CN104119202A - Energy-saving technique for separating methanol-acetone azeotrope by variable-pressure rectification - Google Patents
Energy-saving technique for separating methanol-acetone azeotrope by variable-pressure rectification Download PDFInfo
- Publication number
- CN104119202A CN104119202A CN201410368125.XA CN201410368125A CN104119202A CN 104119202 A CN104119202 A CN 104119202A CN 201410368125 A CN201410368125 A CN 201410368125A CN 104119202 A CN104119202 A CN 104119202A
- Authority
- CN
- China
- Prior art keywords
- tower
- rectification
- under vacuum
- reboiler
- rectification under
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to an energy-saving technique for separating methanol-acetone azeotrope by variable-pressure rectification. By adopting the process composed of a vacuum rectification tower with a middle reboiler and a pressure rectification tower, the methanol-acetone azeotrope firstly enters the vacuum rectification tower with the middle reboiler, the methanol with the mass percent of higher than 99.5% is produced from the bottom of the vacuum rectification tower, the tower top produced fluid is driven into the pressure rectification tower by the pressure pump; the acetone with the mass percent of higher than 99.8% is produced from the bottom of the pressure rectification tower, and the tower top produced fluid supplies heat to the middle reboiler of the vacuum rectification tower and enters the vacuum rectification tower to perform circulation. The vacuum rectification tower with the middle reboiler is utilized to lower the heat load of the tower bottom reboiler; and the tower top produced fluid of the pressure rectification tower is utilized to supply heat to the middle reboiler of the vacuum rectification tower, thereby achieving the goal of energy saving and obtaining the high-purity product.
Description
Technical field
The present invention relates to variable-pressure rectification technical field, be specifically related to a kind of energy-saving technique 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 is to produce formaldehyde.Formaldehyde can be used to produce sizing agent, is mainly used in wood-processing industry, is secondly the treatment agent as moulding compound, coating, yarn fabric and paper etc., wherein accounts for 80% of its total quantity consumed as the sizing agent of wood working.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 account for 25%, directly as solvent account 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 need to be introduced 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 affects follow-up flow process.Variable-pressure rectification does not need to add in addition the 3rd component, as long as by input heat is regulated, just can obtain more highly purified product, but total Financial cost wants high compared with extracting rectifying, 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 for methanol-acetone binary azeotropic system in current techniques the problem of common separation method poor effect, a kind of energy-saving technique of variable-pressure rectification separation of methanol-acetone azeotrope is provided.This technology utilization is with the rectification under vacuum tower of intermediate reboiler, and utilizes compression rectification column overhead Produced Liquid to intermediate reboiler heat supply, in obtaining high purity product, reduced energy consumption, 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 to the rectification under vacuum tower with intermediate reboiler, tower top rising steam is after the first condenser condenses, and phegma is by trim the top of column, and Produced Liquid is squeezed into compression rectification tower through force (forcing) pump; The tower reactor phegma of rectification under vacuum 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, by trim the top of column, after overhead extraction liquid is the intermediate reboiler heat supply of rectification under vacuum tower, returns to rectification under vacuum 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 rectification under vacuum tower is 40-65 piece, and intermediate reboiler is installed on the 35-45 piece column plate place of rectification under vacuum tower.
The thermal load of described intermediate reboiler is equivalent to the 45-71% of the first reboiler.For example can select 45.02%, 49%, 55%, 62%, 64.8%, 68%, 70.9% etc.
The tower top temperature of described rectification under vacuum tower is 40-55 DEG C, and column bottom temperature is 60-70 DEG C.Described tower top temperature can be selected 40.02 DEG C, and 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 be selected 60.03 DEG C, and 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 rectification under vacuum tower adopts rectification under vacuum, and its working pressure is 0.8-0.9atm.Described pressure can be selected 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 1.02,1.13,1.2,1.26,1.35,1.39 etc.
The tower reactor phegma of described rectification under vacuum tower through the first reboiler in 60-70 DEG C boil again after reflux.Described temperature can be selected 60.03 DEG C, and 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 be selected 100.02 DEG C, and 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 be selected 110.03 DEG C, and 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 piece.
