CN211676384U - Coolant circulation type cooling crystallization system - Google Patents
Coolant circulation type cooling crystallization system Download PDFInfo
- Publication number
- CN211676384U CN211676384U CN201921948949.9U CN201921948949U CN211676384U CN 211676384 U CN211676384 U CN 211676384U CN 201921948949 U CN201921948949 U CN 201921948949U CN 211676384 U CN211676384 U CN 211676384U
- Authority
- CN
- China
- Prior art keywords
- refrigerant
- compressor
- crystallizer
- side wall
- outlet
- 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
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a refrigerant circulation type cooling crystallization system, which consists of a crystallizer, a guide cylinder, a distributor, a side stirrer, a discharge pump, a liquid separator, a refrigerant recoverer, a refrigerant recovery compressor, a refrigerant flash evaporation compressor, a condenser and a throttle valve; the refrigerant is a phase-change heat-carrying working medium which has a low boiling point, is not reacted with a crystalline material to be cooled, is insoluble and has a large relative volatility difference; the utility model adopts the contact flash evaporation cooling mode of the refrigerant and the material, the boiling point of the refrigerant is low, the specific volume of the gas is small, and under the same operation condition, the utility model can carry out deep cooling to improve the product yield, obviously reduce the installed capacity of the compressor and reduce the investment of system equipment; compared with the traditional method, the utility model has the characteristics of the material cooling is rapid, and the feed liquid does not have local supercooling, can realize continuous crystallization production etc.
Description
Technical Field
The utility model relates to a crystallization system especially relates to a cryogen circulation type cooling crystallization system, belongs to industry crystallization technical field.
Background
In the crystallization industry, there are a large number of inorganic salts with positive solubility, i.e. the solubility decreases rapidly with decreasing temperature of the solution, so that crystallization and separation of such solutions can be achieved by lowering the temperature of the solution in industrial production, which is called a temperature-lowering crystallization method. The industrial field applicable cooling crystallization product comprises Na2CO3·10H2O、KNO3、Ba(OH)2、KCl、NaNO3、FeSO4·7H2O、Na2SO4·10H2O, citric acid, and the like.
Common cooling crystallization methods include natural cooling, dividing wall cooling and flash evaporation cooling. The natural cooling method has simple equipment structure, but because the cooling is slow, the production efficiency is low, the product quality is not easy to control, and the natural cooling method is not adopted in large-scale production. The cooling wall surface of the dividing wall type cooling method is easy to generate crystal scale, so that the cooling heat transfer coefficient is reduced, and even the problems of pipeline blockage of system equipment and the like are caused, and the normal production operation is influenced. The flash evaporation cooling crystallization method is characterized in that the solution is subjected to flash evaporation under the condition of low pressure and is subjected to adiabatic cooling, and the flash evaporation cooling crystallization method has the characteristics of rapid cooling, high production efficiency and the like.
At present, a multi-stage steam jet pump method is mostly adopted for flash evaporation cooling crystallization, the injection coefficient of the steam jet pump is lower when the steam jet pump is applied to a vacuumizing condition, and the steam energy consumption is larger. The patent with the application number of [ 201610991905.9 ] discloses an equal gradient cooling crystallization system and method, and the patent adopts a large-flow compressor as flash evaporation air extraction equipment of a crystallizer, and has the characteristics of low system energy consumption, high production efficiency and the like. However, when the method is applied to a working condition that the specific volume of the flash steam is large (such as an aqueous solution), the slow speed reduction of the low-temperature section of the solution exists, and in order to ensure the rapid temperature reduction of the system, a steam compressor with an ultra-high flow rate is often configured, so that the popularization and the application of the technology are limited to a certain extent.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a cryogen circulation type cooling crystallization system to the not enough of conventional art existence.
