CN106431880B - Novel variable-pressure rectification acetone, isopropyl ether object system method - Google Patents
Novel variable-pressure rectification acetone, isopropyl ether object system method Download PDFInfo
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- CN106431880B CN106431880B CN201610817101.7A CN201610817101A CN106431880B CN 106431880 B CN106431880 B CN 106431880B CN 201610817101 A CN201610817101 A CN 201610817101A CN 106431880 B CN106431880 B CN 106431880B
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- 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
- C07C45/84—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation by azeotropic distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/34—Separation; Purification; Stabilisation; Use of additives
- C07C41/40—Separation; Purification; Stabilisation; Use of additives by change of physical state, e.g. by crystallisation
- C07C41/42—Separation; Purification; Stabilisation; Use of additives by change of physical state, e.g. by crystallisation by distillation
Abstract
A kind of novel variable-pressure rectification acetone the present invention relates to addition third substance as entrainer, the method of isopropyl ether azeotropic mixture system, this method is using the methyl acetate other than raw material as entrainer, the azeotropic composition for the azeotropic mixture that acetone is formed with isopropyl ether will not change with the change of pressure, the azeotropic composition for the azeotropic mixture that methyl acetate and acetone are formed occurs varying widely this characteristic with pressure change, first use high-pressure rectification tower, low-pressure distillation tower is used again, the acetone in the rectification area newly formed, isopropyl ether azeotropic mixture system, the third component being newly added is recycled in process by way of adding.The quality of product is in turn ensured while save the cost of the present invention；Simple process, device are reasonable；It can simultaneously obtain methanol, the tetrahydrofuran product of high-purity.
Description
[technical field]
The invention belongs to chemical separating purification arts, are related to the separation of a kind of acetone, isopropyl ether azeotropic objects system, especially
A method of novel variable-pressure rectification acetone of the methyl acetate as entrainer, isopropyl ether object system is added.
[background technique]
Acetone is industrially mainly as solvent for industries such as explosive, plastics, rubber, fiber, process hides, grease, spray paintings
In, it also can be used as the objects such as synthesis ketenes, aceticanhydride, iodoform, polyisoprene rubber, methyl methacrylate, chloroform, epoxy resin
The important source material of matter.Isopropyl ether is the good solvent of animal, plant and mineral grease, is the good solvent of paraffin and resin,
Isopropyl ether and other solvents are industrially often mixed to the dewaxing technique for being applied to paraffinic base oil product.As solvent be applied to pharmacy,
Cordite, coating and paint cleaning etc..
During chemical industry, pharmaceutical manufacturing, needs to use acetone and isopropyl ether as organic solvent, often generate acetone
It reduces environmental pollution to reduce production cost with the mixture of isopropyl ether, the mixture to acetone and isopropyl ether is needed to divide
From, but acetone and isopropyl ether form azeotropic mixture, and the azeotropism of the system has pressure non-sensibility, so can not use
Methyl acetate is added in traditional variable-pressure rectification method, carries out height press operation by double tower, can form different rectifying curves,
Original system component is separated in the rectification area newly formed.
About the separation of acetone, isopropyl ether, document report is had not yet to see.
Chinese patent CN104478712A discloses the method for a kind of separation of extractive distillation methyl acetate and methanol, with chlorination
1- hexyl -3- methylimidazole and 1-ethyl-3-methyllimidazolium bromide are extractant, are separated by two step extracting rectifyings, but
This method carries out two step extracting rectifyings, and complex process is not easy to operate.
Chinese patent CN102795957A discloses the method for a kind of separation of extractive distillation m-methyl ethylbenzene and p-methyl-ethylbenzene, with
It is extractant containing nitrogen compound, but the extractant, to m-methyl ethylbenzene and p-methyl-ethylbenzene low separation efficiency, Solvent quantity is big, energy
Consumption is high.
Chinese patent CN104119202A discloses the method for a kind of separation variable-pressure rectification separation methanol and acetone, based on heat
Integrated technique forms power-saving mechanism, but the equipment is comparatively laborious, troublesome in poeration.