Described compression rectification tower adopts compression rectification, and its working pressure is absolute pressure 2-3atm.Described pressure can be selected 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 entered by the 15-25 piece plate of compression rectification tower after force (forcing) pump is forced into 3-4atm.Described pressure can be selected 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.
After the overhead extraction liquid of described compression rectification tower is the intermediate reboiler heat supply of rectification under vacuum tower, return to the 20-25 piece column plate of rectification under vacuum tower.
The tower reactor phegma of described compression rectification tower through the second reboiler in 110-120 DEG C boil again after reflux.Described temperature can be selected 110.04 DEG C, and 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) will under methanol-acetone azeotrope normal temperature, inject the rectification under vacuum tower with intermediate reboiler by the 30th block of plate, tower top rising steam 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 squeezed into compression rectification tower after force (forcing) pump is forced into 3-4atm; The tower reactor phegma of rectification under vacuum tower through the first reboiler in 60-70 DEG C boil again after reflux, tower reactor Produced Liquid is that massfraction is more than 99.5% methyl alcohol; Wherein, the stage number of described rectification under vacuum tower is 40-65 piece, and intermediate reboiler is installed on the 35-45 piece column plate place of rectification under vacuum tower, and its thermal load is equivalent to the 45-71% of the first reboiler; Rectification under vacuum column overhead temperature 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 piece plate of compression rectification tower; Tower top rising steam is after the second condenser condenses, and operating reflux ratio is 2-5, and phegma, by trim the top of column, after overhead extraction liquid is the intermediate reboiler heat supply of rectification under vacuum tower, returns to the 20-25 piece column plate of rectification under vacuum tower, circulates; The tower reactor phegma of compression rectification tower through the second reboiler in 110-120 DEG C boil again after reflux, tower reactor Produced Liquid is more than 99.8% acetone of massfraction; Wherein, the stage number of compression rectification tower is 40-60 piece; Tower top temperature is 100-115 DEG C, and column bottom temperature is 110-125 DEG C, adopts compression rectification, and 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 overhead extraction liquid of compression rectification tower to the intermediate reboiler heat supply of rectification under vacuum tower, can reduce the thermal load 45-71% of rectification under vacuum tower tower reactor reboiler, add after intermediate reboiler, there is change in the pilot wire of stripping section, more near line of balance, also be that in tower, the impellent of sepn process is reduced, thereby improve the reversibility of sepn process, the efficiency that energy is utilized is higher, again because tower reactor reboiler needs high-grade heat energy, and the taste of the heat energy of intermediate reboiler is relatively low, therefore more save process cost.
Brief description of the drawings
Fig. 1 is the schematic flow sheet of variable-pressure rectification separation of methanol-acetone azeotrope of the present invention.
Description of reference numerals:
1-rectification under vacuum tower; 2-the first reboiler; 3-the first condenser; 4-compression rectification tower; 5-the second reboiler; 6-the 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, does not represent or limit the scope of the present invention, and protection scope of the present invention is as the criterion with claims.
Embodiment
Further illustrate technical scheme of the present invention below in conjunction with accompanying drawing and by embodiment.
