CN107337600A - A kind of method and process unit of methanol and methyl acetate production methyl methacrylate - Google Patents
A kind of method and process unit of methanol and methyl acetate production methyl methacrylate Download PDFInfo
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- CN107337600A CN107337600A CN201710536668.1A CN201710536668A CN107337600A CN 107337600 A CN107337600 A CN 107337600A CN 201710536668 A CN201710536668 A CN 201710536668A CN 107337600 A CN107337600 A CN 107337600A
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- tower
- formaldehyde
- methyl acetate
- gas
- raw material
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/30—Preparation of carboxylic acid esters by modifying the acid moiety of the ester, such modification not being an introduction of an ester group
- C07C67/333—Preparation of carboxylic acid esters by modifying the acid moiety of the ester, such modification not being an introduction of an ester group by isomerisation; by change of size of the carbon skeleton
- C07C67/343—Preparation of carboxylic acid esters by modifying the acid moiety of the ester, such modification not being an introduction of an ester group by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
- C07C45/29—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation of hydroxy groups
Abstract
The invention discloses the method and process unit of a kind of methanol and methyl acetate production methyl methacrylate, the present invention, as reaction raw materials, and by the parsing of aldol(s) obtains formaldehyde gas and delivers to fixed bed reactors progress catalytic reaction with methyl acetate formation mixed gas stabilizing simultaneously obtaining target product MMA directly using methanol.The process is phase mixed system, and at utmost reduce water brings the auto polymerization with formaldehyde into so as to improve target product MMA yield and product quality；The reaction raw materials wide material sources of the present invention simultaneously, it is more cheap with respect to paraformaldehyde, formalin and dimethoxym ethane raw material, so as to reduce product cost.
Description
Technical field
The invention belongs to the process units and technique of field of energy and chemical technology, more particularly to methyl methacrylate MMA
Method.
Background technology
Methyl methacrylate (MMA) is mainly used in crowded glass, polyvinyl chloride auxiliary agent, clear and rich production intermediate, uses
Way is extensively.The production method of methyl methacrylate mainly has acetone cyanohydrin hair (ACH methods), ethylene process (BASF methods), different at present
Oxygenizement of butene, improve Acetone cyanohydrin method (MGC methods) and olefine aldehydr method (Alpha methods), wherein ACH methods in the presence of with acrylonitrile it is supporting,
The shortcomings that raw material is limited, by-product ammonium hydrogen sulfate；Ethylene process (BASF methods) process route is longer, technical monopoly, plant investment expense
It is high；The relative monopolization of isobutylene oxidation law technology, isobutene raw material are limited；It is complicated to improve Acetone cyanohydrin method (MGC methods) route, equipment
It is it is required that high；Olefine aldehydr method (Alpha methods) technical monopoly, the country does not apply.
China Patent Publication No. CN104513163A discloses one kind by methyl acetate and Formaldehyde Production methyl methacrylate
The method of ester, using three-step approach, and addition condensation obtains methyl methacrylate in the presence of catalyst.But the first of this method
The source of aldehyde raw material does not refer to and spoken frankly, and the source of formaldehyde raw material is essentially all formalin or by more at present
Point solution such as polyformaldehyde or dimethoxym ethane obtains formaldehyde.If reduced using formalin as formaldehyde source due to the presence of water
MMA yield, while can also improve catalytic reaction observable index；And paraformaldehyde or dimethoxym ethane decompose and be used as formaldehyde source, first
Depolymerization just needs additionally to consume the energy, and causes process complications, improves product cost.
The content of the invention
Goal of the invention：For above-mentioned existing problem and shortage, it is an object of the invention to provide a kind of methanol and vinegar
The method and process unit of sour methyl esters production methyl methacrylate, the process costs are lower, and disposal of pollutants is less.
Technical scheme：In order to solve the above-mentioned technical problem, the present invention uses following technical scheme：A kind of methanol and tumer
The method that ester produces methyl methacrylate, comprises the following steps：
(1) aoxidized using methanol as raw material in oxidator and formaldehyde raw material gas is prepared；
(2) formaldehyde raw material pneumatic transmission is entered to absorb synthesis tower bottom, while absorbs and isooctanol material liquid is sent at the top of synthetic tower,
The formaldehyde raw material gas first pass through absorb synthetic tower column plate section contacted with the mixed liquor containing isooctanol sprayed from top to bottom into
Row absorbing reaction, do not continue to rise to contact with isooctanol raw material further to absorb instead in packing section by the formaldehyde gas of absorbing reaction
Should, it is quiet in the bottom for absorbing synthetic tower to obtain the organic phase of containing alcohol-aldehyde condensate and the aqueous phase of formalin by absorbing reaction
Only it is layered, the organic phase delivers to subsequent handling；
(3) organic phase removes moisture in dehydrating tower, and control water content is below 1%；
(4) organic phase by dehydration is then sent into the middle part of Analytic Tower, and analytically methyl acetate is sent at the top of tower
Material liquid, organic phase in Analytic Tower hypomere and 160~200 DEG C occur parsings obtain formaldehyde gas and isooctanol liquid, it is different
Octanol liquid column plate along Analytic Tower flows down, formaldehyde gas along Analytic Tower column plate rise and with tower top spray and under methyl acetate
Mix and gasify at a temperature of 70~100 DEG C and form the mixed material gas of methyl acetate and formaldehyde；The methyl acetate and first
The molar equivalent of aldehyde is 1.1~3:1；
(5) the mixed material gas of the methyl acetate and formaldehyde, hydrogenation is condensed to yield metering system under catalyst action
Sour methyl esters.
Preferably, the absorption synthetic tower includes static liquid separation section, column plate section and packing section successively from bottom to up,
The packing section is one or more levels, and the column plate section is bubble cap plate section, and formaldehyde raw material gas enters the bottom of towe for absorbing synthetic tower
Temperature is 70 ± 5 DEG C, and the tower top temperature that isooctanol enters absorption synthetic tower is 40 ± 5 DEG C.
Preferably, the gaseous mixture for absorbing the synthesis non-absorbing reaction of column overhead is sent into the middle part on absorption tower,
5~20% dilute formalin is obtained from bottom of towe under the absorption of water, the unabsorbed gaseous mixture of tower top is through over pressurizeed rear portion
As the raw material of prepn. of formaldehyde by oxidation of methanol in step (1), another part is sent into pressure-swing absorption apparatus and obtains hydrogen and nitrogen, hydrogen
Raw material of the gas as condensation reaction in step (5), wherein, absorption tower tower top temperature is less than 30 DEG C, and the temperature of bottom of towe is 35 ± 2
℃。
Preferably, organic phase enters the middle part of dehydrating tower in step (3), is normal pressure in tower, tower top temperature 85
~95 DEG C obtain dilute formaldehyde, column bottom temperature be 100~110 DEG C be dehydrated after organic phase.
Present invention also offers a kind of methanol based on the above method and methyl acetate production methyl methacrylate technique
Device, including oxidation of formaldehyde device, absorption synthetic tower and vent gas treatment tower and Analytic Tower, the oxidation of formaldehyde device enter provided with four vigour
Mouthful, the oxidation of formaldehyde device outlet with absorb synthetic tower bottom inlet pipeline be connected, it is described absorption synthetic tower top with
Top further respectively has isooctanol entrance and offgas outlet, and the bottom for absorbing synthetic tower is additionally provided with organic phase extracting mouth and dilute
Formaldehyde recovery port, the offgas outlet absorbed at the top of synthetic tower are connected with vent gas treatment tower, and described absorb synthesizes tower bottom
Organic phase extracting mouth is connected with the entrance in the middle part of Analytic Tower, and the parsing tower bottom exports provided with isooctanol, the top of Analytic Tower
Methyl acetate entrance and the outlet of MMA unstripped gas are further respectively had with top, the MMA unstripped gas outlet is also connected with methyl in turn
Methyl acrylate reactor and rectifying column.
Preferably, the absorption synthetic tower includes extracting section, column plate section and packing section, the column plate successively from bottom to up
Section is staggered for multiple bubble cap plates and formed, and the packing section is multistage packing section, and every grade of packing section is wrapped successively from bottom to up
Column plate space, packing layer, distributor and spray equipment are included, the column plate is provided with vapor riser, the side in the column plate space
Pipeline pump is connected with wall and is circulated with spray equipment and is connected.
Preferably, also it is sequentially provided with evaporator, blender and filtering before four vigour entrances of the oxidation of formaldehyde device
Device, the offgas outlet being connected with blender circulating line is additionally provided with the top of the vent gas treatment tower.
Beneficial effect：Compared with prior art, the present invention directly uses methanol as reaction raw materials, and passes through aldol condensation
The parsing of thing obtain formaldehyde gas formed simultaneously with methyl acetate mixed gas stabilizing deliver to fixed bed reactors be catalyzed it is anti-
Target product MMA should be obtained.The process is phase mixed system, at utmost reduce water the auto polymerization brought into formaldehyde from
And improve target product MMA yield and product quality；Simultaneously the present invention reaction raw materials wide material sources, with respect to paraformaldehyde,
Formalin and dimethoxym ethane raw material are more cheap, so as to reduce product cost.
Brief description of the drawings
Fig. 1 is the schematic flow sheet of the method for methanol of the present invention and methyl acetate production methyl methacrylate.
Fig. 2 is the connection diagram of absorption synthetic tower and Analytic Tower of the present invention；
Fig. 3 is the structural representation of packing section in absorption synthetic tower of the present invention.
Wherein, evaporator 1, blender 2, filter 3, oxidation of formaldehyde device 4, absorption synthetic tower 5, vent gas treatment tower 6, heat exchange
Device 7, circulating pump 8, Analytic Tower 9, packing section 51, filler 52, gas distributor 53, spray 54, tedge 55.
Embodiment
Below in conjunction with the accompanying drawings and specific embodiment, the present invention is furture elucidated, it should be understood that these embodiments are merely to illustrate
The present invention rather than limitation the scope of the present invention, after the present invention has been read, those skilled in the art are each to the present invention's
The modification of the kind equivalent form of value falls within the application appended claims limited range.
Shown in Fig. 1, the method for alcohol of the invention and methyl acetate production methyl methacrylate, concrete technology step is such as
Under：
(1) aoxidized using methanol as raw material in oxidator and formaldehyde raw material gas is prepared, during being somebody's turn to do, methanol liquid passes through
The mode such as heating evaporation or gas sparging evaporation gasifies and with air and steam and tail gas after filtering, pre- in premixed device
Heat is to 110 DEG C of formation quaternary gaseous mixtures, and oxidation obtains formaldehyde gas and adopted from oxidation of formaldehyde device bottom in oxidation of formaldehyde device
Go out 5KPa, 150 DEG C or so of formaldehyde gas, and be sent into the bottom of follow-up absorption synthetic tower；The top of absorption synthetic tower has more
Level packing section, bottom is then made up of multistage bubble cap plate.
(2) isooctanol material liquid is sent at the top at the same time absorbing synthetic tower, and control absorbs synthesis column bottom temperature and existed
70 ± 2 DEG C, tower top temperature is at 40 ± 2 DEG C.Formaldehyde gas rises upwards after bottom of towe entrance initially enters column plate section, in column plate section
Mixing flow quantity containing isooctanol and formaldehyde and aldol(s) is advantageous to greatly the absorbing reaction of formaldehyde gas；Do not absorbed completely
Formaldehyde gas continue to rise and fully contact absorption condensation reaction in packing section with the isooctanol material liquid having just enter into, it is simultaneously logical
Cross external hanging type pipeline pump will in each layer filler mix hydrops be recycled in spray equipment from top to bottom spray after, pass through distributor
Distribution is recycled into absorption formaldehyde gas again, so that it is guaranteed that formaldehyde gas fully absorbs；And the mixed liquor after absorbing reaction
Further absorbed from upper strata packing section into lower floor's packing section.Because the aldol(s) of adsorption reaction is not soluble in water and density
All it is that the organic phase of aldol(s) preferentially enters lower floor in each layer packing section less than the organic phase of water, and finally in bottom of towe
Static layering, and produce by interface liquid level gauge the organic phase on upper strata in real time.In the step, column plate section using higher temperature and
Larger fluid flow can effectively avoid the auto polymerization of formaldehyde gas, and when rising to packing section, contact surface is increased using filler
Product finally on the premise of formaldehyde gas autohemagglutination is avoided, improves the absorption of formaldehyde isooctanol so as to heighten adsorption efficiency
Efficiency.Packing section in synthetic tower is absorbed forms for multistage filler, as shown in figure 3, one-level filler includes what is set on column plate
Tedge, tedge top is loads filler, and the upper surface for loading filler is liquid distribution trough, and the top of liquid distribution trough is then set
Shower nozzle is equipped with, and the shower nozzle is by pipeline with the hydrops position UNICOM on column plate so that the hydrops on column plate is followed by circulating pump
Ring delivers to shower nozzle ejection, so as to maximumlly improve absorption efficiency and Synthesis conversion.
(3) organic phase removes moisture in dehydrating tower, and control water content is to try to control below 1% and enters MMA
Water content in catalytic tower reaction system, the presence of water is avoided to reduce MMA yield.Specifically having hemiacetal
Mutually 110~110 DEG C of the control tower bottom temperature in column plate type dehydrating tower, tower top are less than the progress isolated tower of rectifying at 100 DEG C to machine
Dilute formaldehyde of less than 20% concentration on top, and bottom of towe obtains anhydrous hemiacetal, and it is sent into follow-up Analytic Tower；
(4) organic phase by dehydration is then sent into the middle part of Analytic Tower, and analytically methyl acetate is sent at the top of tower
Material liquid, organic phase in Analytic Tower hypomere and 160~200 DEG C occur parsings obtain formaldehyde gas and isooctanol liquid.With
Methyl acetate material liquid progressively gasifies after tower top entrance simultaneously for this, and the feeding amount of methyl acetate makes the molar equivalent of parsing formaldehyde
1.2~2 times (more preferably 1.35 times), the formaldehyde gas of itself and rising is formed mixed gas stabilizing and depart from from isooctanol,
The temperature control of tower top is at 70~100 DEG C, it is ensured that analytically tower bottom separation Posterior circle is sent into absorption synthetic tower to isooctanol liquid
(5) parsing column overhead obtains methyl acetate and the mixed gas stabilizing of formaldehyde is sent into MMA fixed bed reactors, is urging
The lower hydrogenation of agent effect is condensed to yield methyl methacrylate.
Claims (7)
1. a kind of method of methanol and methyl acetate production methyl methacrylate, comprises the following steps：
(1) aoxidized using methanol as raw material in oxidator and formaldehyde raw material gas is prepared；
(2) formaldehyde raw material pneumatic transmission is entered to absorb synthesis tower bottom, while absorbs and isooctanol material liquid is sent at the top of synthetic tower, it is described
Formaldehyde raw material gas, which first passes through, to be absorbed the column plate section of synthetic tower and contacts and inhaled with the mixed liquor containing isooctanol sprayed from top to bottom
Reaction is received, do not continue rising by the formaldehyde gas of absorbing reaction contacts in the further absorbing reaction of packing section with isooctanol raw material,
The organic phase of containing alcohol-aldehyde condensate and the aqueous phase of formalin, which are obtained, by absorbing reaction is absorbing static point of the bottom of synthetic tower
Layer, the organic phase deliver to subsequent handling；
(3) organic phase removes moisture in dehydrating tower, and control water content is below 1%；
(4) organic phase by dehydration is then sent into the middle part of Analytic Tower, and analytically methyl acetate raw material is sent at the top of tower
Liquid, organic phase in Analytic Tower hypomere and 160~200 DEG C occur parsings obtain formaldehyde gas and isooctanol liquid, isooctanol
Liquid column plate along Analytic Tower flows down, formaldehyde gas along Analytic Tower column plate rise and with tower top spray and under methyl acetate mix
And gasification forms the mixed material gas of methyl acetate and formaldehyde at a temperature of 70~100 DEG C；The methyl acetate and formaldehyde
Molar equivalent is 1.1~3:1；
(5) the mixed material gas of the methyl acetate and formaldehyde, hydrogenation is condensed to yield methyl methacrylate under catalyst action
Ester.
2. method according to claim 1, the absorption synthetic tower include successively from bottom to up static liquid separation section, column plate section and
Packing section, the packing section are one or more levels, and the column plate section is bubble cap plate section, and formaldehyde raw material gas, which enters, absorbs synthetic tower
Column bottom temperature be 70 ± 5 DEG C, isooctanol enter absorb synthetic tower tower top temperature be 40 ± 5 DEG C.
3. method according to claim 1, the gaseous mixture for absorbing the synthesis non-absorbing reaction of column overhead is sent into absorption tower
Middle part, 5~20% dilute formalin is obtained from bottom of towe under the absorption of water, the unabsorbed gaseous mixture of tower top is after over pressurizeed
Raw material of the part as prepn. of formaldehyde by oxidation of methanol in step (1), another part be sent into pressure-swing absorption apparatus obtain hydrogen with
Nitrogen, raw material of the hydrogen as condensation reaction in step (5), wherein, absorption tower tower top temperature is less than 30 DEG C, the temperature of bottom of towe
For 35 ± 2 DEG C.
4. method according to claim 1, it is characterised in that：Organic phase enters the middle part of dehydrating tower in step (3), is in tower
Normal pressure, tower top temperature be 85~95 DEG C and obtain dilute formaldehyde, column bottom temperature be 100~110 DEG C be dehydrated after organic phase.
5. a kind of methanol and methyl acetate production methyl methacrylate process unit based on claim 1 methods described, its
It is characterised by：Quaternary is provided with including oxidation of formaldehyde device, absorption synthetic tower and vent gas treatment tower and Analytic Tower, the oxidation of formaldehyde device
Gas entrance, the outlet of the oxidation of formaldehyde device is connected with absorbing the bottom inlet pipeline of synthetic tower, described to absorb the upper of synthetic tower
Portion and top further respectively have isooctanol entrance and offgas outlet, and the bottom for absorbing synthetic tower is additionally provided with organic phase extracting mouth
With dilute formaldehyde recovery port, the offgas outlet absorbed at the top of synthetic tower is connected with vent gas treatment tower, the absorption synthetic tower bottom
The organic phase extracting mouth in portion is connected with the entrance in the middle part of Analytic Tower, and the parsing tower bottom exports provided with isooctanol, Analytic Tower
Top and top further respectively have methyl acetate entrance and the outlet of MMA unstripped gas, and the MMA unstripped gas outlet is also connected with turn
Methyl methacrylate reactor and rectifying column.
6. the process unit of methanol and methyl acetate production methyl methacrylate according to claim 5, it is characterised in that：
It is multiple bubble cap plates that the absorption synthetic tower includes extracting section, column plate section and packing section, the column plate section successively from bottom to up
It is staggered and forms, the packing section is multistage packing section, and every grade of packing section includes column plate space, filler successively from bottom to up
Layer, distributor and spray equipment, the column plate are provided with vapor riser, pipeline pump are connected with the side wall in the column plate space
And circulate and connect with spray equipment.
7. the process unit of methanol and methyl acetate production methyl methacrylate according to claim 5, it is characterised in that：
Evaporator, blender and filter, the vent gas treatment tower are also sequentially provided with before four vigour entrances of the oxidation of formaldehyde device
Top be additionally provided with the offgas outlet being connected with blender circulating line.
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| CN201710536668.1A CN107337600A (en) | 2017-07-04 | 2017-07-04 | A kind of method and process unit of methanol and methyl acetate production methyl methacrylate |
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| CN201710536668.1A CN107337600A (en) | 2017-07-04 | 2017-07-04 | A kind of method and process unit of methanol and methyl acetate production methyl methacrylate |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110981727A (en) * | 2019-12-06 | 2020-04-10 | 西南化工研究设计院有限公司 | Methyl methacrylate synthesis process |
| CN111138251A (en) * | 2020-01-19 | 2020-05-12 | 西南化工研究设计院有限公司 | Process method, system and application for producing dimethanol formal by coupling reaction |
| CN111574375A (en) * | 2020-06-22 | 2020-08-25 | 北京旭阳科技有限公司 | Separation method and separation equipment for methyl acrylate crude product gas |
| CN111574370A (en) * | 2020-06-22 | 2020-08-25 | 北京旭阳科技有限公司 | Method and equipment for producing methyl acrylate by anhydrous gas-phase formaldehyde |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110981727A (en) * | 2019-12-06 | 2020-04-10 | 西南化工研究设计院有限公司 | Methyl methacrylate synthesis process |
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| CN111138251A (en) * | 2020-01-19 | 2020-05-12 | 西南化工研究设计院有限公司 | Process method, system and application for producing dimethanol formal by coupling reaction |
| CN111574375A (en) * | 2020-06-22 | 2020-08-25 | 北京旭阳科技有限公司 | Separation method and separation equipment for methyl acrylate crude product gas |
| CN111574370A (en) * | 2020-06-22 | 2020-08-25 | 北京旭阳科技有限公司 | Method and equipment for producing methyl acrylate by anhydrous gas-phase formaldehyde |
| CN111574370B (en) * | 2020-06-22 | 2023-09-12 | 北京旭阳科技有限公司 | Method and equipment for producing methyl acrylate by anhydrous gaseous formaldehyde |
| CN111574375B (en) * | 2020-06-22 | 2023-11-24 | 北京旭阳科技有限公司 | Separation method and separation equipment for methyl acrylate crude product gas |
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