CN106748650A - A kind of apparatus and method of separating isopropanol and diisopropyl ether mixture - Google Patents
A kind of apparatus and method of separating isopropanol and diisopropyl ether mixture Download PDFInfo
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- CN106748650A CN106748650A CN201611186128.7A CN201611186128A CN106748650A CN 106748650 A CN106748650 A CN 106748650A CN 201611186128 A CN201611186128 A CN 201611186128A CN 106748650 A CN106748650 A CN 106748650A
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- fluid passage
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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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
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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
- 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
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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
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- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of separating isopropanol and the apparatus and method of diisopropyl ether mixture, belong to technical field of rectification.After being heated up using compressor boost by the azeotropic vaporization material of low pressure overhead extraction, there is provided to lower pressure column tower reactor and boil institute's calorific requirement again, the condensation of lower pressure column azeotropic vaporization itself is completed simultaneously, after equally being heated up using compressor boost by the azeotropic vaporization material of high pressure overhead extraction, there is provided to high-pressure tower tower reactor and boil institute's calorific requirement again, while completing the condensation of high-pressure tower azeotropic vaporization itself.Realize that tower top material is condensed using cooling water relative to tradition, and the scheme that tower reactor is heated is realized using hot public work.The preheating of raw material and intermediate product rises high-temperature using the waste heat of high and low pressure tower materials at bottom of tower in the present invention, so as to realize that the heat in system is matched, the input of engineering is shared without extraneous heat, the expense of the energy production that compressor is consumed is far below traditional cooling water and hot public work, produces good economic benefit.
Description
Technical field
The present invention relates to rectifying isolation technics, the device of more particularly to a kind of separating isopropanol-diisopropyl ether mixture and
Technique.
Background technology
Isopropanol (IPA) is one of petrochemicals of production earliest in the world mainly for the production of acetone and is used as
Solvent, isopropanol also serves as the raw material of the products such as synthetic glycerine, isopropyl acetate, isopropyl amine salt, nitrous acid diisopropylamine,
Isopropanol is also widely used as oil-fired antifreeze additive.Additionally, isopropanol can be additionally used in manufacture bactericide, insecticide, disappear
Toxic agent and preservative etc..
The production of isopropanol, using acid or cation exchange resin catalyst, is given birth to propylene and water as raw material through hydration
Into isopropanol.During production isopropanol, a large amount of accessory substances containing diisopropyl ether have been obtained.It is isopropanol under normal pressure, two different
Propyl ether forms binary azeotrope, and azeotropic temperature is 66.2 DEG C, and azeotropic composition is isopropanol 16.3%, diisopropyl ether 83.7%
(wt%) minimum azeotropic mixture also, and between two components is formed, high purity product is cannot get with conventional rectification method.
Chinese patent CN105906488 provides a kind of refined purification of accessory substance diisopropyl ether in alcohol production for isopropyl
The method for filling system, using liquid-liquid extraction, the method for azeotropic distillation, carries out four tower continuous operations, is obtained from the refined tower reactor of diisopropyl ether
To diisopropyl ether.Isopropanol in the technique through being obtained by extraction is separated with the mixture of water and is not directed to.The technique uses four
Tower separation process, equipment investment and operating cost are higher.
Chinese patent CN101792367 provides batch extracting rectified point of a kind of isopropanol-diisopropyl ether-aqueous mixtures
From method.The method using including extractive distillation column, the heating kettle of extractive distillation column tower reactor, extractive distillation column overhead condenser and
The rectifier unit that head tank and product receiving tank are constituted, batch fractionating operation separating isopropanol-diisopropyl ether-aqueous mixtures, though
Single-tower operation is so used, operation is flexible, and cost of equipment input is small, but due to needing plus solvent, the quality to product has shadow
Ring.
Variable-pressure rectification method is the characteristics of producing overgauge to Raoult's law using isopropanol-diisopropyl ether system, is passed through
Conversion rectifying column operating pressure, so as to change azeotropic temperature and the azeotropic composition of isopropanol-diisopropyl ether system, is achieved in
The separation of product.Variable-pressure rectification has need not add other materials, it is to avoid solvent in extracting rectifying, azeotropic distillation technique
Reclaim and product purity problem, process is simple.Wang Yu rosy clouds et al. exist《Variable-pressure rectification separating isopropanol-diisopropyl ether technique mould
Intend》, Luo haotao etc. exist《Comparison of Pressure-Swing Distillation and Extractive
Distillation Methods for Isopropyl Alcohol/Diisopropyl Ether Separation》In it is right
Variable-pressure rectification separating isopropanol-diisopropyl ether system is studied in detail, but variable-pressure rectification need to be different to isopropanol-two
Propyl ether system carries out multiple distillation operation, and steam and cooling water consumption are all very big in production, so as to increased technical process energy
Consumption and production cost, these shortcomings greatly reduce the competitiveness of variable-pressure rectification method separating isopropanol-diisopropyl ether system.