For the present invention is described better, 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 comprising of variable-pressure rectification separation of methanol-acetone azeotropic system provided by the invention is described in detail as follows:
1) will under methanol-acetone azeotrope 8 normal temperature, inject the rectification under vacuum tower 1 with intermediate reboiler 7 by the 30th block of plate, tower top rising steam is after the first condenser 3 condensations, operating reflux ratio is 1-4, phegma is by trim the top of column, and Produced Liquid is squeezed into compression rectification tower 4 after force (forcing) pump is forced into 3-4atm; The tower reactor phegma of rectification under vacuum tower 1 through the first reboiler 2 in 60-70 DEG C boil again after reflux, tower reactor Produced Liquid is that massfraction is more than 99.5% methyl alcohol 9; Wherein, the stage number of described rectification under vacuum tower is 40-65 piece, and intermediate reboiler 7 is installed on the 35-45 piece column plate place of rectification under vacuum tower 1, and its thermal load is equivalent to the 45-71% of the first reboiler 2; Rectification under vacuum column overhead temperature 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 tower 1 tower top, after force (forcing) pump pressurization, is entered by the 15-25 piece plate of compression rectification tower 4; Tower top rising steam is after the second condenser 6 condensations, and operating reflux ratio is 2-5, and phegma, by trim the top of column, after overhead extraction liquid is intermediate reboiler 7 heat supplies of rectification under vacuum tower 1, returns to the 20-25 piece column plate of rectification under vacuum tower 1, circulates; The tower reactor phegma of compression rectification tower 4 through the second reboiler 5 in 110-120 DEG C boil again after reflux, tower reactor Produced Liquid is more than 99.8% acetone 10 of massfraction; Wherein, the stage number of compression rectification tower 1 is 40-60 piece; Tower top temperature is 100-115 DEG C, and column bottom temperature is 110-125 DEG C, adopts compression rectification, and its working pressure is absolute pressure 2-3atm.
Rectification under vacuum tower and the compression rectification tower that the present invention relates to are common rectifying tower.
Application example 1:
The actual plate number of rectification under vacuum tower 1 is 50, working pressure is 0.85atm, operating reflux ratio is 2.5, tower top temperature is controlled at 50 DEG C of left and right, tower reactor temperature is 61-62 DEG C, the massfraction of 25 DEG C is that the azeotropic mixture of the acetone of 25% methyl alcohol-75% is entered with the flow of 1000kg/h by the 30th block of plate, and tower top rising steam is by the first condenser 3 condensations.Phegma is by the trim the top of column of rectification under vacuum tower 1, and Produced Liquid is squeezed into compression rectification tower 4 through force (forcing) pump (3atm).The phegma of rectification under vacuum tower 1 through the first reboiler 2 in 60-70 DEG C boil again after reflux, tower reactor Produced Liquid is that massfraction is 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 steams are by the second condenser 6 condensations, operating reflux ratio is 2.7, after overhead extraction liquid is intermediate reboiler 7 heat supplies of rectification under vacuum tower 1, return to the 15th block of column plate of rectification under vacuum tower 1, circulate.Phegma is by the trim the top of column of compression rectification tower 4; The tower reactor phegma of compression rectification tower 4 through the second reboiler 5 in 110-120 DEG C boil again after, return to compression rectification tower 4, the tower reactor Produced Liquid of compression rectification tower 4 is the acetone of massfraction 99.83%.
Be gas chromatographic analysis result with upper reaches thigh concentration.
Calculate by analysis, the intermediate reboiler 7 that compression rectification tower 4 overhead extraction liquid can be rectification under vacuum tower 1 provides the heat of 0.40mw, account for rectification under vacuum tower 1 the first reboiler 2 thermal loads 50%, fully energy-conservation.
Application example 2:
The actual plate number of rectification under vacuum tower 1 is 50, working pressure is 0.85atm, operating reflux ratio is 2.7, tower top temperature is controlled at 50 DEG C of left and right, tower reactor temperature is 61-62 DEG C, the massfraction of 25 DEG C is that the azeotropic mixture of the acetone of 30% methyl alcohol-70% is entered with the flow of 1000kg/h by the 30th block of plate, and tower top rising steam is by the first condenser 3 condensations.Phegma is by the trim the top of column of rectification under vacuum tower 1, and Produced Liquid is squeezed into compression rectification tower 4 through force (forcing) pump (4atm).The phegma of rectification under vacuum tower 1 through the first reboiler 2 in 60-70 DEG C boil again after reflux, tower reactor Produced Liquid is that massfraction is 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 steams are by the second condenser 6 condensations, operating reflux ratio is 2.9, after overhead extraction liquid is intermediate reboiler 7 heat supplies of rectification under vacuum tower 1, return to the 15th block of column plate of rectification under vacuum tower 1, circulate.Phegma is by the trim the top of column of compression rectification tower 4; The tower reactor phegma of compression rectification tower 4 through the second reboiler 5 in 110-120 DEG C boil again after, return to compression rectification tower 4, 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 rectification under vacuum tower 1 provides the heat of 0.39mw, account for rectification under vacuum tower 1 the first reboiler 2 thermal loads 61%, fully energy-conservation.
Application example 3:
The actual plate number of rectification under vacuum tower 1 is 50, working pressure is 0.85atm, operating reflux ratio is 2.4, tower top temperature is controlled at 50 DEG C of left and right, tower reactor temperature is 61-62 DEG C, the massfraction of 25 DEG C is that the azeotropic mixture of the acetone of 20% methyl alcohol-80% is entered with the flow of 1000kg/h by the 30th block of plate, and tower top rising steam is by the first condenser 3 condensations.Phegma is by the trim the top of column of rectification under vacuum tower 1, and Produced Liquid is squeezed into pressurizing tower 4 through force (forcing) pump (3atm).The phegma of rectification under vacuum tower 1 through the first reboiler 2 in 60-70 DEG C boil again after reflux, tower reactor Produced Liquid is that massfraction is 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 steams are by the second condenser 6 condensations, operating reflux ratio is 4.2, after overhead extraction liquid is intermediate reboiler 7 heat supplies of rectification under vacuum tower 1, return to the 15th block of column plate of rectification under vacuum tower 1, circulate.Phegma is by the trim the top of column of compression rectification tower 4; The tower reactor phegma of compression rectification tower 4 through the second reboiler 5 in 110-120 DEG C boil again after, return to compression rectification tower 4, 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 rectification under vacuum tower 1 provides the heat of 0.39mw, account for rectification under vacuum tower 1 the first reboiler 2 thermal loads 71%, fully energy-conservation.
Applicant's statement, 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 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, and the selections of the equivalence replacement to the selected raw material of the present invention and the interpolation of ancillary component, concrete mode etc., within all dropping on 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 characterictic described in above-mentioned embodiment, in reconcilable situation, can combine by any suitable mode, for fear of unnecessary repetition, the present invention is to the explanation no longer separately of various possible array modes.
In addition, also can carry out arbitrary combination between various 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 (10)
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 to the rectification under vacuum tower (1) of being with intermediate reboiler (7), tower top rising steam is after the first condenser (3) condensation, phegma is by trim the top of column, and Produced Liquid is squeezed into compression rectification tower (4) through force (forcing) pump; The tower reactor phegma of rectification under vacuum 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 returns to rectification under vacuum tower (1) and circulates after being intermediate reboiler (7) heat supply of rectification under vacuum tower (1); 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).
2. energy-saving technique as claimed in claim 1, is characterized in that, the stage number of described rectification under vacuum tower (1) is 40-65 piece, and intermediate reboiler (7) is installed on the 35-45 piece column plate place of rectification under vacuum tower (1);
Preferably, the thermal load of described intermediate reboiler (7) is equivalent to the 45-71% of the first reboiler (2).
3. energy-saving technique as claimed in claim 1 or 2, is characterized in that, the tower top temperature of described rectification under vacuum tower (1) is 40-55 DEG C, and column bottom temperature is 60-70 DEG C;
Preferably, described rectification under vacuum tower (1) adopts rectification under vacuum, and its operation absolute pressure is 0.8-0.9atm.
4. the energy-saving technique as described in one of claim 1-3, is characterized in that, the operating reflux ratio of described rectification under vacuum tower (1) tower top is 1-4;
Preferably, the tower reactor phegma of described rectification under vacuum tower (1) through the first reboiler (2) in 60-70 DEG C boil again after reflux.
5. the energy-saving technique as described in one of claim 1-4, is characterized in that, the tower top temperature of described compression rectification tower (1) is 100-115 DEG C, and column bottom temperature is 110-125 DEG C;
Preferably, the stage number of described compression rectification tower (1) is 40-60 piece;
Preferably, described compression rectification tower (1) adopts compression rectification, and its working pressure is absolute pressure 2-3atm.
