CN208898769U - Acyl chlorides product production system - Google Patents
Acyl chlorides product production system Download PDFInfo
- Publication number
- CN208898769U CN208898769U CN201821615481.7U CN201821615481U CN208898769U CN 208898769 U CN208898769 U CN 208898769U CN 201821615481 U CN201821615481 U CN 201821615481U CN 208898769 U CN208898769 U CN 208898769U
- Authority
- CN
- China
- Prior art keywords
- pipeline
- tank
- chloride
- film
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 28
- 150000001263 acyl chlorides Chemical class 0.000 title claims abstract description 21
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 49
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 48
- DGMOBVGABMBZSB-UHFFFAOYSA-N 2-methylpropanoyl chloride Chemical compound CC(C)C(Cl)=O DGMOBVGABMBZSB-UHFFFAOYSA-N 0.000 claims abstract description 46
- 238000004821 distillation Methods 0.000 claims abstract description 33
- ONIKNECPXCLUHT-UHFFFAOYSA-N 2-chlorobenzoyl chloride Chemical compound ClC(=O)C1=CC=CC=C1Cl ONIKNECPXCLUHT-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000007788 liquid Substances 0.000 claims abstract description 21
- 238000010521 absorption reaction Methods 0.000 claims description 59
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 40
- PASDCCFISLVPSO-UHFFFAOYSA-N benzoyl chloride Chemical compound ClC(=O)C1=CC=CC=C1 PASDCCFISLVPSO-UHFFFAOYSA-N 0.000 claims description 15
- 210000003298 dental enamel Anatomy 0.000 claims description 8
- 229910002804 graphite Inorganic materials 0.000 claims description 7
- 239000010439 graphite Substances 0.000 claims description 7
- 238000003860 storage Methods 0.000 claims description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 6
- 239000000463 material Substances 0.000 abstract description 36
- 238000006243 chemical reaction Methods 0.000 abstract description 21
- 238000000034 method Methods 0.000 abstract description 17
- KQNPFQTWMSNSAP-UHFFFAOYSA-N isobutyric acid Chemical compound CC(C)C(O)=O KQNPFQTWMSNSAP-UHFFFAOYSA-N 0.000 abstract description 12
- XEMRAKSQROQPBR-UHFFFAOYSA-N (trichloromethyl)benzene Chemical compound ClC(Cl)(Cl)C1=CC=CC=C1 XEMRAKSQROQPBR-UHFFFAOYSA-N 0.000 abstract description 11
- 238000009835 boiling Methods 0.000 abstract description 10
- 238000000926 separation method Methods 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 abstract description 3
- 239000002699 waste material Substances 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 24
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 12
- 238000010992 reflux Methods 0.000 description 12
- VGCXGMAHQTYDJK-UHFFFAOYSA-N Chloroacetyl chloride Chemical compound ClCC(Cl)=O VGCXGMAHQTYDJK-UHFFFAOYSA-N 0.000 description 10
- 239000003054 catalyst Substances 0.000 description 8
- 238000001514 detection method Methods 0.000 description 8
- 239000007789 gas Substances 0.000 description 8
- 239000012043 crude product Substances 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 6
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 6
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 6
- 238000010792 warming Methods 0.000 description 6
- 239000013058 crude material Substances 0.000 description 4
- 238000003912 environmental pollution Methods 0.000 description 4
- 239000004615 ingredient Substances 0.000 description 4
- 125000000959 isobutyl group Chemical group [H]C([H])([H])C([H])(C([H])([H])[H])C([H])([H])* 0.000 description 3
- -1 isobutyryl Chemical group 0.000 description 3
- 238000012797 qualification Methods 0.000 description 3
- 239000002841 Lewis acid Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- KRCSBYPKUJAPSQ-UHFFFAOYSA-N benzene formyl chloride Chemical compound C(=O)Cl.C1=CC=CC=C1 KRCSBYPKUJAPSQ-UHFFFAOYSA-N 0.000 description 2
