CN104119202B - A kind of energy-saving technique of variable-pressure rectification separation of methanol-acetone azeotrope - Google Patents
A kind of energy-saving technique of variable-pressure rectification separation of methanol-acetone azeotrope Download PDFInfo
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- CN104119202B CN104119202B CN201410368125.XA CN201410368125A CN104119202B CN 104119202 B CN104119202 B CN 104119202B CN 201410368125 A CN201410368125 A CN 201410368125A CN 104119202 B CN104119202 B CN 104119202B
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- 238000000034 method Methods 0.000 title claims abstract description 30
- NIQQIJXGUZVEBB-UHFFFAOYSA-N methanol;propan-2-one Chemical compound OC.CC(C)=O NIQQIJXGUZVEBB-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 238000000926 separation method Methods 0.000 title claims abstract description 14
- 238000007906 compression Methods 0.000 claims abstract description 71
- 230000006835 compression Effects 0.000 claims abstract description 70
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 49
- 239000007788 liquid Substances 0.000 claims abstract description 47
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 claims abstract description 34
- 238000000605 extraction Methods 0.000 claims abstract description 18
- 238000010992 reflux Methods 0.000 claims description 35
- 238000009833 condensation Methods 0.000 claims description 12
- 230000005494 condensation Effects 0.000 claims description 12
- 230000000630 rising effect Effects 0.000 claims description 8
- 238000004134 energy conservation Methods 0.000 abstract description 5
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 6
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- VVQNEPGJFQJSBK-UHFFFAOYSA-N Methyl methacrylate Chemical compound COC(=O)C(C)=C VVQNEPGJFQJSBK-UHFFFAOYSA-N 0.000 description 2
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000004513 sizing Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- MNAHQWDCXOHBHK-UHFFFAOYSA-N 1-phenylpropane-1,1-diol Chemical compound CCC(O)(O)C1=CC=CC=C1 MNAHQWDCXOHBHK-UHFFFAOYSA-N 0.000 description 1
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 1
- MWFMGBPGAXYFAR-UHFFFAOYSA-N 2-hydroxy-2-methylpropanenitrile Chemical compound CC(C)(O)C#N MWFMGBPGAXYFAR-UHFFFAOYSA-N 0.000 description 1
- -1 alcohol aldehyde Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004587 chromatography analysis Methods 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003822 epoxy resin Substances 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000003254 gasoline additive Substances 0.000 description 1
- 238000003306 harvesting Methods 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000000206 moulding compound Substances 0.000 description 1
- 229920005668 polycarbonate resin Polymers 0.000 description 1
- 239000004431 polycarbonate resin Substances 0.000 description 1
- 229920000647 polyepoxide Polymers 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000012264 purified product Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
- C07C45/81—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C45/82—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to the energy-saving technique of a kind of variable-pressure rectification separation of methanol-acetone azeotrope.The present invention adopts with the vacuum rectification tower of intermediate reboiler and the flow process of compression rectification tower simultaneous, first methanol-acetone azeotrope enters the vacuum rectification tower with intermediate reboiler, extraction massfraction at the bottom of vacuum rectification tower tower is the methyl alcohol of more than 99.5%, overhead extraction liquid squeezes into compression rectification tower through force (forcing) pump, at the bottom of compression rectification tower tower, extraction massfraction is the acetone of more than 99.8%, overhead extraction liquid is to after the intermediate reboiler heat supply of vacuum rectification tower, enter vacuum rectification tower again, circulate.The present invention utilizes the vacuum rectification tower with intermediate reboiler, reduces the thermal load of tower reactor reboiler, and provides heat with the intermediate reboiler that compression rectification column overhead Produced Liquid is vacuum rectification tower, thus reach energy-conservation object, and obtain high purity product.
Description
Technical field
The present invention relates to variable-pressure rectification technical field, be specifically related to the energy-saving technique of a kind of variable-pressure rectification separation of methanol-acetone azeotrope.
Background technology
Methyl alcohol and acetone are all very important Organic Chemicals.The field that methyl alcohol is mainly applied produces formaldehyde.Formaldehyde can be used to produce sizing agent, is mainly used in wood-processing industry, and be secondly the treatment agent being used as moulding compound, coating, yarn fabric and paper etc., the sizing agent being wherein used as wood working accounts for 80% of its total quantity consumed.Methyl alcohol is not only important industrial chemicals, but also is the energy and the vehicle fuel of excellent property.Methyl alcohol and isobutene reaction obtain methyl tertiary butyl ether (MTBE), and it is high-octane lead-less gasoline additive, also can be used as solvent.Methyl alcohol itself also can directly use as automobile fuel.
Estimate according to SRIC, within 2007, world's acetone demand is 548.6 ten thousand tons, wherein, the acetone cyanohydrin raw material of methyl methacrylate (MMA produce) consumption accounts for 25%, is directly used as that solvent accounts for 29%, dihydroxyphenyl propane (producing the raw material of polycarbonate and epoxy resin) accounts for 26%, alcohol aldehyde chemical accounts for 9%, other accounts for 11%.
The boiling point of methyl alcohol is 64.53 DEG C, and the boiling point of acetone is 56.14 DEG C, and the two can form minimum azeotropic mixture, and azeotropic temperature is 55.5 DEG C, and azeotropic consists of 22.4% methyl alcohol-77.6% acetone, cannot open by common rectifying separation.For the separation of azeotrope, conventional method has variable-pressure rectification and extracting rectifying.Extracting rectifying needs to introduce separating agent, and the separating agent of conventional separation of methanol-acetone is water and monoethanolamine, and separating agent large usage quantity and inevitably losing, and affect follow-up flow process.Variable-pressure rectification does not need to add three components in addition, as long as by regulating input heat, just more highly purified product can be obtained, total but Financial cost comparatively extracting rectifying want high, so the present invention has carried out energy-saving design on the basis of variable-pressure rectification.
Summary of the invention
The object of the invention is to use the problem of common separation method poor effect for methanol-acetone binary azeotropic system in current techniques, provide the energy-saving technique of a kind of variable-pressure rectification separation of methanol-acetone azeotrope.This technology utilization with the vacuum rectification tower of intermediate reboiler, and utilizes compression rectification column overhead Produced Liquid to intermediate reboiler heat supply, while obtaining high purity product, reduces energy consumption, has saved cost.
For reaching this object, the present invention by the following technical solutions:
An energy-saving technique for variable-pressure rectification separation of methanol-acetone azeotrope, described technique comprises the following steps:
1) methanol-acetone azeotrope is injected the vacuum rectification tower of band intermediate reboiler, tower top upflowing vapor is after the first condenser condenses, and phegma is by trim the top of column, and Produced Liquid squeezes into compression rectification tower through force (forcing) pump; The tower reactor phegma of vacuum rectification tower refluxes after the first reboiler boils again, and tower reactor Produced Liquid is methyl alcohol;
2) the tower top rising steam of compression rectification tower is after the second condenser condenses, and phegma is by trim the top of column, and overhead extraction liquid is after the intermediate reboiler heat supply of vacuum rectification tower, returns vacuum rectification tower and circulates; The tower reactor phegma of compression rectification tower refluxes after the second reboiler boils again, and tower reactor Produced Liquid is acetone.
The stage number of described vacuum rectification tower is 40-65 block, and intermediate reboiler is installed on the 35-45 block column plate place of vacuum rectification tower.
The thermal load of described intermediate reboiler is equivalent to the 45-71% of the first reboiler.Such as can select 45.02%, 49%, 55%, 62%, 64.8%, 68%, 70.9% etc.
The tower top temperature of described vacuum rectification tower is 40-55 DEG C, and column bottom temperature is 60-70 DEG C.Described tower top temperature can select 40.02 DEG C, 42 DEG C, 43.8 DEG C, 45 DEG C, 46.8 DEG C, 48 DEG C, 49.2 DEG C, 50 DEG C, 51.4 DEG C, 53 DEG C, 54.8 DEG C etc.; Described column bottom temperature can select 60.03 DEG C, 61 DEG C, 62.4 DEG C, 63.8 DEG C, 65 DEG C, 65.7 DEG C, 66.3 DEG C, 67.2 DEG C, 69 DEG C, 69.8 DEG C etc.
Described vacuum rectification tower adopts rectification under vacuum, and its working pressure is 0.8-0.9atm.Described pressure can select 0.81atm, 0.823atm, 0.84atm, 0.86atm, 0.88atm, 0.896atm etc.
The operating reflux ratio of described rectification under vacuum column overhead is 1-4.Described operating reflux ratio can select 1.02, and 1.13,1.2,1.26,1.35,1.39 etc.
