CN106699560A - Separation device and separation method of material flow containing methyl methacrylate - Google Patents
Separation device and separation method of material flow containing methyl methacrylate Download PDFInfo
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- CN106699560A CN106699560A CN201510794440.3A CN201510794440A CN106699560A CN 106699560 A CN106699560 A CN 106699560A CN 201510794440 A CN201510794440 A CN 201510794440A CN 106699560 A CN106699560 A CN 106699560A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
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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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
- C07C67/58—Separation; Purification; Stabilisation; Use of additives by liquid-liquid treatment
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- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to the technical field of chemical separation, and more specifically relates to a separation device and a separation method of material flow containing methyl methacrylate (MMA). The separating device comprises a solvent tank, an extraction tower, a methyl propionate recovery tower, a MMA recovery tower, an alcohol ester recovery tower, and an extraction agent recovery tower. The separation method comprises following steps: 1, MMA material flow is extracted with an extraction agent in the extraction tower so as to obtain an extraction phase and a raffinate; 2, the extraction phase is delivered into the alcohol ester recovery tower, alcohols and esters are recycled at tower top, tower bottoms are delivered into the extraction agent recovery tower for recycling of a solvent, and the recycled solvent is delivered back into the solvent tank; 3, the raffinate is delivered through the methyl propionate recovery tower for recycling of MP, and the MMA recovery tower for recycling of MMA successively. Compared with the prior art, the separation method comprises following advantages: the process is simple; the extraction agent is used for breaking a material azeotropic system and reducing separation difficulty; MP recovery rate and MMA recovery rate are both higher than 99.9%; MMA purity is higher than 99.8%; the separation method can be widely applied in preparation of MMA via aldol condensation; and development prospect is promising.
Description
Technical field
The present invention relates to technical field of chemical separation, and in particular to a kind of purity is high, the rate of recovery is high containing methyl-prop
Separation equipment and separation method that e pioic acid methyl ester logistics is separate.
Background technology
Methyl methacrylate is a kind of organic compound, is a kind of important industrial chemicals, is the transparent modeling of production
The monomer of material polymethyl methacrylate (lucite, PMMA).Also can be with other vinyl monomer copolymerization
Product of different nature is obtained for manufacturing lucite, coating, lube oil additive, plastics, adhesive, tree
Fat, timber size, motor coil penetrant, ion exchange resin, paper polish agent, textile auxiliary,
Leather treatment, printing and dyeing assistant and insulating potting material etc..
The main method for producing MMA has Acetone cyanohydrin method, the tert-butyl alcohol/isobutene direct oxidation method, ethenecarbonyl
Change method, methyl propionate aldol condensation method etc..Wherein methyl propionate aldol condensation method is study hotspot in recent years, its
Follow-up MMA product purifications technique also turns into study hotspot.China Patent Publication No. CN101020636A is situated between
Continued a kind of purification that methyl methacrylate during methyl methacrylate is produced by isobutene (or tert-butyl alcohol)
Separation method.The patent first removes unreacted MAL using conventional distillation, then with 0~60 DEG C, matter
Amount concentration is that 20~100% chloroform aqueous solution is extracted, methanol removal and water and organic impurities, is finally carried out
Flash distillation and rectification under vacuum carry out purification to MMA.MMA is only obtained in above-mentioned separation process, to remaining
Material is not reclaimed.China Patent Publication No. CN103833551A describes one kind by the tert-butyl alcohol/isobutylene oxidation
Produce the method for purifying and separating of methyl methacrylate.The patent is extracted by n-hexane and water, and extraction phase is recovered
After n-hexane, then miscellaneous ester is removed, reclaim MMA.Although having obtained MMA in above-mentioned separation process, and return
Receive n-hexane, but to other materials and unrecovered.China Patent Publication No. 103193640A describes a kind of life
Produce the reactive distillation method of methyl methacrylate.The synthesis of methyl methacrylate is completed in a rectifying column,
Target product is completed by azeotropic distillation to be separated with raw material, obtained in tower top and be free of metering system while reaction
The organic phase rich in methyl methacrylate of acid, the solution containing a large amount of methacrylic acids is obtained in tower reactor, while
In tower reactor one thin film evaporator of series connection, to the further concentrate of heavy component of tower reactor.In above-mentioned separation process, material
Originate be methacrylic acid, methyl alcohol reactive distillation gained, it is necessary to separate system material composition it is simple, it is difficult to apply
In product separation and purification process obtained in methyl propionate aldol condensation.