- KCXMKQUNVWSEMD-UHFFFAOYSA-N benzyl chloride Chemical compound ClCC1=CC=CC=C1 KCXMKQUNVWSEMD-UHFFFAOYSA-N 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000010408 film Substances 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 150000007517 lewis acids Chemical group 0.000 description 2
- XHXFXVLFKHQFAL-UHFFFAOYSA-N phosphoryl trichloride Chemical compound ClP(Cl)(Cl)=O XHXFXVLFKHQFAL-UHFFFAOYSA-N 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- FDRCDNZGSXJAFP-UHFFFAOYSA-M sodium chloroacetate Chemical compound [Na+].[O-]C(=O)CCl FDRCDNZGSXJAFP-UHFFFAOYSA-M 0.000 description 2
- FYSNRJHAOHDILO-UHFFFAOYSA-N thionyl chloride Chemical compound ClS(Cl)=O FYSNRJHAOHDILO-UHFFFAOYSA-N 0.000 description 2
- VFWCMGCRMGJXDK-UHFFFAOYSA-N 1-chlorobutane Chemical compound CCCCCl VFWCMGCRMGJXDK-UHFFFAOYSA-N 0.000 description 1
- MTJGVAJYTOXFJH-UHFFFAOYSA-N 3-aminonaphthalene-1,5-disulfonic acid Chemical compound C1=CC=C(S(O)(=O)=O)C2=CC(N)=CC(S(O)(=O)=O)=C21 MTJGVAJYTOXFJH-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- AFCIMSXHQSIHQW-UHFFFAOYSA-N [O].[P] Chemical compound [O].[P] AFCIMSXHQSIHQW-UHFFFAOYSA-N 0.000 description 1
- HFBMWMNUJJDEQZ-UHFFFAOYSA-N acryloyl chloride Chemical compound ClC(=O)C=C HFBMWMNUJJDEQZ-UHFFFAOYSA-N 0.000 description 1
- 125000003236 benzoyl group Chemical group [H]C1=C([H])C([H])=C(C([H])=C1[H])C(*)=O 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical class ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to acyl chlorides product production systems, including crude synthesis reactor, it is connected to by pipeline with dropping tank above the crude synthesis reactor, the first destilling tower is equipped at the top of the crude synthesis reactor, it is sequentially connected at the top of first destilling tower by pipeline and the first condenser, gas-liquid separator, collecting tank, the gas-liquid separator bottom is by pipeline by being connected at the top of return valve and the first destilling tower.Using isobutyric acid and benzotrichloride as raw material, isobutyryl chloride and chlorobenzoyl chloride product are produced using coproduction scheme, carry out distillation separation, in crude heating synthesis process, reaction is continuously generated low boiling material (isobutyryl chloride), it is increased with synthesis temperature, low boiling material (isobutyryl chloride) is largely evaporated, and is gradually separated and collected product (isobutyryl chloride), using same set of equipment, be conducive to material sufficiently to react, finished product can be distilled rapidly to obtain by generating isobutyryl chloride.The utility model has the advantages that process route is simple, easy to operate, " three wastes " discharge amount is few.
Description
Technical field
The utility model relates to organic compound preparation method field, especially a kind of acyl chlorides product production system.
Background technique
Isobutyryl chloride is also known as: chlorination isobutyryl, 2- methyl propionyl chloride,
Its purposes is very extensive, is used as organic synthesis intermediate, is the raw material for producing efficient photoinitiator PI-906, PI-907.
Conventional isobutyryl chloride preparation process is to use isobutyric acid in the presence of a catalyst, is carried out with thionyl chloride or phosphorus oxychloride acylated anti-
It answers, after the reaction was completed, using distillating method by isobutyryl chloride distilation, obtains product, react residual chloride sulfoxide or trichlorine oxygen
Phosphorus and waste liquid are handled with water decomposition, and wastewater flow rate is big, and environmental pollution is serious, and reaction process is complicated for operation.