The content of the invention
For existing variable-pressure rectification separating isopropanol-big shortcoming of diisopropyl ether system energy consumption, the invention provides one
Plant from recuperation of heat variable-pressure rectification separating isopropanol-diisopropyl ether system device and technique.Ensuring that isopropanol-diisopropyl ether is high
While effect is separated, effectively lower the energy consumption of isopropanol-diisopropyl ether separating technology.
It is that, up to this purpose, the present invention uses following technical scheme：
A kind of device of separating isopropanol and diisopropyl ether mixture, including：First Heat Exchanger, the First Heat Exchanger tool
There is spaced first fluid passage and second fluid passage；
Second heat exchanger, second heat exchanger has spaced the 3rd fluid passage and the 4th fluid passage, the
The output end of one fluid passage is connected with the input of the 3rd fluid passage, output end and first cooler of the 4th fluid passage
Input connection；
3rd heat exchanger, the 3rd heat exchanger has spaced the 5th fluid passage and the 6th fluid passage；The
The output end of three fluid passages is connected with the input of the 5th fluid passage；
4th heat exchanger, the 4th heat exchanger has spaced the 7th fluid passage and the 8th fluid passage；The
Seven fluid passage inputs are connected with the outlet of low pressure tower reactor, and the 7th fluid passage output end is connected with low pressure tower reactor, the 8th fluid
The input of passage is connected with the output end of the first compressor, and the 8th fluid passage has the first output end and the second output
End；
5th heat exchanger, the 5th heat exchanger has spaced the 9th fluid passage and the tenth fluid passage；The
Nine fluid passage inputs are connected with the output end of the 8th fluid passage；
6th heat exchanger, the 6th heat exchanger has spaced the 11st fluid passage and the 12nd fluid logical
Road, the 11st fluid path input is connected with the output end of the 9th fluid passage；
7th heat exchanger, the 7th heat exchanger has spaced the 13rd fluid passage and the 14th fluid logical
Road, the 13rd fluid passage input is connected with the outlet of high pressure tower reactor, and the 13rd fluid passage output end is connected with high pressure tower reactor,
The input of the 14th fluid passage is connected with the output end of the second compressor, and the 14th fluid passage has the first output end
With the second output end, the first output end of the 14th fluid passage is connected with the input of the 6th passage, the second output end and the
The input of ten passages is connected；
Lower pressure column, the lower pressure column has first and second charging aperture, and low pressure tower top outlet and low pressure tower reactor are exported, and described the
One charging aperture is connected with the output end of the 5th fluid passage, the output of the second charging aperture and the tenth fluid passage
End is connected, and the outlet of low pressure tower reactor is connected with second fluid path input；
First compressor, the input of first compressor is connected with low pressure tower top outlet；
High-pressure tower, the high-pressure tower has the outlet of the 3rd charging aperture, high pressure tower top outlet and high pressure tower reactor；Described 3rd enters
Material mouth is connected with the output end of the 11st fluid passage, and the outlet of high pressure tower reactor is connected with the 13rd fluid passage input；
Second compressor, the input of second compressor is connected with high pressure tower top outlet.
A kind of device of separating isopropanol and diisopropyl ether mixture, also including the first cooler, the first time cooling
Device is located between the output end of the 4th fluid passage and the overhead reflux of lower pressure column；Second cooler, second cooler
Output end with second fluid passage is connected；The output end of the 3rd cooler, the third time cooler and the 6th fluid passage
It is connected.
The number of theoretical plate of the lower pressure column is 15~25 pieces, and first charging aperture is located at the 12nd block of plate, second charging aperture position
At the 10th block of plate, operating pressure is 0.09MPa~0.1MPa, and 64~67 DEG C of tower top temperature, bottom temperature is 82~86 DEG C.
The number of theoretical plate of the high-pressure tower is 25~35 pieces, and the 3rd charging aperture is located at the 19th block of plate, and operating pressure is
0.35MPa~0.45MPa, 108~117 DEG C of tower top temperature, bottom temperature is 118~127 DEG C.
