CN109988066A - A kind of n-butyl acrylate industrialized producing technology reducing brine waste - Google Patents
A kind of n-butyl acrylate industrialized producing technology reducing brine waste Download PDFInfo
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- CN109988066A CN109988066A CN201910026129.2A CN201910026129A CN109988066A CN 109988066 A CN109988066 A CN 109988066A CN 201910026129 A CN201910026129 A CN 201910026129A CN 109988066 A CN109988066 A CN 109988066A
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- butyl acrylate
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/08—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
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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
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
- C07C67/56—Separation; Purification; Stabilisation; Use of additives by solid-liquid treatment; by chemisorption
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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 Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
The invention discloses a kind of n-butyl acrylate industrialized producing technologies for reducing brine waste.Esterification, obtain n-butyl acrylate crude product after extraction and recovery catalyst, the subsequent treatment process of the n-butyl acrylate crude product is the following steps are included: (1), drying tower are dry；N-butyl acrylate crude product is transferred in the drying tower equipped with molecular sieve, 60-180 min is stopped, n-butyl acrylate crude product is dried；(2), it in solid alkaline tower and deacidifies: n-butyl acrylate crude product after drying being passed through the solid alkaline tower that solid alkaline material is housed, the control residence time is 30-180 min, deacidify to n-butyl acrylate crude product: (3) take off frivolous repurified: by carrying out taking off frivolous repurified with the n-butyl acrylate crude product after deacidification in solid alkaline tower, final n-butyl acrylate can be obtained.The n-butyl acrylate industrialized producing technology of reduction brine waste of the invention has the characteristics that environmentally protective technique, strong applicability, product purity are high and low in cost.
Description
Technical field
The present invention relates to n-butyl acrylate technical field, the n-butyl acrylate industry of specially a kind of hyposaline waste water
Metaplasia production. art.
Background technique
Butyl acrylate is a kind of ten general polymer monomers of application.The production technology of current esters of acrylic acid both domestic and external
Mainly Reppe method, BASF crude acrylic acid direct esterification acrylic acid ester process and Celanese acrylate production technology.Three
Kind technique respectively has advantage and disadvantage, and BASF crude acrylic acid direct esterification acrylic acid ester process is low to ingredient requirement, Celanese propylene
There is acid esters production technology BA and unreacted n-butanol to consume low, the lower advantage of energy consumption.Its shortcoming is that device is general
Property is poor, can only produce a kind of product of butyl ester.Reppe method mature technology, device is versatile, can be according to the market demand at any time
Various esters products are produced due to raw material propylene acid and butanol ample supply of commodities on the market at home, are easy buying, therefore domestic at present
N-butyl acrylate production technology be substantially using BASF crude acrylic acid direct esterification acrylic acid ester process technique, pass through
Highly developed reliable after the running and improvement of domestic many years, no matter the indices such as material consumption, energy consumption are in n-butyl acrylate
Production in all in leading position, safe and environment-friendly aspect is all reliable, and product competitiveness is also relatively strong.But it is domestic at present
Containing washing neutralizing zone in the technique used, the purpose of process is to remove unreacted acrylic acid and the neutralization of remaining catalyst
It goes, but the waste water for generating higher saliferous usually most consumes energy greatly currently, the processing for brine waste is very difficult simultaneously,
It is translated into solids treatment.By taking 80,000 tons/year of n-butyl acrylate production as an example, about 8000 tons of saliferous will be generated every year
Waste water.All there is this technique in the main n-butyl acrylate producers such as magnificent friendship chemical industry domestic at present, Jurong chemical industry, satellite petrochemical industry.
Summary of the invention
The object of the present invention is to provide a kind of n-butyl acrylate industrialized producing technologies of hyposaline waste water, have technique
Feature environmentally protective, product purity is high and low in cost.
The present invention can be achieved through the following technical solutions:
The invention discloses a kind of n-butyl acrylate industrialized producing technologies of hyposaline waste water, in esterification, extract back
N-butyl acrylate crude product is obtained after receiving catalyst, the subsequent treatment process of the n-butyl acrylate crude product includes following
Step:
(1), drying tower is dry；N-butyl acrylate crude product is transferred in the drying tower equipped with molecular sieve, 60-180 is stopped
N-butyl acrylate crude product is dried in min；Moisture content after n-butyl acrylate crude product is dry requires≤
0.08wt%。
(2), it in solid alkaline tower and deacidifies: n-butyl acrylate crude product after drying is passed through equipped with solid alkaline
The solid alkaline tower of material, control residence time are 30-180 min, are deacidified to n-butyl acrylate crude product: through solid
The free acid (with acrylic acid)≤0.01% of his rear n-butyl acrylate crude product of alkalinity.
