate evaporation energy-conservation 20% than two.
Embodiment 2
What produce when handling heavy grease contains furfural 93.89%(matter) 151.5 tons of Extracts/time, heat exchange to 179 ℃ is evaporated in first evaporating column, pressure is the 0.175MPa(absolute pressure); Heat exchange to 190 ℃ is again evaporated in second evaporating column, and pressure is the 0.207MPa(absolute pressure); Be heated to 217 ℃ at last, evaporate in the 3rd evaporating column, pressure is the 0.244(absolute pressure).Extract oil out at the bottom of the last tower and contain alditol 24.9%(matter).Imitate evaporation energy-conservation 30% than two.
Claims (2)
1, a kind of about the method for recovering solvents in the hydro carbons process, it is characterized in that adopting at least three evaporating columns to reclaim solvent, the pressure of three towers is low pressure in turn, medium and high pressure, adopt second evaporating column (medium pressure column) top solvent vapo(u)r to heat second evaporating column self charging in the present invention, and in the first evaporating column feeding preheating process, earlier solvent-laden material being divided equally is other and first evaporating columns of three stocks, second evaporating column and the 3rd evaporation cat head recovered solvent condensate liquid parallel heat exchanging, again with the first evaporation cat head solvent vapo(u)r heat exchange, divide equally is two strands again, respectively with second, the 3rd evaporating column reclaims the condensate liquid parallel heat exchanging of solvent, evaporate the steam heat-exchanging of solvent overhead partial condensation with second again, specifically, evaporation is reclaimed in the furfural feeding preheating process to three towers, earlier charging equality is divided into three strands, with first, the second and the 3rd evaporation cat head solvent condenses liquid heat exchange, make temperature be cooled to 155 to 160 ℃ from 165 to 175 ℃, then with the first evaporation cat head solvent vapo(u)r heat exchange, again material is divided into two stocks not with second, the 3rd evaporating column reclaims the condensed heat transfer fluid of solvent, make temperature reduce to 165 to 175 ℃ from 175 to 190 ℃, in the second evaporating column feeding preheating process, heat second evaporating column self charging with the second evaporation cat head solvent vapo(u)r partial condensation, fully being condensed to 175 to 190 ℃ with the 3rd evaporation overhead vapours again heats, the preheating of the described first and second evaporating column chargings must be implemented simultaneously, just can obtain maximum energy-conservation and minimizing heat transfer area, the described first evaporating column pressure is 0.1 to 0.18MPa absolute pressure, 165 to 180 ℃ of temperature, solvent overhead steam is successively through twice heat exchange, be condenser for the first time, be heat exchanger for the second time, the described second evaporating column pressure is 0.15 to 0.21MPa absolute pressure, 175 to 190 ℃ of temperature, solvent overhead steam is successively through four heat exchange, first, secondary is a condenser, the 3rd, four times is heat exchanger, described the 3rd evaporating column pressure is 0.2 to 0.25MPa absolute pressure, 195 to 220 ℃ of temperature, solvent overhead steam is successively through three heat exchange, be condenser for the first time, second, three times is heat exchanger.
2, method according to claim 1 is characterized in that described solvent can be a furfural, the N-methyl pyrrolidone, butanone-toluene, butanone-toluol-benzene, the recovery of solvent in the methyl iso-butyl ketone (MIBK)-toluene, methyl iso-butyl ketone (MIBK)-toluol-benzene etc. and petroleum hydrocarbon mixture.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN91110451A CN1020745C (en) | 1991-11-08 | 1991-11-08 | Process for recovering solvent during hydrocarbon processing |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN91110451A CN1020745C (en) | 1991-11-08 | 1991-11-08 | Process for recovering solvent during hydrocarbon processing |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1059851A true CN1059851A (en) | 1992-04-01 |
| CN1020745C CN1020745C (en) | 1993-05-19 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN91110451A Expired - Lifetime CN1020745C (en) | 1991-11-08 | 1991-11-08 | Process for recovering solvent during hydrocarbon processing |
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| Country | Link |
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| CN (1) | CN1020745C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1062007C (en) * | 1997-11-11 | 2001-02-14 | 中国石油化工总公司 | Process for regenerating aromatic hydrocarbon extraction solvent |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101280215B (en) * | 2008-05-23 | 2011-07-20 | 金碧华 | Production process of batch process of catalytic oil slurry |
-
1991
- 1991-11-08 CN CN91110451A patent/CN1020745C/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1062007C (en) * | 1997-11-11 | 2001-02-14 | 中国石油化工总公司 | Process for regenerating aromatic hydrocarbon extraction solvent |
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| Publication number | Publication date |
|---|---|
| CN1020745C (en) | 1993-05-19 |
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| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C15 | Extension of patent right duration from 15 to 20 years for appl. with date before 31.12.1992 and still valid on 11.12.2001 (patent law change 1993) | ||
| OR01 | Other related matters | ||
| C17 | Cessation of patent right | ||
| CX01 | Expiry of patent term |
Expiration termination date: 20111108 Granted publication date: 19930519 |
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| DD01 | Delivery of document by public notice |
Addressee: China Petrochemical Corporation Document name: Notification of Expiration of Patent Right Duration |