CN206014730U - A kind of phenylacetic acid continuous production device - Google Patents
A kind of phenylacetic acid continuous production device Download PDFInfo
- Publication number
- CN206014730U CN206014730U CN201621009762.9U CN201621009762U CN206014730U CN 206014730 U CN206014730 U CN 206014730U CN 201621009762 U CN201621009762 U CN 201621009762U CN 206014730 U CN206014730 U CN 206014730U
- Authority
- CN
- China
- Prior art keywords
- water
- phenylacetic acid
- continuous production
- production device
- crystallization kettle
- 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
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a kind of phenylacetic acid continuous production device, is related to phenylacetic acid production equipment technical field.Device includes liquid liquid mixer, water-oil separating tower, crystallization kettle；Wherein there are acid solution import and lye import respectively on liquid liquid mixer.Liquid liquid mixer is connected with position in the tower of water-oil separating tower, water-oil separating tower have oil phase outlet with water mutually export and tower in filler is installed, oil phase outlet is connected with crystallization kettle, crystallization kettle once water water inlet and crystalline product outlet, has stirring and temperature-reducing coil in crystallization kettle.Can realize that phenylacetic acid is continuously produced using this device, production efficiency is high, the artificial of needs is lacked, and labour intensity is low, and process is simplified, few using equipment.
Description
Technical field
The utility model is related to phenylacetic acid production equipment technical field.
Background technology
Phenylacetic acid is colorless plate crystal, and 76.5 DEG C of fusing point is soluble in hot water, is slightly soluble in cold water, is in important medicine
Mesosome, the huge market demand., using the still reaction of interval, low production efficiency, needs set for existing production technology at present
Standby quantity is more, and the demand of operative employee is big.In the face of the chemical industry of high speed development, realize that the serialization of production becomes one kind and becomes
Gesture.
Utility model content
The utility model provides a kind of phenylacetic acid continuous production device, with can realize that phenylacetic acid continuously produces, produces
Efficiency high, needs artificial few, labour intensity is low, process is simplified, using equipment few the characteristics of.
A kind of phenylacetic acid continuous production device that the utility model is provided, including liquid liquid mixer 1,2 and of water-oil separating tower
Crystallization kettle 3；Described 1 one end of liquid liquid mixer has been provided with acid solution import 4 and lye import 5, the other end and the water-oil separating tower 2
Middle part be connected；The water-oil separating tower 2 includes tower body, tower body top be provided be connected with the crystallization kettle 3 for producing oil
The oil phase outlet 6 of phase phenylacetic acid, tower body bottom is provided with and mutually exports 7 for discharging the water of waste water, and inside is provided with filler 8, middle part
There is the device being connected with the liquid liquid mixer 1；The crystallization kettle 3 is additionally provided with a water inlet 9 and crystalline product outlet 10, interior
Portion has been provided with agitator 11 and temperature-reducing coil 12.
Further, filler 8 is installed inside 2 tower body of water-oil separating tower.
Preferably, described filler 8 is ceramic filler.
Preferably, 2 height of water-oil separating tower is 10m～40m.
Further, inside the liquid liquid mixer 1 it is helical fin formula structure.
Further, described crystallization kettle 3 also includes the penstock that can automatically control and blowing operated pneumatic valve.
Preferably, the pipeline for connecting the oil phase outlet 6 with the crystallization kettle 3 is utilidor.
Preferably, the heat exchange area of the temperature-reducing coil 12 is 20m2～40 m2.
Having the beneficial effect that produced by technical scheme described in the utility model：
A kind of phenylacetic acid continuous production device that the utility model is provided can realize that phenylacetic acid is continuously produced, production efficiency
Height, the artificial of needs lack, and labour intensity is low, and process is simplified, few using equipment.
Description of the drawings
Accompanying drawing 1 is device composition schematic diagram of the present utility model.