Summary of the invention
In order to overcome aforesaid operations complicated, problem that environmental pollution is serious.The utility model provides a kind of acyl chlorides production
System carries out isobutyryl chloride production using co-production, and in the synthesis process, isobutyryl chloride is constantly steamed, qualification is obtained
Product, one step of the method can obtain qualified isobutyryl chloride, do not need synthesis after again rectifying collect isobutyryl chloride, it is easy to operate,
Loss of material is small, non-environmental-pollution.
In order to solve the above technical problems, the technical scheme adopted by the utility model is:
A kind of acyl chlorides product production system, including crude synthesis reactor, the crude synthesis reactor top is by pipeline and is added dropwise
Tank connection, the crude synthesis reactor top are equipped with the first destilling tower, pass through pipeline and the first condensation at the top of first destilling tower
Device, gas-liquid separator, collecting tank are sequentially connected, and return valve and the first destilling tower are passed through by pipeline in the gas-liquid separator bottom
Top connection.
Preferably, the collecting tank is isobutyryl chloride collecting tank.
Preferably, the gas-liquid separator is connected to by pipeline with film-falling absorption tower, the falling film absorption tower bottom and salt
Sour tourie connection, the top film-falling absorption tower are connected to by circulating pump with absorption by Hydrochloric Acid tank, and the film-falling absorption tower passes through
Pipeline is connected to oil-sealed rotary pump.
It is further preferred that two film-falling absorption towers are connected in series there are two the film-falling absorption tower sets.
It is further preferred that the collecting tank is enamel storage tank, the absorption by Hydrochloric Acid tank volume is 25m3；The falling liquid film
Absorption tower is graphite film-falling absorption tower, volume 20m2, the circulation pump power is 3KW.
Preferably, the crude synthesis reactor is connected to benzoyl chloride distillation pot by pipeline by pipeline, the benzoyl
After-fractionating tower is equipped at the top of chlorine distillation still, the after-fractionating top of tower is connected to by pipeline with the second condenser, and described the
Two condensers pass through respectively pipeline with before evaporate tank, chlorobenzoyl chloride finished pot is connected to, tank is evaporated before described and passes through pipeline and crude synthesis
Kettle connection.
Using the technique of the system production isobutyryl chloride, response path is as follows:
The technique the following steps are included:
1) benzotrichloride is put into crude synthesis reactor, catalyst is added, is warming up to 90-120 DEG C, dropping tank starts to drip
After adding isobutyric acid, reaction to start, material uses infinite reflux in the first destilling tower when having material to start to be evaporated in the first destilling tower
Operation, after reacting 30 minutes, material regurgitant volume increases, and reduces reflux ratio, and sample detection isobutyryl chloride content (isobutyryl chloride
90.9 DEG C of boiling point), start to collect isobutyryl chloride after reaching quality standards, benzotrichloride is ensured using continuous backflow during collecting
Finished product is not brought into chlorobenzoyl chloride；
2) hydrogen chloride gas of reaction production is absorbed using two-stage film-falling absorption tower, and absorption prepares hydrochloric acid；
3) the crude material in reactor of sample detection, which reaches, after having reacted goes to chlorobenzoyl chloride distillation after crude product quality requires
Kettle (10) distillation；
4), benzoyl chloride distillation pot distills initial stage, and by material collection to before evaporating in tank, ingredient is isobutyryl chloride and benzene first
Acyl chlorides mixed material is collected after distillation to chlorobenzoyl chloride qualification to chlorobenzoyl chloride finished pot；
5) mixed material collected in tank is evaporated before and is brought into crude synthesis reactor in next batch is distilled separation again
Processing；
The technique for completing isobutyryl chloride.
It is further preferred that the step 1) catalyst is lewis acid, the step 1) is warming up to 90-120 DEG C, institute
Stating step 1) quality standard is that isobutyryl chloride content is greater than 99.00%.
It is further preferred that the step 3) crude product quality requires to be material in reactor benzotrichloride≤0.3%, isobutyl
Acid≤0.5%；Step 4) the benzoyl chloride distillation pot distillation initial stage is chlorobenzoyl chloride content less than 99.00%.
The system can also be used in the production that the boiling points such as chloracetyl chloride, chloroacetic chloride or acryloyl chloride are less than crude synthesis temperature
Product production.
The utility model has following technical effect that
1, the utility model is suitable for acyl chlorides system product production of the boiling temperature within 120 DEG C.With isobutyric acid and three
Chlorotoluene is raw material, produces isobutyryl chloride and chlorobenzoyl chloride product using coproduction scheme, carries out distillation separation, crude heating synthesis
In the process, reaction is continuously generated low boiling material (isobutyryl chloride), increases with synthesis temperature, and low boiling material (isobutyryl chloride) is big
Amount evaporation, gradually separates and collects product (isobutyryl chloride), using same set of equipment, this reaction is closed at 100-120 DEG C
At synthesis temperature is more than isobutyryl chloride material evaporation temperature, and material is constantly evaporated discharge during the reaction, is conducive to object
Material sufficiently reaction, finished product can be distilled rapidly to obtain by generating isobutyryl chloride.The utility model have process route it is simple, it is easy to operate,
Prepare the advantage that facility is few, " three wastes " discharge amount is few.
2, corresponding acyl chlorides and chlorobenzoyl chloride under the action of catalyst with benzotrichloride and organic acid, can be synthesized, in order to
Two different acyl chlorides products are more preferably separated, are separated using distillation, distillation separation selection boiling temperature differs larger, ability
It efficiently separates.
3, the utility model carries out isobutyryl chloride production using co-production, and in the synthesis process, not by isobutyryl chloride
It is disconnected to steam, qualified products are obtained, one step of the method can obtain qualified isobutyryl chloride, not need after synthesis that isobutyl is collected in rectifying again
Acyl chlorides, easy to operate, loss of material is small, non-environmental-pollution.
4, a dropping tank is installed on crude synthesis reactor, controls reaction speed, in the case where controlling temperature conditions, is uniformly dripped
Add, guarantees stable reaction.
5, on crude synthesis reactor, condenser is repacked into first destilling tower, top of tower installs the first condenser, carries out object
Reflux is collected in material condensation, and the isobutyryl chloride for reacting generation directly distills collection.
6, gas-liquid separator is installed in condenser, gas phase is discharged into followed by absorption.The installation of gas-liquid separator lower part
Return valve flows back.Return valve is installed on the first destilling tower, according to control of product quality reflux size, guarantees product
It is up-to-standard.
7, according to crude synthesis input quantity, an isobutyryl chloride collecting tank is installed, carries out the collection of isobutyryl chloride product.
8, hydrochloric acid is made using film-falling absorption tower absorption in tail gas hydrogen chloride gas, using oil-sealed rotary pump to whole system shape
At micro-vacuum.
Detailed description of the invention
The utility model is described in further detail with reference to the accompanying drawings and examples:
Fig. 1 is the structural schematic diagram of the utility model.
In figure: crude synthesis reactor 1, dropping tank 2, the first destilling tower 3, the first condenser 4, gas-liquid separator 5, collecting tank 6,
Return valve 7, benzoyl chloride distillation pot 8, after-fractionating tower 9, the second condenser 10 are preceding to evaporate tank 11, chlorobenzoyl chloride finished pot 12, drop
Film absorption tower 13, oil-sealed rotary pump 14, circulating pump 16.
Specific embodiment
Embodiment 1
A kind of acyl chlorides product production system, including crude synthesis reactor 1 pass through pipeline and drop above the crude synthesis reactor 1
Add tank 2 to be connected to, be equipped with the first destilling tower 3 at the top of the crude synthesis reactor 1, passes through pipeline and the at the top of first destilling tower 3
One condenser 4, gas-liquid separator 5, collecting tank 6 are sequentially connected, and return valve 7 is passed through by pipeline in 5 bottom of gas-liquid separator
It is connected to at the top of the first destilling tower 3.
Preferably, the collecting tank 6 is isobutyryl chloride collecting tank.