The content of the invention
The purpose of the present invention is exactly to provide a kind of for aldol contracting for the defect for overcoming above-mentioned prior art to exist
Methyl methacrylate and the methyl propionate rate of recovery in the product stream that legal methyl methacrylate processed is obtained are all
Separation equipment and separation method that logistics containing methyl methacrylate very high is separate.
The purpose of the present invention can be achieved through the following technical solutions：
A kind of separation equipment of the logistics containing methyl methacrylate, the separation equipment include extraction tower, one
Methyl propionate recovery tower, MMA recovery towers, alcohol ester recovery tower, an extractant recovery tower；
Described extraction tower connects an extractant feed pipe, a MMA logistics feed pipe, an extraction respectively
Liquid efferent duct, a raffinate efferent duct；The tower top of the extraction tower obtains raffinate phase, and is exported by raffinate
Pipe connects the methyl propionate recovery tower, and the tower reactor of the extraction tower obtains extraction phase, and by extract efferent duct
Connect the alcohol ester recovery tower；
Described alcohol ester reclaims column overhead and connects the methyl propionate recovery tower, and tower reactor connects the extractant and reclaims
Tower, the extractant recovery tower tower reactor is reclaimed and obtains extractant；
The methyl propionate recovery tower tower reactor connects the MMA recovery towers, and tower top connects methyl propionate output
Pipe, reclaims methyl propionate；
Described MMA reclaims column overhead and connects a MMA efferent ducts, reclaims MMA.
Described extractant is placed in a solvent tank, and the solvent tank connects extraction tower by extractant feed pipe；
Described MMA logistics feed pipes one end connection extraction tower, other end connection methyl propionate aldol reaction
Generation material outlet.
Described extractant reclaims column overhead and obtains methyl alcohol, is reclaimed as product, and tower reactor connects described by connecting tube
Solvent tank, solvent tank is delivered to by the extractant of a part, and another part extractant is directly exported.
A kind of to separate the method containing methyl methacrylate logistics using above-mentioned separation equipment, separation method includes as follows
Step：
(1) extractant feed pipe is located at described extraction column overhead, and the feed pipe of logistics containing MMA is located at described
Extraction tower tower reactor at, the logistics that will contain MMA is extracted in extraction tower with extractant, and tower top obtains raffinate phase,
Tower reactor obtains extraction phase；The raffinate phase enters the methyl propionate recovery tower；Described extraction phase enters the alcohol
Ester recovery tower；
(2) alcohol ester reclaims column overhead and obtains part methyl alcohol and nearly all methyl propionate being dissolved in solvent,
The methyl propionate recovery tower is pipelined to again, is further separated；The alcohol ester recovery tower kettle material is
The unrecovered methyl alcohol of extractant and part, into the extractant recovery tower；
(3) the remaining methyl alcohol of extractant recovery tower recovered overhead is directly exported as product, the extractant
Recovery tower tower reactor obtains extractant, partly returns to the solvent tank recycling, and part directly exports；
(4) the methyl propionate recovery tower recovered overhead obtains a small amount of methyl alcohol and almost all methyl propionate,
Directly export, methyl propionate recovery tower tower reactor heavy constituent logistics is further separated into the MMA recovery towers
Reclaim MMA；
(5) MMA reclaims column overhead and obtains MMA logistics, directly exports, and tower reactor obtains heavy constituent.
The logistics containing MMA described in step (1) is methyl propionate aldol reaction product, including：First
Alcohol, methyl propionate, methyl methacrylate, propionic acid, methacrylic acid and water.