(3) frivolous repurified is taken off: by being taken off in solid alkaline tower with the n-butyl acrylate crude product after deacidification
Final n-butyl acrylate can be obtained in frivolous repurified.
Further, the dry multilevel drying tower that is provided with of step (1) drying tower carries out non-stop run and regeneration.
Further, the n-butyl acrylate crude product is pre-chilled before being transferred into solid alkaline tower from drying tower
Processing, precooling temperature≤20 DEG C.Drying+pre-cooling can prevent the n-butyl acrylate generated hydrolysis, improve raw material availability.
Further, temperature≤30 DEG C of the solid alkaline tower.N-butyl acrylate hydrolysis under lower than 30 degree
Very slowly, the decomposition of finished product is prevented by controlling temperature.
Further, the solid alkaline object of the solid alkaline tower filling is selected from resin anion (R.A.), calcium hydroxide, hydrogen-oxygen
Change one or both of magnesium.
Further, the molecular sieve is 4A molecular sieve.
Further, the condition of the esterification are as follows: acrylic acid and n-butanol, at 90-110 DEG C, catalyst (methyl sulphur
Acid or p-methyl benzenesulfonic acid), residence time 30-60min.
Further, the reaction condition of the extraction and recovery are as follows: use water to make as extraction, extracted at lower than 40 DEG C
Catalyst in reaction mixture, the catalyst being obtained by extraction are reused.
Further, in the specific processing step for taking off frivolous repurified, n-butyl acrylate it is de- gently vacuum (-
Under 0.08Mpa), unreacted n-butanol is removed at 96 DEG C of kettle temperature；De- to focus under vacuum (- 0.08Mpa), kettle temperature is under 112 degree
Remove polymer.
A kind of n-butyl acrylate industrialized producing technology of hyposaline waste water of the present invention, have it is following the utility model has the advantages that
The first, technique is environmentally protective, generally generates high concentration saliferous in washing neutralization procedure relative to existing industrialization process
The thick ester of n-butyl acrylate after washing is mainly passed through in specific solid alkaline tower by waste water, this technique, carries out neutralization reaction,
Acidic materials in crude product are precipitated and separate with liquid, and whole process does not generate brine waste, and technique is environmentally protective；
The second, product purity is high, the crude product after drying tower is dry and solid alkaline tower neutralizing acid again through it is conventional it is de- it is light,
Purity >=99.5%, the n-butyl acrylate product of free acid (with acrylic acid)≤0.01 are obtained after weight-removing column；
Third, low in cost, compared with conventional acrylic N-butyl, present invention process does not generate alkaline waste water, makes Sewage treatment
Tower load is reduced, and waste water salt content greatly reduces.This technique and have significant economy and environmental benefit, be easy to prior art and
Equipment can produce after being transformed.
Specific embodiment
In order that those skilled in the art will better understand the technical solution of the present invention, below with reference to embodiment and to this
Invention product is described in further detail.
The invention discloses a kind of n-butyl acrylate industrialized producing technologies of hyposaline waste water, in esterification, extraction
It fetches and obtains n-butyl acrylate crude product after receiving catalyst, the subsequent treatment process of the n-butyl acrylate crude product includes
Following steps:
(1), drying tower is dry；N-butyl acrylate crude product is transferred in the drying tower equipped with molecular sieve, 60-180 is stopped
N-butyl acrylate crude product is dried in min；Moisture content after n-butyl acrylate crude product is dry requires≤
0.08wt%。
(2), it in solid alkaline tower and deacidifies: n-butyl acrylate crude product after drying is passed through equipped with solid alkaline
The solid alkaline tower of material, control residence time are 30-180 min, are deacidified to n-butyl acrylate crude product: through solid
The free acid (with acrylic acid)≤0.01% of his rear n-butyl acrylate crude product of alkalinity.
(3) frivolous repurified is taken off: by being taken off in solid alkaline tower with the n-butyl acrylate crude product after deacidification
Final n-butyl acrylate can be obtained in frivolous repurified.