6. the energy-saving technique as described in one of claim 1-5, is characterized in that, the Produced Liquid of described rectification under vacuum tower (1) tower top is entered by the 15-25 piece plate of compression rectification tower (4) after force (forcing) pump is forced into 3-4atm.
7. the energy-saving technique as described in one of claim 1-6, is characterized in that, the operating reflux ratio of described compression rectification tower (4) tower top is 2-5.
8. the energy-saving technique as described in one of claim 1-7, it is characterized in that, after the overhead extraction liquid of described compression rectification tower (4) is intermediate reboiler (7) heat supply of rectification under vacuum tower (1), return to the 20-25 piece column plate of rectification under vacuum tower (1).
9. the energy-saving technique as described in one of claim 1-8, is characterized in that, the tower reactor phegma of described compression rectification tower (4) through the second reboiler (5) in 110-120 DEG C boil again after reflux.
10. the energy-saving technique as described in one of claim 1-9, is characterized in that, described technique comprises the following steps:
1) the rectification under vacuum 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 rising steam 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 squeezed into compression rectification tower (4) after force (forcing) pump is forced into 3-4atm; The tower reactor phegma of rectification under vacuum tower (1) through the first reboiler (2) in 60-70 DEG C boil again after reflux, tower reactor Produced Liquid is that massfraction is more than 99.5% methyl alcohol (9); Wherein, the stage number of described rectification under vacuum tower is 40-65 piece, and intermediate reboiler (7) is installed on the 35-45 piece column plate place of rectification under vacuum tower (1), and its thermal load is equivalent to the 45-71% of the first reboiler (2); Rectification under vacuum column overhead temperature 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 tower (1) tower top, after force (forcing) pump pressurization, is entered by the 15-25 piece 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, after overhead extraction liquid is intermediate reboiler (7) heat supply of rectification under vacuum tower (1), the 20-25 piece column plate that returns to rectification under vacuum tower (1), circulates; The tower reactor phegma of compression rectification tower (4) through the second reboiler (5) in 110-120 DEG C boil again after reflux, tower reactor Produced Liquid is more than 99.8% acetone (10) of massfraction; Wherein, the stage number of compression rectification tower (1) is 40-60 piece; Tower top temperature is 100-115 DEG C, and column bottom temperature is 110-125 DEG C, adopts compression rectification, and its working pressure is absolute pressure 2-3atm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410368125.XA CN104119202B (en) | 2014-07-29 | 2014-07-29 | A kind of energy-saving technique of variable-pressure rectification separation of methanol-acetone azeotrope |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410368125.XA CN104119202B (en) | 2014-07-29 | 2014-07-29 | A kind of energy-saving technique of variable-pressure rectification separation of methanol-acetone azeotrope |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104119202A true CN104119202A (en) | 2014-10-29 |
| CN104119202B CN104119202B (en) | 2016-01-13 |
Family
ID=51764872
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410368125.XA Active CN104119202B (en) | 2014-07-29 | 2014-07-29 | A kind of energy-saving technique of variable-pressure rectification separation of methanol-acetone azeotrope |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104119202B (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105001056A (en) * | 2015-09-06 | 2015-10-28 | 青岛科技大学 | Method for separating isobutyl alcohol and normal heptanes azeotropic system by using pressure swing distillation |
| 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 |
| CN108794310A (en) * | 2017-10-27 | 2018-11-13 | 泰州学院 | A kind of method that variable-pressure rectification isolates and purifies two kinds of acetals and raw alcohol |
| 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 |
| US10745337B2 (en) * | 2017-10-06 | 2020-08-18 | Sabic Global Technologies B.V. | Method of purifying acetone |
| CN114191837A (en) * | 2021-12-07 | 2022-03-18 | 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 |
-
2014
- 2014-07-29 CN CN201410368125.XA patent/CN104119202B/en active Active
Patent 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 |
Non-Patent Citations (4)
| Title |
|---|
| GABOR MODLA ET AL.,: "Separation of an Acetone-Methanol Mixture by Pressure-Swing Batch Distillation in a Double-Column System with and without Thermal Integration", 《IND. ENG. CHEM. RES.》, vol. 49, no. 8, 23 March 2010 (2010-03-23), pages 3785 - 3793 * |
| WILLIAM L.LUYBEN ET AL.: "Comparison of extractive distillation and pressure-swing distillation for acetone-methanol separation", 《IND.ENG.CHEM.RES.》, vol. 47, no. 8, 20 March 2008 (2008-03-20), pages 20080320 * |
| 孔鹏等: "变压精馏分离甲醇-丙酮的工艺模拟及优化", 《化工进展》, vol. 32, no. 11, 31 December 2013 (2013-12-31), pages 2583 - 2587 * |
| 李鑫钢: "《蒸馏过程节能与强化技术》", 30 September 2011, article "蒸馏过程节能与强化技术", pages: 83 * |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105001056A (en) * | 2015-09-06 | 2015-10-28 | 青岛科技大学 | Method for separating isobutyl alcohol and normal heptanes azeotropic system by using pressure swing distillation |
| 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 |
| US10745337B2 (en) * | 2017-10-06 | 2020-08-18 | Sabic Global Technologies B.V. | Method of purifying acetone |
| CN108794310A (en) * | 2017-10-27 | 2018-11-13 | 泰州学院 | A kind of method that variable-pressure rectification isolates and purifies two kinds of acetals and raw alcohol |
| 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 |
| CN114191837A (en) * | 2021-12-07 | 2022-03-18 | 大连理工大学 | Device and method for separating methanol-benzene-acetonitrile azeotrope system by extractive distillation |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104119202B (en) | 2016-01-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104119202B (en) | A kind of energy-saving technique of variable-pressure rectification separation of methanol-acetone azeotrope | |
| CN101130484B (en) | Pressure-reducing flow-reversing dual-purpose distillation method and apparatus for refining crude methanol | |
| CN105037094A (en) | Energy coupling distillation method for preparing ethyl alcohol by means of acetic acid ester hydrogenation | |
| CN106946654A (en) | A kind of separation method of biomass ethylene glycol | |
| CN106075947A (en) | Methanol four tower double-effect heat pump energy-saving equipment and method | |
| CN103288601B (en) | Cyclohexanol distillation method | |
| CN104761430A (en) | Process of varying-pressure thermal-coupling rectification separation of methylal from methanol | |
| CN102924211B (en) | Solvent composition for separating m-methyl-ethylbenzene from p-methyl-ethylbenzene by extractive distillation and extractive distillation method | |
| CN107488104B (en) | Energy-saving rectifying system and energy-saving rectifying method for purifying fusel oil | |
| CN105693468B (en) | Isopropyl acetate hydrogenization method production ethanol and the post-processing approach of isopropanol | |
| CN106242948A (en) | A kind of it is thermally integrated variable-pressure rectification separation n-butyl alcohol and the method for octane azeotropic mixture | |
| CN104140357B (en) | Take acetic acid as the method for raw material production ethanol | |
| CN103833537B (en) | Absorption and refining method for high-purity methylacrolein | |
| CN102126923B (en) | Three-tower differential pressure distillation method for preparing azeotropic ethanol | |
| CN103819304B (en) | The high mixture that boils of a kind of epoxy decolours and extracts the processing method of wherein trichloropropane | |
| CN104016833B (en) | The processing method of the integrated rectifying ethanol of three tower heat | |
| CN104693005A (en) | New process for separating methanol-propyl formate azeotrope through extractive distillation | |
| CN205099600U (en) | Fuel ethanol purification system | |
| CN101249311A (en) | Coupled barrier separation rectification technique | |
| CN103896747A (en) | Backpack type circulation production process device of high-concentration methylal | |
| CN202297496U (en) | Heating flash separation device | |
| CN203440262U (en) | Device for producing trans-1, 2-dichloroethylene with acetylene by adopting catalytic chlorination method | |
| CN107778166B (en) | A kind of method of heat pump rectification system recovery of acetic acid from low-concentration acetic acid wastewater | |
| CN205635427U (en) | Continuous negative pressure of acetonitrile distillation extraction device | |
| CN204840983U (en) | Three component batch distillation devices |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |