CN220546585U - Evaporation system for caustic soda flakes preparation - Google Patents
Evaporation system for caustic soda flakes preparation Download PDFInfo
- Publication number
- CN220546585U CN220546585U CN202322069274.3U CN202322069274U CN220546585U CN 220546585 U CN220546585 U CN 220546585U CN 202322069274 U CN202322069274 U CN 202322069274U CN 220546585 U CN220546585 U CN 220546585U
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- China
- Prior art keywords
- flash tank
- caustic soda
- evaporation system
- evaporation
- communicating vessel
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- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 title claims abstract description 135
- 238000001704 evaporation Methods 0.000 title claims abstract description 53
- 230000008020 evaporation Effects 0.000 title claims abstract description 49
- 238000002360 preparation method Methods 0.000 title claims abstract description 8
- 235000011121 sodium hydroxide Nutrition 0.000 title abstract description 44
- 239000003513 alkali Substances 0.000 claims abstract description 47
- 239000011552 falling film Substances 0.000 claims description 16
- 238000004094 preconcentration Methods 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 239000003518 caustics Substances 0.000 claims 1
- 238000009834 vaporization Methods 0.000 claims 1
- 230000008016 vaporization Effects 0.000 claims 1
- 238000005260 corrosion Methods 0.000 abstract description 5
- 230000007797 corrosion Effects 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- 230000000694 effects Effects 0.000 description 7
- 238000012545 processing Methods 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 230000006872 improvement Effects 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 230000008859 change Effects 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000009699 differential effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to the technical field of caustic soda evaporation, and discloses a caustic soda flake preparation evaporation system which comprises a final concentrator, a flash tank, a surface condenser and a vacuum pump, wherein the surface condenser is communicated with the flash tank and the surface condenser is communicated with the vacuum pump through pipelines, and a communicating vessel for simultaneously controlling the pressure in the final concentrator and the flash tank is connected between the final concentrator and the flash tank. The utility model can solve the problems of high temperature of finished alkali produced by the existing caustic soda evaporation system, high energy consumption of the system and quick corrosion of equipment.
Description
Technical Field
The utility model relates to the technical field of caustic soda evaporation, in particular to a caustic soda flake preparation evaporation system.
Background
Caustic soda is a strong alkali with strong corrosiveness, and solid caustic soda is generally in the form of flakes or granules, also known as caustic soda flakes or granules. In the process of processing caustic soda flakes, caustic soda with high concentration is firstly prepared by evaporating caustic soda with low concentration, and then the caustic soda with high concentration is cooled and molded to be shaped into flakes.
In the evaporation system of 99% caustic soda, in the final stage of caustic soda evaporation, in order to ensure the evaporation degree of caustic soda, the final concentration and flash evaporation tank flash evaporation mode is adopted for evaporation treatment, by adopting the evaporation mode, the concentration of the alkali liquor at the outlet of the final concentrator can reach 98%, the temperature is about 390 ℃, the pressure is 40KPa, the back alkali liquor enters the flash evaporation tank for flash evaporation under normal pressure, the concentration of the alkali liquor after flash evaporation can reach about 99%, the alkali liquor produced by adopting the processing mode can better reach the requirement of 99% concentration in concentration, but the temperature of the finished alkali liquor finally coming out of the flash evaporation tank is very high, usually up to about 380 ℃, the system needs to heat the alkali liquor to such high temperature, more heat is consumed in the process, the corresponding natural gas consumed is more, meanwhile, the caustic soda has stronger corrosiveness, and the corrosion to equipment is accelerated when the caustic soda has higher temperature.
Disclosure of Invention
The utility model aims to provide a caustic soda flake preparation evaporation system to solve the problems of high temperature, high energy consumption and quick equipment corrosion of finished caustic soda produced by the existing caustic soda evaporation system.
In order to achieve the above purpose, the utility model adopts the following technical scheme: the caustic soda flake preparation evaporation system comprises a final concentrator and a flash tank, and further comprises a surface condenser and a vacuum pump, wherein the surface condenser is communicated with the flash tank and the surface condenser is communicated with the vacuum pump through pipelines, and a pressure controller for simultaneously controlling the pressure in the final concentrator and the pressure in the flash tank is connected between the final concentrator and the flash tank.