Further, the dry multilevel drying tower that is provided with of step (1) drying tower carries out non-stop run and regeneration.
Further, the n-butyl acrylate crude product is pre-chilled before being transferred into solid alkaline tower from drying tower
Processing, precooling temperature≤20 DEG C.Drying+pre-cooling can prevent the n-butyl acrylate generated hydrolysis, improve raw material availability.
Further, temperature≤30 DEG C of the solid alkaline tower.N-butyl acrylate hydrolysis under lower than 30 degree
Very slowly, the decomposition of finished product is prevented by controlling temperature.
Further, the solid alkaline object of the solid alkaline tower filling is selected from resin anion (R.A.), calcium hydroxide, hydrogen-oxygen
Change one or both of magnesium.
Further, the molecular sieve is 4A molecular sieve.
Further, the condition of the esterification are as follows: acrylic acid and n-butanol, at 90-110 DEG C, catalyst (methyl sulphur
Acid or p-methyl benzenesulfonic acid), residence time 30-60min.
Further, the reaction condition of the extraction and recovery are as follows: use water to make as extraction, extracted at lower than 40 DEG C
Catalyst in reaction mixture, the catalyst being obtained by extraction are reused.
Further, in the specific processing step for taking off frivolous repurified, n-butyl acrylate it is de- gently vacuum (-
Under 0.08Mpa), unreacted n-butanol is removed at 96 DEG C of kettle temperature；De- to focus under vacuum (- 0.08Mpa), kettle temperature is under 112 degree
Remove polymer.
Embodiment 1
The invention discloses a kind of n-butyl acrylate industrialized producing technologies of hyposaline waste water, in esterification, extract back
N-butyl acrylate crude product is obtained after receiving catalyst, the subsequent treatment process of the n-butyl acrylate crude product includes following
Step:
(1), drying tower is dry；N-butyl acrylate crude product is transferred in the drying tower equipped with molecular sieve, stops 180
N-butyl acrylate crude product is dried in min；Moisture content after n-butyl acrylate crude product is dry requires≤
0.08wt%。
(2), it in solid alkaline tower and deacidifies: n-butyl acrylate crude product after drying is passed through equipped with solid alkaline
The solid alkaline tower of material, control residence time are 105 min, are deacidified to n-butyl acrylate crude product: through solid base
Property he after n-butyl acrylate crude product free acid (with acrylic acid)≤0.01%.
(3) frivolous repurified is taken off: by being taken off in solid alkaline tower with the n-butyl acrylate crude product after deacidification
Final n-butyl acrylate can be obtained in frivolous repurified.
In the present embodiment, the dry multilevel drying tower that is provided with of step (1) drying tower carries out non-stop run and regeneration.Institute
It states before n-butyl acrylate crude product is transferred into solid alkaline tower from drying tower and carries out precooling treatment, precooling temperature≤20
℃.Drying+pre-cooling can prevent the n-butyl acrylate generated hydrolysis, improve raw material availability.The temperature of the solid alkaline tower
≤ 30 DEG C of degree.N-butyl acrylate hydrolysis under lower than 30 degree is very slow, prevents point of finished product by controlling temperature
Solution.The solid alkaline object of the solid alkaline tower filling is resin anion (R.A.).The molecular sieve is 4A molecular sieve.The esterification is anti-
The condition answered are as follows: acrylic acid and n-butanol, at 90 DEG C, catalyst (methane sulfonic acid or p-methyl benzenesulfonic acid), residence time 60min.
The reaction condition of the extraction and recovery are as follows: use water to make as extraction, carry out urging in extraction reaction mixture at lower than 40 DEG C
Agent, the catalyst being obtained by extraction are reused.In the specific processing step for taking off frivolous repurified, n-butyl acrylate is de-
Gently at vacuum (- 0.08Mpa), unreacted n-butanol is removed at 96 DEG C of kettle temperature；It is de- to focus under vacuum (- 0.08Mpa), kettle temperature
It is to remove polymer at 112 DEG C.
Embodiment 2
The invention discloses a kind of n-butyl acrylate industrialized producing technologies of hyposaline waste water, in esterification, extract back
N-butyl acrylate crude product is obtained after receiving catalyst, the subsequent treatment process of the n-butyl acrylate crude product includes following
Step:
(1), drying tower is dry；N-butyl acrylate crude product is transferred in the drying tower equipped with molecular sieve, stops 120
N-butyl acrylate crude product is dried in min；Moisture content after n-butyl acrylate crude product is dry requires≤
0.08wt%。
(2), it in solid alkaline tower and deacidifies: n-butyl acrylate crude product after drying is passed through equipped with solid alkaline
The solid alkaline tower of material, control residence time are 30 min, are deacidified to n-butyl acrylate crude product: through solid alkaline
The free acid (with acrylic acid)≤0.01% of n-butyl acrylate crude product after him.
(3) frivolous repurified is taken off: by being taken off in solid alkaline tower with the n-butyl acrylate crude product after deacidification
Final n-butyl acrylate can be obtained in frivolous repurified.
In the present embodiment, the dry multilevel drying tower that is provided with of step (1) drying tower carries out non-stop run and regeneration.Institute
It states before n-butyl acrylate crude product is transferred into solid alkaline tower from drying tower and carries out precooling treatment, precooling temperature≤20
℃.Drying+pre-cooling can prevent the n-butyl acrylate generated hydrolysis, improve raw material availability.The temperature of the solid alkaline tower
≤ 30 DEG C of degree.N-butyl acrylate hydrolysis under lower than 30 degree is very slow, prevents point of finished product by controlling temperature
Solution.The solid alkaline object of the solid alkaline tower filling is calcium hydroxide.The molecular sieve is 4A molecular sieve.The esterification
Condition are as follows: acrylic acid and n-butanol, at 110 DEG C, catalyst (methane sulfonic acid or p-methyl benzenesulfonic acid), residence time 45min.
The reaction condition of the extraction and recovery are as follows: use water to make as extraction, carry out urging in extraction reaction mixture at lower than 40 DEG C
Agent, the catalyst being obtained by extraction are reused.In the specific processing step for taking off frivolous repurified, n-butyl acrylate is de-
Gently at vacuum (- 0.08Mpa), unreacted n-butanol is removed at 96 DEG C of kettle temperature；It is de- to focus under vacuum (- 0.08Mpa), kettle temperature
It is to remove polymer at 112 DEG C.
Embodiment 3
The invention discloses a kind of n-butyl acrylate industrialized producing technologies of hyposaline waste water, in esterification, extract back
N-butyl acrylate crude product is obtained after receiving catalyst, the subsequent treatment process of the n-butyl acrylate crude product includes following
Step:
(1), drying tower is dry；N-butyl acrylate crude product is transferred in the drying tower equipped with molecular sieve, 60 min are stopped,
N-butyl acrylate crude product is dried；Moisture content requirement≤0.08wt% after n-butyl acrylate crude product is dry.
(2), it in solid alkaline tower and deacidifies: n-butyl acrylate crude product after drying is passed through equipped with solid alkaline
The solid alkaline tower of material, control residence time are 180 min, are deacidified to n-butyl acrylate crude product: through solid base
Property he after n-butyl acrylate crude product free acid (with acrylic acid)≤0.01%.
(3) frivolous repurified is taken off: by being taken off in solid alkaline tower with the n-butyl acrylate crude product after deacidification
Final n-butyl acrylate can be obtained in frivolous repurified.
In the present embodiment, the dry multilevel drying tower that is provided with of step (1) drying tower carries out non-stop run and regeneration.Institute
It states before n-butyl acrylate crude product is transferred into solid alkaline tower from drying tower and carries out precooling treatment, precooling temperature≤20
℃.Drying+pre-cooling can prevent the n-butyl acrylate generated hydrolysis, improve raw material availability.The temperature of the solid alkaline tower
≤ 30 DEG C of degree.N-butyl acrylate hydrolysis under lower than 30 degree is very slow, prevents point of finished product by controlling temperature
Solution.The solid alkaline object of the solid alkaline tower filling is magnesium hydroxide.The molecular sieve is 4A molecular sieve.The esterification
Condition are as follows: acrylic acid and n-butanol, at 100 DEG C, catalyst (methane sulfonic acid or p-methyl benzenesulfonic acid), residence time 30min.