The temperature difference >=5 DEG C of each fluid passage.The compression ratio 2.5~3.5 of the first compressor, the pressure of the second compressor
Contracting is than being 1.5~2.5
According to device separating isopropanol and the diisopropyl ether mixing of a kind of above-mentioned separating isopropanol and diisopropyl ether mixture
The method of thing, is carried out as steps described below：
Logistics containing isopropanol-diisopropyl ether mixture is via First Heat Exchanger, the second heat exchanger, the 3rd heat exchanger
After three preheatings, entered from lower pressure column first charging aperture with saturation liquid phase, rectifying, lower pressure column tower kettle product are carried out in lower pressure column
It is isopropanol material, isopropanol material is produced after being cooled down through First Heat Exchanger, the second cooler as product.The tower top of lower pressure column
It is lower pressure column into the 4th heat exchanger as lower pressure column tower reactor thermal source after gaseous phase materials heat up through the supercharging of the first compressor compresses
Boiling hot amount again is provided, is then divided into two strands, second heat exchanger of stock-traders' know-how is exchanged heat with raw material, then flowed back after the first cooler
Lower pressure column is returned, through the 3rd charging aperture into carrying out rectifying in high-pressure tower after the heat exchanger of another stock-traders' know-how the 5th, the preheating of the 6th heat exchanger
Separate, high-pressure tower tower kettle product is diisopropyl ether material, diisopropyl ether material is made after being cooled down through the 3rd heat exchanger, the 3rd cooler
For product is produced.After the top gaseous phase material of high-pressure tower heats up through the supercharging of the second compressor compresses, as high-pressure tower tower reactor thermal source,
Into the 7th heat exchanger, for high-pressure tower provides again boiling hot amount, then it is divided into two strands, after the cooling of the heat exchanger of a stock-traders' know-how the 6th, backflow
Lower pressure column is returned, lower pressure column is returned to from second charging aperture after the cooling of the heat exchanger of another stock-traders' know-how the 5th.
In above-mentioned steps, isopropanol and diisopropyl ether mixture are separated into lower pressure column, isopropanol and diisopropyl ether
Azeotropic mixture as light component from lower pressure column overhead extraction, tower reactor obtains the isopropanol finished product of high-purity, is adopted from low pressure column overhead
The isopropanol and the azeotropic mixture of diisopropyl ether for going out are separated into high-pressure tower, and the change of the operating pressure of high-pressure tower makes isopropanol
Changed with the azeotropic of diisopropyl ether composition, new azeotropic state is reached again, isopropanol now and diisopropyl ether are total to
Used as light component from high-pressure tower overhead extraction, high-pressure tower tower reactor obtains the diisopropyl ether finished product of high-purity to boiling thing.
Compared with prior art, the present invention has advantages below：
The separating technology of isopropanol of the present invention and diisopropyl ether mixture, will be steamed by the azeotropic of low pressure overhead extraction
After vapour material is heated up using compressor boost, provided to lower pressure column tower reactor and boil institute's calorific requirement again, while complete lower pressure column azeotropic steaming
Vapour itself is condensed, and after equally being heated up using compressor boost by the azeotropic vaporization material of high pressure overhead extraction, gives high-pressure tower tower
Kettle is provided and boils institute's calorific requirement again, while completing the condensation of high-pressure tower azeotropic vaporization itself.Relative to tradition tower is realized using cooling water
Top material condensation, and the scheme that tower reactor is heated is realized using hot public work, the present invention is realized from recuperation of heat by compressor
Utilize.In addition conventional raw material preheating typically uses hot public work direct heating, can so cause the degradation of energy, the present invention
The preheating of middle raw material and intermediate product rises high-temperature using the waste heat of high and low pressure tower materials at bottom of tower, so as to realize the heat in system
It is flux matched, the input of engineering is shared without extraneous heat, the expense of the energy production that compressor is consumed is far below tradition
Cooling water and hot public work, produce good economic benefit.
Brief description of the drawings
Fig. 1 is the flow chart of separating isopropanol of the invention and diisopropyl ether mixture
Label is as follows in figure：1- lower pressure columns, 2- high-pressure towers, 3- First Heat Exchangers, the heat exchangers of 4- second, 5- the 3rd
Heat exchanger, the heat exchangers of 6- the 4th, the heat exchangers of 7- the 5th, the heat exchangers of 8- the 6th, the heat exchangers of 9- the 7th, 10- first compresses
Machine, the compressors of 11- second, the coolers of 12- first, the coolers of 13- second, the coolers of 14- the 3rd.