Extractant described in step (1) be selected from one kind in water, ethylene glycol, glycerine, toluene or n-hexane or
It is several, preferred glycerin solution.The Solvent quantity is with the mass flow ratio of the logistics containing MMA
0.1~5:1；
The operating pressure of described extraction tower is 0~1MPa, and operation temperature is 20~80 DEG C.
Described extractant is glycerin solution, the matter of described Solvent quantity and the logistics containing MMA
Amount flow-rate ratio is preferably 0.5~3:1.
The operating pressure of the alcohol ester recovery tower described in step (2) be -0.06~0.5MPa, operation temperature be 50~
150℃；
The operating pressure of the extractant recovery tower described in step (3) be -0.08~0.5MPa, operation temperature be 50~
150℃；
The operating pressure of the methyl propionate recovery tower described in step (4) be -0.05~0MPa, operation temperature be 20~
100℃；
The operating pressure of the MMA recovery towers described in step (5) be -0.098~0MPa, operation temperature be 50~
150℃。
The operating pressure of the separation equipment is -0.098-1.0MPa, and operation temperature is 20-150 DEG C.
Present invention extractant breaks material azeotropic system, greatly reduces separating difficulty, and final methyl propionate is reclaimed
Rate is more than 99.5% more than 99.8%, the MMA rate of recovery more than 99.8%, MMA purity.
Compared with prior art, beneficial effects of the present invention are embodied in following two aspect：
(1) technique that methyl methacrylate is generated particular for methyl propionate aldol reaction, meets methyl
The trend of methyl acrylate production technology adjustment, following market prospects are good.
(2) present invention breaks material azeotropic system using extractant, greatly reduces separating difficulty, and MMA is returned
Yield more than 99.9%, MMA purity be more than 99.8%, the methyl propionate rate of recovery be more than 99.8%, purity with return
Yield is above other separation methods.
Brief description of the drawings
Fig. 1 is connection diagram of the invention：
Wherein V101 is solvent tank；C101 is extraction tower；T101 is methyl propionate recovery tower；T102 is methyl
Methyl acrylate recovery tower；T103 is alcohol ester recovery tower；T104 is solvent recovery tower.
Specific embodiment
Embodiments of the invention are elaborated below, the present embodiment enters under premised on technical solution of the present invention
Row is implemented, and gives detailed implementation method and specific operating process, but protection scope of the present invention is not limited to down
The embodiment stated.
Embodiment 1
As shown in figure 1, a kind of separation equipment for containing methyl methacrylate separate, the separation equipment includes one
Individual solvent tank V101, extraction tower C101, methyl propionate recovery tower T101, a MMA are reclaimed
Tower T102, alcohol ester recovery tower T103, an extractant recovery tower T104；
Extraction tower C101 connects an extractant feed pipe, a MMA logistics feed pipe, an extraction respectively
Liquid efferent duct, a raffinate efferent duct, extractant is placed in solvent tank V101, and solvent tank V101 passes through
Extractant feed pipe connection extraction tower C101, MMA logistics feed pipe one end connection extraction tower C101, the other end
Connection methyl propionate aldol reaction generation material outlet；The tower top of extraction tower C101 is exported by raffinate
Pipe connects the methyl propionate recovery tower T101, and the tower reactor of extraction tower C101 connects alcohol ester by extract efferent duct
Recovery tower T103；
Alcohol ester recovery tower T103 tower tops connect methyl propionate recovery tower T101, tower reactor connection extractant recovery tower
T104, extractant T104 recovery towers tower reactor is reclaimed and obtains extractant；Extractant T104 reclaims column overhead and obtains first
Alcohol, reclaims as product, and tower reactor connects the solvent tank V101, partial extraction agent delivered to molten by connecting tube
Agent tank V101.
Methyl propionate recovery tower T101 tower reactors connect MMA recovery tower T102, and tower top connects methyl propionate output
Pipe, reclaims methyl propionate；
MMA recovery tower T102 tower tops connect a MMA efferent ducts, reclaim MMA, and tower reactor is reclaimed and obtains weight
Component.
Method containing methyl methacrylate material is separated using above-mentioned equipment respectively as follows：
Raw material is the logistics containing MMA, consisting of：Methyl alcohol 9%, water 3%, methyl propionate 70%, methyl
Methyl acrylate 15%, propionic acid 1.5%, methacrylic acid 1.5%.
Logistics containing MMA is input into from extraction tower C101 lower ends, extraction column overhead is input into from solvent tank V101
The extractant glycerine water solution that comes of conveying, qualities of glycerin concentration is 30%, extractant and MMA logistics qualities
Flow-rate ratio is 0.1:1.
The theoretical version number of extraction tower C101 is 5, operating pressure 0.1MPa, and operation temperature is 40 DEG C, extraction tower
C101 tower tops raffinate phase enters methyl propionate recovery tower T101, and extraction tower C101 tower reactors extraction phase is returned into alcohol ester
Receive tower T103.
The number of theoretical plate of alcohol ester recovery tower T103 is 35 pieces, and feed entrance point is the 17th piece, and tower top pressure is air
Pressure, 71 DEG C of tower top temperature, 105 DEG C of bottom temperature.
38 pieces of the number of theoretical plate of methyl propionate recovery tower T101, raffinate feedstock position is the 20th piece, propionic acid first
Ester recovery tower T103 overhead streams feed entrance point is the 18th piece, and tower top pressure is -0.06MPa, and tower top obtains third
Sour methyl esters, temperature is 60 DEG C, 95 DEG C of tower reactor stream temperature, into MMA recovery towers T102.
MMA recovery tower T102 number of theoretical plates are 45, and feed entrance point is the 20th piece, and tower top pressure is -0.08MPa,
61 DEG C of temperature, is methyl methacrylate, 125 DEG C of bottom temperature.
The tower number of theoretical plate that extractant reclaims T104 is 20, and feed entrance point is the 12nd piece, and tower top pressure is air
Pressure, tower top obtains methanol stream, and 64 DEG C of temperature, 118 DEG C of bottom temperature, partial discharge, part returns to solvent tank
V101。
Each column overhead, kettle material composition are as shown in table 1.
Each column overhead kettle material composition of table 1
As can be seen from the above table：T102 tower top MMA concentration reaches 99.80%, and purity is higher, reaches top grade
Product, the methyl propionate rate of recovery is that 99.97%, the MMA rate of recovery is 99.87%.
Embodiment 2
Raw material is constituted with embodiment 1.
Logistics containing MMA is input into from extraction tower C101 lower ends, extraction column overhead is input into from solvent tank V101
The extractant water that conveying comes, water is 5 with MMA logistics qualities flow-rate ratio:1.
The theoretical version number of C101 extraction towers is 6, operating pressure 0.1MPa, and operation temperature is 30 DEG C, C101 towers
Top raffinate phase enters T101 methyl propionate recovery towers, and C101 tower reactors extraction phase enters T103 alcohol ester recovery towers.
T103 alcohol ester recovery towers number of theoretical plate is 40 pieces, and feed entrance point is the 20th piece, and tower top pressure is atmospheric pressure,
73 DEG C of tower top temperature, 102 DEG C of bottom temperature.
40 pieces of T101 methyl propionate recovery towers number of theoretical plate, raffinate feedstock position is the 22nd piece, T103 tower tops
Logistics feed entrance point is the 23rd piece, and tower top pressure is -0.05MPa, and tower top obtains methyl propionate, and temperature is 50 DEG C,
85 DEG C of tower reactor stream temperature, into T102 methyl methacrylate recovery towers.
T102 methyl methacrylate recovery towers number of theoretical plate is 40, and feed entrance point is the 20th piece, tower top pressure
It is -0.07MPa, 61 DEG C of temperature is methyl methacrylate, 117 DEG C of bottom temperature.
T104 extractant recovery towers number of theoretical plate is 20, and feed entrance point is the 8th piece, and tower top pressure is atmospheric pressure,
Tower top obtains methanol stream, and 64 DEG C of temperature, 99 DEG C of bottom temperature, partial discharge, part returns to V101 extractions
Agent storage tank.
Each column overhead, kettle material composition are as shown in table 2.
Each column overhead kettle material composition of table 2
As can be seen from the above table：T102 tower top MMA concentration reaches 99.80%, and purity is higher, reaches top grade
Product, the methyl propionate rate of recovery is that 99.94%, the MMA rate of recovery is 100%.
Embodiment 3
Raw material is constituted with embodiment 1.
Logistics containing MMA is input into from extraction tower C101 lower ends, extraction column overhead is input into from solvent tank V101
The extractant water that conveying comes, water is 0.4 with MMA logistics qualities flow-rate ratio:1.
The theoretical version number of C101 extraction towers is 6, operating pressure 0.1MPa, and operation temperature is 30 DEG C, C101 towers
Top raffinate phase enters T101 methyl propionate recovery towers, and C101 tower reactors extraction phase enters T103 alcohol ester recovery towers.
T103 alcohol ester recovery towers number of theoretical plate is 40 pieces, and feed entrance point is the 20th piece, and tower top pressure is atmospheric pressure,
64 DEG C of tower top temperature, 88 DEG C of bottom temperature.
40 pieces of T101 methyl propionate recovery towers number of theoretical plate, raffinate feedstock position is the 22nd piece, T103 tower tops
Logistics feed entrance point is the 23rd piece, and tower top pressure is -0.05MPa, and tower top obtains methyl propionate, and temperature is 50 DEG C,
81 DEG C of tower reactor stream temperature, into T102 methyl methacrylate recovery towers.
T102 methyl methacrylate recovery towers number of theoretical plate is 40, and feed entrance point is the 20th piece, tower top pressure
It is -0.07MPa, 64 DEG C of temperature is methyl methacrylate, 117 DEG C of bottom temperature.
T104 extractant recovery towers number of theoretical plate is 20, and feed entrance point is the 8th piece, and tower top pressure is atmospheric pressure,
Tower top obtains methanol stream, and 64 DEG C of temperature, 99 DEG C of bottom temperature, partial discharge, part returns to V101 extractions
Agent storage tank.
Each column overhead, kettle material composition are as shown in table 2.
Each column overhead kettle material composition of table 3
As can be seen from the above table：T102 tower top MMA concentration reaches 99.83%, and purity is higher, reaches top grade
Product, the methyl propionate rate of recovery is that 99.98%, the MMA rate of recovery is 100%.
Claims (9)
1. a kind of separation equipment of the logistics containing methyl methacrylate, it is characterised in that the separation equipment includes
One extraction tower, methyl propionate recovery tower, MMA recovery towers, alcohol ester recovery tower, an extraction
Take agent recovery tower；
Described extraction tower connects an extractant feed pipe, a MMA logistics feed pipe, an extraction respectively
Liquid efferent duct, a raffinate efferent duct；The tower top of the extraction tower connects the propionic acid by raffinate efferent duct
Methyl esters recovery tower, the tower reactor of the extraction tower connects the alcohol ester recovery tower by extract efferent duct；
Described alcohol ester reclaims column overhead and connects the methyl propionate recovery tower, and tower reactor connects the extractant and reclaims
Tower, the extractant recovery tower tower reactor is reclaimed and obtains extractant；
The methyl propionate recovery tower tower reactor connects the MMA recovery towers, and tower top connects methyl propionate output
Pipe, reclaims methyl propionate；
Described MMA reclaims column overhead and connects a MMA efferent ducts, reclaims MMA.
2. a kind of separation equipment of logistics containing methyl methacrylate according to claim 1, its feature
It is that described extractant is placed in a solvent tank, the solvent tank connects extraction tower by extractant feed pipe；
Described MMA logistics feed pipes one end connection extraction tower, other end connection methyl propionate aldol reaction
Generation material outlet.