In above-mentioned accompanying drawing, mark corresponding relation is：1 liquid liquid mixer；2 water-oil separating towers；3 crystallization kettles；4 acid
Liquid import；5 lye imports；6 oil phases are exported；7 water are mutually exported；8 fillers；9 water inlets；10 crystalline products
Outlet；11 agitators；12 temperature-reducing coils.
Specific embodiment
With reference to the accompanying drawings and detailed description the utility model is described in further detail.
Refer to the attached drawing 1, a kind of phenylacetic acid continuous production device that the utility model is provided, one kind that the utility model is provided
Phenylacetic acid continuous production device, including liquid liquid mixer 1, water-oil separating tower 2 and crystallization kettle 3；Described 1 one end of liquid liquid mixer sets
There are acid solution import 4 and lye import 5, the other end to be connected with the middle part of the water-oil separating tower 2；The water-oil separating tower 2 is wrapped
Tower body is included, tower body top is provided with the oil phase for producing oil phase phenylacetic acid being connected with the crystallization kettle 3 and exports 6, tower body bottom
Being provided with and 7 mutually being exported for discharging the water of waste water, inside is provided with filler 8, and there is the dress being connected with the liquid liquid mixer 1 at middle part
Put；The crystallization kettle 3 is additionally provided with a water inlet 9 and crystalline product outlet 10, and inside has been provided with agitator 11 and temperature-reducing coil
12.
The diluted acid that reaction needs is continuously added to liquid liquid mixer 1 by acid solution import 4, the phenylacetate that reaction is needed
Alkaline feed liquid is continuously added to liquid liquid mixer 1 by lye import 5, and after reaction, reactant liquor enters oil under certain pressure conditions
Water separation column 2, oil phase and water are mutually separated under gravity, and heavy constituent salting liquid is mutually moved down, and mutually exports 7 by water
Cause waste water workshop to be processed, light component oil phase phenylacetic acid is moved up, crystallization kettle 3 is caused by oil phase outlet 6, while to knot
Water of injection in brilliant kettle 3, cooling under the stirring action of agitator 11 generation of the oil phase phenylacetic acid by temperature-reducing coil 12
The mixture of crystalline solid, crystalline solid and water isolates phenylacetic acid crystalline solid by 10 continuous extraction separator of crystalline product outlet,
The serialization of production technology is completed.
Filler 8 is installed inside 2 tower body of water-oil separating tower, oil phase and water are separated in the presence of filler 8
More abundant.
Described filler 8 is ceramic filler.
2 height of water-oil separating tower is 10m～40m.
It is helix tube type structure inside the liquid liquid mixer 1, its objective is to increase resistance, liquid liquid is fully contacted instead
Should.In a specific embodiment, helical curve fin in liquid liquid mixer 1, is provided with.
Described crystallization kettle 3 also includes the penstock that can automatically control and blowing operated pneumatic valve, in order to automatic
Change control, blowing operated pneumatic valve is located on the pipeline that water-oil separating tower 2 is connected with crystallization kettle 3.
The pipeline for connecting the oil phase outlet 6 with the crystallization kettle 3 is utilidor, to prevent oil phase phenylacetic acid from crystallizing.
The heat exchange area of the temperature-reducing coil 12 is 20m2～40 m2.
Those skilled in the art according to practical operation it needs to be determined that the size of each section of the device.
Embodiment：
In a specific embodiment, a diameter of 200 millimeters in liquid liquid mixer 1, the length of liquid liquid mixer 1 is 2
Rice, the height of water-oil separating tower 2 is 10 meters, and reactant liquor is fed by 5 meters of height of water-oil separating tower 2, and crystallization kettle 3 is 10 cubes
The open type retort of rice, built-in heat exchange area are 30 square meters.
Under the conditions of certain pressure, sodium phenylacetate solution is entered from the lye import 5 of liquid liquid mixer 1 with constant flow velocity
Enter, dilution heat of sulfuric acid is entered from acid solution import 4 with constant flow velocity, after reacting, reactant liquor is entered in water-oil separating tower 2 and divided
Phase, upper strata products benzene acetic acid oil phase enter crystallization kettle 3 from oil phase outlet 6, and lower floor's water mutually exports 7 discharges by water, enters useless
Between water treatment vehicle.Oil phase continuously enters crystallization kettle 3, from a 9 continuous moisturizing of water inlet, by controlling the circulation of temperature-reducing coil 12
The water yield controlling crystallization temperature, constantly goes to be centrifuged from 10 extraction of crystalline product outlet in the presence of agitator 11 by final feed liquid.
Whole device achieves phenylacetic acid and continuously produces.
By 30% sodium phenylacetate and 40% sulfuric acid according to 1:0.25 mass ratio is thrown in liquid liquid mixer 1 simultaneously
Material, the temperature control in liquid liquid mixer 1 are 70 DEG C～75 DEG C, and now in liquid liquid mixer 1, the pH of feed liquid is 1.5.Feed liquid is passed through
After crossing water-oil separating tower 2, the water continuously produced from tower reactor mutually enters into effluent treatment plant, and the oil phase of overhead extraction is continuously entered
Crystallization kettle 3.The mass ratio of the water phase and oil phase that enter crystallization kettle 3 is 1:2,3 temperature of open cycle water management crystallization kettle 35 DEG C～
40 DEG C, continuously enter centrifuge from the extraction of crystallization kettle 3 feed liquid.Whole production process adopts PLC automatic control system, it is achieved that benzene second
The continuous prodution of acid.Product yield reaches 99.75%, and product content is 99.91%, and product liquid phase purity is 99.83%.
A kind of phenylacetic acid continuous production device that the present embodiment is provided can realize that phenylacetic acid is continuously produced, production efficiency
Height, the artificial of needs lack, and labour intensity is low, and process is simplified, few using equipment.
Specific case used herein is set forth to the principle of the present invention and embodiment, and above example is said
Bright it is only intended to help and understands the method for the present invention and its core concept.It should be pointed out that the ordinary skill for the art
For personnel, under the premise without departing from the principles of the invention, some improvement and modification can also be carried out to the present invention, these improvement
Also fall in the protection domain of the claims in the present invention with modification.
Claims (8)
1. a kind of phenylacetic acid continuous production device, it is characterised in that including liquid liquid mixer（1）, water-oil separating tower（2）And crystallization
Kettle（3）；The liquid liquid mixer（1）One end has been provided with acid solution import（4）And lye import（5）, the other end and the profit point
From tower（2）Middle part be connected；The water-oil separating tower（2）Including tower body, tower body top is provided with and the crystallization kettle（3）Connected
Export for producing the oil phase of oil phase phenylacetic acid（6）, tower body bottom is provided with and mutually exports for discharging the water of waste water（7）, middle part has
With the liquid liquid mixer（1）Connected device；The crystallization kettle（3）It is additionally provided with a water inlet（9）Export with crystalline product
（10）, inside has been provided with agitator（11）And temperature-reducing coil（12）.
2. a kind of phenylacetic acid continuous production device according to claim 1, it is characterised in that the water-oil separating tower（2）
Filler is installed inside tower body（8）.
3. a kind of phenylacetic acid continuous production device according to claim 2, it is characterised in that described filler（8）For pottery
Structured packing.
4. a kind of phenylacetic acid continuous production device according to claim 1, it is characterised in that the water-oil separating tower（2）
Highly it is 10m～40m.
5. a kind of phenylacetic acid continuous production device according to claim 1, it is characterised in that the liquid liquid mixer（1）
Internal is helical fin formula structure.
6. a kind of phenylacetic acid continuous production device according to claim 1, it is characterised in that described crystallization kettle（3）Also
Including a penstock can automatically controlling and blowing operated pneumatic valve.
7. a kind of phenylacetic acid continuous production device according to claim 1, it is characterised in that the connection oil phase outlet
（6）With the crystallization kettle（3）Pipeline be utilidor.
8. a kind of phenylacetic acid continuous production device according to claim 1, it is characterised in that the temperature-reducing coil（12）'s
Heat exchange area is 20m2～40 m2.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621009762.9U CN206014730U (en) | 2016-08-31 | 2016-08-31 | A kind of phenylacetic acid continuous production device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621009762.9U CN206014730U (en) | 2016-08-31 | 2016-08-31 | A kind of phenylacetic acid continuous production device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206014730U true CN206014730U (en) | 2017-03-15 |
Family
ID=58255635
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201621009762.9U Active CN206014730U (en) | 2016-08-31 | 2016-08-31 | A kind of phenylacetic acid continuous production device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206014730U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113548954A (en) * | 2021-07-30 | 2021-10-26 | 四川信乙化工有限公司 | Phenylacetic acid preparation system |
| CN113548956A (en) * | 2021-07-30 | 2021-10-26 | 四川信乙化工有限公司 | Continuous production system of phenylacetic acid |
-
2016
- 2016-08-31 CN CN201621009762.9U patent/CN206014730U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113548954A (en) * | 2021-07-30 | 2021-10-26 | 四川信乙化工有限公司 | Phenylacetic acid preparation system |
| CN113548956A (en) * | 2021-07-30 | 2021-10-26 | 四川信乙化工有限公司 | Continuous production system of phenylacetic acid |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105623861B (en) | A kind of glycerine esterification reaction unit | |
| CN206014730U (en) | A kind of phenylacetic acid continuous production device | |
| CN102961984B (en) | Dissolution tank for drug level benzoic acid production and operation method | |
| CN109608353B (en) | Continuous production process and device for m-aminoacetanilide | |
| CN103242966A (en) | Technology process for producing biodiesel and key preparation device | |
| CN109011682A (en) | Manganese sulfate, zinc sulfate class material MVR system-specific crystallizing evaporator and method | |
| CN205152122U (en) | Methyl chloroacetate preparation facilities | |
| CN201969551U (en) | Separation kettle for producing T acid | |
| CN206372821U (en) | A kind of device for producing DOTP | |
| CN1900085A (en) | Trimethyl phosphite producing process | |
| CN209138035U (en) | Manganese sulfate, zinc sulfate class material MVR system-specific crystallizing evaporator | |
| CN208553201U (en) | A kind of crystallizer for ion-exchange-resin process synthesis of bisphenol A | |
| CN105272815A (en) | Method for extracting methylnaphthalene in C10 aromatics | |
| CN106365976B (en) | A kind of phenylacetic acid continuous production processes | |
| CN214680164U (en) | Automatic washing device for chloralkane | |
| CN107201685B (en) | The pilot production line and its technique of Cellulose nanocrystal are extracted from biomass resource | |
| CN205616574U (en) | Use coking desulfurization waste liquid to carry device of salt extraction filter residue as raw materials purification sodium hyposulfite | |
| CN201644079U (en) | Gas-liquid contact reactor | |
| CN207891285U (en) | Organic diammonium compound production line | |
| CN112062101A (en) | Energy-saving continuous sulfur melting device and process thereof | |
| CN206381687U (en) | A kind of two grades of gas-liquid separation purifiers for sulfonation workshop | |
| CN101941721B (en) | Technique for producing medicinal mirabilite by continuous crystallization | |
| CN104162389B (en) | Reactor for liquid-solid two-phase continuous reaction and on-line separation | |
| CN104945290B (en) | System for industrial preparation of 2-amino-5-naphtol7-sulfoacid | |
| CN206008090U (en) | A kind of static board-like melting crystallizer |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 051130 Yuanshi County, Shijiazhuang, Hebei Province, yuan Zhao Lunan Patentee after: Hebei Chengxin Group Co., Ltd. Address before: 051130 Yuanshi County, Shijiazhuang, Hebei Province, yuan Zhao Lunan Patentee before: Hebei Chengxin Co., Ltd. |
|
| CP01 | Change in the name or title of a patent holder |