CN211561855U - Chemical product purification system - Google Patents
Chemical product purification system Download PDFInfo
- Publication number
- CN211561855U CN211561855U CN201922188134.1U CN201922188134U CN211561855U CN 211561855 U CN211561855 U CN 211561855U CN 201922188134 U CN201922188134 U CN 201922188134U CN 211561855 U CN211561855 U CN 211561855U
- Authority
- CN
- China
- Prior art keywords
- evaporator
- receiving tank
- boiling
- liquid receiving
- product
- 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
Images
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model provides a chemical product purification system, which comprises a primary evaporator and a secondary evaporator which are arranged in sequence; the primary evaporator is simultaneously connected with a low-boiling condenser and a crude product liquid receiving tank; the low-boiling condenser is connected with a low-boiling liquid receiving tank, and a first return pipeline connected with the primary evaporator is arranged on a connecting pipeline between the low-boiling condenser and the low-boiling liquid receiving tank; the crude product liquid receiving tank is connected with the second-stage evaporator, and a second-stage evaporator cut-off valve is arranged on a connecting pipeline of the crude product liquid receiving tank and the second-stage evaporator. The utility model provides a rely on two-stage evaporator and auxiliary assembly's purification method is simple effective, can also can detach the impurity of high molecular weight with the impurity of desorption small molecular weight, and technical reliability is high, and the product quality of purifying is more stable.
Description
Technical Field
The invention belongs to the technical field of chemical production equipment, and particularly relates to a chemical product purification system.
Background
In the petrochemical production process, substances with different boiling points are purified by adopting a rectifying tower; for fine chemical production, acid-base or other adsorption filtration products are often used to purify the crude product. In the existing purification method, a method of distilling, condensing and slicing under a vacuum state is generally adopted to obtain a product with higher purity. Adding the chemical products into a distillation kettle, heating to melt, then pulling vacuum, evaporating the target products, and condensing and crystallizing to obtain the target products with high content. The tower equipment is not suitable for the purification of high-viscosity chemical products, and particularly, when acid-base or other adsorption filtration products are adopted to purify a crude product, waste liquid or waste solids can be generated, the treatment difficulty can be increased while the investment is increased, and the environment friendliness is not facilitated. Meanwhile, the temperature in the distillation process is as high as 150-; in the later stage of distillation, the heat exchange area is continuously reduced, the distillation efficiency is continuously reduced, the temperature is required to be continuously increased, and the material is coked, so that improvement is urgently needed.
Disclosure of Invention
In view of this, the present invention provides a chemical product purification system to overcome the defects in the prior art.
In order to achieve the purpose, the technical scheme of the invention is realized as follows:
a chemical product purification system comprises a primary evaporator and a secondary evaporator which are sequentially arranged; the primary evaporator is simultaneously connected with a low-boiling condenser and a crude product liquid receiving tank; the low-boiling condenser is connected with a low-boiling liquid receiving tank, and a first return pipeline connected with the primary evaporator is arranged on a connecting pipeline between the low-boiling condenser and the low-boiling liquid receiving tank; the crude product liquid receiving tank is connected with the secondary evaporator, and a secondary evaporator cut-off valve is arranged on a connecting pipeline of the crude product liquid receiving tank and the secondary evaporator;
the secondary evaporator is simultaneously connected with a product condenser and a high-boiling intermediate tank, the product condenser is connected with a product liquid receiving tank, and a connecting pipeline between the product condenser and the product liquid receiving tank is provided with a second return pipeline connected with the secondary evaporator; the product liquid receiving tank is connected with a normal pressure product intermediate tank.
Further, a low-boiling cut-off valve is arranged in front of the low-boiling liquid receiving tank.
Further, a product removing and liquid receiving tank stop valve is arranged before the product receiving tank.
Further, a barrel removing and cutting valve is arranged on a pipeline at the rear end of the high-boiling intermediate tank.
Furthermore, a third return pipeline is arranged between the crude product liquid receiving tank and the primary evaporator, and a primary evaporator cut-off valve is arranged in the third return pipeline.
Further, a fourth return pipeline is arranged between the high-boiling intermediate tank and the second-stage evaporator, and a second-stage evaporator cut-off valve is arranged in the fourth return pipeline.
Compared with the prior art, the invention has the following advantages:
the purification method provided by the invention is simple and effective, and can remove impurities with small molecular weight and impurities with high molecular weight. Meanwhile, continuous automatic operation can be realized, the temperature and the pressure are relatively stable, the technical reliability is high, and the quality of the purified product is more stable.
And moreover, the purification yield is high, the cost is low, the purification device does not need to be heated and cooled frequently when being used, the heat loss is small, the energy is saved, the labor consumption is reduced more effectively, waste acid, waste alkali and waste water are not generated, and the process is more environment-friendly.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and, together with the description, serve to explain the invention without limitation. In the drawings:
FIG. 1 is a schematic diagram of the inventive system;
fig. 2 is a schematic diagram of the work flow of the invention.
Description of reference numerals:
1-first-stage evaporator; 2-a secondary evaporator; 3-low boiling condenser; 4-crude product liquid receiving tank; 5-low boiling liquid receiving tank; 6-a first return line; 7-removing a second-stage evaporator cut-off valve; 8-product condenser; 9-high boiling intermediate tank; 10-product receiving tank; 11-a second return line; 12-normal pressure product intermediate tank; 13-removing a low-boiling cut-off valve; 14-removing a product and receiving a liquid tank stop valve; 15-removing the barreling stop valve; 16-a third return line; 17-removing a first-stage evaporator cut-off valve; 18-a fourth return line; 19-a second-stage evaporator cut-off valve.
Detailed Description
It should be noted that the embodiments and features of the embodiments of the present invention may be combined with each other without conflict.
In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are used in the orientation or positional relationship indicated in the drawings, which are merely for convenience in describing the invention and to simplify the description, and are not intended to indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be construed as limiting the invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the invention, the meaning of "a plurality" is two or more unless otherwise specified.
In the description of the invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted", "connected" and "connected" are to be construed broadly, e.g. as being fixed or detachable or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the creation of the present invention can be understood by those of ordinary skill in the art through specific situations.
The invention will be described in detail with reference to the following embodiments with reference to the attached drawings.
A chemical product purification system, as shown in FIG. 1 and FIG. 2, comprises a first-stage evaporator 1 and a second-stage evaporator 2 which are arranged in sequence;
the first-stage evaporator is simultaneously connected with a low-boiling condenser 3 and a crude product liquid receiving tank 4; the low-boiling condenser is connected with a low-boiling liquid receiving tank 5, a first return pipeline 6 connected with the primary evaporator is arranged on a connecting pipeline between the low-boiling condenser and the low-boiling liquid receiving tank, and the temperature of a return liquid phase of the primary evaporator is controlled by using a hot water return regulating valve as a controller;
the crude product liquid receiving tank is connected with the secondary evaporator, and a secondary evaporator cut-off valve 7 is arranged on a connecting pipeline of the crude product liquid receiving tank and the secondary evaporator; a low-boiling cut-off valve 13 is arranged in front of the low-boiling liquid receiving tank. In addition, a third return pipeline 16 is arranged between the crude product liquid receiving tank and the primary evaporator, and a primary evaporator cut-off valve 17 is arranged in the third return pipeline.
A crude product feeding regulating valve can be arranged in front of a crude product liquid inlet pipe to be used as a controller for controlling the feeding rate; a steam feeding regulating valve is arranged at the primary evaporator and used as a controller to control the liquid phase discharging temperature of the primary evaporator; the vacuum regulating valve can also be used for controlling the gas phase pressure of a primary system (consisting of the primary evaporator and corresponding auxiliary equipment) to maintain the vacuum stability of the system.
The secondary evaporator is simultaneously connected with a product condenser 8 and a high-boiling intermediate tank 9, the product condenser is connected with a product liquid receiving tank 10, and a connecting pipeline between the product condenser and the product liquid receiving tank is provided with a second return pipeline 11 connected with the secondary evaporator; the product liquid receiving tank is connected with a normal pressure product intermediate tank 12. A product removing and liquid receiving tank stop valve 14 is arranged before the product is connected with the liquid tank, and a barreling stop valve 15 is arranged on a pipeline at the rear end of the high-boiling intermediate tank.
In addition, a fourth return pipeline 18 is arranged between the high-boiling intermediate tank and the second-stage evaporator, and a second-stage evaporator cut-off valve 19 is arranged in the fourth return pipeline. The vacuum regulating valve can be used for controlling the gas phase pressure of a secondary system (consisting of the secondary evaporator and corresponding auxiliary equipment) to maintain the vacuum stability of the system.
The specific working process is as follows:
feeding the crude product into a first-stage evaporator; the first-stage evaporator uses steam as a heat source, the gas phase enters a low-boiling condenser, and the liquid phase enters a crude product intermediate tank;
the low-boiling condenser condenses low-boiling point substances, the condensate is closed to the low-boiling liquid-receiving tank cut-off valve at the early stage, the materials flow back to the primary evaporator completely, the condensate is opened to the low-boiling liquid-receiving tank cut-off valve only when the gas phase pressure and the gas phase temperature reach the required pressure and temperature, and the condensate is completely extracted to the low-boiling liquid-receiving tank at the moment; after the liquid level in the low-boiling liquid receiving tank reaches a certain height, barreling low-boiling impurities in the low-boiling liquid receiving tank for subsequent treatment;
the crude product liquid receiving tank receives liquid phase materials of the primary evaporator, a cut-off valve of the primary evaporator is opened in the early stage, a cut-off valve of the secondary evaporator is closed at the same time, the materials flow back to the primary evaporator completely, after the liquid phase temperature of the primary evaporator reaches a set value, the cut-off valve of the primary evaporator is closed, the cut-off valve of the secondary evaporator is opened, and all the materials are pumped into the secondary evaporator;
the second-stage evaporator uses heat-conducting oil as a heat source, the gas phase enters a product condenser, and the liquid phase enters a high-boiling intermediate tank; the heat-conducting oil feeding regulating valve is used as a controller to control the liquid-phase discharging temperature of the secondary evaporator;
opening a secondary evaporator cut-off valve at the earlier stage of the materials in the high-boiling intermediate tank, closing the secondary evaporator cut-off valve after the temperature of the secondary evaporator reaches a set value, opening a barreling cut-off valve after the liquid level reaches the height capable of uniformly barreling a batch of materials, and barreling;
the product condenser condenses the product, the product-removing and liquid-receiving tank cut-off valve is closed in the early stage, the material completely flows back to the secondary evaporator, and when the gas phase pressure and the gas phase temperature reach the required pressure and temperature, the condensate-removing and product-receiving tank cut-off valve is opened, and all the condensate is extracted to the product-receiving tank;
after the liquid level in the product liquid receiving tank reaches the vacuum breaking level difference height, the vacuum pressure difference can be counteracted by utilizing the installation height difference and the liquid level height difference, so that the vacuum is broken by utilizing the level difference, and the continuous discharging is carried out to the normal-pressure product intermediate tank; and after the liquid level in the product intermediate tank reaches the height corresponding to the batch of materials required by production, subsequent granulation or other procedures can be carried out.
Of course, each valve involved in the above process can be controlled by a manual valve according to actual use requirements.
In other alternative embodiments, if the material composition targeted for purification is more complex, an additional set of evaporation systems may be added depending on the separation difficulty of the material. That is, for the design of the two sets of evaporators in the above embodiment, if high boiling point impurities still exist in the product, one or more sets of evaporators can be added after the second stage. If the material still has low boiling point impurity after the first order evaporimeter, then can select to increase a set of evaporimeter that corresponds the boiling point again behind the evaporimeter that steam is the medium according to the boiling point of low boiling point impurity, and the same reason also can increase the multiunit.
It should be noted that, when the system is arranged, one or more groups of evaporators can be added according to the composition of materials, and the evaporator is determined by the separation difficulty and the boiling point of impurities; if the low boiling point of the material is difficult to separate and the high boiling point of the material is easy to separate, the material can pass through the heat conducting oil evaporator firstly, and then the product is condensed and then passes through the low boiling point condenser.
The purification device provided by the invention can effectively get rid of the limitation of viscosity on tower equipment by means of two-stage evaporators and auxiliary equipment, and meanwhile, the DCS can be used for controlling various components such as stop valves, thermometers, regulating valves and the like, so that the automation of the production flow is realized, the batch difference is eliminated, and the product quality and the yield are stable. By utilizing the characteristic that the vacuum degree has different influences on the boiling points of different substances, the separation of the substances with different boiling points can be realized by changing the vacuum degree.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and should not be taken as limiting the invention, so that any modifications, equivalents, improvements and the like, which are within the spirit and principle of the present invention, should be included in the scope of the present invention.
Claims (6)
1. A chemical product purification system is characterized by comprising a primary evaporator and a secondary evaporator which are sequentially arranged;
the primary evaporator is simultaneously connected with a low-boiling condenser and a crude product liquid receiving tank; the low-boiling condenser is connected with a low-boiling liquid receiving tank, and a first return pipeline connected with the primary evaporator is arranged on a connecting pipeline between the low-boiling condenser and the low-boiling liquid receiving tank; the crude product liquid receiving tank is connected with the secondary evaporator, and a secondary evaporator cut-off valve is arranged on a connecting pipeline of the crude product liquid receiving tank and the secondary evaporator;
the secondary evaporator is simultaneously connected with a product condenser and a high-boiling intermediate tank, the product condenser is connected with a product liquid receiving tank, and a connecting pipeline between the product condenser and the product liquid receiving tank is provided with a second return pipeline connected with the secondary evaporator; the product liquid receiving tank is connected with a normal pressure product intermediate tank.
2. The chemical product purification system of claim 1, wherein: a low-boiling cut-off valve is arranged in front of the low-boiling liquid receiving tank.
3. The chemical product purification system of claim 1, wherein: and a product removing and liquid receiving tank stop valve is arranged before the product receiving tank.
4. The chemical product purification system of claim 1, wherein: and a barreling cut-off valve is arranged on the pipeline at the rear end of the high-boiling intermediate tank.
5. The chemical product purification system of claim 1, wherein: and a third return pipeline is arranged between the crude product liquid receiving tank and the first-stage evaporator, and a first-stage evaporator cut-off valve is arranged in the third return pipeline.
6. The chemical product purification system of claim 1, wherein: and a fourth return pipeline is arranged between the high-boiling intermediate tank and the second-stage evaporator, and a second-stage evaporator cut-off valve is arranged in the fourth return pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201922188134.1U CN211561855U (en) | 2019-12-09 | 2019-12-09 | Chemical product purification system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201922188134.1U CN211561855U (en) | 2019-12-09 | 2019-12-09 | Chemical product purification system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211561855U true CN211561855U (en) | 2020-09-25 |
Family
ID=72534758
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201922188134.1U Active CN211561855U (en) | 2019-12-09 | 2019-12-09 | Chemical product purification system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211561855U (en) |
-
2019
- 2019-12-09 CN CN201922188134.1U patent/CN211561855U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7228713B2 (en) | Multi-stage vacuum distilling, cooling and freezing processes and apparatuses for solution separation and seawater desalination | |
| US3236747A (en) | Process for separating volatile material from a liquid mixture by a series of vaporization stages | |
| CN100432248C (en) | Very-pure metal lithium refining and purification process | |
| CN202387237U (en) | Device for purifying and regenerating waste organic solvent | |
| CN211561855U (en) | Chemical product purification system | |
| CN102266677B (en) | High vacuum distillation purification device | |
| CN202155061U (en) | High vacuum distillation purification device | |
| CN214382573U (en) | High-efficient cooling body of water distiller | |
| CN209596589U (en) | A kind of refining plant for ethylene glycol | |
| CN205649873U (en) | Refining plant of trimellitic acid acid anhydride | |
| CN101829434A (en) | Convective heat exchange fractionation device | |
| CN108191595A (en) | For detaching C10The distillation system of heavy aromatics | |
| CN109251140A (en) | Benzoic acid method of purification and purifying plant | |
| CN217489767U (en) | Crystallizer and device for producing phase-change wax | |
| RU2012105698A (en) | METHOD AND INSTALLATION FOR HYDROGEN PROCESSING IN A NODE FOR CLEANING THE DEVICE FOR CLEANING TERPHTHALIC ACID | |
| CN210448130U (en) | Distillation recovery plant | |
| CN206121310U (en) | Styrene technology condensate stripper gas separation purifier | |
| CN112694404A (en) | Method and device for purifying vinyl acetate in EVOH production process | |
| CN208372506U (en) | A kind of solvent recovery purification distilling apparatus | |
| CN220012579U (en) | Combined cooling distillation equipment | |
| CN211383861U (en) | Two-stage series rectifying tower | |
| CN220131929U (en) | Desalination treatment facility for sewage treatment | |
| CN211912772U (en) | Multi-stage condensation and heating separation device | |
| CN213994879U (en) | Three-function fractionating device | |
| CN210138476U (en) | Rectification device for preventing crystallization blockage in preparation of flunixin meglumine intermediate MTA |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |