CN104447199B - The method that extractive distillation with salt method acetone hydrogenation reaction product prepares isopropanol - Google Patents
The method that extractive distillation with salt method acetone hydrogenation reaction product prepares isopropanol Download PDFInfo
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- CN104447199B CN104447199B CN201310418885.2A CN201310418885A CN104447199B CN 104447199 B CN104447199 B CN 104447199B CN 201310418885 A CN201310418885 A CN 201310418885A CN 104447199 B CN104447199 B CN 104447199B
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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
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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
- C07C29/82—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation by azeotropic distillation
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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
- C07C29/86—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by liquid-liquid treatment
Abstract
A kind of method that the present invention relates to extractive distillation with salt method acetone hydrogenation reaction product, separating technology mainly includes rough segmentation, extracts, is dehydrated three distillation column, and extractive distillation with salt method is mainly used in extraction tower.Acetone hydrogenation product separates light component and azeotropic mixture at crude tower tower top, is back to reactor inlet and recycles, tower reactor extraction heavy constituent, crude tower bottom side take-off isopropanol water solution.Using extractive distillation with salt method separating isopropanol aqueous solution in extraction tower, overhead extraction satisfactory isopropanol product, tower reactor is extractant aqueous solution, is sent to dehydrating tower.Dehydrating tower is used for reclaiming extractant.Use the separation method, solvent ratio can be substantially reduced, reduce energy consumption.
Description
Technical field
The present invention relates to the separating technology of a kind of preparing isopropyl alcohol by acetone hydrogenation, specifically, relate to a kind of profit
Process by extractive distillation with salt method acetone hydrogenation reaction product.
Background technology
Isopropanol is the organic solvent of a kind of function admirable, be widely used as Lac, NC Nitroncellulose, alkaloid,
The solvent of rubber and oils and fats etc.；Isopropanol still produces the important intermediate of multiple organic compound, available
Make the raw material of synthetic glycerine, isopropyl acetate etc., be also widely used as oil-fired antifreeze additive, at vapour
The aspects such as car and aviation fuel has application.Additionally, isopropanol can be additionally used in manufacture antibacterial, insecticide,
Cleaning agent and disinfection preservative etc., it can be used alone, it is also possible to and other alcohol, surfactant use,
Have in fields such as pesticide, electronics industry, medicine, coating, daily-use chemical industry and organic synthesiss and use widely
On the way, exploitation prospect is wide.
At present, the production method of industrial isopropanol mainly has propylene indirect hydration method, propylene direct hydration method.
The major defect using hydration method has: it is low that propylene converts selectivity, and equipment corrosion is serious, and catalyst life is short.
Preparing isopropyl alcohol by acetone hydrogenation uses copper or catalyst that zinc oxide is carrier or nickel-base catalyst, Ke Yixian
Write and improve selectivity, alleviate equipment corrosion, additionally, due to industrial major part acetone is all by isopropylbenzene mistake
Oxidizing process obtain, and with phenol coproduction；Due to the increase of the demand of phenol, produce substantial amounts of acetone,
Occur in that unbalanced supply-demand, frequently result in the situation of acetone overproduction.The most just make to be prepared by acetone hydrogenation
Isopropanol becomes an economically viable route.
While acetone and hydrogen react generation isopropanol in the reactor, owing to acetone or product isopropanol can
The condensation of energy, it is possible to obtain many undesirable by-products, and some in these by-products can enter one
Step reaction dehydration, generates the heavy constituent such as 4-methyl-2-amylalcohol, thus reactor outlet material be containing isopropanol,
The mixture of the components such as acetone, different methyl ether, propane, water, hydrogen, 4-methyl-2-amylalcohol.In this logistics many
Easily and water forms azeotropic mixture to plant component, uses common distillating method to be difficult to by component each in this mixture separately.