Specific embodiment
The equipment of a kind of separating isopropanol and diisopropyl ether mixture, wherein First Heat Exchanger 3 have spaced the
One fluid passage and second fluid passage, the wherein intake pipeline of first fluid passage are material feeding tube 15；
Second heat exchanger 4 has spaced the 3rd fluid passage and the 4th fluid passage, first fluid passage it is defeated
Go out end to be connected with the input of the 3rd fluid passage, connecting pipeline is 16, output end and first cooler of the 4th fluid passage
Input connection, connecting pipeline is 19；
3rd heat exchanger 5 has spaced the 5th fluid passage and the 6th fluid passage；3rd fluid passage it is defeated
Go out end to be connected with the input of the 5th fluid passage, connecting pipeline is 17；
4th heat exchanger 6 has spaced the 7th fluid passage and the 8th fluid passage；7th fluid passage is input into
End with low pressure tower reactor outlet be connected, the 7th fluid passage output end is connected with low pressure tower reactor, the input of the 8th fluid passage and
The output end of the first compressor is connected, and connecting pipeline is 22, and the 8th fluid passage has the first output end and the second output end,
First output end of the 8th fluid passage is connected with the input of fourth lane, and connecting pipeline is 24；
5th heat exchanger 7 has spaced the 9th fluid passage and the tenth fluid passage；9th fluid passage is input into
End is connected with the second output end of the 8th fluid passage, and connecting pipeline is 30；
6th heat exchanger 8 has spaced the 11st fluid passage and the 12nd fluid passage, and the 11st fluid leads to
Road input is connected with the output end of the 9th fluid passage, and connecting pipeline is 31；
7th heat exchanger 9 has spaced the 13rd fluid passage and the 14th fluid passage, and the 13rd fluid leads to
Road input is connected with the outlet of the tower reactor of high-pressure tower 2, and the 13rd fluid passage output end is connected with the tower reactor of high-pressure tower 2, the 14th stream
The input of body passage is connected with the output end of the second compressor 11, and connecting pipeline is 27, and the 14th fluid passage has the
One output end and the second output end, the first output end of the 14th fluid passage are connected with the input of the 6th passage, connecting tube
Line is that the second output end of the 40, the 14th fluid passage is connected with the input of the tenth passage, and connecting pipeline is 36；
Lower pressure column 1 has first and second charging aperture low pressure tower top outlet and the outlet of low pressure tower reactor, first charging aperture and the 5th liquid
The output end of body passage is connected, and connecting pipeline is 18, and second charging aperture is connected with the output end of the tenth fluid passage, connecting pipeline
It is 37, the outlet of low pressure tower reactor is connected with second fluid path input, and connecting pipeline is 25；The input of the first compressor 10 with
The ejection mouth of lower pressure column 1 is connected, and connecting pipeline is 21；There is high-pressure tower 2 the 3rd charging aperture, high pressure tower top outlet and high pressure tower reactor to go out
Mouthful；3rd charging aperture is connected with the output end of the 11st fluid passage, and connecting pipeline is 32, and high pressure tower reactor is exported and the 6th fluid
Path input is connected, and connecting pipeline is 40；The input of the second compressor 11 is connected with high pressure tower top outlet, and connecting pipeline is
33。
First cooler 12 is located between the 4th fluid passage and the tower top of lower pressure column, and connecting pipeline is 19, fluid cooling
Lower pressure column 1 is back to by connecting pipeline 20.Second cooler 13 is connected with the output end of second fluid passage, and connecting pipeline is
26, product isopropanol is produced through connecting pipeline S27；3rd cooler 14 is connected with the output end of the 6th fluid passage, connecting tube
Line is 28, and product diisopropyl ether is produced through connecting pipeline 29.
The number of theoretical plate of lower pressure column 1 is 15~25 pieces, and first charging aperture is located at the 12nd~15 block of plate, second charging aperture position
At the 10th~12 block of plate, operating pressure is 0.09MPa~0.1MPa, and 64~67 DEG C of tower top temperature, bottom temperature is 82~86
℃。
The number of theoretical plate of high-pressure tower 2 is 25~35 pieces, and the 3rd charging aperture is located at the 19th~22 block of plate, and operating pressure is
0.35MPa~0.45MPa, 108~117 DEG C of tower top temperature, bottom temperature is 118~127 DEG C.
The temperature difference >=5 DEG C of each fluid passage.The compression ratio 2.5~3.5 of the first compressor 10, the second compressor 11
Compression ratio K1 be 1.5~2.5
The technique of a kind of separating isopropanol-diisopropyl ether mixture implemented according to the present invention, according to any of the above-described institute
The equipment of the separating isopropanol stated-diisopropyl ether mixture is carried out, and is comprised the following steps：
Through 15 by First Heat Exchanger 3, the second heat exchanger 4, the 3rd changes raw material containing isopropanol-diisopropyl ether mixture
After the preheating of hot device 5 three times, with saturation liquid phase through 18 from lower pressure column first charging aperture into lower pressure column 1 in carry out rectifying, lower pressure column 1
Tower kettle product is isopropanol material, and isopropanol material is adopted through 27 after being cooled down through First Heat Exchanger 3, the second cooler 13 as product
Go out.After the top gaseous phase material of lower pressure column 1 heats up through the compression supercharging of the first compressor 10, as the tower reactor thermal source of lower pressure column 1, enter
4th heat exchanger 6 is exchanged heat with materials at bottom of tower, is that lower pressure column 1 provides again boiling hot amount, is then divided into two strands, and a stock-traders' know-how second is changed
After hot device 4 and raw material are exchanged heat, then lower pressure column 1 is back to after the first cooler 12, the heat exchanger 7 of another stock-traders' know-how the 5th, the
Six heat exchanger 8 through the 3rd charging aperture into rectifying separation, the tower kettle product of high-pressure tower 2 is carried out in high-pressure tower 2 is diisopropyl after preheating
Ether material, diisopropyl ether material is produced after being cooled down through the 3rd heat exchanger 5, the 3rd cooler 14 as product.The tower top of high-pressure tower 2
After gaseous phase materials heat up through the compression boosting of the second compressor 11, as the tower reactor thermal source of high-pressure tower 2, into the 7th heat exchanger 9 and height
The pressure materials at bottom of tower of tower 2 is exchanged heat, and is that high-pressure tower 2 provides again boiling hot amount, is then divided into two strands, and the heat exchanger 8 of a stock-traders' know-how the 6th is cold
But after, lower pressure column 1 is back to, another the 5th heat exchanger of stock-traders' know-how 7 returns to lower pressure column after cooling down from second charging aperture.
In the present invention, isopropanol and diisopropyl ether mixture are separated into lower pressure column 1, isopropanol and diisopropyl ether
Used as gently constituting from the overhead extraction of lower pressure column 1, tower reactor obtains the isopropanol finished product of high-purity to azeotropic mixture, is adopted from the tower top of lower pressure column 1
The isopropanol and the azeotropic mixture of diisopropyl ether for going out are separated into high-pressure tower 2, and the change of the operating pressure of high-pressure tower makes isopropyl
The azeotropic composition of alcohol and diisopropyl ether is changed, and new azeotropic state is reached again, isopropanol now and diisopropyl ether
Azeotropic mixture obtains the diisopropyl ether finished product of high-purity as light component from the overhead extraction of high-pressure tower 2, the tower reactor of high-pressure tower 2.
From heat recovery section refer to after being compressed using compressor to lower pressure column and high-pressure tower overhead vapours in the present invention
Supercharging is heated up, and lower pressure column and high-pressure tower tower reactor heat supply are then given respectively, while reclaimed to its waste heat, use it for raw material and
The preheating of intermediate product, so as to realize that the heat in system is matched, the input of engineering is shared without extraneous heat.
Embodiment 1
Filling 500Y type structured packings in the tower of lower pressure column 1,19 pieces of the number of plates, first charging aperture is the 12nd block of plate, and second enters
Material mouth is the 10th block of plate, and operating pressure is 0.1MPa, and tower top temperature is 66 DEG C, and bottom temperature is 84.7 DEG C, the pressure of compressor 10
Contracting is than being 2.6.Filling 500Y type structured packings in the tower of high-pressure tower 2,27 pieces of the number of plates, the 3rd charging aperture is the 19th block of plate, operation
Pressure is 0.4MPa, and tower top temperature is 110.8 DEG C, and bottom temperature is 120.1 DEG C, and the compression ratio of compressor 11 is 1.8.
Material liquid inlet amount containing isopropanol-diisopropyl ether mixture is 7061kg/h, and the composition of material liquid is：It is different
Propyl alcohol 63.8%, diisopropyl ether 36.2% (mass percent).