The tower reactor phegma of described vacuum rectification tower refluxes after the first reboiler boils in 60-70 DEG C again.Described temperature can select 60.03 DEG C, 61 DEG C, 62.4 DEG C, 63.8 DEG C, 65 DEG C, 65.7 DEG C, 66.3 DEG C, 67.2 DEG C, 69 DEG C, 69.8 DEG C etc.
The tower top temperature of described compression rectification tower is 100-115 DEG C, and column bottom temperature is 110-125 DEG C.Described tower top temperature can select 100.02 DEG C, 100.2 DEG C, 103 DEG C, 105.5 DEG C, 108 DEG C, 111 DEG C, 112.7 DEG C, 114 DEG C, 114.8 DEG C; Described column bottom temperature can select 110.03 DEG C, 110.2 DEG C, 113 DEG C, 115.8 DEG C, 118 DEG C, 120.3 DEG C, 122 DEG C, 124.7 DEG C etc.
The stage number of described compression rectification tower is 40-60 block.
Described compression rectification tower adopts compression rectification, and its working pressure is absolute pressure 2-3atm.Described pressure can select 2.02atm, 2.1atm, 2.24atm, 2.31atm, 2.39atm, 2.5atm, 2.68atm, 2.8atm, 2.89atm, 2.96atm etc.
The Produced Liquid of described rectification under vacuum column overhead is forced into after 3-4atm through force (forcing) pump and is entered by the 15-25 block plate of compression rectification tower.Described pressure can select 3.01atm, 3.12atm, 3.2atm, 3.28atm, 3.5atm, 3.55atm, 3.8atm, 3.98atm etc.
The operating reflux ratio of described compression rectification column overhead is 2-5.Described operating reflux ratio is 2.02,2.2,2.8,3.25,3.9,4.2,4.7,4.95 etc.
The overhead extraction liquid of described compression rectification tower is after the intermediate reboiler heat supply of vacuum rectification tower, returns the 20-25 block column plate of vacuum rectification tower.
The tower reactor phegma of described compression rectification tower refluxes after the second reboiler boils in 110-120 DEG C again.Described temperature can select 110.04 DEG C, 110.8 DEG C, 112 DEG C, 114.8 DEG C, 117 DEG C, 118.6 DEG C, 119.6 DEG C etc.
An energy-saving technique for variable-pressure rectification separation of methanol-acetone azeotrope, described technique comprises the following steps:
1) vacuum rectification tower of band intermediate reboiler will be injected under methanol-acetone azeotrope normal temperature by the 30th block of plate, tower top upflowing vapor is after the first condenser condenses, operating reflux ratio is 1-4, and phegma is by trim the top of column, and Produced Liquid is forced into after 3-4atm through force (forcing) pump and squeezes into compression rectification tower; The tower reactor phegma of vacuum rectification tower refluxes after the first reboiler boils in 60-70 DEG C again, tower reactor Produced Liquid to be massfraction be more than 99.5% methyl alcohol; Wherein, the stage number of described vacuum rectification tower is 40-65 block, and intermediate reboiler is installed on the 35-45 block column plate place of vacuum rectification tower, and its thermal load is equivalent to the 45-71% of the first reboiler; Rectification under vacuum column overhead temperatures is 40-55 DEG C, and column bottom temperature is 60-70 DEG C, adopts rectification under vacuum, and its operation absolute pressure is 0.8-0.9atm;
2) Produced Liquid of rectification under vacuum column overhead, after force (forcing) pump pressurization, is entered by the 15-25 block plate of compression rectification tower; Tower top rising steam is after the second condenser condenses, and operating reflux ratio is 2-5, and phegma is by trim the top of column, and overhead extraction liquid is after the intermediate reboiler heat supply of vacuum rectification tower, returns the 20-25 block column plate of vacuum rectification tower, circulates; The tower reactor phegma of compression rectification tower refluxes after the second reboiler boils in 110-120 DEG C again, and tower reactor Produced Liquid is the acetone of massfraction more than 99.8%; Wherein, the stage number of compression rectification tower is 40-60 block; Tower top temperature is 100-115 DEG C, and column bottom temperature is 110-125 DEG C, and adopt compression rectification, its working pressure is absolute pressure 2-3atm.
Compared with prior art scheme, the present invention has following beneficial effect:
The present invention utilizes the intermediate reboiler heat supply of overhead extraction liquid to vacuum rectification tower of compression rectification tower, the thermal load 45-71% of vacuum rectification tower tower reactor reboiler can be reduced, after adding intermediate reboiler, the pilot wire of stripping section there occurs change, more near line of balance, namely also the impellent of sepn process is reduced in tower, thus improve the reversibility of sepn process, make the efficiency of Energy harvesting higher, again because tower reactor reboiler needs high-grade heat energy, and the heat energy taste of intermediate reboiler is relatively low, therefore more save process cost.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of variable-pressure rectification of the present invention separation of methanol-acetone azeotrope.
Description of reference numerals:
1-vacuum rectification tower; 2-first reboiler; 3-first condenser; 4-compression rectification tower; 5-second reboiler; 6-second condenser; 7-intermediate reboiler; 8-methanol-acetone azeotrope; 9-methyl alcohol; 10-acetone.
The present invention is described in more detail below.But following example is only simple and easy example of the present invention, and do not represent or limit the scope of the present invention, protection scope of the present invention is as the criterion with claims.
Embodiment
Technical scheme of the present invention is further illustrated by embodiment below in conjunction with accompanying drawing.
For better the present invention being described, be convenient to understand technical scheme of the present invention, typical but non-limiting embodiment of the present invention is as follows:
As shown in Figure 1, the energy-conservation step comprised of variable-pressure rectification separation of methanol provided by the invention-acetone azeotropic system is described in detail as follows:
1) vacuum rectification tower 1 of band intermediate reboiler 7 will be injected under methanol-acetone azeotrope 8 normal temperature by the 30th block of plate, tower top upflowing vapor is after the first condenser 3 condensation, operating reflux ratio is 1-4, phegma is by trim the top of column, and Produced Liquid is forced into after 3-4atm through force (forcing) pump and squeezes into compression rectification tower 4; The tower reactor phegma of vacuum rectification tower 1 refluxes after the first reboiler 2 boils in 60-70 DEG C again, tower reactor Produced Liquid to be massfraction be more than 99.5% methyl alcohol 9; Wherein, the stage number of described vacuum rectification tower is 40-65 block, and intermediate reboiler 7 is installed on the 35-45 block column plate place of vacuum rectification tower 1, and its thermal load is equivalent to the 45-71% of the first reboiler 2; Rectification under vacuum column overhead temperatures is 40-55 DEG C, and column bottom temperature is 60-70 DEG C, adopts rectification under vacuum, and its operation absolute pressure is 0.8-0.9atm;
2) Produced Liquid of vacuum rectification tower 1 tower top is after force (forcing) pump pressurization, is entered by the 15-25 block plate of compression rectification tower 4; Tower top rising steam is after the second condenser 6 condensation, and operating reflux ratio is 2-5, and phegma is by trim the top of column, and overhead extraction liquid is after intermediate reboiler 7 heat supply of vacuum rectification tower 1, returns the 20-25 block column plate of vacuum rectification tower 1, circulates; The tower reactor phegma of compression rectification tower 4 refluxes after the second reboiler 5 boils in 110-120 DEG C again, and tower reactor Produced Liquid is the acetone 10 of massfraction more than 99.8%; Wherein, the stage number of compression rectification tower 1 is 40-60 block; Tower top temperature is 100-115 DEG C, and column bottom temperature is 110-125 DEG C, and adopt compression rectification, its working pressure is absolute pressure 2-3atm.
The vacuum rectification tower that the present invention relates to and compression rectification tower are common rectifying tower.