US6939995 discloses a kind of technique utilizing and containing propiophenone Hydrogenation for isopropanol, owing to containing in raw material
There is a small amount of benzene, so in hydrogenation process, acetone and benzene react with hydrogen, and reactor outlet is simultaneously
Isopropanol and the hydrogenation reaction product of benzene.The hydrogenation products of benzene mainly has hexamethylene, cyclohexene or cyclohexadiene,
Therefore this technique later separation part is mainly isopropanol and benzene and the separation process of the hydrogenation products of benzene.In order to
Obtain the isopropanol with required purity, need to comprise the complicated post processor of total of four distillation column.
EP2045232A1 discloses a kind of method that isopropanol is prepared in liquid-phase hydrogenatin, the later separation work of the method
Skill uses a next door distillation column to carry out reclaiming clean isopropanol, the side take-off isopropanol product containing a small amount of water,
Further obtain satisfactory isopropanol product by molecular sieve drying.This technique is disadvantageous in that,
In order to utilize a next door tower isolated product, the outlet material composition requirement of reactor is relatively stricter, and third
The amount of ketone and other by-products needs strict restriction, additionally, due to the azeotropic mixture of isopropanol and water is from tower top
Extraction, and this tower top material is expelled directly out, and have impact on isopropanol yield.
CN99119158.7 invents a kind of method of adding salt extraction-azeotropic distillation combined process refining isopropanol, first
First isopropanol floride aqueous solution is slightly carried through rectification and obtain the first isopropanol concentrated in tower top, then use C6 aliphatic hydrocarbon
Aqueous solution as extractant, inorganic sodium or potassium salt carries out saline extraction as salting-out separation agent to it, will
After extraction, organic facies feeding azeotropic distillation dehydrating tower refines, and the concentrated device of separating medium reclaims Posterior circle and uses,
Tower reactor can obtain the product that isopropanol content is more than 99.5%.Although this technique only separating isopropanol and water, but stream
Journey is complicated, and equipment investment is higher.
CN200810138752.9 proposes one and utilizes bulkhead azeotropy rectification column to produce anhydrous isopropyl alcohol technique side
Method, uses the entrainers such as hexamethylene to be taken out of by the water in isopropanol, the dewatering period tower reactor extraction isopropyl of next door tower
Alcohol product, side line rectifying section tower reactor extracted waste water solution.This patent of invention is also only for isopropanol water solution
Separate, and be applicable to the isopropanol floride aqueous solution that water content is bigger, additionally, tower top phase separator is not easy to control
System.
Patent 2012104078561 proposes a kind of acetone hydrogenation preparing isopropanol separating technology, in treating column
Utilize azeotropic distillation principle, by the azeotropic mixture of light component and isopropanol, diisopropyl ether etc. and water from overhead extraction,
Tower top material is sent to follow-up tower and continues dehydration, and tower reactor obtains heavy constituent, and tower body portion side take-off isopropanol produces
Product.Reactor outlet acetone, by-product and water content are not the most specially required by this technique, and flow process is simple,
Easily operated.But, due to side take-off isopropanol product, in order to control the water content in product and restructuring
Dividing content, the yield of isopropanol is under some influence.
The present invention is directed to the problems such as acetone hydrogenation product separating technology flow process is complicated, yield is low, energy consumption is high,
Proposing a kind of new extractive distillation with salt separation method, this separation method is to reactor outlet acetone, by-product
And water content does not the most specially require, isopropanol recovering rate is high, and extraction distillation solvent ratio is low, can be obvious
Reduce process energy consumption.
Summary of the invention
The present invention is directed to the situations such as acetone hydrogenation product separating technology flow process is complicated, yield is low, energy consumption is high,
Propose a kind of method utilizing extractive distillation with salt technology to separate preparation high-purity isopropanol.
Concrete technical scheme is as follows:
The acetone hydrogenation preparing isopropanol separating technology of the present invention refers to Fig. 1, comprises the following steps:
(1) rough segmentation: by acetone hydrogenation product 4) send into crude tower 1, utilize azeotropic distillation principle, will
Light component and diisopropyl ether are formed with diisopropyl ether with the azeotropic mixture of water, isopropanol with the azeotropic mixture of water, acetone
Azeotropic mixture 7, from overhead extraction, is back to reactor inlet and recycles；Tower reactor obtains heavy constituent 6, tower body side
The a large amount of isopropanol water solution of line extraction 5；
(2) extraction: the isopropanol water solution 5 of crude tower side take-off is introduced in the middle part of extraction tower 2, salt adding
Extractant 11 enter in tower from extraction tower upper end, tower top obtains isopropanol product 8, and tower reactor is rich in extraction
The aqueous solution of agent is sent to follow-up dehydrating tower 3；
(3) dehydration: extraction tower tower reactor logistics 9 enters dehydrating tower 3, the water in extractant from overhead extraction 10,
Extractant 11, from tower reactor extraction, recycles to extraction tower 2；
Rectifying column described in step (1) is common rectifying tower, and this rectifying column can be stuffing rectification column,
Can also be plate distillation column, preferred filler rectifying column, reflux ratio preferably 1～40, tower top temperature be preferred
30～110 DEG C.
Extraction tower described in step (2), described extractant goes for any solvent, and such as two
Glycol, ethylene glycol, propyl butyrate, ethylene glycol monomethyl ether, methyl phenyl ethers anisole, essence of Niobe, 3-methyl-1-butanol,
N-butyl ether, ethyl hexanoate, isobutyl isobutyrate etc..Preferably extractant has diethylene glycol, ethylene glycol, butanoic acid
Propyl ester, ethylene glycol monomethyl ether.Described salt has potassium salt, sodium salt etc..Described saline extraction tower number of theoretical plate is 10～80,
Extractant is 1～10 with the mass ratio of the material entering extraction tower.
The most described dehydrating tower Optimization Theory plate number 10～120 pieces, reflux ratio preferably 1～10, tower
The top preferred scope of temperature is 40～60 DEG C.
The acetone hydrogenation preparing isopropanol separating technology that the present invention proposes has the following characteristics that
(1), in the method for the present invention, the light component of rough segmentation tower top returns to reactor inlet, circulation
Utilize, reduce consumption of raw materials.
(2) in the method for the present invention, to the isopropanol water solution of crude tower tower body side take-off without any
The requirement such as constituent content, quality, is therefore easily controlled isopropanol yield.
(3), in the method for the present invention, extraction tower uses saline extraction method, can effectively reduce into tower molten
Agent ratio and reflux ratio, reduce energy consumption.
(4) method flow of the present invention is simple, it is easy to operation controls.
Accompanying drawing explanation
Fig. 1 is the acetone hydrogenation preparing isopropanol separating technology schematic diagram of the present invention.
Description of reference numerals:
1 crude tower；2 extraction towers；3 dehydrating towers；4 acetone hydrogenation reactor outlet logistics；5 isopropanols are water-soluble
Liquid；6 heavy constituents；7 light component and azeotropic mixtures；8 isopropanol products；9 extractant aqueous solutions；10 water；11
Extractant.
Detailed description of the invention
Below in conjunction with embodiment, further illustrate the present invention.
Embodiment:
As it is shown in figure 1, acetone hydrogenation preparing isopropanol separating technology comprises the following steps:
(1) rough segmentation: acetone hydrogenation reactor outlet logistics 4 is sent to crude tower 1, crude tower number of theoretical plate
40, reflux ratio 15, tower top temperature 40 DEG C.In this logistics, diisopropyl ether and water, acetone and water, isopropanol with
Diisopropyl ether is respectively formed azeotropic mixture 7, forms extraction from tower top with azeotropic, and the light component such as methane, hydrogen, propane is also
From overhead extraction, it is vented as fixed gas.Tower reactor production is mainly the heavy constituents 6 such as 4-methyl-2 amylalcohol,
From tower body middle and lower part side take-off isopropanol water solution 5, it is sent to extraction tower 2；Tower top makes to be cooled with circulating water,
Tower reactor uses low-pressure steam heating.
