CN108658753A - A kind of continuous production device and technique of 2,2- dihydromethyl propionic acids - Google Patents
A kind of continuous production device and technique of 2,2- dihydromethyl propionic acids Download PDFInfo
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- CN108658753A CN108658753A CN201810637252.3A CN201810637252A CN108658753A CN 108658753 A CN108658753 A CN 108658753A CN 201810637252 A CN201810637252 A CN 201810637252A CN 108658753 A CN108658753 A CN 108658753A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/285—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with peroxy-compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0093—Microreactors, e.g. miniaturised or microfabricated reactors
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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
- C07C45/45—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by condensation
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Abstract
The present invention relates to a kind of continuous production device and technique of 2,2 dihydromethyl propionic acids, process units is made of the first chip seedpod of the lotus microreactor, the second chip seedpod of the lotus microreactor, economic benefits and social benefits continuous evaporating crystallizer.First, second chip seedpod of the lotus microreactor is composed in series by 5~6,6~8 the stage pieces reactor that declines respectively, and chip microreactor includes reacting pipe, seedpod of the lotus distributor and hot water or cold water's pipeline.During positive propionic aldehyde solution, formaldehyde and water catalyst solution carry out in the first chip seedpod of the lotus microreactor after continuous condensating and, and with hydrogen peroxide in the second chip seedpod of the lotus microreactor continuous oxidation；The post-processings such as the concentrated crystallization of oxidation product, obtain 2,2 dihydromethyl propionic acid products.The present invention provide one kind can 2,2 dihydromethyl propionic acid of continuous production device and technique, have many advantages, such as investment it is low, product yield is high, recruitment land used is few, environmental-friendly, labor intensity is low and safety is good.
Description
Technical field
The continuous production device and technique of one kind 2,2- dihydromethyl propionic acids of the invention particularly belong to organic chemical industry's technology neck
Domain.
Background technology
2,2- dihydromethyl propionic acids are a kind of environmental type chemicals, it is not required to by the effect of two primary OHs
Protect third carboxyl can easily methyl carbamate or esterification, then in ammonium hydroxide in and unreacted carboxyl,
Make its water-solubleization.In terms of dissolubility, dihydromethyl propionic acid has the unique advantage of oneself, and fabulous dissolubility can be significantly
Improve working efficiency.2,2- dihydromethyl propionic acids can be widely used for soluble polyurethane, polyester, epoxy resin etc..
But due to the difficulty in technology of preparing, there is also catalyst choices and reactivity for the synthetic technology having at present
The problems such as difference, process route complexity, high energy consumption, serious environmental pollution, the Green Chemistry that pollution is effectively reduced from source is not met
Mentality of designing.Mainly method carries out synthesis 2,2- dihydromethyl propionic acids in two steps both at home and abroad at present.First, in basic catalyst
In the presence of, formaldehyde and butyraldehyde carry out aldol reaction, generate 2,2- dihydroxymethyl butyraldehyde；It is again oxidation with hydrogen peroxide
Agent obtains 2,2- dihydromethyl propionic acid white crystals by the oxidation of 2,2- dihydroxymethyl butyraldehyde, crystallization.Wherein aldol condensation is anti-
Should be the committed step of two-step method, basic catalyst mostly uses inorganic base (Na2CO3, NaOH), organic base (triethylamine) etc..By
In there are the side reactions such as cannizzaro's reaction in condensation reaction, causes the pH value of reaction system to change larger, exist
The problems such as catalyst choice is poor, reactivity is poor, product yield is low.
In above-mentioned domestic and international two-step method synthesis 2,2- dihydromethyl propionic acids, condensation reaction and oxidation reaction are all to react
It is carried out in kettle, entire technical process is also all that interval carries out, therefore causes process route complexity, high energy consumption, environment dirty again
Contaminate the problems such as serious.This batch process does not meet the mentality of designing for the Green Chemistry that pollution is effectively reduced from source.
The patents such as Publication No. CN102911038A, CN103242154A, CN105152907A are about 2,2- dihydroxymethyls
The report of the preparation method of propionic acid is all two-step method production 2,2- dihydromethyl propionic acids, and used catalyst is mixed base (Na2CO3+
NaOH), wherein aldol reaction and oxidation reaction carry out in glass-lined kettle respectively, are typical batch production technique.
Practical application shows that the production technology is unstable, and control is difficult, and conversion ratio is low.In order to improve conversion ratio, need ceaselessly to carry out work
Skill adjusts, and process route is long and complex, and high energy consumption, pollutant emission is serious, and conversion ratio improves seldom, and production cost is high not
Under, do not meet the mentality of designing for the green chemical that pollutant emission is effectively reduced from source.
All it is with the batch process of two-step method to the production technology of 2,2- dihydromethyl propionic acids preparation industrially at this stage
Basis focuses mostly in the optimization of aldol reaction condition, but all because of the presence of side reaction, the bad control of production technology, production
The problems such as product yield is low, product energy consumption is big, the discharge of contamination of products object is serious is unresolved.And it is set existing for batch process
It is standby take up a large area, labor intensity is big, production cost is high, security risk is more, there are no from obtaining for the problems such as being not easy of expanding production
It solves.
Invention content
For the shortcomings of the prior art, the present invention provide one kind can be continuously produced, production environment cleaning,
High income and the good 2,2- dihydromethyl propionic acids process units and technique of safety.
The continuous production device and technique of one kind 2,2- dihydromethyl propionic acids of the invention, the continuous production device is by raw material
Storage tank, metering pump, the first chip seedpod of the lotus microreactor, condensation liquid collecting tank, the second chip seedpod of the lotus microreactor, economic benefits and social benefits continuous steaming
Send out crystallizer, recrystallization kettle, centrifuge, double conic rotary vacuum dryer and vibrating screen composition；The first, second chip seedpod of the lotus
Microreactor is composed in series by 5~6,6~8 stage piece formula seedpod of the lotus microreactors respectively；Reaction in chip seedpod of the lotus microreactor
Pipeline, hot water pipeline and cold water pipes are arranged at the centre of supporting base material, in being laid with back and forth, spaced set in reacting pipe
Seedpod of the lotus distributor；The seedpod of the lotus distributor is by single tube group seedpod of the lotus shape in pairs, the distance between both ends end face single tube of seedpod of the lotus 8mm,
The diameter 20mm of end face, consistent with reacting pipe, the height of the single head seedpod of the lotus is 360mm, two seedpod of the lotus distributors in reacting pipe
Spacing be 500mm.
The technique：
The positive propionic aldehyde solution of aqueous catalyst solution, 99wt%, 37wt% formaldehyde are molten to continuously enter the first micro- reaction of the chip seedpod of the lotus
In device, the continuous condensating in reacting pipe；Condensation product the first chip seedpod of the lotus microreactor bottom discharge pipeline with
85wt% formic acid pipelines communicate, and condensation product and 85wt% formic acid are after premixing, into the condensation liquid collecting tank with stirring
Neutralization reaction is carried out, is carried out continuously oxidation with reacting pipe of the hydrogen peroxide in the second chip seedpod of the lotus microreactor thereafter；Oxygen
Change product enter economic benefits and social benefits continuous evaporating crystallizer condensing crystallizing, using filter, except iron, decoloration, concentration, crystallization, filtering, drying and
Sieving is handled, and obtains 2,2- dihydromethyl propionic acids；Filtrated stock recycles 2,2- dihydromethyl propionic acids therein through reprocessing.
The condensation course：Na in aqueous catalyst solution2CO3：The mass ratio of water is 1：16；Aqueous catalyst solution, formaldehyde are molten
It is respectively through dissolving into the flow into the first chip seedpod of the lotus microreactor with positive propionic aldehyde：526.00L/h、442.20L/h、162.80L/
H, flow control is in 0.3~1.2m/s；Reaction temperature is 70~100 DEG C, and pressure is 0.2~0.6MPa, and the time is 15~30s.
The N-process：The formic acid of 85wt% is squeezed into formic acid pipeline with the flow of 6.50L/h, makes itself and condensation product
Mixing neutralizes.
The oxidation process：The flow velocity that condensation liquid after neutralization presses 0.3~1.2m/s with 35wt% hydrogen peroxide enters the
Two-chip type seedpod of the lotus microreactor, flow are respectively 1137.50L/h, 220.95L/h, and reaction temperature is 70~100 DEG C, pressure 0.2
~0.6MPa, 15~30s of time.
Supporting base material is 304 stainless steels, reacting pipe, seedpod of the lotus distributor, hot-water line in the chip seedpod of the lotus microreactor
Road and cold water pipe are 316 stainless steels.
Beneficial effects of the present invention
1) condensation reaction and oxidation reaction have been all made of chip seedpod of the lotus microreactor, the spaced set seedpod of the lotus in reacting pipe
Distributor, can effectively improve the flow velocity of fluid, and reaction raw materials mix evenly, more fully；It is fiercer to react under a certain pressure,
It is fully reacted in a short time；Concentration on each section of material flowed through, temperature base are in homogeneous, close to flat-pushing
Stream；Conversion ratio on each section is also identical, and controls suitable temperature and flow, product yield higher.With traditional autoclave
Reaction is compared, and reaction temperature is stablized, and can obtain best reaction temperature, and pH stable, can greatly improve reaction speed, significantly
Shorten the reaction time, save energy consumption, mitigate labor intensity, production environment is greatly improved.
2) oxidation of 2,2- dihydroxymethyls butyraldehyde is also to use successive reaction, compared with traditional still reaction, reaction temperature
Degree is stablized, and the production cycle is substantially reduced, and improves production environment, energy-saving consumption-reducing, and product yield improves 20% or more；
3) condensation reaction and oxidation reaction have been all made of continuous reaction, and reaction condition is easy optimization, easy to implement automatic
Change and workshop labor, while shop safety is greatly saved in computer control, the overall process operation of realization 1-2 people workshop
It greatly improves；
4) condensation reaction and oxidation reaction have been all made of chip seedpod of the lotus microreactor, and occupation area of equipment is greatly decreased, several
The hundreds of even occupation of land of thousands of sides of the alternative former autoclave of chip seedpod of the lotus microreactor area of ten square meters, it is very easy to expand production；
5) using continuous process residues of formaldehyde is greatly decreased, dioxygen water consumption is also reduced, pollutant total release
It is greatly reduced, wastewater flow rate only has 30% of still reaction or so.
Description of the drawings
Fig. 1 is continuous production 2,2- dihydromethyl propionic acid process flow charts of the present invention；
Fig. 2 is chip seedpod of the lotus microreactor structural schematic diagram of the present invention；
Wherein：1, reacting pipe；2, hot water pipeline；3, cold water pipes；4, supporting base material；5, seedpod of the lotus distributor；
Fig. 3 is seedpod of the lotus dispensing arrangement figure of the present invention；
Wherein：Dimensional units are millimeter；
Fig. 4 is seedpod of the lotus distributor of the present invention in reacting pipe position schematic diagram；
Wherein：Dimensional units are millimeter.
Specific implementation mode
Embodiment 1
As shown in Figs. 1-2, by aqueous catalyst solution, positive propionic aldehyde solution, each personal positive battery metering pump of formalin by design
Flow squeeze into serialgram decline reactor carry out continuous condensating reaction.It is 5 to be condensed chip microreactor, and the flow velocity of each solution is pressed
1m/s is carried out, the flow Q of catalystCatalyst=526.00L/h；The flow Q of formaldehydeFormaldehyde=442.20L/h；The flow of positive propionic aldehyde
QPositive propionic aldehyde=162.80L/h.The flow of formic acid is QFormic acid=6.50L/h；It is 80 DEG C to control condensation temp.Hydrogen peroxide respectively uses boost gauge
Amount pump squeeze into serialgram decline reactor carry out continuous oxidation reaction.It is 7 to aoxidize chip microreactor, the flow of hydrogen peroxide
QHydrogen peroxide=220.95L/h；The content of hydrogen peroxide is 35%.Control 90 DEG C of oxidizing temperature.Oxidation product is again through economic benefits and social benefits continuous evaporation
2,2- dihydromethyl propionic acid crude products obtained by crystallization, centrifugal dehydration.Again (iron, decoloration, filtering, crystallization, centrifugation and bipyramid are removed through refined
Rotary vacuum dryer and sieving etc.) processing, obtain 2,2- dihydromethyl propionic acid products.Centrifuge mother liquor is further recycled.
It is 85.88% relative to positive propionic aldehyde molar product yield.
Embodiment 2
Using the equipment of embodiment 1, condensation chip microreactor is 5, and the flow velocity of each solution is carried out by 0.3m/s, catalysis
The flow Q of agentCatalyst=157.80L/h；The flow Q of formaldehydeFormaldehyde=132.66L/h；The flow Q of positive propionic aldehydePositive propionic aldehyde=48.84L/h.
The flow of formic acid is QFormic acid=2.00L/h；It is 75 DEG C to control condensation temp.Hydrogen peroxide positive battery metering pump squeezes into serialgram and declines
Reactor carries out continuous oxidation reaction.It is 7 to aoxidize chip microreactor, the flow Q of hydrogen peroxideHydrogen peroxide=66.30L/h；Dioxygen
The content of water is 35%, controls 85 DEG C of oxidizing temperature.Oxidation product is again through 2,2- obtained by economic benefits and social benefits continuous evaporative crystallization, centrifugal dehydration
Dihydromethyl propionic acid crude product.Again (iron, decoloration, filtering, crystallization, centrifugation and double conic rotary vacuum dryer and sieving are removed through refined
Deng) processing, obtain 2,2- dihydromethyl propionic acid products.Centrifuge mother liquor is further recycled.Relative to positive propionic aldehyde molar product
Yield is 83.80%.
Embodiment 3
Using the equipment of embodiment 1, condensation chip microreactor is 5, and the flow velocity of each solution is carried out by 0.6m/s, catalysis
The flow Q of agentCatalyst=315.60L/h；The flow Q of formaldehydeFormaldehyde=265.32L/h；The flow Q of positive propionic aldehydePositive propionic aldehyde=97.68L/h.
The flow of formic acid is QFormic acid=4.00L/h；It is 90 DEG C to control condensation temp.Hydrogen peroxide positive battery metering pump squeezes into serialgram and declines
Reactor carries out continuous oxidation reaction.It is 8 to aoxidize chip microreactor, and the flow velocity of two solution is carried out by 0.6m/s, hydrogen peroxide
Flow QHydrogen peroxide=132.57L/h；The content of hydrogen peroxide is 35%, controls 90 DEG C of oxidizing temperature.Oxidation product connects through economic benefits and social benefits again
2,2- dihydromethyl propionic acid crude products obtained by continuous evaporative crystallization, centrifugal dehydration.Again through refined (except iron, decoloration, filtering, crystallization, centrifugation
And double conic rotary vacuum dryer and sieving etc.) processing, obtain 2,2- dihydromethyl propionic acid products.Centrifuge mother liquor further recycles
Processing.It is 87.60% relative to positive propionic aldehyde molar product yield.
Embodiment 4
Using the equipment of embodiment 1, condensation chip microreactor is 5, and the flow velocity of each solution is carried out by 0.8m/s, catalysis
The flow Q of agentCatalyst=420.80L/h；The flow Q of formaldehydeFormaldehyde=353.76L/h；The flow Q of positive propionic aldehydePositive propionic aldehyde=130.24L/h.
The flow of formic acid is QFormic acid=5.20L/h；It is 80 DEG C to control condensation temp.Hydrogen peroxide positive battery metering pump squeezes into serialgram and declines
Reactor carries out continuous oxidation reaction.It is 8 to aoxidize chip microreactor, and the flow velocity of two solution is carried out by 0.8m/s, hydrogen peroxide
Flow QHydrogen peroxide=176.76L/h；The content of hydrogen peroxide is 35%, controls 85 DEG C of oxidizing temperature.Oxidation product connects through economic benefits and social benefits again
2,2- dihydromethyl propionic acid crude products obtained by continuous evaporative crystallization, centrifugal dehydration.Again through refined (except iron, decoloration, filtering, crystallization, centrifugation
And double conic rotary vacuum dryer and sieving etc.) processing, obtain 2,2- dihydromethyl propionic acid products.Centrifuge mother liquor further recycles
Processing.It is 84.6% relative to positive propionic aldehyde molar product yield.
Finally, it should also be noted that it is listed above be only the present invention several specific embodiments.Obviously, this hair
Bright to be not limited to above example, acceptable there are many deformations.Those skilled in the art can be from present disclosure
All deformations for directly exporting or associating, are considered as protection scope of the present invention.
Claims (2)
1. one kind 2, the continuous production device and technique of 2- dihydromethyl propionic acids, it is characterised in that：The continuous production device by
Raw material storage tank, metering pump, the first chip seedpod of the lotus microreactor, condensation liquid collecting tank, the second chip seedpod of the lotus microreactor, economic benefits and social benefits connect
Continuous crystallizing evaporator, recrystallization kettle, centrifuge, double conic rotary vacuum dryer and vibrating screen composition；Described first, second
Formula seedpod of the lotus microreactor is composed in series by 5~6,6~8 stage piece formula seedpod of the lotus microreactors respectively；In chip seedpod of the lotus microreactor
Reacting pipe, hot water pipeline and cold water pipes be arranged at the centre of supporting base material, in being laid with back and forth, between equal in reacting pipe
Away from setting seedpod of the lotus distributor；The seedpod of the lotus distributor is by single tube group seedpod of the lotus shape in pairs, between the both ends end face single tube of the seedpod of the lotus
Distance 8mm, the diameter 20mm of end face, consistent with reacting pipe, the height of the single head seedpod of the lotus is 360mm, two lotuses in reacting pipe
The spacing of fluffy distributor is 500mm；
The technique：
The positive propionic aldehyde solution of aqueous catalyst solution, 99wt%, 37wt% formaldehyde are molten to be continuously entered in the first chip seedpod of the lotus microreactor,
Continuous condensating in reacting pipe；Bottom discharge pipeline and 85wt% formic acid pipe of the condensation product in the first chip seedpod of the lotus microreactor
Road communicates, and after premixing, neutralization reaction is carried out into the condensation liquid collecting tank stirred with 85wt% formic acid for condensation product,
Thereafter it is carried out continuously oxidation with reacting pipe of the hydrogen peroxide in the second chip seedpod of the lotus microreactor；Oxidation product enters economic benefits and social benefits
Continuous evaporating crystallizer condensing crystallizing using filter, removes iron, decoloration, concentration, crystallization, filtering, drying and sieving processing, obtains
2,2- dihydromethyl propionic acids；Filtrated stock recycles 2,2- dihydromethyl propionic acids therein through reprocessing；
The condensation course：Na in aqueous catalyst solution2CO3：The mass ratio of water is 1：16；Aqueous catalyst solution, formaldehyde it is molten warp and
Positive propionic aldehyde dissolves into the flow into the first chip seedpod of the lotus microreactor：526.00L/h, 442.20L/h, 162.80L/h, stream
Speed control is in 0.3~1.2 m/s；Reaction temperature is 70~100 DEG C, and pressure is 0.2~0.6MPa, and the time is 15~30s；
The N-process：The formic acid of 85wt% is squeezed into formic acid pipeline with the flow of 6.50 L/h, keeps it mixed with condensation product
It closes, neutralize；
The oxidation process：The flow velocity that condensation liquid after neutralization presses 0.3~1.2m/s with 35wt% hydrogen peroxide enters the second chip
Seedpod of the lotus microreactor, flow are respectively 1137.50L/h, 220.95L/h, and reaction temperature is 70~100 DEG C, and pressure 0.2~
0.6MPa, 15~30s of time.
2. one kind 2, the continuous production device and technique of 2- dihydromethyl propionic acids, it is characterised in that：The micro- reaction of the chip seedpod of the lotus
Supporting base material is 304 stainless steels in device, and reacting pipe, seedpod of the lotus distributor, hot water pipeline and cold water pipe are 316 stainless steels.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110305003A (en) * | 2019-08-02 | 2019-10-08 | 昆山复希工程技术有限公司 | A kind of process using microreactor continuous production 2,2- dihydromethyl propionic acid |
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| CN1473142A (en) * | 2000-11-08 | 2004-02-04 | �����ɷ� | Method for producing poly-or monomethylol alkanoic acids |
| CN101381300A (en) * | 2008-10-14 | 2009-03-11 | 山东轻工业学院 | Method for synthesizing 2,2-bis(hydroxymenthyl)propinonic acid |
| CN102911038A (en) * | 2012-10-30 | 2013-02-06 | 李先明 | Preparation method of 2,2-dimethylolpropionic acid |
| CN103242154A (en) * | 2013-04-27 | 2013-08-14 | 杭州同禾化工技术开发有限公司 | Preparation method of 2,2-dimethylolpropionic acid |
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2018
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| JPS62263141A (en) * | 1986-05-08 | 1987-11-16 | Mitsubishi Chem Ind Ltd | Production of 2,2-bis(hydroxymethyl)alkanoic acid |
| CN1473142A (en) * | 2000-11-08 | 2004-02-04 | �����ɷ� | Method for producing poly-or monomethylol alkanoic acids |
| CN101381300A (en) * | 2008-10-14 | 2009-03-11 | 山东轻工业学院 | Method for synthesizing 2,2-bis(hydroxymenthyl)propinonic acid |
| CN102911038A (en) * | 2012-10-30 | 2013-02-06 | 李先明 | Preparation method of 2,2-dimethylolpropionic acid |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110305003A (en) * | 2019-08-02 | 2019-10-08 | 昆山复希工程技术有限公司 | A kind of process using microreactor continuous production 2,2- dihydromethyl propionic acid |
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