A refrigerant circulation type cooling crystallization system is characterized in that: the system comprises a crystallizer, a liquid separator, a refrigerant recoverer, a refrigerant recovery compressor, a refrigerant flash evaporation compressor and a condenser;
the crystallizer is a cylindrical conical bottom type closed container, a feed inlet, a cryogen inlet and a cryogen reflux port are arranged on the side wall, a cryogen steam outlet and an evacuation port are arranged at the top, a discharge port is arranged at the bottom, a guide cylinder is arranged at the axial middle position of the crystallizer, and a distributor is arranged at the central position of the lower port of the guide cylinder; a side stirrer is arranged at the lower side part of the crystallizer;
the liquid separator is a cylinder type closed container, the side wall of the liquid separator is provided with a discharge port and a refrigerant outlet, the bottom of the liquid separator is provided with a feed port, and the top of the liquid separator is provided with a drain port;
the refrigerant recoverer is a cylinder type closed container, a feed inlet is formed in the side wall of the refrigerant recoverer, a refrigerant recovery air outlet and an emptying port are formed in the top of the refrigerant recoverer, and a discharge port is formed in the bottom of the refrigerant recoverer;
the condenser is provided with a refrigerant steam inlet, a refrigerant condensate outlet, a cooling water inlet and a cooling water outlet;
a refrigerant vapor outlet at the top of the crystallizer is connected with an air inlet of the refrigerant flash compressor, an air outlet of the refrigerant flash compressor is connected with a refrigerant vapor inlet of the condenser, a refrigerant condensate outlet of the condenser is connected with the distributor, and a throttle valve is arranged on the connecting pipeline; the discharge port at the bottom of the crystallizer is connected with the inlet of a discharge pump, and the outlet of the discharge pump is connected with the feed inlet at the bottom of the liquid separator; a cryogen outlet on the side wall of the liquid separator is connected with a cryogen reflux opening on the side wall of the crystallizer, and a discharge opening on the side wall of the liquid separator is connected with a feed inlet on the side wall of the cryogen recoverer; and a refrigerant recovery air outlet at the top of the refrigerant recoverer is connected with an air inlet of the refrigerant recovery compressor, and an air outlet of the refrigerant recovery compressor is connected with an air inlet of the refrigerant flash evaporation compressor.
Preferably: the guide cylinder is of a cylinder structure with openings at two ends, and the diameter of the guide cylinder is 1/5-1/2 of the diameter of the crystallizer.
Preferably: and a valve is respectively arranged on a pipeline connecting a refrigerant outlet on the side wall of the liquid separator and a refrigerant return opening on the side wall of the crystallizer and a pipeline connecting a discharge opening on the side wall of the liquid separator and a feed inlet on the side wall of the refrigerant recoverer.
Preferably: the refrigerant is Freon refrigerant, liquid hydrocarbon, butane, ethylene, ethane, water, carbon dioxide, ammonia or air.
Preferably: the volume ratio of the refrigerant to the materials in the system is 1: 100-1: 10.
Preferably: and baffling baffles which are arranged in a staggered manner are arranged in the liquid distributor.
Preferably: the refrigerant recovery compressor is a screw compressor, a roots compressor, a centrifugal compressor, a piston compressor or an axial flow compressor.
Preferably: the refrigerant flash evaporation compressor is a screw compressor, a Roots compressor, a centrifugal compressor, a piston compressor or an axial flow compressor.
Preferably: the condenser is a plate heat exchanger, a tube type heat exchanger, a spiral plate heat exchanger or a sleeve type heat exchanger.
The refrigerant is a working medium with low boiling point, non-reaction with the material to be cooled, non-solubility and larger relative volatility.
The working method of the refrigerant circulation type cooling crystallization system is as follows: when the system is operated for the first time, air in the system is discharged through an evacuation port at the top of the crystallizer, after the crystallizer is fed completely, refrigerant with proper material characteristics is filled into the crystallizer, a refrigerant flash compressor is started, low-boiling-point refrigerant in the crystallizer is quickly flashed and vaporized, heat is absorbed from solution, the temperature of feed liquid is continuously reduced, the flashed refrigerant steam is pressurized and heated by the refrigerant flash compressor and then discharged into a condenser for heat release and condensation, refrigerant condensate is throttled and depressurized by a throttle valve and then returns into the crystallizer through a distributor, the refrigerant is contacted with the feed liquid and absorbs heat for vaporization in a guide cylinder of the crystallizer, and due to the difference of gas content inside and outside the guide cylinder, an upper liquid phase circulation and a lower liquid phase circulation are formed inside and outside the guide cylinder, so that supersaturated solution on the surface of the crystallizer is continuously contacted with a crystal bed layer at the; after the crystal granularity meets the requirement, conveying the crystal slurry to a liquid separator through a discharge pump, simultaneously supplementing feeding to the crystallizer, and refluxing the cryogen at the upper layer in the liquid separator to the crystallizer through density difference after the discharged crystal slurry liquid is settled by the liquid separator; and then the crystal slurry liquid is conveyed into a refrigerant recoverer, a refrigerant recovery compressor is started to carry out flash recovery on the residual refrigerant in the crystal slurry in the refrigerant recoverer again, and the refrigerant steam recovered by flash evaporation is discharged to an inlet of the refrigerant flash compressor to start the next cycle operation.
Compared with the prior art, the beneficial effects of the utility model are that:
the refrigerant circulation type cooling crystallization system adopts the refrigerant flash evaporation and the direct contact type heat exchange with the material, compared with the traditional cooling crystallization method, the material cooling is rapid, the continuous cooling crystallization production operation can be realized, and the system has no dividing wall type heat exchange wall surface, thereby avoiding the crystal scar and crystal scale problem caused by local supercooling; in addition, the cryogen all has the boiling point low, and gaseous specific volume is little characteristics, consequently, under equal operating condition, the utility model discloses can reduce the feed liquid to lower temperature, improve crystal product yield to can show the installed capacity who reduces the compressor, reduce the initial investment of system's equipment.
Drawings
FIG. 1 is a schematic diagram of a refrigerant circulation type cooling crystallization system of the present invention;
FIG. 2 is a schematic diagram of the distribution of the flow field in the crystallizer according to the present invention;
in the figure, 1 is a crystallizer, 2 is a guide shell, 3 is a distributor, 4 is a side stirrer, 5 is a discharge pump, 6 is a liquid separator, 7 is a refrigerant recoverer, 8 is a refrigerant recovery compressor, 9 is a refrigerant flash evaporation compressor, 10 is a condenser, 11 is a throttle valve, and 12 is a refrigerant.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments, which are given by way of illustration only and are not intended to limit the scope of the present invention.
The first embodiment is as follows:
as shown in fig. 1, a cooling crystallization system of refrigerant circulation type comprises a crystallizer 1, a draft tube 2, a distributor 3, a side stirrer 4, a discharge pump 5, a knockout 6, a refrigerant recoverer 7, a refrigerant recovery compressor 8, a refrigerant flash evaporation compressor 9, a condenser 10, a throttle valve 11 and a refrigerant 12.
The crystallizer 1 is a cylindrical conical bottom type closed container, a feed inlet, a refrigerant inlet and a refrigerant return port are formed in the side wall of the closed container, a refrigerant steam outlet and an evacuation port are formed in the top of the closed container, a discharge port is formed in the bottom of the closed container, the guide cylinder 2 is arranged in the axial middle position of the crystallizer, and the guide cylinder is of a cylindrical structure and has the diameter of 1/3 of the diameter of the crystallizer; the side stirrer 4 is arranged at the lower side part of the crystallizer; the distributor 3 is arranged at the center of the lower opening of the guide shell; the liquid separator 6 is a cylindrical closed container, the side wall of the liquid separator is provided with a discharge port and a refrigerant outlet, the bottom of the liquid separator is provided with a feed port, and the top of the liquid separator is provided with a drain port; the refrigerant recoverer 7 is a cylinder type closed container, the side wall of the refrigerant recoverer is provided with a feed inlet, the top of the refrigerant recoverer is provided with a refrigerant recovery air outlet and an emptying port, and the bottom of the refrigerant recoverer is provided with a discharge port; the condenser 10 is provided with a refrigerant steam inlet, a refrigerant condensate outlet, a cooling water inlet and a cooling water outlet.