(2) extraction: solvent for use is ethylene glycol-potassium acetate aqueous solution, solvent is from the 4th piece of plate note of extraction tower
Entering, the number of theoretical plate of extraction tower is 20, and operating condition is: solvent ratio 1.4, tower top temperature 55 DEG C, backflow
Ratio 1.2.Meet the isopropanol product 8 of national standard from overhead extraction, rich in the aqueous solution 9 of extractant from tower
Still extraction, is sent to dehydrating tower 3；Tower top circulating water, tower reactor middle pressure steam heats.
(3) dehydration: solvent ethylene glycol-potassium acetate aqueous solution 9 is sent to dehydrating tower 3, and water 10 is from tower top quilt
Steaming, extractant ethylene glycol-potassium acetate 11 is sent to extraction tower from tower reactor extraction and recycles.Dehydrating tower is theoretical
Plate number 10, reflux ratio is 27, tower top temperature 44 DEG C.Tower top circulating water, tower reactor middle pressure steam heats.
Gained isopropanol product quality composition is shown in Table 1.
Table 1
| Isopropanol | Water | 4-methyl-2-amylalcohol | |
| Mass fraction % | 99.9 | 0.09 | 12ppm |
As it can be seen from table 1 isopropanol mass fraction is 99.9%, water content is 0.09%.To different in GB
The purity requirement water content of propanol is less than or equal to 0.2%, and the present embodiment can obtain complying fully with requiring product.
Isopropanol respectively in raw material and product stream stock flow analysis be shown in Table 2.
Table 2
| Raw material stream stock 4 | 8249.7kg/h |
| Product stream stock 8 | 8030.4kg/h |
Isopropanol flow from table 2 raw material and product stream stock, it can be deduced that, the response rate of isopropanol is 97.3%.
Table 3 is this flow process energy consumption analysis result.
Table 3
| Recirculated water | 1095.90 | Ton/time |
| Low-pressure steam | 6.83 | Ton/time |
| Middle pressure steam | 3.42 | Ton/time |
| Comprehensive energy consumption | 107.34 | Kg marks oil/ton product |
| 104.5 | Kg marks oil/ton raw material |
From table 3 it can be seen that extractive distillation with salt method acetone hydrogenation reaction product comprehensive energy consumption is 107.34kg
Mark oil/ton product.
Comparative example:
To flow process shown in Fig. 1, crude tower operating condition is identical with embodiment, and extractive distillation column is only with second two
Alcohol is extractant, and solvent injects from the 4th block of plate of extraction tower, and the number of theoretical plate of extraction tower is 20, operating condition
For: solvent ratio 1.6, tower top temperature 55 DEG C, reflux ratio 2.Meet the isopropanol product of national standard from tower top
Extraction, rich in the aqueous solution of extractant from tower reactor extraction, is sent to dehydrating tower；Dehydrating tower operating condition and enforcement
Identical.In the case of product purity is identical with yield, this process synthesis energy consumption is that 129.83kg marks oil/ton
Product.
Contrast result above, use the inventive method acetone hydrogenation products to prepare the technique of isopropanol,
Process energy consumption can be significantly reduced, and flow process is simple, it is easy to operate and control.
Claims (7)
1. the method that an extractive distillation with salt method acetone hydrogenation reaction product prepares isopropanol, it is characterised in that
The method comprises the following steps:
(1) rough segmentation: acetone hydrogenation product (4) is sent into crude tower (1), utilizes azeotropic distillation principle,
By light component and diisopropyl ether with the azeotropic mixture of water, acetone with the azeotropic mixture of water, isopropanol with different
The azeotropic mixture (7) that propyl ether is formed is back to reactor inlet after overhead extraction and recycles, tower
Still obtains heavy constituent (6), a large amount of isopropanol water solution of tower body side take-off (5)；
(2) extraction: the isopropanol water solution (5) of crude tower side take-off is introduced extraction tower (2) middle part,
The extractant (11) of salt adding enters in tower from extraction tower upper end, and tower top obtains isopropanol product (8),
Tower reactor is that the aqueous solution (9) rich in extractant is sent to follow-up dehydrating tower (3)；
(3) dehydration: extraction tower tower reactor logistics (9) enters dehydrating tower (3), and the water in extractant is adopted from tower top
Going out (10), extractant (11), from tower reactor extraction, recycles to extraction tower (2)；
Crude tower optional filler rectifying column described in step (1) or plate distillation column；
Wherein: in step (2), extractant is 1～1.4 with the mass ratio of the material entering extraction tower.