The reaction condition of the extraction and recovery are as follows: use water to make as extraction, carry out urging in extraction reaction mixture at lower than 40 DEG C
Agent, the catalyst being obtained by extraction are reused.In the specific processing step for taking off frivolous repurified, n-butyl acrylate is de-
Gently at vacuum (- 0.08Mpa), unreacted n-butanol is removed at 96 DEG C of kettle temperature；It is de- to focus under vacuum (- 0.08Mpa), kettle temperature
It is to remove polymer at 112 DEG C.
Embodiment 4
The invention discloses a kind of n-butyl acrylate industrialized producing technologies of hyposaline waste water, in esterification, extract back
N-butyl acrylate crude product is obtained after receiving catalyst, the subsequent treatment process of the n-butyl acrylate crude product includes following
Step:
(1), drying tower is dry；N-butyl acrylate crude product is transferred in the drying tower equipped with molecular sieve, stops 100
N-butyl acrylate crude product is dried in min；Moisture content after n-butyl acrylate crude product is dry requires≤
0.08wt%。
(2), it in solid alkaline tower and deacidifies: n-butyl acrylate crude product after drying is passed through equipped with solid alkaline
The solid alkaline tower of material, control residence time are 100 min, are deacidified to n-butyl acrylate crude product: through solid base
Property he after n-butyl acrylate crude product free acid (with acrylic acid)≤0.01%.
(3) frivolous repurified is taken off: by being taken off in solid alkaline tower with the n-butyl acrylate crude product after deacidification
Final n-butyl acrylate can be obtained in frivolous repurified.
In the present embodiment, the dry multilevel drying tower that is provided with of step (1) drying tower carries out non-stop run and regeneration.Institute
It states before n-butyl acrylate crude product is transferred into solid alkaline tower from drying tower and carries out precooling treatment, precooling temperature≤20
℃.Drying+pre-cooling can prevent the n-butyl acrylate generated hydrolysis, improve raw material availability.The temperature of the solid alkaline tower
≤ 30 DEG C of degree.N-butyl acrylate hydrolysis under lower than 30 degree is very slow, prevents point of finished product by controlling temperature
Solution.The solid alkaline object of the solid alkaline tower filling is resin anion (R.A.), calcium hydroxide, magnesium hydroxide.The molecular sieve is
4A molecular sieve.The condition of the esterification are as follows: acrylic acid and n-butanol, at 95 DEG C, catalyst (methane sulfonic acid or to toluene sulphur
Acid), residence time 40min.The reaction condition of the extraction and recovery are as follows: use water to make as extraction, carried out at lower than 40 DEG C
The catalyst in reaction mixture is extracted, the catalyst being obtained by extraction is reused.The specific processing for taking off frivolous repurified
In step, n-butyl acrylate is de- gently at vacuum (- 0.08Mpa), removes unreacted n-butanol at 96 DEG C of kettle temperature；It is de- to focus on
Under vacuum (- 0.08Mpa), kettle temperature is to remove polymer at 112 DEG C.
Application Example 1
After esterification, n-butyl acrylate (n-butyl acrylate=85%, moisture content=1.5%, trip through water phase extracting catalyst
From acid=0.3%) it is passed into drying tower, dry tower diameter is 20cm, long 3m, residence time 200min, then will be after drying
Material cools to 20 oC through heat exchanger, and is sent into solid washing tower (for removing CO2), and washing tower (for removing CO2) diameter is 20cm, and long 3m, residence time 200min are obtained
To crude acrylic acid N-butyl (n-butyl acrylate=85%, moisture content=0.03%, free acid=0.005%), hyposaline in the process
Waste water.By obtained crude product through it is conventional take off frivolous repurified after to obtain content be 99.8%, moisture content 0.03%, free acid
0.01% product.Wherein washing tower (for removing CO2) uses macroporous strong-base type phenylethylene resin series；Drying tower uses 4A molecular sieve.
Application Example 2
After esterification, n-butyl acrylate (n-butyl acrylate=82%, moisture content=1.3%, trip through water phase extracting catalyst
From acid=0.4%) it is passed into drying tower, dry tower diameter is 20cm, long 3m, residence time 150min, then will be after drying
Material cools to 20 oC through heat exchanger, and is sent into solid washing tower (for removing CO2), and washing tower (for removing CO2) diameter is 20cm, and long 3m, residence time 150min are obtained
To crude acrylic acid N-butyl (n-butyl acrylate=82%, moisture content=0.04%, free acid=0.008%), hyposaline in the process
Waste water.By obtained crude product through it is conventional take off frivolous repurified after to obtain content be 99.7%, moisture content 0.03%, free acid≤
0.01% product.
Application Example 3
After esterification, n-butyl acrylate (n-butyl acrylate=80%, moisture content=1.5%, trip through water phase extracting catalyst
From acid=0.3%) it is passed into drying tower, dry tower diameter is 20cm, long 3m, residence time 150min, then will be after drying
Material cools to 20 oC through heat exchanger, and is sent into solid washing tower (for removing CO2), and washing tower (for removing CO2) diameter is 20cm, and long 3m, residence time 60min are obtained
To crude acrylic acid N-butyl (n-butyl acrylate=80%, moisture content=0.05%, free acid=0.01%), hyposaline is useless in the process
Water.By obtained crude product through it is conventional take off frivolous repurified after to obtain content be 99.5%, moisture content 0.03%, free acid≤
0.01% product.
The foregoing is only a preferred embodiment of the present invention, is not intended to limit the present invention in any form；It is all
The those of ordinary skill of the industry can be shown in by specification and described above and swimmingly implement the present invention；But it is all familiar
Professional and technical personnel without departing from the scope of the present invention, makes using disclosed above technology contents
A little variation, modification and evolution equivalent variations, be equivalent embodiment of the invention；Meanwhile all realities according to the present invention
The variation, modification and evolution etc. of matter technology any equivalent variations to the above embodiments, still fall within technology of the invention
Within the protection scope of scheme.
Claims (7)
1. a kind of n-butyl acrylate industrialized producing technology for reducing brine waste, in esterification, extraction and recovery catalyst
After obtain n-butyl acrylate crude product, it is characterised in that: the subsequent treatment process of the n-butyl acrylate crude product includes
Following steps:
(1), drying tower is dry；N-butyl acrylate crude product is transferred in the drying tower equipped with molecular sieve, 60-180 is stopped
N-butyl acrylate crude product is dried in min；
(2), it in solid alkaline tower and deacidifies: n-butyl acrylate crude product after drying is passed through equipped with solid alkaline material
Solid alkaline tower, the control residence time be 30-180 min, deacidify to n-butyl acrylate crude product:
(3) frivolous repurified is taken off: frivolous take off by the n-butyl acrylate crude product in solid alkaline tower and after deacidification
Final n-butyl acrylate can be obtained in repurified.
2. the n-butyl acrylate industrialized producing technology according to claim 1 for reducing salt waste water, it is characterised in that: step
Suddenly the dry multilevel drying tower that is provided with of (1) drying tower carries out non-stop run and regeneration.
3. the n-butyl acrylate industrialized producing technology according to claim 2 for reducing brine waste, it is characterised in that:
The n-butyl acrylate crude product carries out precooling treatment, precooling temperature≤20 before being transferred into solid alkaline tower from drying tower
℃。
4. the n-butyl acrylate industrialized producing technology according to claim 3 for reducing brine waste, it is characterised in that:
Temperature≤30 DEG C of the solid alkaline tower.
5. reducing the n-butyl acrylate industrialized producing technology of brine waste according to claim 4, it is characterised in that: institute
The solid alkaline object of solid alkaline tower filling is stated selected from one or both of resin anion (R.A.), calcium hydroxide, magnesium hydroxide.
6. the n-butyl acrylate industrialized producing technology according to claim 4 or 5 for reducing brine waste, feature exist
In: the molecular sieve is 4A molecular sieve.
7. reducing the n-butyl acrylate industrialized producing technology of brine waste according to claim 6, it is characterised in that: institute
Moisture content requirement≤0.08wt% after stating crude product drying；After washing tower (for removing CO2) the free acid (with acrylic acid) of crude product≤
0.01%。
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Cited By (1)
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| CN110937997A (en) * | 2019-12-09 | 2020-03-31 | 东营海德新材料有限公司 | Production process for improving purity of butyl acrylate |
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| CN206473977U (en) * | 2017-02-23 | 2017-09-08 | 铜仁学院 | Organic amine dehydration device and dewatering system |
| CN108689381A (en) * | 2018-06-26 | 2018-10-23 | 武汉轻工大学 | A kind of area of refinery oil loading platform gas recovery system for oil and its recovery method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110937997A (en) * | 2019-12-09 | 2020-03-31 | 东营海德新材料有限公司 | Production process for improving purity of butyl acrylate |
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