The refrigerant 12 of the present embodiment employs freon R134 a; the refrigerant recovery compressor 8 adopts a screw compressor; the refrigerant flash evaporation compressor 9 adopts a Roots compressor; the condenser adopts a tube type heat exchanger. A refrigerant vapor outlet at the top of the crystallizer is connected with an air inlet of the refrigerant flash compressor, an air outlet of the refrigerant flash compressor is connected with a refrigerant vapor inlet of the condenser, a refrigerant condensate outlet of the condenser is connected with the distributor, and the throttle valve 11 is arranged on the connecting pipeline; the discharge outlet at the bottom of the crystallizer is connected with the inlet of the discharge pump 5, and the outlet of the discharge pump is connected with the feed inlet at the bottom of the liquid separator; a refrigerant outlet on the side wall of the liquid separator is connected with a refrigerant reflux port on the side wall of the crystallizer, a valve is arranged on a connecting pipeline, a discharge port on the side wall of the liquid separator is connected with a feed port on the side wall of the refrigerant recoverer, and the valve is arranged on the connecting pipeline; and a refrigerant recovery air outlet at the top of the refrigerant recoverer is connected with an air inlet of the refrigerant recovery compressor, and an air outlet of the refrigerant recovery compressor is connected with an air inlet of the refrigerant flash evaporation compressor.
The working method of the refrigerant circulation type cooling crystallization system is as follows: when the system is in operation, exhausting air in the system through an evacuation port at the top of the crystallizer 1 to obtain FeSO4The solution is cooled and crystallized, the feeding temperature is 65 ℃, and the initial feeding amount is 30m3The specific gravity of the solution is about 1.5; freon R134a is selected as refrigerant, and the dosage of refrigerant is 0.5m3At 65 deg.C, the specific gravity of refrigerant is about 1.02, and the pressure in the kettle is about 19 bar. Starting the refrigerant flash compressor 9, the low boiling point refrigerant R134a in the crystallizer is rapidly flash vaporized and is separated from FeSO4Absorbing heat in the solution to ensure that FeSO is generated4The temperature of the solution is continuously reduced, the flashed R134a refrigerant steam is discharged into a condenser for heat release and condensation after passing through a refrigerant flash compressor, the R134a refrigerant condensate is throttled by a throttle valve and reduced in pressure and then returns into the crystallizer through the distributor, and the liquid R134a refrigerant and FeSO are in a guide shell of the crystallizer4The feed liquid contacts and absorbs heat to vaporize. As shown in figure 2, due to the difference of gas content inside and outside the guide shell, an upper and lower liquid phase circulation is formed inside and outside the guide shell, so that the supersaturated solution on the surface of the crystallizer and FeSO at the lower part of the crystallizer are ensured to be continuously contacted4The contact of crystal bed layers promotes FeSO4The rapid growth of the crystal; when FeSO4When the temperature of the solution is reduced to 20 ℃, the pressure in the crystallization kettle is 5.7bar, the magma is conveyed to the liquid distributor 6 through the discharging pump 5, meanwhile, the crystallizer is supplemented with feeding materials, and after the discharged magma liquid is settled in the liquid distributor, the R134a refrigerant on the upper layer of the liquid distributor flows back to the crystallizer through the specific gravity difference between the magma and the refrigerant (the specific gravity of the magma at 20 ℃ is 1.65, and the specific gravity of the R134a refrigerant at 20 ℃ is 1.23); then FeSO4And conveying the crystal slurry liquid into a refrigerant recoverer, starting a refrigerant recovery compressor to carry out flash recovery on the R134a refrigerant remained in the crystal slurry in the refrigerant recoverer, and discharging the R134a refrigerant steam subjected to flash recovery to an inlet of the refrigerant flash compressor to start the next cycle operation.
The true bookExample R134a was used as refrigerant for flash evaporation and was reacted with FeSO4Direct contact heat exchange with FeSO4Compared with the traditional cooling crystallization method, the material cooling is rapid, the continuous cooling crystallization production operation can be realized, the system has no partition wall type heat exchange wall surface, the problem of crystal scab and crystal scale caused by local supercooling is avoided, and the FeSO can be flashed by the refrigerant in the embodiment4Lowering the temperature of the solution to a lower temperature and increasing the FeSO4The product yield.
Although the present invention has been described with reference to the accompanying drawings, the present invention is not limited to the above embodiments, which are only illustrative and not restrictive, and those skilled in the art can make many modifications without departing from the spirit of the present invention, and all of them belong to the protection scope of the present invention.
Claims (9)
1. A refrigerant circulation type cooling crystallization system is characterized in that: the system comprises a crystallizer, a liquid separator, a refrigerant recoverer, a refrigerant recovery compressor, a refrigerant flash evaporation compressor and a condenser;
the crystallizer is a cylindrical conical bottom type closed container, a feed inlet, a cryogen inlet and a cryogen reflux port are arranged on the side wall, a cryogen steam outlet and an evacuation port are arranged at the top, a discharge port is arranged at the bottom, a guide cylinder is arranged at the axial middle position of the crystallizer, and a distributor is arranged at the central position of the lower port of the guide cylinder; a side stirrer is arranged at the lower side part of the crystallizer;
the liquid separator is a cylinder type closed container, the side wall of the liquid separator is provided with a discharge port and a refrigerant outlet, the bottom of the liquid separator is provided with a feed port, and the top of the liquid separator is provided with a drain port;
the refrigerant recoverer is a cylinder type closed container, a feed inlet is formed in the side wall of the refrigerant recoverer, a refrigerant recovery air outlet and an emptying port are formed in the top of the refrigerant recoverer, and a discharge port is formed in the bottom of the refrigerant recoverer;
the condenser is provided with a refrigerant steam inlet, a refrigerant condensate outlet, a cooling water inlet and a cooling water outlet;
a refrigerant vapor outlet at the top of the crystallizer is connected with an air inlet of the refrigerant flash compressor, an air outlet of the refrigerant flash compressor is connected with a refrigerant vapor inlet of the condenser, a refrigerant condensate outlet of the condenser is connected with the distributor, and a throttle valve is arranged on the connecting pipeline; the discharge port at the bottom of the crystallizer is connected with the inlet of a discharge pump, and the outlet of the discharge pump is connected with the feed inlet at the bottom of the liquid separator; a cryogen outlet on the side wall of the liquid separator is connected with a cryogen reflux opening on the side wall of the crystallizer, and a discharge opening on the side wall of the liquid separator is connected with a feed inlet on the side wall of the cryogen recoverer; and a refrigerant recovery air outlet at the top of the refrigerant recoverer is connected with an air inlet of the refrigerant recovery compressor, and an air outlet of the refrigerant recovery compressor is connected with an air inlet of the refrigerant flash evaporation compressor.
2. The refrigerant cycle type cooling crystallization system of claim 1, wherein: the guide cylinder is of a cylinder structure with openings at two ends, and the diameter of the guide cylinder is 1/5-1/2 of the diameter of the crystallizer.
3. The refrigerant cycle type cooling crystallization system according to claim 2, wherein: and a valve is respectively arranged on a pipeline connecting a refrigerant outlet on the side wall of the liquid separator and a refrigerant return opening on the side wall of the crystallizer and a pipeline connecting a discharge opening on the side wall of the liquid separator and a feed inlet on the side wall of the refrigerant recoverer.
4. The refrigerant cycle type cooling crystallization system of claim 3, wherein: the refrigerant is Freon refrigerant, liquid hydrocarbon, butane, ethylene, ethane, water, carbon dioxide, ammonia or air.
5. The refrigerant cycle type cooling crystallization system of claim 4, wherein: the volume ratio of the refrigerant to the materials in the system is 1: 100-1: 10.
6. The refrigerant cycle type cooling crystallization system of claim 5, wherein: and baffling baffles which are arranged in a staggered manner are arranged in the liquid distributor.
7. The refrigerant cycle type cooling crystallization system of claim 6, wherein: the refrigerant recovery compressor is a screw compressor, a roots compressor, a centrifugal compressor, a piston compressor or an axial flow compressor.
8. The refrigerant cycle type cooling crystallization system of claim 7, wherein: the refrigerant flash evaporation compressor is a screw compressor, a Roots compressor, a centrifugal compressor, a piston compressor or an axial flow compressor.
9. The refrigerant cycle type cooling crystallization system of claim 8, wherein: the condenser is a plate heat exchanger, a tube type heat exchanger, a spiral plate heat exchanger or a sleeve type heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921948949.9U CN211676384U (en) | 2019-11-13 | 2019-11-13 | Coolant circulation type cooling crystallization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921948949.9U CN211676384U (en) | 2019-11-13 | 2019-11-13 | Coolant circulation type cooling crystallization system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211676384U true CN211676384U (en) | 2020-10-16 |
Family
ID=72786766
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921948949.9U Active CN211676384U (en) | 2019-11-13 | 2019-11-13 | Coolant circulation type cooling crystallization system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211676384U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115594202A (en) * | 2022-09-06 | 2023-01-13 | 湖南化工设计院有限公司（Cn） | Separation method for separating potassium nitrate from mixed liquor containing potassium nitrate |
-
2019
- 2019-11-13 CN CN201921948949.9U patent/CN211676384U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115594202A (en) * | 2022-09-06 | 2023-01-13 | 湖南化工设计院有限公司（Cn） | Separation method for separating potassium nitrate from mixed liquor containing potassium nitrate |
| CN115594202B (en) * | 2022-09-06 | 2024-05-28 | 湖南化工设计院有限公司 | Separation method for separating potassium nitrate from mixed solution containing potassium nitrate |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102698451A (en) | Heat pump type low-temperature evaporating device and method | |
| CN202620748U (en) | Heat-pump type low-temperature evaporation device | |
| CN106196727B (en) | A kind of heat pump system and its operation method | |
| CN211676384U (en) | Coolant circulation type cooling crystallization system | |
| CN105819531A (en) | Energy-saving heat pump type intermediate-temperature spray evaporation system | |
| CN108558629A (en) | A kind of production system and production method of refined cyclohexanone | |
| CN203540090U (en) | Itaconic acid energy-saving-type four-effect concentrating and crystallizing device | |
| CN106196718B (en) | Absorption type heat pump system and its round-robin method | |
| CN102267868A (en) | Industrial production apparatus for trichloroethylene | |
| CN209685646U (en) | A kind of production system refining cyclohexanone | |
| CN109896950A (en) | A kind of system and technique of calcium gluconate continuous crystallisation | |
| CN104390492B (en) | A kind of horizontal pair of phase-change heat-exchanger | |
| CN201762266U (en) | Trichloroethylene industrialized production device | |
| CN108525338A (en) | Alcohol recycle rectifying device and alcohol recycle rectificating method | |
| CN104524806B (en) | A kind of hexamethylenamine complete continuous crystallisation production technology and equipments | |
| CN110882553A (en) | Low-temperature vacuum evaporator | |
| CN202315342U (en) | Horizontal pipe falling film evaporation tower | |
| CN102512833A (en) | Horizontal-pipe falling-film evaporation method coupling distillation and device thereof | |
| CN116282282A (en) | MVR evaporation system for wheat starch process wastewater | |
| CN205740412U (en) | A kind of energy saving heat pump middle temperature spray evaporation system | |
| CN106091477B (en) | Absorption heat pump and its condenser and method | |
| CN104258583A (en) | MVR evaporator and evaporation method | |
| CN103467401B (en) | Production method and device for ametryn | |
| CN204485341U (en) | Full heat and latent heat recovery type multiple-effect vacuum evaporation concentration device | |
| CN203946915U (en) | Negative pressure ammonia evaporation system taking cyclic ammonia water as thermal source |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |