CN217409792U - Production device for controlling granularity of sodium citrate - Google Patents
Production device for controlling granularity of sodium citrate Download PDFInfo
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- CN217409792U CN217409792U CN202123232156.7U CN202123232156U CN217409792U CN 217409792 U CN217409792 U CN 217409792U CN 202123232156 U CN202123232156 U CN 202123232156U CN 217409792 U CN217409792 U CN 217409792U
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Abstract
The utility model belongs to the technical field of sodium citrate preparation, in particular to a production device for controlling the granularity of sodium citrate, which comprises a condenser, a crystallizer, a circulating pipeline, a forced circulating pump, a centrifuge, a primary crystal slurry tank and a secondary crystal slurry tank; the primary crystal slurry tank is connected with a circulating pipeline through a feeding pipeline, the primary crystal slurry tank is respectively connected with a primary crystal slurry backflow pipeline and a centrifugal discharging pipeline through a discharging pipeline, and a particle size tester is arranged on the discharging pipeline; the primary crystal slurry backflow pipeline is connected with the crystallizer, and the centrifugal discharge pipeline is connected with the centrifuge; the primary crystal slurry tank is connected with the secondary crystal slurry tank through an overflow pipeline, and the secondary crystal slurry tank is connected with the crystallizer through a secondary crystal slurry return pipeline; crystal slurry pumps are arranged on the discharge pipeline and the secondary crystal slurry return pipeline; all be provided with the governing valve on charge-in pipeline, one-level magma return line, centrifugation ejection of compact pipeline and the second grade magma return line, adopt the device can effective control sodium citrate granularity, reduce into manufacturing cost.
Description
Technical Field
The utility model belongs to the technical field of sodium citrate's preparation, concretely relates to apparatus for producing of control sodium citrate granularity.
Background
Sodium citrate is currently the most important citrate, and is widely used in the industries of food, beverage, medicine, detergent, brewing, photography, electroplating and the like.
At present, a common method for producing sodium citrate crystals is a continuous crystallization method, wherein a sodium citrate solution is firstly fed into a crystallizer in the crystallization process to be continuously evaporated, concentrated and crystallized to obtain crystal slurry. The continuous crystallization method can continuously carry out crystallization operation while feeding and discharging, is beneficial to large-scale industrial production, has high production efficiency, and is commonly used in industrial production at present. However, after the sodium citrate prepared by the existing continuous crystallization equipment is crystallized in the crystallizer, a forced circulation pump of the crystallizer drives the sodium citrate crystal slurry to grow in the crystallizer in a circulating way, and then the sodium citrate crystal slurry is discharged into a crystal slurry tank and fed into a centrifuge through a crystal slurry pump. The sodium citrate production device cannot control the particle size of sodium citrate crystals, so that the produced sodium citrate product has insufficient uniform particle size. In order to meet the requirements of different customers on the product granularity, the product is usually dried and then screened, while the product which does not meet the granularity requirement is reused as waste material for melting and returning, and the recycling of intermediate materials increases the preparation cost of the sodium citrate.
SUMMERY OF THE UTILITY MODEL
To the technical problem that exists at present, the utility model provides a apparatus for producing of control sodium citrate granularity adopts the device can the effective control sodium citrate granularity, and the different demands in the market that satisfy have reduced artifical working strength and this cost of people, have reduced the process.
The technical scheme of the utility model as follows:
a production device for controlling the granularity of sodium citrate comprises a condenser, a crystallizer, a circulating pipeline, a forced circulating pump, a crystal slurry tank and a centrifuge, wherein a stirring device is arranged in the crystal slurry tank, and the crystal slurry tank comprises a primary crystal slurry tank and a secondary crystal slurry tank; a feed port of the primary crystal slurry tank is connected with a circulating pipeline through a feed pipeline, a discharge port of the primary crystal slurry tank is respectively connected with a primary crystal slurry backflow pipeline and a centrifugal discharge pipeline through a discharge pipeline, and a particle size tester is arranged on the discharge pipeline; the primary crystal slurry backflow pipeline is connected with the crystallizer, and the centrifugal discharge pipeline is connected with the centrifuge; the primary crystal slurry tank is connected with the secondary crystal slurry tank through an overflow pipeline, and a discharge port of the secondary crystal slurry tank is connected with the crystallizer through a secondary crystal slurry reflux pipeline; crystal slurry pumps are arranged on the discharge pipeline and the secondary crystal slurry return pipeline; and the feeding pipeline, the primary crystal slurry backflow pipeline, the centrifugal discharging pipeline and the secondary crystal slurry backflow pipeline are all provided with regulating valves.