Chinese patent CN105111046A discloses a kind of separation of extractive distillation isopropanol and isopropyl ether azeotropic mixture
New process, with emerging ionic liquid [emim]+[BF4]-、[bmim]+[BF4]-For extractant, but the extraction that the technique uses
Agent is expensive, is unfavorable for large-scale industrialization application.
The method that the present invention uses the novel variable-pressure rectification using methyl acetate as entrainer.Former acetone, isopropyl ether object system
There are azeotropisms, and the azeotropic mixture system is nonpressure sensitive system, can not be carried out using the method for traditional variable-pressure rectification
Separation, invention introduce methyl acetate on the basis of original system, form another pressure-sensitive azeotropic mixture with the acetone in original system
System, then double tower carries out distillation operation at various pressures, so that substance obtains in the rectification area newly formed in original system
To separate, the methyl acetate of addition is recycled in a manner of adding on a small quantity in an operating system.Disclosure is particularly well suited to acetone
Quality composition accounts for 60% or more acetone, isopropyl ether object system in original system.The invention proposes a kind of novel variable-pressure rectifications
Method solves the problems, such as that the acetone of non-sensitive property, isopropyl ether separation are difficult, and rationally, high-purity can be obtained in simple process, operation
Acetone, isopropyl ether product, save the cost while ensure that product quality.
[summary of the invention]
[technical problems to be solved]
The novel variable-pressure rectification separation third that the object of the present invention is to provide a kind of in the case where methyl acetate is participated in as entrainer
The separator of ketone, isopropyl ether mixture.
Described device variable-pressure rectification acetone isopropyl ether mixture is used it is a further object to provide a kind of
Method.
It is a further object to provide methyl acetate novel variable-pressure rectification acetone isopropyl ether mixtures herein
The middle purposes as entrainer.
[technical solution]
The present invention is achieved through the following technical solutions.
A kind of methyl acetate participated in as entrainer under novel variable-pressure rectification acetone, isopropyl ether azeotropic mixture system side
Method, it is characterised in that this method is used with the device formed as follows:
This method includes the first pressure reducing valve (V1), high-pressure tower (HT), the first condenser (C1), the first return tank (A1), the
One force (forcing) pump (P1), the first reboiler (R1), the second pressure reducing valve (V2), lower pressure column (LT), the second condenser (C2), the second reflux
Tank (A2), the second force (forcing) pump (P2), third force (forcing) pump (P3), the second reboiler (R2), wherein high-pressure tower (HT) tower top, first cold
Condenser (C1), the first return tank (A1), the first force (forcing) pump (P1), the second pressure reducing valve (V2), lower pressure column (LT) feed inlet successively with
Piping connection, high-pressure tower (HT) tower bottom, the first reboiler (R1) are successively connected with pipeline, lower pressure column (LT) tower top, the second condensation
Device (C2), the second return tank (A2), the second force (forcing) pump (P2), third force (forcing) pump (P3), high-pressure tower (HT) recycle stock feed inlet
Successively with piping connection, lower pressure column (LT) tower bottom, the second reboiler (R2) are successively with piping connection；
The novel variable-pressure rectification technique acetone, isopropyl ether system method include the following steps:
(1) acetone, isopropyl ether mixed material deliver into high-pressure tower (HT) through the first pressure reducing valve (V1) and carry out a rectifying,
High-pressure tower (HT) overhead stream is condensed by the first condenser (C1), is subsequently entered the first return tank (A1), the first reflux
Material parts flow back into high-pressure tower (HT) through the first force (forcing) pump (P1) in tank (A1), and part is then as material through the second pressure reducing valve
(V2) enter lower pressure column (LT) and carry out secondary rectifying；
(2) partial high pressure tower (HT) materials at bottom of tower enters high-pressure tower (HT) after the first reboiler (R1) boils again, and part is then
It is produced as product acetone；
(3) logistics of lower pressure column (LT) tower top is condensed by the second condenser (C2), subsequently enters the second return tank
(A2), partial material by pipeline passes back into lower pressure column (LT), fraction of stream through the second force (forcing) pump (P2) in the second return tank (A2)
High-pressure tower (HT) then, which is recycled back to, through third force (forcing) pump (P3) after entrainer ethyl acetate is added carries out rectifying again；
(4) lower pressure column (LT) tower bottom fraction of stream enters lower pressure column (LT) after the second reboiler (R2) boils again, and part is then
It is produced as isopropyl ether product.
In accordance with another preferred embodiment of the present invention, which is characterized in that 40 pieces of number of theoretical plate of high-pressure tower (HT), feedboard
Position 20~28, recycle flow into flitch position 10~15；20 pieces of number of theoretical plate of lower pressure column (LT) feeds Board position 8~12.
In accordance with another preferred embodiment of the present invention, it is characterised in that；90~110 DEG C of tower top temperature of high-pressure tower (HT),
115~130 DEG C of column bottom temperature, 15~25 DEG C of tower top temperature, 50~65 DEG C of column bottom temperature of lower pressure column (LT).
In accordance with another preferred embodiment of the present invention, it is characterised in that；High-pressure tower (HT) operating pressure is 5atm, reflux
Than being 1~2.5, lower pressure column (LT) operating pressure is 0.3atm, and reflux ratio is 1~2.
In accordance with another preferred embodiment of the present invention, which is characterized in that after separation the purity of acetone be 99.80%~
99.99%, the rate of recovery of acetone is 99.80%~99.99%, and the purity of isopropyl ether is 99.82%~99.99%, isopropyl ether
The rate of recovery be 99.82%~99.99%.
First high-pressure tower rectifying, the again atmospheric tower, it is rectificating method acetone using methyl acetate as entrainer, different
The device of propyl ether azeotropic mixture system rectifying separate acetone quality composition in former feed composition account for 60% or more acetone, isopropyl ether it is total
Boil the application in objects system.
Under acetone according to the present invention, isopropyl ether azeotropic mixture system situation, since acetone, isopropyl ether form azeotropic
Object, and the azeotropic mixture has nonpressure sensitive, i.e. and azeotropic composition is smaller with the change azeotropic composition variation pressed, this is special
Point so that it differs widely with simple binary azeotrope, separating difficulty also obviously increases, thus using simple voltage-transforming method without
Method realization efficiently separates, and does not search out suitable extractant also at present and separates to the object system, the application overcomes the prior art
Middle disadvantage, discovery methyl acetate can form new azeotropic mixture with the acetone in original system, and be pressure sensibility azeotropic mixture
System, the separation of former charging object system is carried out using double column pressure swing in the rectification area newly formed, so proposing a kind of first high pressure
Tower rectifying, again lower pressure column rectifying are using methyl acetate as entrainer acetone, the method for isopropyl ether azeotropic mixture system.
The present invention can form non-sensitive property azeotropic system using acetone and isopropyl ether, and methyl acetate and acetone can form pressure-sensitive
Property azeotropic system this characteristic, the method for introducing entrainer rectifying using two tower differential pressures, that both realizes efficiently separates.This method
It solves the problems, such as that non-sensitive property Azeotrope separation difficulty is reduced separation costs, improves product purity at this stage.
The novel double column pressure swing rectifying separator that the present invention provides a kind of simple process, is easily achieved, and using should
The method that device introduces acetone of the entrainer acetone quality composition greater than 60%, isopropyl ether azeotropic mixture system.
In accordance with another preferred embodiment of the present invention, which is characterized in that 40 pieces of number of theoretical plate of high-pressure tower (HT), feedboard
Position 20~28, recycle flow into flitch position 10~15；20 pieces of number of theoretical plate of lower pressure column (LT) feeds Board position 8~12.
The present invention is novel double column pressure swing rectifying acetone, the isopropyl ether object system, method for introducing entrainer, is specifically described
It is as follows:
Under room temperature, acetone, isopropyl ether mixed liquor 1 are first delivered to high-pressure tower (HT) via the first pressure reducing valve (V1) by the road,
Carry out a rectifying acetone, isopropyl ether, methyl acetate mixture.Liquid flow to tower bottom in tower, and partial material 3 is made by the road
For product acetone extraction, partial material then enters the first reboiler of tower bottom (R1), and upflowing vapor 2 entrance by the road is generated after heating
In high-pressure tower (HT).Overhead vapours exchanges heat in the first condenser of tower top (C1) with cooling water, all condenses, the liquid condensed out
Body is collected in the first return tank (A1), and 4 reflux return in high-pressure tower (HT) partial condensation liquid by the road, partial condensation liquid (D1)
Enter lower pressure column through the second pressure reducing valve (V2) and carries out secondary rectifying.