The principle of the scheme is as follows: in this scheme, through connecting the surface condenser on the flash tank, and further connect the vacuum pump on the surface condenser, when the vacuum pump is during operation, it takes out the noncondensable gas in flash tank and the surface condenser. Meanwhile, along with the work of a vacuum pump, water vapor generated by evaporation in the flash tank enters a surface condenser, the surface condenser condenses the entered water vapor into a liquid state, and the volume of the water vapor is reduced at the moment; as the surface condenser continues to operate for a period of time, the pressure differential effect of the change in water vapor volume causes a negative pressure to be created within the flash tank, which enters a higher negative pressure operating state. In the state of negative pressure operation of the flash tank, the boiling point of the lye is reduced, and the water in the lye is largely evaporated. Because the flash tank adopts the negative pressure flash evaporation with low boiling point to evaporate the alkali liquor, the temperature of the finished alkali product after the evaporation is lower, thereby effectively reducing the energy consumption of an evaporation system and simultaneously avoiding the problem of quick equipment corrosion caused by high alkali liquor temperature. In addition, the alkali liquor is evaporated more thoroughly in the negative pressure environment of the flash tank, so that the water content of the finished alkali obtained after evaporation is lower, and the problem of hardening of the solid alkali in subsequent production can be effectively prevented.
Because the flash tank is negative pressure operation, there is certain pressure differential between it and final concentrator, through connecting between the two and setting up pressure controller, can control and balance respectively the pressure between the two to make flash tank and final concentrator can independent operation, avoid the flash tank when carrying out the negative pressure flash distillation of alkali lye, inhale the alkali lye in the final concentrator in a large number, thereby influence alkali lye flash evaporation effect.
The adoption of the scheme has the advantages that:
1. the temperature of the finished alkali is lower, the energy consumed by the system for heating the caustic soda is less, and meanwhile, the corrosion to equipment is reduced;
2. the vacuum pump only works in the initial stage, and after a negative pressure environment is formed in the flash tank, the vacuum pump stops working, so that compared with an evaporation system with the continuous working of the vacuum pump, the energy consumption of the whole system can be reduced, and the energy saving is effectively realized;
3. the caustic soda is evaporated more thoroughly, and hardening phenomenon after the caustic soda is solidified is effectively prevented.
Preferably, as an improvement, the pressure controller comprises a communicating vessel, one end of the communicating vessel is connected with the final concentrator, the other end of the communicating vessel is connected with the flash tank, and a pressure control valve is arranged on the communicating vessel.
By adopting the scheme, the flow control and adjustment of the alkali liquor are realized through the pressure control valve, and the purposes of adjusting and controlling the operation pressure in the final concentrator and the flash tank respectively can be better achieved by matching with the pressure balance effect of the communicating vessel, so that the independent work of each device is ensured. The pressure control valve is adopted to regulate and control the pressure, so that the pressure control is more convenient, and the communicating vessel assists the pressure control valve to control the pressure of the equipment on two sides, so that each equipment works independently.
Preferably, as a modification, the height of the communicating vessel is less than 5m.
By adopting the scheme, when the height of the communicating vessel is kept in the range, the pressure control valve can be assisted to realize the respective control of the operation pressure of the final concentrator and the flash tank, and meanwhile, the height of the communicating vessel is smaller, so that the equipment is more convenient to construct and maintain.
Preferably, as a modification, the final concentrator comprises a finished product separator, the inlet of which is connected to a falling film pipe, and the finished product separator is provided with a steam outlet.
By adopting the scheme, when the alkali liquor is evaporated, the falling film evaporation is carried out through the falling film pipe, then the alkali liquor enters the finished product separator, steam and the alkali liquor which are evaporated are split in the finished product separator, the steam is discharged out of the finished product separator through the steam outlet, and the alkali liquor flows into the flash tank to enter the flash evaporation, so that the evaporation effect of the caustic soda and the quality of the finished product alkali are ensured.
Preferably, as an improvement, the steam outlet is connected to a pre-concentration system for pre-concentrating the lye.
By adopting the scheme, in the finished product separator, the evaporated steam and alkali liquor are split, wherein the steam flows back to the pre-concentration system again and is used for evaporating caustic soda so as to utilize the waste heat in the pre-concentration system, thereby reducing the energy consumption of the whole system.
Preferably, as an improvement, the falling film pipes are provided with a plurality of groups, and the outlets of the groups of falling film pipes are connected with the finished product separator.
By adopting the scheme, the falling film evaporation is carried out on caustic soda by the plurality of groups of falling film pipes simultaneously, so that the efficiency of caustic soda evaporation is quickened, and the productivity is improved.
Preferably, as an improvement, an alkali liquor distributor is connected to the alkali liquor outlet of the flash tank.
By adopting the scheme, the alkali liquor dispenser dispenses finished alkali and is used for subsequent processing.
Drawings
FIG. 1 is a schematic diagram of an embodiment of the present utility model.
Detailed Description
The following is a detailed description of embodiments, but embodiments of the utility model are not limited thereto. The technical means used in the following embodiments are conventional means well known to those skilled in the art unless otherwise specified; the experimental methods used are all conventional methods; the materials, reagents, and the like used are all commercially available.
Reference numerals in the drawings of the specification include: a falling film pipe 1, a finished product separator 2, a communicating vessel 3, a flash tank 4, a surface condenser 5 and a vacuum pump 6.
An embodiment is shown in fig. 1: the caustic soda flake preparation evaporation system comprises a final concentrator, wherein the final concentrator comprises a finished product separator 2, and further comprises a flash tank 4, a surface condenser 5 and a vacuum pump 6, wherein the surface condenser 5 and the flash tank 4 and the surface condenser 5 and the vacuum pump 6 are communicated through pipelines, and a pressure controller for simultaneously controlling the pressure in the final concentrator and the pressure in the flash tank 4 is connected between the finished product separator 2 and the flash tank 4.
The pressure controller in this embodiment includes a U-shaped communicating vessel 3, a pressure control valve (not shown in the figure) is installed on the communicating vessel 3, one end of the communicating vessel 3 is connected with the lye outlet of the finished product separator 2, the other end is connected with the lye inlet at the bottom of the flash tank 4, the height of the communicating vessel 3 is less than 5m, and the height of the communicating vessel 3 in this embodiment is 2m. The inlet of the finished product separator 2 is connected with a plurality of groups of falling film pipes 1, the outlets of the groups of falling film pipes 1 are connected with the alkali liquor inlet of the finished product separator 2, the steam outlet of the finished product separator 2 is connected with a pre-concentration system (not shown in the figure) for concentrating alkali liquor, the pre-concentration system in the embodiment is a common evaporation system, the specific structure of the pre-concentration system is not repeated here, and the pre-concentration system is connected with the alkali liquor inlet of the falling film pipe 1. The bottom alkali liquor outlet of the flash tank 4 is connected with an alkali liquor distributor.
In practical application, the caustic soda is evaporated by the evaporation system, and then enters the falling film pipe 1 after being evaporated by the pre-concentration system, and is evaporated in the falling film pipe 1 and then enters the finished product separator 2, the caustic soda and the water vapor generated by evaporation are separated in the finished product separator 2, the water vapor enters the pre-concentration system from the top outlet of the finished product separator 2 and is used for evaporating alkali liquor in the pre-concentration system, and the caustic soda enters the communicating vessel 3 along the finished product separator 2 and then enters the flash tank 4 along the communicating vessel 3. At the beginning, the flash tank 4 only performs normal-pressure flash evaporation, at this time, the vacuum pump 6 is started, the vacuum pump 6 sucks non-condensable gas in the flash tank 4 and the surface condenser 5 and discharges the non-condensable gas out of the boundary region, meanwhile, water vapor generated by evaporation in the flash tank 4 enters the surface condenser 5 from the top of the flash tank 4, the surface condenser 5 condenses the incoming vapor into liquid, the volume of the water vapor is reduced, due to the volume change of the water vapor, negative pressure is formed in the flash tank 4, the negative pressure effect of the surface condenser 5 on the generated negative pressure in the flash tank 4 is continuously enhanced along with continuous liquefaction of the water vapor, after a period of time, the flash tank 4 starts to enter a negative pressure working state after the non-condensable gas in the flash tank 4 and the surface condenser 5 is discharged, at this time, the vacuum pump 6 is stopped, and the negative pressure operation of the flash tank 4 is maintained by the surface condenser 5. In the negative pressure working state of the flash tank 4, the boiling point of alkali liquor in the flash tank 4 is reduced, the evaporation degree of caustic soda is increased, and the caustic soda is separated more thoroughly. The evaporated caustic soda enters the alkali liquid distributor along the outlet at the bottom of the flash tank 4, and is distributed by the alkali liquid distributor for subsequent processing. In the process, as the caustic soda is evaporated with low boiling point under the negative pressure operation environment of the flash tank 4, the temperature of the finished alkali liquor is reduced, so that the consumption of the whole system on energy is reduced, and the problem that the equipment is corroded by high-temperature alkali liquor is avoided.
When the flash tank 4 carries out negative pressure flash evaporation on caustic soda, the communicating vessel 3 adjusts the pressure at two sides, and the pressure control valve controls the flow of caustic soda, so that the pressure in the final concentrator and the flash tank 4 is better controlled and adjusted together with the cooperation of the communicating vessel 3, the final concentrator and the flash tank 4 can work independently, and the alkali liquor entering the finished product separator 2 is prevented from being sucked into the flash tank 4 under the negative pressure effect of the flash tank 4, so that the evaporating effect of the flash tank 4 on caustic soda is ensured.
The alkali liquor after flash evaporation enters an alkali liquor distributor from an outlet at the bottom of the flash evaporation tank 4, and enters a subsequent processing link after being distributed by the alkali liquor distributor.
The foregoing is merely exemplary of the present utility model, and specific technical solutions and/or features that are well known in the art have not been described in detail herein. It should be noted that, for those skilled in the art, several variations and modifications can be made without departing from the technical solution of the present utility model, and these should also be regarded as the protection scope of the present utility model, which does not affect the effect of the implementation of the present utility model and the practical applicability of the patent. The protection scope of the present application shall be subject to the content of the claims, and the description of the specific embodiments and the like in the specification can be used for explaining the content of the claims.
Claims (7)
1. The utility model provides a flake caustic manufacturing vaporization system, includes final concentrator and flash tank, its characterized in that: the device comprises a flash tank, a surface condenser, a flash tank, a pressure controller and a vacuum pump, wherein the surface condenser and the flash tank are communicated through pipelines, and the pressure controller is connected between the final concentrator and the flash tank and is used for simultaneously controlling the operating pressure in the final concentrator and the flash tank.
2. The caustic soda flake production evaporation system of claim 1, wherein: the pressure controller comprises a communicating vessel, one end of the communicating vessel is connected with the final concentrator, the other end of the communicating vessel is connected with the flash tank, and a pressure control valve is arranged on the communicating vessel.
3. The caustic soda flake production evaporation system of claim 2, wherein: the height of the communicating vessel is less than 5m.
4. A caustic soda flake preparation evaporation system according to claim 3, wherein: the final concentrator comprises a finished product separator, the inlet of the finished product separator is connected with a falling film pipe, and the finished product separator is provided with a steam outlet.
5. The caustic soda flake production evaporation system of claim 4, wherein: the steam outlet is connected with a pre-concentration system for pre-concentrating alkali liquor.
6. The caustic soda flake production evaporation system of claim 5, wherein: the falling film pipes are provided with a plurality of groups, and the outlets of the groups of falling film pipes are connected with the finished product separator.
7. The caustic soda flake production evaporation system of claim 6, wherein: an alkali liquor distributor is connected to the alkali liquor outlet of the flash tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322069274.3U CN220546585U (en) | 2023-08-01 | 2023-08-01 | Evaporation system for caustic soda flakes preparation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322069274.3U CN220546585U (en) | 2023-08-01 | 2023-08-01 | Evaporation system for caustic soda flakes preparation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220546585U true CN220546585U (en) | 2024-03-01 |
Family
ID=90004241
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322069274.3U Active CN220546585U (en) | 2023-08-01 | 2023-08-01 | Evaporation system for caustic soda flakes preparation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220546585U (en) |
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2023
- 2023-08-01 CN CN202322069274.3U patent/CN220546585U/en active Active
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