Preferably, at least two overflow pipelines are arranged; further preferably, the overflow pipe comprises a first overflow pipe and a second overflow pipe, the first overflow pipe is arranged at the position 2/3 of the height of the straight barrel body of the primary crystal slurry tank, and the second overflow pipe is arranged at the position 1/2 of the height of the straight barrel body of the primary crystal slurry tank; more preferably, the position of each overflow pipeline connected with the primary crystal slurry tank is higher than the position of each overflow pipeline connected with the secondary crystal slurry tank.
Preferably, the overflow pipe is provided with a regulating valve.
Preferably, the PLC control system is electrically connected with the regulating valves and the particle size measuring instruments on the feeding pipeline, the primary crystal slurry return pipeline, the centrifugal discharging pipeline and the secondary crystal slurry return pipeline and on the overflow pipeline, after the particle size measuring instruments detect, signals are transmitted to the PLC control system, and the PLC control system controls the regulating valves.
Preferably, the regulating valve is a V-shaped stainless steel regulating valve without a sealing gasket.
Preferably, a tee joint is arranged at the joint of the discharge pipeline, the primary crystal slurry backflow pipeline and the centrifugal discharge pipeline.
Preferably, the negative pressure evaporation mode is adopted in the crystallizer.
Preferably, the discharge ports of the primary crystal slurry tank and the secondary crystal slurry tank are arranged at the bottom, and the feed port of the primary crystal slurry tank is arranged at the top.
The utility model discloses, increase second grade brilliant thick liquid jar and brilliant thick liquid pump behind original brilliant thick liquid jar, original brilliant thick liquid jar is as the brilliant thick liquid jar of one-level, and two overflow pipe ways are installed respectively to the brilliant thick liquid jar of one-level and the brilliant thick liquid jar of second grade, and every pipe-line erection governing valve, the brilliant thick liquid of the brilliant thick liquid jar of second grade returns to the crystallizer again through brilliant thick liquid backward flow and carries out the secondary growth. By adopting the design, the crystal slurry in the crystallizer firstly enters the primary crystal slurry tank, the particles in the crystal slurry are screened in a layered manner by controlling the stirring speed of the primary crystal slurry tank, meanwhile, the overflow speed is controlled by utilizing an overflow pipeline between the primary crystal slurry tank and the secondary crystal slurry tank through an adjusting valve, the fine particles on the upper part of the primary crystal slurry tank overflow into the secondary crystal slurry tank, and then the fine particles return to the crystallizer through a secondary crystal slurry backflow pipeline for secondary growth of the crystal slurry fine particles; detecting whether the crystal slurry in the primary crystal slurry tank meets the requirement of the particle size through a particle size tester on a discharge pipeline by a primary crystal slurry pump, and if the requirement of the particle size is not met, refluxing the crystal slurry to a crystallizer for secondary growth; when the particle size tester detects that the particle size meets the requirement, the crystal slurry enters a centrifuge through a centrifugal discharge pipeline for solid-liquid separation, and a sodium citrate product with proper particle size is obtained. By adopting the design, the aim of preparing the sodium citrate with specific granularity can be achieved by screening crystal slurry particles discharged from the crystallizer and simultaneously utilizing a crystal slurry backflow mode.
The utility model provides a pair of production device of control sodium citrate granularity can effective control sodium citrate granularity, and the different demands in the market that satisfy have reduced artifical working strength and this cost, have reduced the process, have avoided sodium citrate product granularity inhomogeneous, and various granularities exist simultaneously, and lead to not being conform to the problem that the sodium citrate of granularity requirement returned the chemical material, have reduced sodium citrate's manufacturing cost.