3. a kind of separation equipment of logistics containing methyl methacrylate according to claim 2, its feature
It is that described extractant reclaims column overhead and obtains methyl alcohol, is reclaimed as product, and tower reactor connects institute by connecting tube
State solvent tank.
4. it is a kind of that logistics containing methyl methacrylate is separated using the separation equipment as described in any in claim 1-3
Method, it is characterised in that the method comprises the following steps：
(1) logistics containing MMA is extracted in extraction tower with extractant, tower top obtains raffinate phase, and tower reactor is obtained
To extraction phase；The raffinate phase enters the methyl propionate recovery tower；Described extraction phase is reclaimed into the alcohol ester
Tower；
(2) alcohol ester reclaims column overhead and obtains methyl alcohol and the methyl propionate being dissolved in solvent, then defeated by pipeline
The methyl propionate recovery tower is sent to, is further separated；The alcohol ester recovery tower kettle material is extractant and part
Unrecovered methyl alcohol, into the extractant recovery tower；
(3) the remaining methyl alcohol of extractant recovery tower recovered overhead is directly exported as product, the extractant
Recovery tower tower reactor obtains extractant, partly returns to the solvent tank recycling, and part directly exports；
(4) the methyl propionate recovery tower recovered overhead obtains methyl propionate, the methyl propionate recovery tower tower reactor
Heavy constituent logistics further separates and recovers MMA into the MMA recovery towers；
(5) MMA reclaims column overhead and obtains MMA logistics, and tower reactor obtains heavy constituent.
5. a kind of separation method of logistics containing methyl methacrylate according to claim 4, its feature
It is that the logistics containing MMA described in step (1) is methyl propionate aldol reaction product, including：
Methyl alcohol, methyl propionate, methyl methacrylate, propionic acid, methacrylic acid and water.
6. a kind of separation method of logistics containing methyl methacrylate according to claim 4, its feature
It is that the extractant described in step (1) is selected from the one kind in water, ethylene glycol, glycerine, toluene or n-hexane
Or it is several, the Solvent quantity is 0.1~5 with the mass flow ratio of the logistics containing MMA:1；
The operating pressure of described extraction tower is 0~1MPa, and operation temperature is 20~80 DEG C.
7. a kind of separation method of logistics containing methyl methacrylate according to claim 6, its feature
It is that described extractant is glycerin solution, described Solvent quantity and the logistics containing MMA
Mass flow ratio is 0.5~3:1.
8. a kind of separation method of logistics containing methyl methacrylate according to claim 4, its feature
It is that the operating pressure of the alcohol ester recovery tower described in step (2) is -0.06~0.5MPa, operation temperature is 50~
150℃；
The operating pressure of the extractant recovery tower described in step (3) be -0.08~0.5MPa, operation temperature be 50~
150℃；
The operating pressure of the methyl propionate recovery tower described in step (4) be -0.05~0MPa, operation temperature be 20~
100℃；
The operating pressure of the MMA recovery towers described in step (5) be -0.098~0MPa, operation temperature be 50~
150℃。
9. a kind of separation method of logistics containing methyl methacrylate according to claim 3, its feature
It is that the operating pressure of the separation equipment is -0.098-1.0MPa, and operation temperature is 20-150 DEG C.
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| CN201510794440.3A CN106699560B (en) | 2015-11-18 | 2015-11-18 | Separation equipment and separation method for methyl methacrylate-containing material flow |
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| CN201510794440.3A CN106699560B (en) | 2015-11-18 | 2015-11-18 | Separation equipment and separation method for methyl methacrylate-containing material flow |
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| CN115246773A (en) * | 2021-04-26 | 2022-10-28 | 上海浦景化工技术股份有限公司 | System for separating MMA from aldol condensation product |
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| CN115246773A (en) * | 2021-04-26 | 2022-10-28 | 上海浦景化工技术股份有限公司 | System for separating MMA from aldol condensation product |
| CN115246773B (en) * | 2021-04-26 | 2024-05-10 | 上海浦景化工技术股份有限公司 | System for separating MMA from aldol condensation product |
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