Application example 1:
The actual plate number of vacuum rectification tower 1 is 50, working pressure is 0.85atm, operating reflux ratio is 2.5, tower top temperature controls at about 50 DEG C, bottom temperature is 61-62 DEG C, the massfraction of 25 DEG C is that the azeotropic mixture of the acetone of the methyl alcohol-75% of 25% is entered with the flow of 1000kg/h by the 30th block of plate, and tower top upflowing vapor is by the first condenser 3 condensation.Phegma is by the trim the top of column of vacuum rectification tower 1, and Produced Liquid squeezes into compression rectification tower 4 through force (forcing) pump (3atm).The phegma of vacuum rectification tower 1 refluxes after the first reboiler 2 boils in 60-70 DEG C again, tower reactor Produced Liquid to be massfraction be 99.52% methyl alcohol.The actual plate number of compression rectification tower 4 is 50, take compression rectification, absolute pressure is 2atm, compression rectification tower 4 tower top rising steam is by the second condenser 6 condensation, operating reflux ratio is 2.7, overhead extraction liquid is after intermediate reboiler 7 heat supply of vacuum rectification tower 1, returns the 15th block of column plate of vacuum rectification tower 1, circulates.Phegma is by the trim the top of column of compression rectification tower 4; The tower reactor phegma of compression rectification tower 4, after the second reboiler 5 boils in 110-120 DEG C again, returns compression rectification tower 4, and the tower reactor Produced Liquid of compression rectification tower 4 is the acetone of massfraction 99.83%.
Gas chromatographic analysis result is with upper reaches stock concentration.
Calculate by analysis, the intermediate reboiler 7 that compression rectification tower 4 overhead extraction liquid can be vacuum rectification tower 1 provides the heat of 0.40mw, accounts for 50% of the first reboiler 2 thermal load of vacuum rectification tower 1, fully energy-conservation.
Application example 2:
The actual plate number of vacuum rectification tower 1 is 50, working pressure is 0.85atm, operating reflux ratio is 2.7, tower top temperature controls at about 50 DEG C, bottom temperature is 61-62 DEG C, the massfraction of 25 DEG C is that the azeotropic mixture of the acetone of the methyl alcohol-70% of 30% is entered with the flow of 1000kg/h by the 30th block of plate, and tower top upflowing vapor is by the first condenser 3 condensation.Phegma is by the trim the top of column of vacuum rectification tower 1, and Produced Liquid squeezes into compression rectification tower 4 through force (forcing) pump (4atm).The phegma of vacuum rectification tower 1 refluxes after the first reboiler 2 boils in 60-70 DEG C again, tower reactor Produced Liquid to be massfraction be 99.53% methyl alcohol.The actual plate number of compression rectification tower 4 is 50, take compression rectification, absolute pressure is 3atm, compression rectification tower 4 tower top rising steam is by the second condenser 6 condensation, operating reflux ratio is 2.9, overhead extraction liquid is after intermediate reboiler 7 heat supply of vacuum rectification tower 1, returns the 15th block of column plate of vacuum rectification tower 1, circulates.Phegma is by the trim the top of column of compression rectification tower 4; The tower reactor phegma of compression rectification tower 4, after the second reboiler 5 boils in 110-120 DEG C again, returns compression rectification tower 4, and the tower reactor Produced Liquid of compression rectification tower 4 is the acetone of massfraction 99.81%.
Calculate by analysis, the intermediate reboiler 7 that compression rectification tower 4 overhead extraction liquid can be vacuum rectification tower 1 provides the heat of 0.39mw, accounts for 61% of the first reboiler 2 thermal load of vacuum rectification tower 1, fully energy-conservation.
Application example 3:
The actual plate number of vacuum rectification tower 1 is 50, working pressure is 0.85atm, operating reflux ratio is 2.4, tower top temperature controls at about 50 DEG C, bottom temperature is 61-62 DEG C, the massfraction of 25 DEG C is that the azeotropic mixture of the acetone of the methyl alcohol-80% of 20% is entered with the flow of 1000kg/h by the 30th block of plate, and tower top upflowing vapor is by the first condenser 3 condensation.Phegma is by the trim the top of column of vacuum rectification tower 1, and Produced Liquid squeezes into pressurizing tower 4 through force (forcing) pump (3atm).The phegma of vacuum rectification tower 1 refluxes after the first reboiler 2 boils in 60-70 DEG C again, tower reactor Produced Liquid to be massfraction be 99.51% methyl alcohol.The actual plate number of compression rectification tower 4 is 50, take compression rectification, absolute pressure is 2atm, compression rectification tower 4 tower top rising steam is by the second condenser 6 condensation, operating reflux ratio is 4.2, overhead extraction liquid is after intermediate reboiler 7 heat supply of vacuum rectification tower 1, returns the 15th block of column plate of vacuum rectification tower 1, circulates.Phegma is by the trim the top of column of compression rectification tower 4; The tower reactor phegma of compression rectification tower 4, after the second reboiler 5 boils in 110-120 DEG C again, returns compression rectification tower 4, and the tower reactor Produced Liquid of compression rectification tower 4 is the acetone of massfraction 99.84%.
Calculate by analysis, the intermediate reboiler 7 that compression rectification tower 4 overhead extraction liquid can be vacuum rectification tower 1 provides the heat of 0.39mw, accounts for 71% of the first reboiler 2 thermal load of vacuum rectification tower 1, fully energy-conservation.
Applicant states, the present invention illustrates technique of the present invention by above-described embodiment, but the present invention is not limited to aforesaid operations step, does not namely mean that the present invention must rely on aforesaid operations step and could implement.Person of ordinary skill in the field should understand, any improvement in the present invention, to equivalence replacement and the interpolation of ancillary component, the concrete way choice etc. of raw material selected by the present invention, all drops within protection scope of the present invention and open scope.
More than describe the preferred embodiment of the present invention in detail; but the present invention is not limited to the detail in above-mentioned embodiment, within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each concrete technical characteristic described in above-mentioned embodiment, in reconcilable situation, can be combined by any suitable mode, in order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible array mode.
In addition, also can carry out arbitrary combination between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (12)
1. an energy-saving technique for variable-pressure rectification separation of methanol-acetone azeotrope, is characterized in that, described technique comprises the following steps:
1) methanol-acetone azeotrope (8) is injected the vacuum rectification tower (1) of band intermediate reboiler (7), tower top upflowing vapor is after the first condenser (3) condensation, phegma is by trim the top of column, and Produced Liquid squeezes into compression rectification tower (4) through force (forcing) pump; The tower reactor phegma of vacuum rectification tower (1) refluxes after the first reboiler (2) boils again, and tower reactor Produced Liquid is methyl alcohol (9);
2) the tower top rising steam of compression rectification tower (4) is after the second condenser (6) condensation, phegma is by trim the top of column, overhead extraction liquid is after intermediate reboiler (7) heat supply of vacuum rectification tower (1), returns vacuum rectification tower (1) and circulates; The tower reactor phegma of compression rectification tower (4) refluxes after the second reboiler (5) boils again, and tower reactor Produced Liquid is acetone (10);
The thermal load of described intermediate reboiler (7) is equivalent to the 45-71% of the first reboiler (2);
Described vacuum rectification tower (1) adopts rectification under vacuum, and its operation absolute pressure is 0.8-0.9atm;
Described compression rectification tower (4) adopts compression rectification, and its working pressure is absolute pressure 2-3atm.
2. energy-saving technique as claimed in claim 1, it is characterized in that, the stage number of described vacuum rectification tower (1) is 40-65 block, and intermediate reboiler (7) is installed on the 35-45 block column plate place of vacuum rectification tower (1).
3. energy-saving technique as claimed in claim 1, it is characterized in that, the tower top temperature of described vacuum rectification tower (1) is 40-55 DEG C, and column bottom temperature is 60-70 DEG C.
4. energy-saving technique as claimed in claim 1, it is characterized in that, the operating reflux ratio of described vacuum rectification tower (1) tower top is 1-4.
5. energy-saving technique as claimed in claim 1, it is characterized in that, the tower reactor phegma of described vacuum rectification tower (1) refluxes after the first reboiler (2) boils in 60-70 DEG C again.
6. energy-saving technique as claimed in claim 1, it is characterized in that, the tower top temperature of described compression rectification tower (4) is 100-115 DEG C, and column bottom temperature is 110-125 DEG C.
7. energy-saving technique as claimed in claim 1, it is characterized in that, the stage number of described compression rectification tower (4) is 40-60 block.
8. energy-saving technique as claimed in claim 1, it is characterized in that, the Produced Liquid of described vacuum rectification tower (1) tower top is forced into after 3-4atm through force (forcing) pump and is entered by the 15-25 block plate of compression rectification tower (4).
9. energy-saving technique as claimed in claim 1, it is characterized in that, the operating reflux ratio of described compression rectification tower (4) tower top is 2-5.
10. energy-saving technique as claimed in claim 1, it is characterized in that, the overhead extraction liquid of described compression rectification tower (4) is after intermediate reboiler (7) heat supply of vacuum rectification tower (1), returns the 20-25 block column plate of vacuum rectification tower (1).
11. energy-saving techniques as claimed in claim 1, is characterized in that, the tower reactor phegma of described compression rectification tower (4) refluxes after the second reboiler (5) boils in 110-120 DEG C again.