Drawings
Fig. 1 is a schematic structural view of the present invention;
in the figure, 1 is the crystallizer, 2 is the force circulation pump, 3 is the charge-in pipeline, 4 is the brilliant thick liquid jar of one-level, 5 is agitating unit, 6 is the brilliant thick liquid pump of one-level, 7 is the discharge pipeline, 8 is the particle size apparatus, 9 is the centrifugation discharge pipeline, 10 is the brilliant thick liquid return line of one-level, 11 is centrifuge, 12 is the overflow pipe way, 13 is the brilliant thick liquid jar of second grade, 14 is the brilliant thick liquid pump of second grade, 15 is the brilliant thick liquid return line of second grade, 16 is the condenser.
Detailed Description
In order to make the technical solution of the present invention clearer, the following description, with reference to the accompanying drawings, further illustrates the present invention in detail, and the specific examples described herein are only used for explaining the present invention, and are not used for limiting the present invention.
As shown in the figure, the production device for controlling the granularity of the sodium citrate comprises a condenser 16, a crystallizer 1, a circulating pipeline, a forced circulating pump 2, a crystal slurry tank and a centrifuge 11, wherein the crystal slurry tank comprises a primary crystal slurry tank 4 and a secondary crystal slurry tank 13, the primary crystal slurry tank 4 and the secondary crystal slurry tank 13 are both provided with a stirring device 5, and the stirring device 5 is a conventional stirring device, such as the conventional stirring device comprising a stirring blade and a motor; a feed inlet of the primary crystal slurry tank 4 is connected with a circulating pipeline through a feed pipeline 3, a feed regulating valve is installed for facilitating the control of feeding to regulate the feeding speed, and the feed inlet is arranged at the top of the primary crystal slurry tank 4; a discharge port of the primary crystal slurry tank 4 is respectively connected with a primary crystal slurry backflow pipeline 10 and a centrifugal discharge pipeline 9 through a discharge pipeline 7, a tee joint is arranged at the joint of the discharge pipeline 7, the primary crystal slurry backflow pipeline 10 and the centrifugal discharge pipeline 9, a particle size tester 8 is arranged on the discharge pipeline 7, and the discharge port is arranged at the bottom of the primary crystal slurry tank 4; the primary crystal slurry backflow pipeline 10 is connected with a backflow port of the crystallizer 1, and the centrifugal discharge pipeline 9 is connected with the centrifugal machine 11; the primary crystal slurry tank 4 is connected with the secondary crystal slurry tank 13 through an overflow pipeline 12, a discharge port of the secondary crystal slurry tank 13 is connected with a reflux port of the crystallizer 1 through a secondary crystal slurry reflux pipeline 15, and the discharge port is arranged at the bottom of the secondary crystal slurry tank 13; the crystal slurry pump comprises a primary crystal slurry pump 6 and a secondary crystal slurry pump 14, the primary crystal slurry pump 6 is arranged on the discharge pipeline 7, and the secondary crystal slurry pump 14 is arranged on the secondary crystal slurry return pipeline 15; two overflow pipelines 12 are arranged, the first overflow pipeline 12 is arranged at the position 2/3 of the height of the straight cylinder body of the primary crystal slurry tank 4, the second overflow pipeline 12 is arranged at the position 1/2 of the height of the straight cylinder body of the primary crystal slurry tank 4, in order to ensure smooth overflow, the position of each overflow pipeline 12 connected with the primary crystal slurry tank 4 is higher than the position of each overflow pipeline 12 connected with the secondary crystal slurry tank 13, and each overflow pipeline 12 is provided with an overflow regulating valve for controlling the overflow speed; feed line 3, one-level magma return line 10, centrifugation ejection of compact pipeline 9, second grade magma return line 15, all be provided with the governing valve on the overflow pipeline 12, the governing valve, the equal electric PLC control system of connecting of particle size apparatus 8, the steerable governing valve of PLC control system, 8 back of detecting of particle size apparatus simultaneously, give PLC control system with signal transmission, PLC control system control governing valve, the steerable size of opening, closing and regulating flow of governing valve.
In order to avoid the crystal slurry particles from wearing a valve sealing washer, the regulating valve adopts a V-shaped stainless steel regulating valve without the sealing washer.
Preferably, the crystallizer 1 is in a negative pressure evaporation mode, and in order to ensure stable evaporation of the crystallizer 1, the equipment associated with the crystallizer 1 needs to be ensured with tightness, and necessary tightness tests need to be carried out to ensure the tightness of all the equipment.
The utility model discloses, increase second grade brilliant thick liquid jar 13 and brilliant thick liquid pump behind original brilliant thick liquid jar, original brilliant thick liquid jar is as one-level brilliant thick liquid jar 4, and two overflow pipeline 12 every pipe installation governing valves are installed respectively to one-level brilliant thick liquid jar 4 and second grade brilliant thick liquid jar 13, and the brilliant thick liquid of second grade brilliant thick liquid jar 13 returns again through brilliant thick liquid backward flow and carries out the secondary growth in crystallizer 1. By adopting the design, the crystal slurry in the crystallizer 1 firstly enters the primary crystal slurry tank 4, the particles in the crystal slurry are screened in a layered manner by controlling the stirring speed of the primary crystal slurry tank 4, meanwhile, the overflow speed is controlled by using an overflow pipeline 12 between the primary crystal slurry tank 4 and the secondary crystal slurry tank 13 through a regulating valve to overflow the fine particles on the upper part of the primary crystal slurry tank 4 to the secondary crystal slurry tank 13, and then the fine particles are returned to the crystallizer 1 through a secondary crystal slurry return pipeline to carry out secondary growth of the crystal slurry fine particles; detecting whether the crystal slurry in the primary crystal slurry tank 4 meets the requirement of the particle size or not through a particle size tester 8 on a discharge pipeline by a primary crystal slurry pump 6, and if the requirement of the particle size is not met, refluxing the crystal slurry to the crystallizer 1 for secondary growth; when the particle size tester 8 detects that the particle size meets the requirement, the crystal slurry enters a centrifuge 11 through a centrifugal discharge pipeline 9 for solid-liquid separation, and a sodium citrate product with proper particle size is obtained. By adopting the design, the purpose of preparing the sodium citrate with specific granularity can be achieved by screening the crystal mush particles discharged from the crystallizer 1 and simultaneously utilizing the crystal mush backflow mode.
In the utility model, the material is circulated, evaporated and crystallized in the crystallizer 1 by the forced circulation pump 2, and the evaporated material is condensed by the condenser 16; sodium citrate crystal slurry is fed into a primary crystal slurry tank 4 through a feeding pipeline 3, and after entering the primary crystal slurry tank 4, the sodium salt crystal slurry is subjected to particle layering under the action of a stirring device 5 of the primary crystal slurry tank 4, and large particles are controlled to be positioned above the primary crystal slurry tank 4 in a manner that fine particles below the large particles are positioned; detecting whether the crystal slurry in the primary crystal slurry tank 4 meets the requirement of the particle size or not through a particle size tester 8 on a discharge pipeline 7 by a primary crystal slurry pump 6, if the requirement of the particle size is not met, enabling an adjusting valve on a primary crystal slurry return pipeline 10 to be in an open state, keeping the adjusting valve on a centrifugal discharge pipeline 9 in a closed state, and enabling the crystal slurry in the primary crystal slurry tank 4 to flow back into the crystallizer 1 for secondary growth; when the particle size tester 8 detects that the particle size meets the requirement, the regulating valve on the centrifugal discharge pipeline 9 is opened, the regulating valve on the primary crystal slurry backflow pipeline 10 is closed, and the crystal slurry enters the centrifuge 11 through the centrifugal discharge pipeline 9 to be subjected to solid-liquid separation; under the action of the stirring device 5 of the primary crystal slurry tank 4, the crystal slurry in the primary crystal slurry tank 4 overflows the fine crystal slurry above the primary crystal slurry tank 4 in a particle layering manner to the secondary crystal slurry tank 13 through the overflow pipeline 12, the overflow speed of the fine crystal slurry in the secondary crystal slurry tank 13 is adjusted through the adjusting valve arranged on the overflow pipeline 12, and the fine crystal slurry in the secondary crystal slurry tank 13 returns to the crystallizer 1 through the secondary crystal slurry return pipeline under the action of the secondary crystal slurry pump 14 to perform secondary growth.
Adopt the utility model discloses, the effect is very ideal, can produce the sodium citrate of specific granularity. The problem that the sodium citrate which does not meet the requirement of granularity is returned to the feeding material due to the uneven granularity of the sodium citrate product and the existence of various granularities is avoided, and the production cost of the sodium citrate is reduced.