Logistics delivery carries out secondary rectifying to lower pressure column (LT).A part of tower top mix products 8 are used as recycle by the road
Material is recycled back to high-pressure tower (HT), and another then 6 passes back into vacuum tower (LT) by the road by force (forcing) pump P2.The low product section of tower is through
Two reboilers (R2) heating enters lower pressure column (LT) after boiling again, and part is then produced as isopropyl ether product.
In the present invention, high-pressure tower (HT) operating pressure be 5atm, 90~110 DEG C of tower top temperature, column bottom temperature 115~130
DEG C, 40 pieces of number of theoretical plate, Board position 20~28 is fed, recycle flows into flitch position 10~15, reflux ratio 1~2.5；Lower pressure column
(LT) tower operating pressure be 0.3atm, 15~25 DEG C of tower top temperature, 50~65 DEG C of column bottom temperature, 20 pieces of number of theoretical plate, feedboard
Position 8~12, reflux ratio 1~2.Pressure above numerical value indicates absolute pressure.
Acetone and isopropyl ether product can be obtained simultaneously using this method, and the purity of acetone is 99.80%~99.99%, different
The purity of propyl ether is 99.82%~99.99%；
Acetone and isopropyl ether product can be obtained simultaneously using this method, the rate of recovery of acetone is 99.80%~99.99%,
The rate of recovery of isopropyl ether is 99.82%~99.99%.
[beneficial effect]
The present invention compared with prior art, mainly have it is following the utility model has the advantages that
(1) a kind of method for separating non-sensitive property azeotropic mixture system is proposed.
(2) recycling of entrainer is simple, and entrainer is simple and easy to get, simple process, and device is reasonable.
(3) acetone, isopropyl ether product yield improve.
[Detailed description of the invention]
Fig. 1 is the Novel bunk pressure double column pressure swing rectifying schematic diagram of acetone, isopropyl ether azeotropic mixture system, wherein HT- high
Press tower；LT- lower pressure column；A1, A2- return tank；C1, C2- overhead condenser；R1, R2- tower bottom reboiler；P1, P2, P3- pressurization
Pump；V1, V2- pressure reducing valve；Digital representation pipeline.
[specific embodiment]
Embodiment 1
Feed rate is 1000kg/h, and 30 DEG C of temperature, pressure 6atm (absolute pressure), quality forms: acetone 60%, isopropyl ether
40%.40 pieces of number of theoretical plate of high-pressure tower (HT) is fed at the 20th piece, and circulation logistics is returned in the 11st piece of plate charging of high-pressure tower (HT)
For stream than being 1, tower top temperature is 90 DEG C, and column bottom temperature is 115 DEG C.20 pieces of number of theoretical plate of lower pressure column (LT) feeds at the 12nd piece, returns
For stream than being 1, tower top temperature is 15 DEG C, and column bottom temperature is 55 DEG C.
After separation: product acetone quality purity is up to 99.8%；Isopropyl ether product quality purity is up to 99.82%；The receipts of acetone
Rate is up to 99.89%；The yield of isopropyl ether is up to 99.85%.
Embodiment 2:
Feed rate is 1000kg/h, and 30 DEG C of temperature, pressure 1atm (absolute pressure), quality forms: acetone 70%, isopropyl ether
30%.40 pieces of number of theoretical plate of high-pressure tower (HT) is fed at the 28th piece, and circulation logistics is returned in the 13rd piece of plate charging of high-pressure tower (HT)
For stream than being 1.5, tower top temperature is 96 DEG C, and column bottom temperature is 125 DEG C.20 pieces of number of theoretical plate of lower pressure column (LT) is fed at the 8th piece,
Reflux ratio is 1.5, and tower top temperature is 20 DEG C, and column bottom temperature is 50 DEG C.
After separation: product acetone quality purity is up to 99.99%；Isopropyl ether product quality purity is up to 99.99%；The receipts of acetone
Rate is up to 99.9%；The yield of isopropyl ether is up to 99.92%.
Embodiment 3:
Feed rate is 1000kg/h, and 30 DEG C of temperature, pressure 1atm (absolute pressure), quality forms: acetone 85%, isopropyl ether
15%.40 pieces of number of theoretical plate of high-pressure tower (HT) is fed at the 26th piece, and circulation logistics is returned in the 10th piece of plate charging of high-pressure tower (HT)
For stream than being 2.5, tower top temperature is 110 DEG C, and column bottom temperature is 130 DEG C.20 pieces of number of theoretical plate of lower pressure column (LT), the 10th piece into
Material, reflux ratio 1, tower top temperature are 25 DEG C, and column bottom temperature is 60 DEG C.
After separation: product acetone quality purity is up to 99.92%；Isopropyl ether product quality purity is up to 99.9%；The receipts of acetone
Rate is up to 99.8%；The yield of isopropyl ether is up to 99.82%.
Embodiment 4:
Feed rate is 1000kg/h, and 30 DEG C of temperature, pressure 1atm (absolute pressure), quality forms: acetone 95%, isopropyl ether
5%.40 pieces of number of theoretical plate of high-pressure tower (HT) is fed at the 25th piece, and circulation logistics is in the 15th piece of plate charging of high-pressure tower (HT), reflux
Than being 1.9, tower top temperature is 98 DEG C, and column bottom temperature is 125 DEG C.20 pieces of number of theoretical plate of lower pressure column (LT) feeds at the 11st piece, returns
For stream than being 2, tower top temperature is 19 DEG C, and column bottom temperature is 65 DEG C.
After separation: product acetone quality purity is up to 99.95%；Isopropyl ether product quality purity is up to 99.93%；The receipts of acetone
Rate is up to 99.99%；The yield of isopropyl ether is up to 99.99%.
Claims (6)
1. the method for variable-pressure rectification acetone, isopropyl ether object system, it is characterised in that required device includes:
This method includes pressure reducing valve (V1), high-pressure tower (HT), condenser (C1), return tank (A1), force (forcing) pump (P1), reboiler
(R1), pressure reducing valve (V2), lower pressure column (LT), condenser (C2), return tank (A2), force (forcing) pump (P2), force (forcing) pump (P3), reboiler
(R2), wherein high pressure column overhead, condenser (C1), return tank (A1), force (forcing) pump (P1), pressure reducing valve (V2), lower pressure column feed inlet
Successively with piping connection, high-pressure tower (HT) tower bottom, reboiler (R1) are successively connected with pipeline, low pressure column overhead, condenser (C2),
Return tank (A2), force (forcing) pump (P2), force (forcing) pump (P3), high-pressure tower recycle stock feed inlet are successively with piping connection, lower pressure column tower
Bottom, reboiler (R2) are successively with piping connection；
The variable-pressure rectification technique acetone, isopropyl ether system method include the following steps:
(1) acetone, isopropyl ether mixed material deliver into high-pressure tower (HT) through pressure reducing valve (V1) and carry out a rectifying, high-pressure tower
(HT) overhead stream is condensed by condenser (C1), is subsequently entered return tank (A1), and material parts pass through in return tank (A1)
Force (forcing) pump (P1) flows back into high-pressure tower (HT), and it is secondary that part then enters lower pressure column (LT) progress through pressure reducing valve (V2) as material
Rectifying；
(2) partial high pressure tower (HT) materials at bottom of tower enters high-pressure tower (HT) after reboiler (R1) boils again, and part is then used as acetone
Product extraction；
(3) logistics of lower pressure column (LT) tower top is condensed by condenser (C2), is subsequently entered return tank (A2), in return tank
(A2) partial material is passed back into lower pressure column (LT) by the pressurized pump (P2) of pipeline, and fraction of stream then passes through entrainer ethyl acetate benefit
High-pressure tower (HT), which is recycled back to, through force (forcing) pump (P3) after adding carries out rectifying again；
(4) lower pressure column (LT) tower bottom fraction of stream enters lower pressure column (LT) after reboiler (R2) boils again, and part is then used as isopropyl
Ether product extraction.
2. the method for variable-pressure rectification acetone according to claim 1, isopropyl ether object system, it is characterised in that the height
The operating pressure for pressing tower is 5atm, and the operating pressure of lower pressure column is 0.3atm, and the theoretical cam curve of high-pressure tower is 40, acetone and different
The feed entrance point of ether mixture material is 20~28, and the feed entrance point of recycle stock is 10~15, and reflux ratio is 1~2.5, tower top
Temperature is 90~110 DEG C, and column bottom temperature is 115~130 DEG C；The theoretical cam curve of lower pressure column is 20, feed entrance point 8~12,
Reflux ratio is 1~2, and tower top temperature is at 15~25 DEG C, and column bottom temperature is at 50~65 DEG C.
3. the method for variable-pressure rectification acetone according to claim 1, isopropyl ether object system, methyl acetate is in transformation essence
It evaporates acetone, use as entrainer in isopropyl ether technique.
4. the method for variable-pressure rectification acetone according to claim 1, isopropyl ether object system, it is characterised in that required
The mass ratio of the third substance and acetone, isopropyl ether mixed material is 0.2~0.5.
5. variable-pressure rectification acetone according to claim 1, isopropyl ether object system method in rectifying acetone quality
Acetone of the composition greater than 60%, the application in isopropyl ether azeotropic mixture system.
6. the method for variable-pressure rectification acetone according to claim 1, isopropyl ether object system, it is characterised in that third after separation
The purity of ketone is 99.80% ~ 99.99%, and the rate of recovery of acetone is 99.80% ~ 99.99%, the purity of isopropyl ether is 99.82% ~
99.99%, the rate of recovery of isopropyl ether is 99.82% ~ 99.99%.
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| CN106966866B (en) * | 2017-04-21 | 2020-07-07 | 青岛科技大学 | Method for separating butanone-isopropanol-ethanol azeotrope through three-tower 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 |
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|---|---|---|---|---|
| US4459179A (en) * | 1983-01-06 | 1984-07-10 | Lloyd Berg | Separation of isopropyl ether from acetone by extractive distillation |
| US4551207A (en) * | 1983-01-06 | 1985-11-05 | Lloyd Berg | Separation of isopropyl ether from acetone by extractive distillation |
| CN103394209A (en) * | 2013-07-22 | 2013-11-20 | 青岛科技大学 | Method for rectifying and separating ethanol and tetrahydrofuran azeotrope system by low-pressure tower and high-pressure tower |
| CN104151137A (en) * | 2014-08-08 | 2014-11-19 | 洪泽县恒泰科工贸有限公司 | High pressure and normal pressure double-tower rectification method used for separating n-butanol and MIBK azeotrope |
| CN104177224A (en) * | 2014-08-08 | 2014-12-03 | 洪泽县恒泰科工贸有限公司 | Method for rectifying and separating normal butanol and MIBK (methyl isobutyl ketone) azeotrope system by virtue of decompression and atmospheric towers |
-
2016
- 2016-09-12 CN CN201610817101.7A patent/CN106431880B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4459179A (en) * | 1983-01-06 | 1984-07-10 | Lloyd Berg | Separation of isopropyl ether from acetone by extractive distillation |
| US4551207A (en) * | 1983-01-06 | 1985-11-05 | Lloyd Berg | Separation of isopropyl ether from acetone by extractive distillation |
| CN103394209A (en) * | 2013-07-22 | 2013-11-20 | 青岛科技大学 | Method for rectifying and separating ethanol and tetrahydrofuran azeotrope system by low-pressure tower and high-pressure tower |
| CN104151137A (en) * | 2014-08-08 | 2014-11-19 | 洪泽县恒泰科工贸有限公司 | High pressure and normal pressure double-tower rectification method used for separating n-butanol and MIBK azeotrope |
| CN104177224A (en) * | 2014-08-08 | 2014-12-03 | 洪泽县恒泰科工贸有限公司 | Method for rectifying and separating normal butanol and MIBK (methyl isobutyl ketone) azeotrope system by virtue of decompression and atmospheric towers |
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