CN212854705U - Continuous crystallization production system - Google Patents
Continuous crystallization production system Download PDFInfo
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- CN212854705U CN212854705U CN202021436729.0U CN202021436729U CN212854705U CN 212854705 U CN212854705 U CN 212854705U CN 202021436729 U CN202021436729 U CN 202021436729U CN 212854705 U CN212854705 U CN 212854705U
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Abstract
The utility model provides a continuous crystallization production system, belonging to the technical field of evaporative crystallization, comprising a plurality of crystallization devices and a residual liquid storage tank which are connected in sequence; the crystallization device comprises a raw liquid tank, a heater communicated with the raw liquid tank, an evaporator, a crystallizer, a centrifugal machine and a container communicated with one end of the centrifugal machine; the other end of the centrifuge is communicated with a raw liquid tank of a next-stage crystallization device; the stock solution tank adds solution to the heater through a power pump; adding the solution into a centrifugal machine by a crystallizer through a power pump; the other end intercommunication of raffinate storage jar and final stage's crystallizer, the utility model provides a continuous crystallization production system adopts a plurality of crystallizers's purification crystallization many times in succession to place the solid of crystallization at every turn in the container that corresponds, and the crystallization liquid purification crystallization once more, in the raffinate storage jar is injected into to the solution of remaining after the purification crystallization at last many times, improved the crystallization effect of sodium thiocyanate solution.
Description
Technical Field
The utility model belongs to the technical field of the evaporation crystallization, more specifically say, relate to a continuous crystallization production system.
Background
Sodium thiocyanate is an important chemical production raw material and has wide application in the industries of medicine, textile, pesticide, building materials and the like, and a crystallization production device of sodium thiocyanate is not reported in documents. The continuous evaporation crystallization device for the solid has two types of intermittent evaporation and continuous evaporation, and the intermittent evaporation crystallization has the problems of high energy consumption and low efficiency. The continuous evaporation crystallization mostly adopts the evaporation of the effect bodies, and the steam vaporized by the former effect body is used for providing steam heating for the lower effect bodies. However, the sodium thiocyanate solution has the properties of large specific heat and high temperature rise, and if continuous multi-effect evaporation is adopted, a heat exchanger with a large heat exchange surface is required, so that industrialization is not easy to realize. And continuous multi-effect evaporation often has the problems of mother liquor back mixing and impurity accumulation.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a continuous crystallization production system to solve the relatively poor technical problem of sodium thiocyanate production process crystallization effect that exists among the prior art.
In order to achieve the above object, the utility model adopts the following technical scheme: providing a continuous crystallization production system, which comprises a plurality of crystallization devices and a residual liquid storage tank which are connected in sequence;
the crystallization device comprises a raw liquid tank, a heater communicated with the raw liquid tank, an evaporator communicated with the heater, a crystallizer communicated with the evaporator, a centrifuge communicated with the crystallizer and a container communicated with one end of the centrifuge and used for containing solids; the other end of the centrifuge is communicated with the stock solution tank of the next-stage crystallization device and is used for discharging solution; the stock solution tank adds solution to the heater through a power pump; the crystallizer adds solution to the centrifuge through a power pump;
the raffinate storage tank is communicated with the other end of the centrifuge of the crystallization device at the last stage.
As another embodiment of the application, a preheater is also arranged between the stock solution tank and the heater and used for preheating the solution.
As another embodiment of the present application, the preheater is a heat exchanger, the preheater is provided with two sets of inlets and outlets, one set of the inlets and outlets are respectively communicated with the stock solution tank and the heater, and the other set of the inlets and outlets are respectively communicated with the evaporator and the crystallizer.
As another embodiment of the present application, the preheater is a spiral plate heat exchanger.
As another embodiment of the present application, the number of the crystallization apparatuses is three, and the three crystallization apparatuses are divided into a first-stage crystallization apparatus, a second-stage crystallization apparatus and a third-stage crystallization apparatus; the other end of the centrifugal machine of the three-stage crystallizing device is communicated with the residual liquid storage tank.
As another embodiment of the present application, a heating area of the heater of the secondary crystallization apparatus is 50% of a heating area of the heater of the primary crystallization apparatus, and a heating area of the heater of the tertiary crystallization apparatus is 30% of the heating area of the heater of the secondary crystallization apparatus.
As another embodiment of the present application, the volumes of the evaporator and the crystallizer of the secondary crystallization device are 50% of the volumes of the evaporator and the crystallizer of the primary crystallization device, respectively, and the volumes of the evaporator and the crystallizer of the tertiary crystallization device are 30% of the volumes of the evaporator and the crystallizer of the secondary crystallization device, respectively.
As another embodiment of the application, a negative pressure machine is connected to the evaporator.
As another embodiment of the present application, the container is a dryer.
The utility model provides a continuous crystallization production system's beneficial effect lies in: compared with the prior art, the utility model discloses continuous crystallization production system, in the stock solution jar that gets into one-level crystallization device with the sodium thiocyanate solution during the use, and heat the heater of solution pump income one-level crystallization device by the power pump, solution after the heating gets into the evaporimeter and evaporates, improve the concentration of sodium thiocyanate solution, then flow to cooling crystallization in the crystallizer, crystalline solid and crystallization liquid are pumped into the centrifuge by the power pump, crystalline solid gets into in the container after the centrifuge centrifugation, the crystallization liquid gets into in the stock solution jar of second grade crystallization device, again through the heating, evaporation, after the crystallization, further purify the crystallization liquid, isolate crystalline solid in the corresponding container, and make the crystallization liquid get into next grade crystallization device and purify the crystallization, this kind of mode adopts the continuous many purification crystallization of a plurality of crystallization devices crystallization device crystallization, and place crystalline solid in the container that corresponds at every turn, and the crystallization liquid is purified and crystallized again, and the residual solution after the last purification and crystallization for many times is injected into a residual liquid storage tank, so that the crystallization effect of the sodium thiocyanate solution is improved.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for the embodiments or the prior art descriptions will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a continuous crystallization production system provided by an embodiment of the present invention;
FIG. 2 is a schematic view of a first partial view of a continuous crystallization production system according to an embodiment of the present invention;
fig. 3 is a partial schematic view of a continuous crystallization production system according to an embodiment of the present invention.
Wherein, in the figures, the respective reference numerals:
1. a crystallization device; 11. a stock solution tank; 12. a heater; 13. an evaporator; 14. a crystallizer; 15. a centrifuge; 16. a container; 161. a dryer; 17. a preheater; 171. an inlet; 172. an outlet; 18. a power pump; 2. and (4) storing the residual liquid.
Detailed Description
In order to make the technical problem, technical solution and advantageous effects to be solved by the present invention more clearly understood, the following description is given in conjunction with the accompanying drawings and embodiments to illustrate the present invention in further detail. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Referring to fig. 1 to 3, a continuous crystallization production system according to the present invention will now be described. A continuous crystallization production system comprises a plurality of crystallization devices 1 and a raffinate storage tank 2 which are connected in sequence; the crystallization device 1 comprises a raw liquid tank 11, a heater 12 communicated with the raw liquid tank 11, an evaporator 13 communicated with the heater 12, a crystallizer 14 communicated with the evaporator 13, a centrifuge 15 communicated with the crystallizer 14 and a container 16 communicated with one end of the centrifuge 15 and used for containing solids; the other end of the centrifuge 15 is communicated with the raw liquid tank 11 of the next-stage crystallization device 1 and used for discharging the solution; the stock solution tank 11 adds solution to the heater 12 through the power pump 18; crystallizer 14 adds solution to centrifuge 15 through power pump 18; the raffinate holding tank 2 communicates with the other end of the centrifuge 15 of the final crystallization apparatus 1.
The utility model provides a continuous crystallization production system, compared with the prior art, in the raw liquid tank 11 that gets into one-level crystallization device 1 with the sodium thiocyanate solution during the use, and heat by power pump 18 pump solution pump into the heater 12 of one-level crystallization device 1, solution after the heating gets into evaporimeter 13 and evaporates, improve the concentration of sodium thiocyanate solution, then flow to cooling crystallization in crystallizer 14, crystalline solid and crystalline liquid pump into centrifuge 15 in by power pump 18, crystalline solid gets into in the container 16 after centrifuge 15 centrifugation, crystalline liquid gets into in the raw liquid tank 11 of second grade crystallization device 1, again through heating, evaporate, after the crystallization, further purify crystalline liquid, isolate crystalline solid in the container 16 that corresponds, and make crystalline liquid get into next grade crystallization device 1 and purify the crystallization, this kind of mode adopts the continuous many times purification crystallization of a plurality of crystallization device 1, and the solid crystallized each time is placed in the corresponding container 16, the crystallized liquid is purified and crystallized again, and the residual solution after the last purification and crystallization for many times is injected into the residual liquid storage tank 2, so that the crystallization effect of the sodium thiocyanate solution is improved.
The sodium thiocyanate solution is heated to 80 ℃ in the heater 12, and the solution entering the crystallizer 14 is rapidly cooled to 25-35 ℃ for crystallization. In the mode, the purity of the crystallized solid at each level is different, and the product obtained by the first-level crystallizing device 1 is more than or equal to 99.5 percent and is a superior product when the third-level crystallizing device 1 is arranged below; the purity of the product obtained by the secondary crystallization device 1 is more than or equal to 99.0 percent and is a first-class product; the purity of the product obtained by the third-stage crystallization device 1 is more than or equal to 98.5 percent and is a qualified product; fully meet the requirements of different customers on the quality of the sodium thiocyanate.
Referring to fig. 1 to 3, as a specific embodiment of the continuous crystallization production system provided by the present invention, a preheater 17 is further disposed between the raw liquid tank 11 and the heater 12 for preheating the solution, and the preheater 17 is configured to preheat the sodium thiocyanate solution, thereby reducing the workload of the heater 12. The preheating temperature is about 40 ℃.
Referring to fig. 2 and fig. 3, as a specific embodiment of the continuous crystallization production system provided by the present invention, the preheater 17 is a heat exchanger, the preheater 17 is provided with two sets of inlets and outlets 172, one set of the inlets and outlets 172 is respectively communicated with the raw liquid tank 11 and the heater 12, the other set of the inlets and outlets 172 is respectively communicated with the evaporator 13 and the crystallizer 14, the raw liquid tank 11 and the heater 12 are respectively communicated with the inlet 171 and the outlet 172 of the set of the inlets and outlets 172, so that the solution pumped out from the raw liquid tank 11 is preheated by the preheater 17 and then enters the heater 12 for heating; the inlet 171 and the outlet 172 of the other set of the inlet and the outlet 172 are respectively communicated with the evaporator 13 and the crystallizer 14, and the concentration of the evaporated solution is increased, so that cooling crystallization is needed, therefore, the preheater 17 adopts a heat exchanger, the solution flows out of the evaporator 13, firstly passes through the preheater 17, and exchanges heat with the low-temperature solution pumped out of the raw solution tank 11 in the preheater 17, and by the way, waste is changed into valuable, the heat energy of the high-temperature solution flowing out of the evaporator 13 is effectively utilized, the energy utilization rate is improved, and the cost is saved.
Referring to fig. 1 to 3, as a specific embodiment of the continuous crystallization production system provided by the present invention, the preheater 17 is a spiral plate heat exchanger, which has good heat transfer efficiency and strong operation stability, and can effectively recover low-temperature heat energy to save energy; the end face of the spiral channel of the spiral plate type heat exchanger is sealed by welding, so that the sealing performance is high, two working media are guaranteed not to be mixed, and mutual influence is avoided.
Referring to fig. 1, as a specific embodiment of the continuous crystallization production system of the present invention, there are three crystallization apparatuses 1, which are divided into a first-stage crystallization apparatus 1, a second-stage crystallization apparatus 1 and a third-stage crystallization apparatus 1; the other end of tertiary crystallization device 1's centrifuge 15 communicates with raffinate storage jar 2, set up three crystallization device 1 and communicate in proper order, sodium thiocyanate solution at first gets into one-level crystallization device 1, through heating, evaporation, crystallization and centrifugal operation output crystallization solid, and make the solution after the crystallization get into second grade crystallization device 1, after second grade crystallization device 1 crystallization, after reentrant tertiary crystallization device 1 crystallization formation solid, the solvent that contains in the sodium thiocyanate solution reduces, discharge to raffinate storage jar 2 as the waste liquid from centrifuge 15 in tertiary crystallization device 1.
Referring to fig. 1 to 3, as a specific embodiment of the continuous crystallization production system provided by the present invention, the heating area of the heater 12 of the second crystallization device 1 is 50% of the heating area of the heater 12 of the first crystallization device 1, the heating area of the heater 12 of the third crystallization device 1 is 30% of the heating area of the heater 12 of the second crystallization device 1, the solution of the second evaporation is the solution after the first crystallization, the solution of the third evaporation is the solution after the second crystallization, the solution amount is gradually reduced, therefore, the heating area of the heater 12 of the last device is reduced compared with the previous device, the solution can be heated by fully utilizing energy, and unnecessary energy waste is avoided.
Referring to fig. 1 to 3, as a specific embodiment of the continuous crystallization production system provided by the present invention, the volumes of the evaporator 13 and the crystallizer 14 of the second-stage crystallization device 1 are respectively 50% of the volumes of the evaporator 13 and the crystallizer 14 of the first-stage crystallization device 1, the volumes of the evaporator 13 and the crystallizer 14 of the third-stage crystallization device 1 are respectively 30% of the volumes of the evaporator 13 and the crystallizer 14 of the second-stage crystallization device 1, the solution of the second-stage evaporation is the solution after the first-stage crystallization, the solution of the third-stage evaporation is the solution after the second-stage crystallization, and the amount of the solution is gradually reduced, so that the volumes of the evaporator 13 and the crystallizer 14 of the second-stage device are reduced compared with the previous first-stage, it is ensured that the evaporated solution is crystallized in the corresponding crystallizer 14 as soon as possible, and the problem that the crystal grains generated in the slow; meanwhile, the volume of the evaporator 13 and the crystallizer 14 is reduced, so that energy can be effectively and fully utilized, and unnecessary energy waste is avoided.
Please refer to fig. 1 to 3, as the utility model provides a continuous crystallization production system's a specific implementation, be connected with the negative pressure machine on the evaporimeter 13, the moisture gasification forms into vapor in the sodium thiocyanate solution at evaporimeter 13, and the vapor is taken out rapidly under the effect of negative pressure machine, has improved the evaporation effect of evaporimeter 13, improves the concentration of sodium thiocyanate solution, is favorable to crystallization operation in crystallizer 14 on next step.
Referring to fig. 1 and 2, as a specific embodiment of the continuous crystallization production system provided by the present invention, the container 16 is a dryer 161, the crystallized solid directly enters the dryer 161 from one end of the centrifuge 15, and the dryer 161 dries the moisture on the crystallized solid, so as to facilitate direct use of the subsequent work or calculation of purity.
The above description is only exemplary of the present invention and should not be construed as limiting the present invention, and any modifications, equivalents and improvements made within the spirit and principles of the present invention are intended to be included within the scope of the present invention.
Claims (9)
1. The continuous crystallization production system is characterized by comprising a plurality of crystallization devices and a residual liquid storage tank which are connected in sequence;
the crystallization device comprises a raw liquid tank, a heater communicated with the raw liquid tank, an evaporator communicated with the heater, a crystallizer communicated with the evaporator, a centrifuge communicated with the crystallizer and a container communicated with one end of the centrifuge and used for containing solids; the other end of the centrifuge is communicated with the stock solution tank of the next-stage crystallization device and is used for discharging solution; the stock solution tank adds solution to the heater through a power pump; the crystallizer adds solution to the centrifuge through a power pump;
the raffinate storage tank is communicated with the other end of the centrifuge of the crystallization device at the last stage.
2. The continuous crystal production system of claim 1, wherein a preheater is further provided between the stock tank and the heater for preheating the solution.
3. The continuous crystal production system of claim 2, wherein the preheater is a heat exchanger and the preheater is provided with two sets of inlet and outlet ports, one set of the inlet and outlet ports being in communication with the feed tank and the heater, respectively, and the other set of the inlet and outlet ports being in communication with the evaporator and the crystallizer, respectively.
4. The continuous crystallization production system of claim 2, wherein the preheater is a spiral plate heat exchanger.
5. The continuous crystallization production system of claim 1, wherein the number of crystallization apparatuses is three, and the three crystallization apparatuses are divided into a primary crystallization apparatus, a secondary crystallization apparatus, and a tertiary crystallization apparatus; the other end of the centrifugal machine of the three-stage crystallizing device is communicated with the residual liquid storage tank.
6. The continuous crystallization production system of claim 5, wherein the heating area of the heater of the secondary crystallization device is 50% of the heating area of the heater of the primary crystallization device, and the heating area of the heater of the tertiary crystallization device is 30% of the heating area of the heater of the secondary crystallization device.
7. The continuous crystallization production system of claim 5, wherein the volumes of the evaporator and the crystallizer of the secondary crystallization device are 50% of the volumes of the evaporator and the crystallizer of the primary crystallization device, respectively, and the volumes of the evaporator and the crystallizer of the tertiary crystallization device are 30% of the volumes of the evaporator and the crystallizer of the secondary crystallization device, respectively.
8. The continuous crystal production system of any one of claims 1 to 7, wherein a negative pressure machine is connected to the evaporator.
9. A continuous crystal production system as claimed in any one of claims 1 to 7, wherein said container is a dryer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021436729.0U CN212854705U (en) | 2020-07-20 | 2020-07-20 | Continuous crystallization production system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021436729.0U CN212854705U (en) | 2020-07-20 | 2020-07-20 | Continuous crystallization production system |
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| CN212854705U true CN212854705U (en) | 2021-04-02 |
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| CN202021436729.0U Active CN212854705U (en) | 2020-07-20 | 2020-07-20 | Continuous crystallization production system |
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