Claims (10)
1. A production device for controlling the granularity of sodium citrate comprises a condenser (16), a crystallizer (1), a circulating pipeline, a forced circulating pump (2), a crystal slurry tank and a centrifuge (11), wherein a stirring device (5) is arranged in the crystal slurry tank, and the production device is characterized in that the crystal slurry tank comprises a primary crystal slurry tank (4) and a secondary crystal slurry tank (13); a feed inlet of the primary crystal slurry tank (4) is connected with a circulating pipeline through a feed pipeline (3), a discharge outlet of the primary crystal slurry tank (4) is respectively connected with a primary crystal slurry backflow pipeline (10) and a centrifugal discharge pipeline (9) through a discharge pipeline (7), and a particle size tester (8) is arranged on the discharge pipeline (7); the primary crystal slurry backflow pipeline (10) is connected with the crystallizer (1), and the centrifugal discharge pipeline (9) is connected with the centrifuge (11); the primary crystal slurry tank (4) is connected with the secondary crystal slurry tank (13) through an overflow pipeline (12), and a discharge port of the secondary crystal slurry tank (13) is connected with the crystallizer (1) through a secondary crystal slurry reflux pipeline (15); crystal slurry pumps are arranged on the discharge pipeline (7) and the secondary crystal slurry backflow pipeline (15); and regulating valves are arranged on the feeding pipeline (3), the primary crystal slurry backflow pipeline (10), the centrifugal discharging pipeline (9) and the secondary crystal slurry backflow pipeline (15).
2. The production device for controlling the granularity of sodium citrate according to claim 1, wherein at least two overflow pipelines (12) are arranged.
3. The production device for controlling the granularity of sodium citrate according to claim 2, wherein the overflow pipeline (12) comprises a first overflow pipeline and a second overflow pipeline, the first overflow pipeline is installed at the position of 2/3 of the height of the straight cylinder of the primary slurry tank (4), and the second overflow pipeline is installed at the position of 1/2 of the height of the straight cylinder of the primary slurry tank (4).
4. The production device for controlling the granularity of the sodium citrate as claimed in claim 2, wherein the position of each overflow pipeline (12) connected with the primary crystal slurry tank (4) is higher than the position of each overflow pipeline (12) connected with the secondary crystal slurry tank (13).
5. The production device for controlling the granularity of the sodium citrate according to the claim 1, characterized in that the overflow pipeline (12) is provided with a regulating valve.
6. The production device for controlling the granularity of the sodium citrate according to the claim 5, wherein the feeding pipeline (3), the primary crystal slurry return pipeline (10), the centrifugal discharging pipeline (9), the secondary crystal slurry return pipeline (15), the regulating valve on the overflow pipeline (12) and the particle size tester (8) are all electrically connected with a PLC control system.
7. The production device for controlling the granularity of the sodium citrate as claimed in claim 6, wherein the regulating valve is a V-shaped stainless steel regulating valve without a sealing washer.
8. The production device for controlling the granularity of the sodium citrate according to the claim 1, wherein a tee joint is arranged at the joint of the discharge pipeline (7), the primary crystal slurry backflow pipeline (10) and the centrifugal discharge pipeline (9).
9. The production device for controlling the granularity of sodium citrate according to claim 1, characterized in that the inside of the crystallizer (1) is in a negative pressure evaporation mode.
10. The production device for controlling the granularity of the sodium citrate according to the claim 1, wherein the discharge ports of the primary crystal slurry tank (4) and the secondary crystal slurry tank (13) are arranged at the bottom, and the feed port of the primary crystal slurry tank (4) is arranged at the top.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123232156.7U CN217409792U (en) | 2021-12-21 | 2021-12-21 | Production device for controlling granularity of sodium citrate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123232156.7U CN217409792U (en) | 2021-12-21 | 2021-12-21 | Production device for controlling granularity of sodium citrate |
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| Publication Number | Publication Date |
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| CN217409792U true CN217409792U (en) | 2022-09-13 |
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| CN202123232156.7U Active CN217409792U (en) | 2021-12-21 | 2021-12-21 | Production device for controlling granularity of sodium citrate |
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- 2021-12-21 CN CN202123232156.7U patent/CN217409792U/en active Active
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