CN105733636A - Heat integration distillation deep processing method and device of absorber oil - Google Patents
Heat integration distillation deep processing method and device of absorber oil Download PDFInfo
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- CN105733636A CN105733636A CN201610240440.3A CN201610240440A CN105733636A CN 105733636 A CN105733636 A CN 105733636A CN 201610240440 A CN201610240440 A CN 201610240440A CN 105733636 A CN105733636 A CN 105733636A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
- C10C1/04—Working-up tar by distillation
- C10C1/08—Winning of aromatic fractions
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
- C10C1/04—Working-up tar by distillation
- C10C1/08—Winning of aromatic fractions
- C10C1/12—Winning of aromatic fractions naphthalene fraction heavy fraction
Abstract
The invention relates to a heat integration distillation deep processing method and device of absorber oil.The device comprises a methyl naphthalene tower, a medium-quality absorber oil tower, an acenaphthene fractionating tower, a dibenzofuran tower, a fluorene tower and a beta-methyl naphthalene tower; the heat integration distillation is adopted, a six-tower continuous distillation device is utilized, a high-purity naphthalene oil fraction, a beta-methyl naphthalene fraction, an acenaphthylene fraction, a dibenzofuran fraction, a fluorine fraction and a high-value medium-quality absorber oil fraction can be obtained, meanwhile heat of different qualities in the absorber oil deep processing process is fully utilized, process optimization is conducted, energy consumption is lowered by 35% or above compared with a traditional process, consumption of condensate water is lowered by 40% or above, and purity of all fractions is improved; the distillation range is simple and easy to implement, and economic benefits and social benefits of enterprises are greatly raised.
Description
Technical field
The invention belongs to Coal Chemical Industry manufacture field, relate to the subtractive process of washing oil in coal tar, be specifically related to a kind of washing oil is thermally integrated rectification deep working method and device.
Background technology
Wash oil fraction is that to cut boiling range be 230 DEG C～the fraction of 300 DEG C to tar distillation, and productivity is generally the 4.5%～6.5% of anhydrous tar, the most mainly neutral component (accounting for 90%), and remaining is alkalescence, acidic components.Washing oil is rich in the basic organic chemical industry raw material of the preciousnesses such as quinoline, alpha-methyl-naphthalene, beta-methylnaphthalene, biphenyl, indole, acenaphthene, fluorenes, and these products are respectively provided with DEVELOPMENT PROSPECT widely.
Patent CN1078991A uses the oil-washing deep processing technology of twin furnace double tower, two towers are all respectively arranged with a side line, extraction naphthalene fraction, mixed methylnaphthalene fraction, middle matter washing oil, acenaphthene fraction and five kinds of fractions of heavy wash oil, the producer's major part using this kind of technique is the intermission utilizing twin furnace double tower to process crude naphthalene to process washing oil.This twin furnace double tower process subject matter is that the fraction of extraction is fine not, makes following process become difficulty.
Patent CN1208727A proposes three stove three towers and produces crude naphthalene and the technique of methyl naphthalene, i.e. on the basis of crude naphthalene twin furnace double tower, set up similar or identical rectifying column and tube furnace, with mixing naphtalene oil as raw material, 3rd tower extraction methylnaphthalene and demethylation naphthalene washing oil, three rectifying columns all do not have side line, they also propose another kind of processing scheme simultaneously, the demethylation naphthalene washing oil produced of looking unfamiliar before i.e. is raw material, the course of processing is similar to, and produces lightweight washing oil, acenaphthene fraction, dibenzofuran fraction and four kinds of fraction products of fluorenes fraction.This technique subject matter is that equipment is many, and investment is big, it is impossible to obtain beta-methylnaphthalene product.
Patent CN101899313A proposes the oil-washing deep processing technology of a kind of eight tower continuous rectifications, is separated by eight kinds of materials such as alpha-methyl-naphthalene, beta-methylnaphthalene.This technological equipment investment is too big, and eight tower continuous rectification operation easier are very big, and washing oil treating capacity must go up certain scale could be economical.Furthermore, complicated components in washing oil, wherein congruent melting, azeotropic component a lot, only just obtaining content 2 more than 99%, 6-dimethylnaphthalene, acenaphthene, dibenzofuran, fluorenes etc. by rectification, to implement difficulty very big.
Chinese patent CN102268273A proposes a kind of deep processing technology for coking wash oil, coking washing oil sequentially passes through respectively three continuous rectifying towers with a side take-off mouth, can once extract containing the naphthalene naphthalene fraction more than 80%, containing the beta-methylnaphthalene beta-methylnaphthalene fraction more than 70%, containing the alpha-methyl-naphthalene alpha-methyl-naphthalene fraction more than 60%, middle matter washing oil, containing the acenaphthene acenaphthene fraction more than 60%, containing the dibenzofuran dibenzofuran fraction more than 55% with containing the fluorenes fluorenes fraction more than 50%.This technique is by extraction beta-methylnaphthalene fraction while the first rectifying column extraction naphthalene fraction, beta-methylnaphthalene fraction purity is the highest, although the fluorenes fraction that the 3rd rectification tower reactor extraction simultaneously is more than 50%, but kettle material complicated components, crystallization difficulty, when kettle material to crystallizer prepares Industrial fluorene, difficulty is bigger.
Meanwhile, above-mentioned patent does not the most mention the energy consumption problem of washing oil deep processing.Washing oil deep processing is the operation that in coal tar processing, energy consumption is bigger, how by improving technique, reduce washing oil deep processing after energy consumption is also necessary faced by problem.
The deep working method of the new washing oil that the present invention proposes, employing is thermally integrated rectification process, by six tower continuous rectification devices, the higher fraction of naphthalene oil of purity, beta-methylnaphthalene fraction, acenaphthene fraction, dibenzofuran fraction, fluorenes fraction can not only be obtained and be worth higher middle matter wash oil fraction, take full advantage of the heat of different tastes in washing oil deep-processing process simultaneously, pass through process optimization, more than 35% is reduced than the energy consumption of traditional handicraft, condensed water consumption reduces by more than 40%, and boiling range is simple, it is easily achieved, substantially increases economic benefit and the social benefit of enterprise.
Summary of the invention
The present invention propose new a kind of washing oil be thermally integrated rectification deep processing device and method, employing is thermally integrated rectificating method, by six tower continuous rectification devices, the fraction of naphthalene oil that purity is higher can not only be obtained, beta-methylnaphthalene fraction, acenaphthene fraction, dibenzofuran fraction, fluorenes fraction and be worth higher middle matter wash oil fraction, take full advantage of the heat of different tastes in washing oil deep-processing process simultaneously, pass through process optimization, more than 35% is reduced than the energy consumption of traditional handicraft, condensed water consumption reduces by more than 40%, and boiling range is simple, it is easily achieved, substantially increase economic benefit and the social benefit of enterprise.
For achieving the above object, the present invention adopts the following technical scheme that and realizes:
The inventive system comprises methyl naphthalene tower, middle matter washing oil tower, acenaphthene fractionating column, dibenzofuran tower, fluorenes tower and beta-methylnaphthalene tower, it is characterized in that methyl naphthalene tower T101 is provided with washing oil charging aperture, top gaseous phase extraction mouth, backflow material inlet, survey line extraction mouth, tower reactor extraction mouth, reboiler return port and heat exchanger E101 return port, wherein top gaseous phase extraction mouth connects condenser, condenser connects backflow material inlet, survey line extraction mouth connects washes quinoline device, tower reactor extraction mouth connects reboiler, heat exchanger E101 and middle matter washing oil tower T102 material inlet, reboiler connects reboiler return port, heat exchanger E101 connects heat exchanger E101 return port；Middle matter washing oil tower T102 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, tower reactor extraction mouth and heat exchanger E102 return port, wherein material inlet connects methyl naphthalene tower T101 tower reactor extraction mouth, top gaseous phase extraction mouth connects condenser, condenser connects reflux stream import, tower reactor extraction mouth connects heat exchanger E102 and acenaphthene fractionating column T103 material inlet, and heat exchanger E102 connects heat exchanger E102 return port；Acenaphthene fractionating column T103 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, tower reactor extraction mouth and reboiler return port, matter washing oil tower T102 tower reactor extraction mouth during wherein material inlet connects, top gaseous phase extraction mouth connects heat exchanger E103, heat exchanger E103 connects condenser, condenser connects reflux stream import, tower reactor extraction mouth connects reboiler and dibenzofuran tower T104 material inlet, and reboiler connects reboiler return port；Dibenzofuran tower T104 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, tower reactor extraction mouth and reboiler return port, wherein material inlet connects acenaphthene fractionating column T103 tower reactor extraction mouth, top gaseous phase extraction mouth connects heat exchanger E101, heat exchanger E101 connects reflux stream import, tower reactor extraction mouth connects reboiler and fluorenes tower T105 material inlet, and reboiler connects reboiler return port；Fluorenes tower T105 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, tower reactor extraction mouth and reboiler return port, wherein material inlet connects dibenzofuran tower T104 tower reactor extraction mouth, top gaseous phase extraction mouth connects heat exchanger E102, heat exchanger E102 connects reflux stream import, tower reactor extraction mouth connects reboiler, and reboiler connects reboiler return port；The outlet washing quinoline device connects beta-methylnaphthalene tower T106 material inlet, beta-methylnaphthalene tower T106 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, survey line extraction mouth, tower reactor extraction mouth and heat exchanger E101 return port, wherein top gaseous phase extraction mouth connects condenser, condenser connects backflow material inlet, survey line extraction mouth extraction product, tower reactor extraction mouth connects heat exchanger E101, heat exchanger E101 and connects heat exchanger E101 return port.
A kind of washing oil be thermally integrated rectification deep process method, including the washing oil deep-processing system being made up of methyl naphthalene tower, middle matter washing oil tower, acenaphthene fractionating column, dibenzofuran tower, fluorenes tower and beta-methylnaphthalene tower, it is characterized in that: washing oil raw material adds in the middle part of methyl naphthalene tower T101 tower, methyl naphthalene tower T101 overhead extraction naphthalene fraction, side take-off mixed methylnaphthalene fraction, kettle material is partially into heat exchanger E101 and carries out heat exchange with dibenzofuran tower T104 top gaseous phase, it is partially into tower reactor reboiler, is partially into middle matter washing oil tower T102；Matter washing oil in middle matter washing oil tower T102 overhead extraction, kettle material is partially into heat exchanger E102 and carries out heat exchange with fluorenes tower T105 top gaseous phase, is partially into acenaphthene fractionating column T103；Acenaphthene fractionating column T103 top gaseous phase is introduced into heat exchanger E103 and beta-methylnaphthalene tower T106 kettle material heat exchange, after condensing subsequently into overhead condenser, a part returns acenaphthene fractionating column T103 as backflow, and a part enters dibenzofuran tower T104 as product extraction, acenaphthene fractionating column T103 tower reactor extraction；After dibenzofuran tower T104 top gaseous phase entrance heat exchanger E101 carries out heat exchange condensation with methyl naphthalene tower T101 kettle material, part returns dibenzofuran tower T104 as backflow, and a part is as product extraction, dibenzofuran tower T104 tower reactor extraction entrance fluorenes tower T105；After fluorenes tower T105 top gaseous phase enters heat exchanger E102 and middle matter washing oil tower T102 kettle material heat exchange cooling, a part returns acenaphthene fluorenes tower T105 as backflow, and a part is as product extraction, fluorenes tower T105 tower reactor extraction heavy residual stocks；Beta-methylnaphthalene tower T106 is entered after the preprocessed device of mixed methylnaphthalene fraction of methyl naphthalene tower T101 survey line extraction, beta-methylnaphthalene tower T106 overhead extraction mixed methylnaphthalene fraction, side take-off beta-methylnaphthalene product, matter washing oil head tank during matter washing oil returns in tower reactor extraction.
Methyl naphthalene tower T101 overhead extraction fraction of naphthalene oil naphthalene content >=70%, acenaphthene content >=65% in acenaphthene fractionating column T103 overhead extraction acenaphthene fraction, dibenzofuran content >=75% in the dibenzofuran fraction of dibenzofuran tower T104 overhead extraction, fluorenes content >=65% in the fluorenes fraction of fluorenes tower T105 overhead extraction, methyl naphthalene content >=65% in the mixed methylnaphthalene fraction of beta-methylnaphthalene tower T106 overhead extraction, beta-methylnaphthalene content >=98% in the beta-methylnaphthalene fraction of side take-off.
The tower of the present invention can be packed tower can also be plate column.
The process conditions of the present invention are: methyl naphthalene tower T101 operation pressure is 10-60kPa, middle matter washing oil tower T102 operation pressure is 10-60kPa, acenaphthene fractionating column T103 operation pressure is 101-150kPa, dibenzofuran tower T104 operation pressure is 101-150kPa, the operation pressure of fluorenes tower T105 is 101-150kPa, and beta-methylnaphthalene tower T106 operation pressure is 10-60kPa.
The deep working method of the new washing oil that the present invention proposes, compared with traditional handicraft, employing is thermally integrated rectification process, by six tower continuous rectification processes, the higher fraction of naphthalene oil of purity, beta-methylnaphthalene fraction, acenaphthene fraction, dibenzofuran fraction, fluorenes fraction can not only be obtained and be worth higher middle matter wash oil fraction, energy-saving and water-saving.The useful achievement of the present invention is:
A) saving energy consumption, observable index tradition oil-washing deep processing technology saves more than 35%.
B) reducing quantity of circulating water, recirculated water saves more than 40% than traditional handicraft.
C) improve the purity of various fraction.
Accompanying drawing explanation
Fig. 1: washing oil be thermally integrated rectification deep process schematic flow sheet.
Matter washing oil tower in T101 methyl naphthalene tower, T102, T103 acenaphthene fractionating column, T104 dibenzofuran tower, T105 fluorenes tower, T106 beta-methylnaphthalene tower, 1 fraction of naphthalene oil, matter wash oil fraction, 3 acenaphthene fractions, 4 dibenzofuran fractions, 5 fluorenes fractions, 6 mixed methylnaphthalene fractions, 7 beta-methylnaphthalene fractions, 8 Residual oils in 2.
Detailed description of the invention
The rectification deep process method that is thermally integrated of a kind of washing oil of the present invention uses and is thermally integrated rectification process, by six tower continuous rectification processes, the higher fraction of naphthalene oil of purity, beta-methylnaphthalene fraction, acenaphthene fraction, dibenzofuran fraction, fluorenes fraction can not only be obtained and be worth higher middle matter wash oil fraction, energy-saving and water-saving simultaneously.Below in conjunction with application example, implementation is further described.
Embodiment 1
Below in conjunction with the accompanying drawings 1 and detailed description of the invention the invention will be further described.
The inventive system comprises methyl naphthalene tower, middle matter washing oil tower, acenaphthene fractionating column, dibenzofuran tower, fluorenes tower and beta-methylnaphthalene tower, it is characterized in that methyl naphthalene tower T101 is provided with washing oil charging aperture, top gaseous phase extraction mouth, backflow material inlet, survey line extraction mouth, tower reactor extraction mouth, reboiler return port and heat exchanger E101 return port, wherein top gaseous phase extraction mouth connects condenser, condenser connects backflow material inlet, survey line extraction mouth connects washes quinoline device, tower reactor extraction mouth connects reboiler, heat exchanger E101 and middle matter washing oil tower T102 material inlet, reboiler connects reboiler return port, heat exchanger E101 connects heat exchanger E101 return port；Middle matter washing oil tower T102 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, tower reactor extraction mouth and heat exchanger E102 return port, wherein material inlet connects methyl naphthalene tower T101 tower reactor extraction mouth, top gaseous phase extraction mouth connects condenser, condenser connects reflux stream import, tower reactor extraction mouth connects heat exchanger E102 and acenaphthene fractionating column T103 material inlet, and heat exchanger E102 connects heat exchanger E102 return port；Acenaphthene fractionating column T103 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, tower reactor extraction mouth and reboiler return port, matter washing oil tower T102 tower reactor extraction mouth during wherein material inlet connects, top gaseous phase extraction mouth connects heat exchanger E103, heat exchanger E103 connects condenser, condenser connects reflux stream import, tower reactor extraction mouth connects reboiler and dibenzofuran tower T104 material inlet, and reboiler connects reboiler return port；Dibenzofuran tower T104 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, tower reactor extraction mouth and reboiler return port, wherein material inlet connects acenaphthene fractionating column T103 tower reactor extraction mouth, top gaseous phase extraction mouth connects heat exchanger E101, heat exchanger E101 connects reflux stream import, tower reactor extraction mouth connects reboiler and fluorenes tower T105 material inlet, and reboiler connects reboiler return port；Fluorenes tower T105 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, tower reactor extraction mouth and reboiler return port, wherein material inlet connects dibenzofuran tower T104 tower reactor extraction mouth, top gaseous phase extraction mouth connects heat exchanger E102, heat exchanger E102 connects reflux stream import, tower reactor extraction mouth connects reboiler, and reboiler connects reboiler return port；The outlet washing quinoline device connects beta-methylnaphthalene tower T106 material inlet, beta-methylnaphthalene tower T106 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, survey line extraction mouth, tower reactor extraction mouth and heat exchanger E101 return port, wherein top gaseous phase extraction mouth connects condenser, condenser connects backflow material inlet, survey line extraction mouth extraction product, tower reactor extraction mouth connects heat exchanger E101, heat exchanger E101 and connects heat exchanger E101 return port.
Washing oil raw material adds in the middle part of methyl naphthalene tower T101 tower, methyl naphthalene tower T101 overhead extraction naphthalene fraction, side take-off mixed methylnaphthalene fraction, kettle material is partially into heat exchanger E101 and carries out heat exchange with dibenzofuran tower T104 top gaseous phase, it is partially into tower reactor reboiler, is partially into middle matter washing oil tower T102；Matter washing oil in middle matter washing oil tower T102 overhead extraction, kettle material is partially into heat exchanger E102 and carries out heat exchange with fluorenes tower T105 top gaseous phase, is partially into acenaphthene fractionating column T103；Acenaphthene fractionating column T103 top gaseous phase is introduced into heat exchanger E103 and beta-methylnaphthalene tower T106 kettle material heat exchange, after condensing subsequently into overhead condenser, a part returns acenaphthene fractionating column T103 as backflow, and a part enters dibenzofuran tower T104 as product extraction, acenaphthene fractionating column T103 tower reactor extraction；After dibenzofuran tower T104 top gaseous phase entrance heat exchanger E101 carries out heat exchange condensation with methyl naphthalene tower T101 kettle material, part returns dibenzofuran tower T104 as backflow, and a part is as product extraction, dibenzofuran tower T104 tower reactor extraction entrance fluorenes tower T105；After fluorenes tower T105 top gaseous phase enters heat exchanger E102 and middle matter washing oil tower T102 kettle material heat exchange cooling, a part returns acenaphthene fluorenes tower T105 as backflow, and a part is as product extraction, fluorenes tower T105 tower reactor extraction heavy residual stocks；Beta-methylnaphthalene tower T106 is entered after the preprocessed device of mixed methylnaphthalene fraction of methyl naphthalene tower T101 survey line extraction, beta-methylnaphthalene tower T106 overhead extraction mixed methylnaphthalene fraction, side take-off beta-methylnaphthalene product, matter washing oil head tank during matter washing oil returns in tower reactor extraction.
The number of theoretical plate of each tower, operation pressure is as follows:
The number of theoretical plate of T101 methyl naphthalene tower is 80, operates pressure 50kPa；In T102, matter washing oil tower number of theoretical plate is 60, operates pressure 60kPa；T103 acenaphthene fractionating column number of theoretical plate is 60, and operation pressure is normal pressure；T104 dibenzofuran tower number of theoretical plate is 80, and operation pressure is normal pressure；T105 fluorenes tower number of theoretical plate is 80, and operation pressure is normal pressure, and T106 beta-methylnaphthalene tower number of theoretical plate is 150, operates pressure 30kPa.
Washing oil be thermally integrated rectification deep process effect:
Energy-saving and water-saving effect (inlet amount 1000kg/h):
| Condenser kcal/h | Reboiler kcal/h | |
| Traditional handicraft | -794062 | 886775 |
| It is thermally integrated technique | -435444 | 538545 |
| Energy-conservation % | 45.2 | 39.3 |
Embodiment 2
Washing oil raw material adds in the middle part of methyl naphthalene tower T101 tower, methyl naphthalene tower T101 overhead extraction naphthalene fraction, side take-off mixed methylnaphthalene fraction, kettle material is partially into heat exchanger E101 and carries out heat exchange with dibenzofuran tower T104 top gaseous phase, it is partially into tower reactor reboiler, is partially into middle matter washing oil tower T102；Matter washing oil in middle matter washing oil tower T102 overhead extraction, kettle material is partially into heat exchanger E102 and carries out heat exchange with fluorenes tower T105 top gaseous phase, is partially into acenaphthene fractionating column T103；Acenaphthene fractionating column T103 top gaseous phase is introduced into heat exchanger E103 and beta-methylnaphthalene tower T106 kettle material heat exchange, after condensing subsequently into overhead condenser, a part returns acenaphthene fractionating column T103 as backflow, and a part enters dibenzofuran tower T104 as product extraction, acenaphthene fractionating column T103 tower reactor extraction；After dibenzofuran tower T104 top gaseous phase entrance heat exchanger E101 carries out heat exchange condensation with methyl naphthalene tower T101 kettle material, part returns dibenzofuran tower T104 as backflow, and a part is as product extraction, dibenzofuran tower T104 tower reactor extraction entrance fluorenes tower T105；After fluorenes tower T105 top gaseous phase enters heat exchanger E102 and middle matter washing oil tower T102 kettle material heat exchange cooling, a part returns acenaphthene fluorenes tower T105 as backflow, and a part is as product extraction, fluorenes tower T105 tower reactor extraction heavy residual stocks；Beta-methylnaphthalene tower T106 is entered after the preprocessed device of mixed methylnaphthalene fraction of methyl naphthalene tower T101 survey line extraction, beta-methylnaphthalene tower T106 overhead extraction mixed methylnaphthalene fraction, side take-off beta-methylnaphthalene product, matter washing oil head tank during matter washing oil returns in tower reactor extraction.
The number of theoretical plate of each tower, operation pressure is as follows:
The number of theoretical plate of T101 methyl naphthalene tower is 80, operates pressure 10kPa；In T102, matter washing oil tower number of theoretical plate is 60, operates pressure 10kPa；T103 acenaphthene fractionating column number of theoretical plate is 60, and operation pressure is normal pressure；T104 dibenzofuran tower number of theoretical plate is 80, and operation pressure is normal pressure；T105 fluorenes tower number of theoretical plate is 80, and operation pressure is normal pressure, and T106 beta-methylnaphthalene tower number of theoretical plate is 150, operates pressure 60kPa.
Washing oil be thermally integrated rectification deep process effect:
Energy-saving and water-saving effect (inlet amount 1000kg/h):
| Condenser kcal/h | Reboiler kcal/h | |
| Traditional handicraft | -839737 | 921088 |
| It is thermally integrated technique | -481119 | 570385 |
| Energy-conservation % | 42.7 | 38.1 |
Embodiment 3
Washing oil raw material adds in the middle part of methyl naphthalene tower T101 tower, methyl naphthalene tower T101 overhead extraction naphthalene fraction, side take-off mixed methylnaphthalene fraction, kettle material is partially into heat exchanger E101 and carries out heat exchange with dibenzofuran tower T104 top gaseous phase, it is partially into tower reactor reboiler, is partially into middle matter washing oil tower T102；Matter washing oil in middle matter washing oil tower T102 overhead extraction, kettle material is partially into heat exchanger E102 and carries out heat exchange with fluorenes tower T105 top gaseous phase, is partially into acenaphthene fractionating column T103；Acenaphthene fractionating column T103 top gaseous phase is introduced into heat exchanger E103 and beta-methylnaphthalene tower T106 kettle material heat exchange, after condensing subsequently into overhead condenser, a part returns acenaphthene fractionating column T103 as backflow, and a part enters dibenzofuran tower T104 as product extraction, acenaphthene fractionating column T103 tower reactor extraction；After dibenzofuran tower T104 top gaseous phase entrance heat exchanger E101 carries out heat exchange condensation with methyl naphthalene tower T101 kettle material, part returns dibenzofuran tower T104 as backflow, and a part is as product extraction, dibenzofuran tower T104 tower reactor extraction entrance fluorenes tower T105；After fluorenes tower T105 top gaseous phase enters heat exchanger E102 and middle matter washing oil tower T102 kettle material heat exchange cooling, a part returns acenaphthene fluorenes tower T105 as backflow, and a part is as product extraction, fluorenes tower T105 tower reactor extraction heavy residual stocks；Beta-methylnaphthalene tower T106 is entered after the preprocessed device of mixed methylnaphthalene fraction of methyl naphthalene tower T101 survey line extraction, beta-methylnaphthalene tower T106 overhead extraction mixed methylnaphthalene fraction, side take-off beta-methylnaphthalene product, matter washing oil head tank during matter washing oil returns in tower reactor extraction.
The number of theoretical plate of each tower, operation pressure is as follows:
The number of theoretical plate of T101 methyl naphthalene tower is 80, operates pressure 60kPa；In T102, matter washing oil tower number of theoretical plate is 60, operates pressure 60kPa；T103 acenaphthene fractionating column number of theoretical plate is 60, and operation pressure is normal pressure；T104 dibenzofuran tower number of theoretical plate is 80, and operation pressure is normal pressure；T105 fluorenes tower number of theoretical plate is 80, and operation pressure is normal pressure, and T106 beta-methylnaphthalene tower number of theoretical plate is 150, operates pressure 10kPa.
Washing oil be thermally integrated rectification deep process effect:
Energy-saving and water-saving effect (inlet amount 1000kg/h):
| Condenser kcal/h | Reboiler kcal/h | |
| Traditional handicraft | -815760 | 906480 |
| It is thermally integrated technique | -459171 | 563054 |
| Energy-conservation % | 43.7 | 37.9 |
Claims (5)
1. a washing oil be thermally integrated rectification deep working method, it is characterized in that employing is thermally integrated rectificating method, six tower continuous rectifications being made up of methyl naphthalene tower, middle matter washing oil tower, acenaphthene fractionating column, dibenzofuran tower, fluorenes tower and beta-methylnaphthalene tower, washing oil raw material adds in the middle part of methyl naphthalene tower T101 tower, methyl naphthalene tower T101 overhead extraction naphthalene fraction, side take-off mixed methylnaphthalene fraction, kettle material is partially into heat exchanger E101 and carries out heat exchange with dibenzofuran tower T104 top gaseous phase, it is partially into tower reactor reboiler, is partially into middle matter washing oil tower T102；Matter washing oil in middle matter washing oil tower T102 overhead extraction, kettle material is partially into heat exchanger E102 and carries out heat exchange with fluorenes tower T105 top gaseous phase, is partially into acenaphthene fractionating column T103；Acenaphthene fractionating column T103 top gaseous phase is introduced into heat exchanger E103 and beta-methylnaphthalene tower T106 kettle material heat exchange, after condensing subsequently into overhead condenser, a part returns acenaphthene fractionating column T103 as backflow, and a part enters dibenzofuran tower T104 as product extraction, acenaphthene fractionating column T103 tower reactor extraction；After dibenzofuran tower T104 top gaseous phase entrance heat exchanger E101 carries out heat exchange condensation with methyl naphthalene tower T101 kettle material, part returns dibenzofuran tower T104 as backflow, and a part is as product extraction, dibenzofuran tower T104 tower reactor extraction entrance fluorenes tower T105；After fluorenes tower T105 top gaseous phase enters heat exchanger E102 and middle matter washing oil tower T102 kettle material heat exchange cooling, a part returns acenaphthene fluorenes tower T105 as backflow, and a part is as product extraction, fluorenes tower T105 tower reactor extraction heavy residual stocks；Beta-methylnaphthalene tower T106 is entered after the preprocessed device of mixed methylnaphthalene fraction of methyl naphthalene tower T101 survey line extraction, beta-methylnaphthalene tower T106 overhead extraction mixed methylnaphthalene fraction, side take-off beta-methylnaphthalene product, matter washing oil head tank during matter washing oil returns in tower reactor extraction.
2. the method for claim 1, it is characterized in that including a kind of washing oil is thermally integrated rectification deep processing device: methyl naphthalene tower, middle matter washing oil tower, acenaphthene fractionating column, dibenzofuran tower, fluorenes tower and beta-methylnaphthalene tower；It is characterized in that methyl naphthalene tower T101 is provided with washing oil charging aperture, top gaseous phase extraction mouth, backflow material inlet, survey line extraction mouth, tower reactor extraction mouth, reboiler return port and heat exchanger E101 return port, wherein top gaseous phase extraction mouth connects condenser, condenser connects backflow material inlet, survey line extraction mouth connects washes quinoline device, tower reactor extraction mouth connects reboiler, heat exchanger E101 and middle matter washing oil tower T102 material inlet, reboiler connects reboiler return port, and heat exchanger E101 connects heat exchanger E101 return port；Middle matter washing oil tower T102 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, tower reactor extraction mouth and heat exchanger E102 return port, wherein material inlet connects methyl naphthalene tower T101 tower reactor extraction mouth, top gaseous phase extraction mouth connects condenser, condenser connects reflux stream import, tower reactor extraction mouth connects heat exchanger E102 and acenaphthene fractionating column T103 material inlet, and heat exchanger E102 connects heat exchanger E102 return port；Acenaphthene fractionating column T103 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, tower reactor extraction mouth and reboiler return port, matter washing oil tower T102 tower reactor extraction mouth during wherein material inlet connects, top gaseous phase extraction mouth connects heat exchanger E103, heat exchanger E103 connects condenser, condenser connects reflux stream import, tower reactor extraction mouth connects reboiler and dibenzofuran tower T104 material inlet, and reboiler connects reboiler return port；Dibenzofuran tower T104 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, tower reactor extraction mouth and reboiler return port, wherein material inlet connects acenaphthene fractionating column T103 tower reactor extraction mouth, top gaseous phase extraction mouth connects heat exchanger E101, heat exchanger E101 connects reflux stream import, tower reactor extraction mouth connects reboiler and fluorenes tower T105 material inlet, and reboiler connects reboiler return port；Fluorenes tower T105 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, tower reactor extraction mouth and reboiler return port, wherein material inlet connects dibenzofuran tower T104 tower reactor extraction mouth, top gaseous phase extraction mouth connects heat exchanger E102, heat exchanger E102 connects reflux stream import, tower reactor extraction mouth connects reboiler, and reboiler connects reboiler return port；The outlet washing quinoline device connects beta-methylnaphthalene tower T106 material inlet, beta-methylnaphthalene tower T106 is provided with material inlet, top gaseous phase extraction mouth, backflow material inlet, survey line extraction mouth, tower reactor extraction mouth and heat exchanger E101 return port, wherein top gaseous phase extraction mouth connects condenser, condenser connects backflow material inlet, survey line extraction mouth extraction product, tower reactor extraction mouth connects heat exchanger E101, heat exchanger E101 and connects heat exchanger E101 return port.
3. the method for claim 1, it is characterized in that methyl naphthalene tower T101 overhead extraction fraction of naphthalene oil naphthalene content >=70%, acenaphthene content >=65% in acenaphthene fractionating column T103 overhead extraction acenaphthene fraction, dibenzofuran content >=75% in the dibenzofuran fraction of dibenzofuran tower T104 overhead extraction, fluorenes content >=65% in the fluorenes fraction of fluorenes tower T105 overhead extraction, methyl naphthalene content >=65% in the mixed methylnaphthalene fraction of beta-methylnaphthalene tower T106 overhead extraction, beta-methylnaphthalene content >=98% in the beta-methylnaphthalene fraction of side take-off.
4. the method for claim 1, it is characterized in that methyl naphthalene tower T101 operation pressure is 10-60kPa, middle matter washing oil tower T102 operation pressure is 10-60kPa, acenaphthene fractionating column T103 operation pressure is 101-150kPa, dibenzofuran tower T104 operation pressure is 101-150kPa, the operation pressure of fluorenes tower T105 is 101-150kPa, and beta-methylnaphthalene tower T106 operation pressure is 10-60kPa.
5. the method for claim 1, is characterized in that the tower of six towers is packed tower or plate column.
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| CN201610240440.3A CN105733636A (en) | 2016-04-15 | 2016-04-15 | Heat integration distillation deep processing method and device of absorber oil |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108607231A (en) * | 2018-06-26 | 2018-10-02 | 南京工业大学 | A kind of rectifier unit and rectificating method |
| CN110527540A (en) * | 2019-09-30 | 2019-12-03 | 河南博海化工有限公司 | A kind of wash oil device |
-
2016
- 2016-04-15 CN CN201610240440.3A patent/CN105733636A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108607231A (en) * | 2018-06-26 | 2018-10-02 | 南京工业大学 | A kind of rectifier unit and rectificating method |
| CN108607231B (en) * | 2018-06-26 | 2023-11-10 | 南京工业大学 | Rectifying device and rectifying method |
| CN110527540A (en) * | 2019-09-30 | 2019-12-03 | 河南博海化工有限公司 | A kind of wash oil device |
| CN110527540B (en) * | 2019-09-30 | 2024-02-02 | 河南博海化工有限公司 | Washing oil distillation device |
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