12. energy-saving techniques as described in one of claim 1-11, it is characterized in that, described technique comprises the following steps:
1) vacuum rectification tower (1) of band intermediate reboiler (7) will be injected under methanol-acetone azeotrope (8) normal temperature by the 30th block of plate, tower top upflowing vapor is after the first condenser (3) condensation, operating reflux ratio is 1-4, phegma is by trim the top of column, and Produced Liquid is forced into after 3-4atm through force (forcing) pump and squeezes into compression rectification tower (4); The tower reactor phegma of vacuum rectification tower (1) refluxes after the first reboiler (2) boils in 60-70 DEG C again, tower reactor Produced Liquid to be massfraction be more than 99.5% methyl alcohol (9); Wherein, the stage number of described vacuum rectification tower is 40-65 block, and intermediate reboiler (7) is installed on the 35-45 block column plate place of vacuum rectification tower (1), and its thermal load is equivalent to the 45-71% of the first reboiler (2); Rectification under vacuum column overhead temperatures is 40-55 DEG C, and column bottom temperature is 60-70 DEG C, adopts rectification under vacuum, and its operation absolute pressure is 0.8-0.9atm;
2) Produced Liquid of vacuum rectification tower (1) tower top is after force (forcing) pump pressurization, is entered by the 15-25 block plate of compression rectification tower (4); Tower top rising steam is after the second condenser (6) condensation, operating reflux ratio is 2-5, phegma is by trim the top of column, overhead extraction liquid is after intermediate reboiler (7) heat supply of vacuum rectification tower (1), return the 20-25 block column plate of vacuum rectification tower (1), circulate; The tower reactor phegma of compression rectification tower (4) refluxes after the second reboiler (5) boils in 110-120 DEG C again, and tower reactor Produced Liquid is the acetone (10) of massfraction more than 99.8%; Wherein, the stage number of compression rectification tower (4) is 40-60 block; Tower top temperature is 100-115 DEG C, and column bottom temperature is 110-125 DEG C, and adopt compression rectification, its working pressure is absolute pressure 2-3atm.
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| CN105001056B (en) * | 2015-09-06 | 2016-06-08 | 青岛科技大学 | A kind of method of variable-pressure rectification separation isobutanol and normal heptane azeotropic system |
| CN106925191A (en) * | 2015-12-29 | 2017-07-07 | 辽宁奥克化学股份有限公司 | A kind of continuous alkoxylation device and technique |
| EP3466915B1 (en) * | 2017-10-06 | 2019-11-27 | SABIC Global Technologies B.V. | Method of purifying acetone |
| CN108794310B (en) * | 2017-10-27 | 2021-08-31 | 泰州学院 | Method for separating and purifying two acetals and raw material alcohol by pressure swing distillation |
| CN109608320A (en) * | 2019-01-09 | 2019-04-12 | 天津精分科技发展有限公司 | A kind of separation method of acetone and water mixed solvent |
| CN114191837B (en) * | 2021-12-07 | 2023-02-14 | 大连理工大学 | Device and method for separating methanol-benzene-acetonitrile azeotrope system by extractive distillation |
| CN114956961A (en) * | 2022-04-21 | 2022-08-30 | 科富恺工艺设备(上海)有限公司 | Separation method of methanol acetone azeotrope |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5346593A (en) * | 1993-06-18 | 1994-09-13 | The M. W. Kellogg Company | Intermediate reboiler for a methanol plant |
-
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US5346593A (en) * | 1993-06-18 | 1994-09-13 | The M. W. Kellogg Company | Intermediate reboiler for a methanol plant |
Non-Patent Citations (3)
| Title |
|---|
| Comparison of extractive distillation and pressure-swing distillation for acetone-methanol separation;William L.Luyben et al.;《Ind.Eng.Chem.Res.》;20080320;第47卷(第8期);20080320 * |
| Separation of an Acetone-Methanol Mixture by Pressure-Swing Batch Distillation in a Double-Column System with and without Thermal Integration;Gabor Modla et al.,;《Ind. Eng. Chem. Res.》;20100323;第49卷(第8期);3785–3793 * |
| 变压精馏分离甲醇-丙酮的工艺模拟及优化;孔鹏等;《化工进展》;20131231;第32卷(第11期);第2583-2587页 * |
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