Preferably, the gas-liquid separator 5 is connected to by pipeline with film-falling absorption tower 13,13 bottom of film-falling absorption tower
Portion is connected to absorption by Hydrochloric Acid tank 15, and the top film-falling absorption tower 13 is connected to by circulating pump 16 with absorption by Hydrochloric Acid tank 15, described
Film-falling absorption tower 13 is connected to by pipeline with oil-sealed rotary pump 14.
It is further preferred that two film-falling absorption towers 13 are connected in series there are two the film-falling absorption tower 13 sets.
It is further preferred that the collecting tank 6 is enamel storage tank, 15 volume of absorption by Hydrochloric Acid tank is 25m3；It is described
Film-falling absorption tower 13 is graphite film-falling absorption tower, volume 20m2, 16 power of circulating pump is 3KW.
Preferably, the crude synthesis reactor 1 is connected to benzoyl chloride distillation pot 8 by pipeline by pipeline, the benzene first
It is equipped with after-fractionating tower 9 at the top of acyl chlorides distillation still 8, is connected to by pipeline with the second condenser 10 at the top of the after-fractionating tower 9,
Second condenser 10 respectively by pipeline with before evaporate tank 11, chlorobenzoyl chloride finished pot 12 is connected to, tank 11 is evaporated before described and is passed through
Pipeline is connected to crude synthesis reactor 1.
Embodiment 2
A kind of acyl chlorides product production system, including crude synthesis reactor 1 pass through pipeline and drop above the crude synthesis reactor 1
Add tank 2 to be connected to, be equipped with the first destilling tower 3 at the top of the crude synthesis reactor 1, passes through pipeline and the at the top of first destilling tower 3
One condenser 4, gas-liquid separator 5, collecting tank 6 are sequentially connected, and return valve 7 is passed through by pipeline in 5 bottom of gas-liquid separator
It is connected to at the top of the first destilling tower 3.
Preferably, the collecting tank 6 is isobutyryl chloride collecting tank.
Preferably, the gas-liquid separator 5 is connected to by pipeline with film-falling absorption tower 13,13 bottom of film-falling absorption tower
Portion is connected to absorption by Hydrochloric Acid tank 15, and the top film-falling absorption tower 13 is connected to by circulating pump 16 with absorption by Hydrochloric Acid tank 15, described
Film-falling absorption tower 13 is connected to by pipeline with oil-sealed rotary pump 14.
It is further preferred that two film-falling absorption towers 13 are connected in series there are two the film-falling absorption tower 13 sets.
It is further preferred that the collecting tank 6 is enamel storage tank, 15 volume of absorption by Hydrochloric Acid tank is 25m3；It is described
Film-falling absorption tower 13 is graphite film-falling absorption tower, volume 20m2, 16 power of circulating pump is 3KW.
Preferably, the crude synthesis reactor 1 is connected to benzoyl chloride distillation pot 8 by pipeline by pipeline, the benzene first
It is equipped with after-fractionating tower 9 at the top of acyl chlorides distillation still 8, is connected to by pipeline with the second condenser 10 at the top of the after-fractionating tower 9,
Second condenser 10 respectively by pipeline with before evaporate tank 11, chlorobenzoyl chloride finished pot 12 is connected to, tank 11 is evaporated before described and is passed through
Pipeline is connected to crude synthesis reactor 1.
Using the technique of the system production isobutyryl chloride, response path is as follows:
The technique the following steps are included:
1) benzotrichloride is put into crude synthesis reactor 1, catalyst is added, is warming up to 90-120 DEG C, dropping tank 2 is opened
Begin that isobutyric acid is added dropwise, after reaction starts, material is used in first destilling tower 3 when having material to start to be evaporated in the first destilling tower 3
Total reflux operation, after reacting 30 minutes, material regurgitant volume increases, and reduces reflux ratio, and sample detection isobutyryl chloride content is (different
90.9 DEG C of butyl chloride boiling point), start to collect isobutyryl chloride after reaching quality standards, ensures three using continuous backflow during collecting
Chlorotoluene and chlorobenzoyl chloride do not bring finished product into；
2) hydrogen chloride gas of reaction production is absorbed using two-stage film-falling absorption tower 13, and absorption prepares hydrochloric acid；
3) the crude material in reactor of sample detection, which reaches, after having reacted goes to chlorobenzoyl chloride distillation after crude product quality requires
Kettle 10 distills；
4), benzoyl chloride distillation pot distills initial stage, and by material collection to before evaporating 11 in tank, ingredient is isobutyryl chloride and benzene
Formyl chloride mixed material is collected after distillation to chlorobenzoyl chloride qualification to chlorobenzoyl chloride finished pot 12；
5) mixed materials that 11 collect are evaporated in tank before and are brought into crude synthesis reactor 1 in next batch is distilled again point
From processing；
The technique for completing isobutyryl chloride.
It is further preferred that the step 1) catalyst is lewis acid, the step 1) is warming up to 90-120 DEG C, institute
Stating step 1) quality standard is that isobutyryl chloride content is greater than 99.00%.
It is further preferred that the step 3) crude product quality requires to be material in reactor benzotrichloride≤0.3%, isobutyl
Acid≤0.5%；Step 4) the benzoyl chloride distillation pot distillation initial stage is chlorobenzoyl chloride content less than 99.00%.
It is further preferred that the collecting tank 6 is enamel storage tank, 15 volume of absorption by Hydrochloric Acid tank is 25m3；It is described
Film-falling absorption tower 13 is graphite film-falling absorption tower, volume 20m2, 16 power of circulating pump is 3KW.
The crude synthesis reactor 1 is connected to benzoyl chloride distillation pot 8 by pipeline by pipeline, the chlorobenzoyl chloride distillation
It is equipped with after-fractionating tower 9 at the top of kettle 8, is connected to by pipeline with the second condenser 10 at the top of the after-fractionating tower 9, described second
Condenser 10 respectively by pipeline with before evaporate tank 11, chlorobenzoyl chloride finished pot 12 be connected to, evaporated before described tank 11 by pipeline with slightly
Synthesis reactor 1 processed is connected to.The crude synthesis reactor 1 uses 2000L enamel reaction still, and dropping tank 2 uses 1000L polypropylene plastics
Tank, the first destilling tower 3 use enamel tower, and the first condenser 4 uses 20m2Graphite condenser, reflux control use glass valves
Door control reflux size, collecting tank 6 use 2000L enamel storage tank, and absorption by Hydrochloric Acid uses a fiberglass-reinforced glass storage tank 25m3, two
Graphite film-falling absorption tower 20m2An and 3KW HCl solution circulating pump.Gas-liquid separator is installed in condenser, after gas phase is discharged into
Face is absorbed.5 lower part of gas-liquid separator installation return valve 7 flows back.Benzotrichloride is put into crude synthesis reactor 1
Catalyst is added in 1850kg, is warming up to 100 DEG C, and isobutyric acid is added dropwise, and rate of addition is determined according to reaction condition, until drop
It adds into.Dropwise reaction initial stage, material use infinite reflux, and sample detection isobutyryl chloride content, start after reaching quality standards
Isobutyryl chloride is collected, ensures that benzotrichloride does not bring finished product into using continuous backflow during collecting.React the hydrogen chloride gas of production
Body is absorbed using two-stage serous coat absorption tower, and absorption prepares hydrochloric acid.Insulation reaction after dropwise reaction is complete, isobutyryl chlorine dose in kettle
Infinite reflux is used when less, guarantees that the product collected is qualified.The crude material in reactor content of sample detection, reaches after having reacted
Crude product quality goes to benzoyl chloride distillation pot distillation after requiring.Benzoyl chloride distillation pot distills initial stage, by material collection to before evaporating
In tank, ingredient is isobutyryl chloride and chlorobenzoyl chloride mixed material, distillation to chlorobenzoyl chloride it is qualified after collect to chlorobenzoyl chloride at
Product tank.Mixed material is brought into crude synthesis reactor in next batch and is handled.
Embodiment 3
Chloracetyl chloride production is carried out using system described in embodiment 1:
1) monoxone is put into crude synthesis reactor 1, catalyst is added, be warming up to 90-120 DEG C, dropping tank 2 starts
Benzotrichloride is added dropwise, after reaction starts, has the generation of chloracetyl chloride material, as reaction temperature increases, has material to start to be evaporated to
Material uses total reflux operation in first destilling tower 3 when in the first destilling tower 3, and after reaction temperature is more than 105 DEG C, material is returned
Flow increases, and reduces reflux ratio, and sample detection chloracetyl chloride content (105 DEG C of chloracetyl chloride boiling point), reaches quality standards
Start to collect chloracetyl chloride after (chloracetyl chloride content is greater than 99.00%), three chloromethanes are ensured using continuous backflow during collecting
Benzene and chlorobenzoyl chloride do not bring finished product into；
2) hydrogen chloride gas of reaction production is absorbed using two-stage film-falling absorption tower 13, and absorption prepares hydrochloric acid；
3) the crude material in reactor of sample detection reaches crude product quality and requires that (benzotrichloride content is less than after having reacted
0.30%, monoxone is distilled less than benzoyl chloride distillation pot 10 is gone to after 0.50%)；
4), benzoyl chloride distillation pot distills initial stage, and by material collection to before evaporating 11 in tank, ingredient is chloracetyl chloride and benzene
Formyl chloride mixed material, distillation to chlorobenzoyl chloride qualified (chlorobenzoyl chloride content is greater than 99.00%) collect afterwards to chlorobenzoyl chloride at
Product tank 12；
5) mixed materials that 11 collect are evaporated in tank before and are brought into crude synthesis reactor 1 in next batch is distilled again point
From processing；
The technique for completing chloracetyl chloride.
Claims (6)
1. a kind of acyl chlorides product production system, including crude synthesis reactor (1), it is characterised in that: above the crude synthesis reactor (1)
It is connected to by pipeline with dropping tank (2), is equipped with the first destilling tower (3) at the top of the crude synthesis reactor (1), first destilling tower
(3) top is sequentially connected by pipeline with the first condenser (4), gas-liquid separator (5), collecting tank (6), the gas-liquid separator
(5) bottom is by pipeline by being connected at the top of return valve (7) and the first destilling tower (3).
2. acyl chlorides product production system according to claim 1, it is characterised in that: the collecting tank (6) is isobutyryl chloride
Collecting tank.
3. acyl chlorides product production system according to claim 1, it is characterised in that: the gas-liquid separator (5) passes through pipe
Road is connected to film-falling absorption tower (13), and film-falling absorption tower (13) bottom is connected to absorption by Hydrochloric Acid tank (15), the top drop
Film absorption tower (13) is connected to by circulating pump (16) with absorption by Hydrochloric Acid tank (15), and the film-falling absorption tower (13) passes through pipeline and machine
Tool vacuum pump (14) connection.
4. acyl chlorides product production system according to claim 3, it is characterised in that: the film-falling absorption tower (13) is equipped with two
A, two film-falling absorption towers (13) are connected in series.
5. acyl chlorides product production system according to claim 3, it is characterised in that: the collecting tank (6) is enamel storage
Tank, the film-falling absorption tower (13) are graphite film-falling absorption tower.
6. acyl chlorides product production system according to claim 1, it is characterised in that: the crude synthesis reactor (1) passes through pipe
Road is connected to benzoyl chloride distillation pot (8) by pipeline, is equipped with after-fractionating tower (9) at the top of the benzoyl chloride distillation pot (8),
It is connected to by pipeline with the second condenser (10) at the top of the after-fractionating tower (9), second condenser (10) passes through respectively
Pipeline with before evaporate tank (11), chlorobenzoyl chloride finished pot (12) is connected to, tank (11) are evaporated before described and pass through pipeline and crude synthesis reactor (1)
Connection.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821615481.7U CN208898769U (en) | 2018-09-30 | 2018-09-30 | Acyl chlorides product production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821615481.7U CN208898769U (en) | 2018-09-30 | 2018-09-30 | Acyl chlorides product production system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208898769U true CN208898769U (en) | 2019-05-24 |
Family
ID=66574747
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201821615481.7U Active CN208898769U (en) | 2018-09-30 | 2018-09-30 | Acyl chlorides product production system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208898769U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109081778A (en) * | 2018-09-30 | 2018-12-25 | 宜都市友源实业有限公司 | A kind of acyl chlorides product production system and technique |
-
2018
- 2018-09-30 CN CN201821615481.7U patent/CN208898769U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109081778A (en) * | 2018-09-30 | 2018-12-25 | 宜都市友源实业有限公司 | A kind of acyl chlorides product production system and technique |
| CN109081778B (en) * | 2018-09-30 | 2023-10-27 | 宜都市友源实业有限公司 | System and process for producing acyl chloride product |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102079512B (en) | Process for recovering sulfuric acid and sulfate from waste acid generated in preparation of titanium dioxide by using sulfuric acid method | |
| CN104973638B (en) | Processing technology of high-salt high-concentration organic waste liquid | |
| CN105693585B (en) | A kind of separation N-Methyl pyrrolidone/chloroform system and method | |
| CN211445385U (en) | Contain organic solvent's salt waste water evaporation equipment | |
| CN109081778A (en) | A kind of acyl chlorides product production system and technique | |
| CN208898769U (en) | Acyl chlorides product production system | |
| CN112374967A (en) | System and method for recovering ethanol from organic waste liquid | |
| CN104311382B (en) | The method of monochloroethane is prepared by chlorination byproduct hydrogen chloride | |
| CN103539763B (en) | A kind of Reaction Separation coupling technique by dichlorohydrin continuous production epoxychloropropane | |
| CN106379952A (en) | Apparatus and process for treating ammonia nitrogen wastewater and recycling ammonia | |
| CN107899261A (en) | Standardize low-temperature evaporation equipment | |
| CN108479653A (en) | Integral microchannels reaction unit and utilization device preparation two-（2- chloroethyls）The method of di-phosphate ester | |
| CN110330418B (en) | Method for recovering formaldehyde gas volatilized in normal pressure device in pentaerythritol production | |
| CN207722395U (en) | Standardize low-temperature evaporation equipment | |
| CN215137004U (en) | Continuous rectification and purification device for nitromethane | |
| CN212403459U (en) | Deep analytical equipment of olefine acid concentration | |
| CN210434014U (en) | Novel trinity rectifying column apparatus for producing of industry hydrogen peroxide solution enrichment facility | |
| US3870606A (en) | Process for preparing heavy water from sea water | |
| CN205501169U (en) | System for separation N - methyl 2 pyrrolidone chloroform | |
| CN107055550A (en) | A kind of method for preparing dichlororosilane eiectronic grade | |
| CN106744720A (en) | The circulation recycling system and its operation process of trichloroacetaldehyde by-product dilute sulfuric acid | |
| CN220559183U (en) | 3-methoxy-N, N-dimethyl propionamide production system | |
| CN105237399B (en) | The reactive distillation process of heavy constituent residual liquid in a kind of carbonylation production process of acetic acid | |
| CN216571620U (en) | Device for purifying 5-chloro-1-indanone by steam distillation | |
| CN218357428U (en) | Serial-type rectification recovery device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: Acyl chloride product production system Effective date of registration: 20220722 Granted publication date: 20190524 Pledgee: Bank of China Limited by Share Ltd. Three Gorges Branch Pledgor: YIDU JOVIAN INDUSTRY CO.,LTD. Registration number: Y2022420000231 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Granted publication date: 20190524 Pledgee: Bank of China Limited by Share Ltd. Three Gorges Branch Pledgor: YIDU JOVIAN INDUSTRY CO.,LTD. Registration number: Y2022420000231 |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: Acyl chloride product production system Granted publication date: 20190524 Pledgee: Bank of China Limited by Share Ltd. Three Gorges Branch Pledgor: YIDU JOVIAN INDUSTRY CO.,LTD. Registration number: Y2024980026986 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right |