Material liquid containing isopropanol-diisopropyl ether mixture is through 15 by First Heat Exchanger 3, the second heat exchanger 4, the 3rd
After the preheating of heat exchanger 5 three times, with saturation liquid phase through 18 from the first charging aperture of lower pressure column 1 into lower pressure column 1 in carry out rectifying, tower reactor
The isopropanol product of 4530kg/h is produced, the wherein mass fraction of isopropanol is 99.5%.The top gaseous phase material warp of lower pressure column 1
After the compression boosting of first compressor 10 heats up, as the tower reactor thermal source of lower pressure column 1, carried out into the 4th heat exchanger 6 and materials at bottom of tower
Heat exchange, is that lower pressure column 1 provides again boiling hot amount, is then divided into two strands, after second heat exchanger of stock-traders' know-how 4 is exchanged heat with raw material, then
It is back to lower pressure column 1 after the first cooler 12, another plume amount is 5624kg/h, constitutes and be：Isopropanol 14.9%, diisopropyl
Ether 85.9% (mass percent).Enter in high-pressure tower 2 through the 3rd charging aperture after being preheated through the 5th heat exchanger 7, the 6th heat exchanger 8
Rectifying separation is carried out, the tower reactor of high-pressure tower 2 produces the diisopropyl ether product of 2531kg/h, and the mass fraction of wherein diisopropyl ether is
99.9%, a portion diisopropyl ether material returns to the bottom of high-pressure tower 2 after being exchanged heat through the 7th heat exchanger 9.Another part two
Isopropyl ether material is produced after being cooled down through the 3rd heat exchanger 5, the 3rd cooler 14 as product.The top gaseous phase material of high-pressure tower 2
After being heated up through the compression boosting of the second compressor 11, do as the tower reactor thermal source of high-pressure tower 2, into the 7th heat exchanger 9 and the tower of high-pressure tower 2
Substrate material is exchanged heat, and is that high-pressure tower 2 provides again boiling hot amount, is then divided into two strands, after the 6th heat exchanger of stock-traders' know-how 8 is cooled down, and is returned
Flow back to lower pressure column 1, another plume amount is 3093kg/h, constitute and be：Isopropanol 27.0%, (the quality percentage of diisopropyl ether 73.0%
Number).After being cooled down through the 5th heat exchanger 7 lower pressure column is returned to from second charging aperture.During stable operation, high-pressure tower and lower pressure column tower reactor institute
Calorific requirement is provided after being heated up by the compressed supercharging of overhead vapours, and waste heat is preheated to raw material and intermediate product, whole flow process
In, it is not necessary to external heat public work, only the wasted work 173.4kW of compressor 10, the wasted work 62.2kW of compressor 11, while three condensations
Thermic load -76.0kW needed for device.
Embodiment 2
Filling 500Y type structured packings in the tower of lower pressure column 1,24 pieces of the number of plates, first charging aperture is the 15th block of plate, and second enters
Material mouth is the 12nd block of plate, and operating pressure is 0.1MPa, and tower top temperature is 66 DEG C, and bottom temperature is 85.1 DEG C, the pressure of compressor 10
Contracting is than being 2.8.Filling 500Y type structured packings in the tower of high-pressure tower 2,30 pieces of the number of plates, the 3rd charging aperture is the 21st block of plate, operation
Pressure is 0.45MPa, and tower top temperature is 115.1 DEG C, and bottom temperature is 125.2 DEG C, and the compression ratio of compressor 11 is 2.
Material liquid inlet amount containing isopropanol-diisopropyl ether mixture is 7061kg/h, and the composition of material liquid is：It is different
Propyl alcohol 63.8%, diisopropyl ether 36.2% (mass percent).
Material liquid containing isopropanol-diisopropyl ether mixture is through 15 by First Heat Exchanger 3, the second heat exchanger 4, the 3rd
After the preheating of heat exchanger 4 three times, with saturation liquid phase through 18 from the tower first charging aperture of low pressure 1 into lower pressure column 1 in carry out rectifying, tower reactor
The isopropanol product of 4528kg/h is produced, the wherein mass fraction of isopropanol is 99.5%.The top gaseous phase material warp of lower pressure column 1
After the compression boosting of first compressor 10 heats up, as the tower reactor thermal source of lower pressure column 1, carried out into the 4th heat exchanger 6 and materials at bottom of tower
Heat exchange, is that lower pressure column 1 provides again boiling hot amount, is then divided into two strands, after second heat exchanger of stock-traders' know-how 4 is exchanged heat with raw material, then
It is back to lower pressure column 1 after the first cooler 12, another plume amount is 5622kg/h, constitutes and be：Isopropanol 14.9%, diisopropyl
Ether 85.9% (mass percent), enters in high-pressure tower 2 after being preheated through the 5th heat exchanger 7, the 6th heat exchanger 8 through the 3rd charging aperture
Rectifying separation is carried out, the tower reactor of high-pressure tower 2 produces the diisopropyl ether product of 2534kg/h, and the mass fraction of wherein diisopropyl ether is
99.8%, a portion diisopropyl ether material returns to the bottom of high-pressure tower 2 after being exchanged heat through the 7th heat exchanger 9.Another part two
Isopropyl ether material is produced after being cooled down through the 3rd heat exchanger 5, the 3rd cooler 14 as product.The top gaseous phase material of high-pressure tower 2
After being heated up through the compression boosting of the second compressor 11, as the tower reactor thermal source of high-pressure tower 2, into the 7th heat exchanger 9 and the bottom of towe of high-pressure tower 2
Material is exchanged heat, and is that high-pressure tower 2 provides again boiling hot amount, is then divided into two strands, after the 6th heat exchanger of stock-traders' know-how 8 is cooled down, backflow
Lower pressure column 1 is returned, another plume amount is 3089kg/h, constitutes and is：Isopropanol 27.3%, (the quality percentage of diisopropyl ether 72.7%
Number).After being cooled down through the 5th heat exchanger 7 lower pressure column is returned to from second charging aperture.During stable operation, high-pressure tower and lower pressure column tower reactor institute
Calorific requirement is provided after being heated up by the compressed supercharging of overhead vapours, and waste heat is preheated to raw material and intermediate product, whole flow process
In, it is not necessary to external heat public work, only the wasted work 245.1kW of compressor 10, the wasted work 96.6kW of compressor 11, while three condensations
Thermic load needed for device is -149.8kW.
Claims (7)
1. the device of a kind of separating isopropanol and diisopropyl ether mixture, it is characterised in that including：First Heat Exchanger, described first
Heat exchanger has spaced first fluid passage and second fluid passage；
Second heat exchanger, second heat exchanger has spaced the 3rd fluid passage and the 4th fluid passage, first-class
The output end of body passage is connected with the input of the 3rd fluid passage, and the output end of the 4th fluid passage is defeated with the first cooler
Enter end connection；
3rd heat exchanger, the 3rd heat exchanger has spaced the 5th fluid passage and the 6th fluid passage；3rd stream
The output end of body passage is connected with the input of the 5th fluid passage；
4th heat exchanger, the 4th heat exchanger has spaced the 7th fluid passage and the 8th fluid passage；7th stream
Body path input is connected with the outlet of low pressure tower reactor, and the 7th fluid passage output end is connected with low pressure tower reactor, the 8th fluid passage
Input be connected with the output end of the first compressor, the 8th fluid passage have the first output end and the second output end；
5th heat exchanger, the 5th heat exchanger has spaced the 9th fluid passage and the tenth fluid passage；9th stream
Body path input is connected with the output end of the 8th fluid passage；
6th heat exchanger, the 6th heat exchanger has spaced the 11st fluid passage and the 12nd fluid passage, the
11 fluid path inputs are connected with the output end of the 9th fluid passage；
7th heat exchanger, the 7th heat exchanger has spaced the 13rd fluid passage and the 14th fluid passage, the
13 fluid passage inputs are connected with the outlet of high pressure tower reactor, and the 13rd fluid passage output end is connected with high pressure tower reactor, and the tenth
The input of four fluid passages is connected with the output end of the second compressor, and the 14th fluid passage has the first output end and the
Two output ends, the first output end of the 14th fluid passage is connected with the input of the 6th passage, and the second output end is led to the tenth
The input in road is connected；
Lower pressure column, the lower pressure column has first and second charging aperture, and low pressure tower top outlet and low pressure tower reactor are exported, and described first enters
Material mouth is connected with the output end of the 5th fluid passage, the output end phase of the second charging aperture and the tenth fluid passage
Even, low pressure tower reactor outlet is connected with second fluid path input；
First compressor, the input of first compressor is connected with low pressure tower top outlet；
High-pressure tower, the high-pressure tower has the outlet of the 3rd charging aperture, high pressure tower top outlet and high pressure tower reactor；3rd charging aperture
Output end with the 11st fluid passage is connected, and the outlet of high pressure tower reactor is connected with the 13rd fluid passage input；
Second compressor, the input of second compressor is connected with high pressure tower top outlet.
2. the device of a kind of separating isopropanol according to claim 1 and diisopropyl ether mixture, it is characterised in that also wrap
The first cooler is included, the first time cooler is located between the output end of the 4th fluid passage and the overhead reflux of lower pressure column；
Second cooler, second cooler is connected with the output end of second fluid passage；3rd cooler, the third time is cold
But device is connected with the output end of the 6th fluid passage.
3. the device of a kind of separating isopropanol according to claim 1 and diisopropyl ether mixture, it is characterised in that described
The number of theoretical plate of lower pressure column is 15~25 pieces, and first charging aperture is located at the 12nd block of plate, and second charging aperture is located at the 10th block of plate,
Operating pressure is 0.09MPa~0.1MPa, and 64~67 DEG C of tower top temperature, bottom temperature is 82~86 DEG C.
4. the device of a kind of separating isopropanol according to claim 1 and diisopropyl ether mixture, it is characterised in that described
The number of theoretical plate of high-pressure tower be 25~35 pieces, the 3rd charging aperture be located at the 19th block of plate at, operating pressure be 0.35MPa~
0.45MPa, 108~117 DEG C of tower top temperature, bottom temperature is 118~127 DEG C.
5. the device of a kind of separating isopropanol according to claim 1 and diisopropyl ether mixture, it is characterised in that described
The temperature difference >=5 DEG C of each fluid passage.The compression ratio 2.5~3.5 of the first compressor, the compression ratio of the second compressor for 1.5~
2.5。
6. according to a kind of above-mentioned separating isopropanol and the device separating isopropanol and diisopropyl ether mixture of diisopropyl ether mixture
Method, it is characterised in that carry out as steps described below：
Logistics containing isopropanol-diisopropyl ether mixture is via First Heat Exchanger, the second heat exchanger, the 3rd heat exchanger three times
After preheating, entered from lower pressure column first charging aperture with saturation liquid phase, rectifying is carried out in lower pressure column, lower pressure column tower kettle product is different
Propyl alcohol material, isopropanol material is produced after being cooled down through First Heat Exchanger, the second cooler as product；The top gaseous phase of lower pressure column
After material heats up through the supercharging of the first compressor compresses, as lower pressure column tower reactor thermal source, into the 4th heat exchanger, for lower pressure column is provided
Boiling hot amount, is then divided into two strands again, and second heat exchanger of stock-traders' know-how is exchanged heat with raw material, then is back to after the first cooler low
Pressure tower, through the 3rd charging aperture into carrying out rectifying separation in high-pressure tower after the heat exchanger of another stock-traders' know-how the 5th, the preheating of the 6th heat exchanger,
High-pressure tower tower kettle product is diisopropyl ether material, and conduct is produced after diisopropyl ether material is cooled down through the 3rd heat exchanger, the 3rd cooler
Product are produced；After the top gaseous phase material of high-pressure tower heats up through the supercharging of the second compressor compresses, as high-pressure tower tower reactor thermal source, enter
7th heat exchanger, for high-pressure tower provides again boiling hot amount, is then divided into two strands, after the cooling of the heat exchanger of a stock-traders' know-how the 6th, is back to low
Pressure tower, lower pressure column is returned to after the cooling of the heat exchanger of another stock-traders' know-how the 5th from second charging aperture.
7. the device separating isopropanol of a kind of separating isopropanol according to claim 6 and diisopropyl ether mixture and two different
The method of ether mixture, it is characterised in that in above-mentioned steps, isopropanol and diisopropyl ether mixture are divided into lower pressure column
From used as light component from lower pressure column overhead extraction, tower reactor obtains the isopropanol of high-purity to the azeotropic mixture of isopropanol and diisopropyl ether
Finished product, the azeotropic mixture of isopropanol and diisopropyl ether from lower pressure column overhead extraction is separated into high-pressure tower, the behaviour of high-pressure tower
Making the change of pressure makes the azeotropic composition of isopropanol and diisopropyl ether change, and new azeotropic state is reached again, now
The azeotropic mixture of isopropanol and diisopropyl ether is used as light component from high-pressure tower overhead extraction, and it is two different that high-pressure tower tower reactor obtains high-purity
Propyl ether finished product.
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| CN107417497A (en) * | 2017-07-24 | 2017-12-01 | 江苏新化化工有限公司 | Propylene hydration method coproduction isopropanol and diisopropyl ether process units |
| CN107875664A (en) * | 2017-12-21 | 2018-04-06 | 新疆工程学院 | Propylene propane thermal coupling Finestill energy-saving apparatus |
| CN109180435A (en) * | 2018-10-12 | 2019-01-11 | 常州大学 | A kind of device and method preparing isopropanol from recuperation of heat reactive distillation |
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| CN110028385A (en) * | 2019-04-26 | 2019-07-19 | 山东科技大学 | A kind of method and apparatus of separating isopropanol diisopropyl ether aqueous solution |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107417497A (en) * | 2017-07-24 | 2017-12-01 | 江苏新化化工有限公司 | Propylene hydration method coproduction isopropanol and diisopropyl ether process units |
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| CN109180435A (en) * | 2018-10-12 | 2019-01-11 | 常州大学 | A kind of device and method preparing isopropanol from recuperation of heat reactive distillation |
| CN109438179A (en) * | 2018-10-24 | 2019-03-08 | 常州大学 | A kind of reactive distillation prepares the power-economizing method of isopropanol |
| CN110028385A (en) * | 2019-04-26 | 2019-07-19 | 山东科技大学 | A kind of method and apparatus of separating isopropanol diisopropyl ether aqueous solution |
| CN110028385B (en) * | 2019-04-26 | 2022-08-09 | 山东科技大学 | Method and device for separating isopropyl alcohol diisopropyl ether aqueous solution |
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