Extractive distillation with salt method acetone hydrogenation reaction product the most according to claim 1 prepares isopropanol
Method, it is characterised in that the crude tower described in step (1) is stuffing rectification column, reflux ratio 1～40, tower
Top temperature 30～110 DEG C.
Extractive distillation with salt method acetone hydrogenation reaction product the most according to claim 1 prepares isopropanol
Method, it is characterised in that the extractant described in step (2) be diethylene glycol, ethylene glycol, propyl butyrate,
Ethylene glycol monomethyl ether, methyl phenyl ethers anisole, essence of Niobe, 3-methyl-1-butanol, n-butyl ether, ethyl hexanoate, different
One in isobutyl isobutyrate (IBIB).
Extractive distillation with salt method acetone hydrogenation reaction product the most according to claim 1 prepares isopropanol
Method, it is characterised in that the extractant described in step (2) be diethylene glycol, ethylene glycol, propyl butyrate,
One in ethylene glycol monomethyl ether.
Extractive distillation with salt method acetone hydrogenation reaction product the most according to claim 1 prepares isopropanol
Method, it is characterised in that the salt described in step (2) is potassium salt or sodium salt.
Extractive distillation with salt method acetone hydrogenation reaction product the most according to claim 1 prepares isopropanol
Method, it is characterised in that described in step (2), extraction tower number of theoretical plate is 10～80.
Extractive distillation with salt method acetone hydrogenation reaction product the most according to claim 1 prepares isopropanol
Method, it is characterised in that described in step (3), dehydrating tower number of theoretical plate is 10～120, reflux ratio is 1～10,
Tower top temperature is 40～60 DEG C.
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| CN106242958B (en) * | 2016-07-21 | 2018-11-23 | 青岛科技大学 | A kind of method of separation of extractive distillation acetone and isopropyl ether mixture |
| CN106928027B (en) * | 2017-03-03 | 2020-10-02 | 南京师范大学 | Method for extracting methanol from acetaldehyde-methyl acetate-methanol-butanol-water mixed solution |
| CN115353441B (en) * | 2022-08-25 | 2024-01-30 | 江苏瑞恒新材料科技有限公司 | Method for improving purity of recovered methanol |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1249294A (en) * | 1999-09-17 | 2000-04-05 | 清华大学 | Process for refining isopropanol by salting extraction and azeotropy rectification |
| CN101815695A (en) * | 2007-10-04 | 2010-08-25 | 英尼奥斯石炭酸两合公司 | Process for the production of iso-propanol by liquid phase hydrogenation |
| CN102531836A (en) * | 2010-12-07 | 2012-07-04 | 淮安万邦香料工业有限公司 | Method for recycling solvent, namely isopropanol, during production of carvone |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1249294A (en) * | 1999-09-17 | 2000-04-05 | 清华大学 | Process for refining isopropanol by salting extraction and azeotropy rectification |
| CN101815695A (en) * | 2007-10-04 | 2010-08-25 | 英尼奥斯石炭酸两合公司 | Process for the production of iso-propanol by liquid phase hydrogenation |
| CN102531836A (en) * | 2010-12-07 | 2012-07-04 | 淮安万邦香料工业有限公司 | Method for recycling solvent, namely isopropanol, during production of carvone |
Non-Patent Citations (1)
| Title |
|---|
| "异丙醇-水共沸物系分离技术进展";王惠媛 等;《第九届全国化学工艺学术年会论文集》;20050430;145-150 * |
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