CN215136953U - Double-effect evaporation system - Google Patents
Double-effect evaporation system Download PDFInfo
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- CN215136953U CN215136953U CN202121391229.4U CN202121391229U CN215136953U CN 215136953 U CN215136953 U CN 215136953U CN 202121391229 U CN202121391229 U CN 202121391229U CN 215136953 U CN215136953 U CN 215136953U
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Abstract
The utility model provides a double-effect evaporation system, which comprises a buffer tank, a preheater, an evaporation unit and a condenser which are connected in sequence, wherein the evaporation unit comprises a first-effect evaporation unit and a second-effect evaporation unit, the first-effect evaporation unit comprises a first-effect forced circulation heat exchanger, a first circulation pump and a first-effect separator, the top of the first-effect forced circulation heat exchanger is connected with the first-effect separator, and the bottom of the first-effect forced circulation heat exchanger is connected with the first-effect separator through the first circulation pump; the two-effect evaporation unit comprises a two-effect forced circulation heat exchanger, a second circulating pump and a second-effect separator, the top of the two-effect forced circulation heat exchanger is connected with the second-effect separator, the bottom of the two-effect forced circulation heat exchanger is connected with the second-effect separator through the second circulating pump, and the second-effect forced circulation heat exchanger is connected with the top of the first-effect separator; the top of the double-effect separator is connected with a condenser, and the bottom of the double-effect separator is also connected with a thick system. The utility model discloses evaporation efficiency is high, has better cost advantage, and the system takes up an area of the space littleer, and can control the liquid level height of one effect separator and two effect separators more conveniently and keep in predetermineeing the within range.
Description
Technical Field
The utility model belongs to contain salt waste water evaporating system, concretely relates to economic benefits and social benefits evaporating system.
Background
At present, the number of the current day,the high-salt wastewater discharged by industrial production contains various non-metallic ions, wherein Cl is used-High concentration of Cl with maximum content-If the water is directly discharged, the salinity of the water is increased, so that soil salinization and plant growth are difficult, pipelines are easy to corrode, and the health of human bodies is possibly harmed. Due to Cl-Are stable and therefore difficult to remove using conventional chemical precipitation methods, and because microorganisms cannot utilize Cl-Making it difficult to remove again by biological methods. Therefore, physical methods such as membrane concentration method, evaporation method and the like are generally used.
In the prior art, document CN201823328U provides a vacuum multiple-effect forced circulation evaporation device, which includes a multiple-effect forced circulation evaporation device and a vacuum extractor for extracting gas in the multiple-effect forced circulation evaporation device, wherein the multiple-effect forced circulation evaporation device includes: the feeding main pipe is provided with a feeding main valve; at least two effect forced circulation evaporators which are communicated in sequence; each effect forced circulation evaporator comprises a heater communicated with a feeding main pipe, an evaporation chamber communicated with the heater through a circulating pipe, a forced circulation pump communicated with the circulating pipe, and a discharge hole arranged at the lower part of the circulating pipe; a steam outlet is arranged at the top of the evaporation chamber in the former effect forced circulation evaporator and is connected with a heater of the latter effect forced circulation evaporator through a pipeline; the condensation drainage device is communicated with a steam outlet at the top of the evaporation chamber of the last effect forced circulation evaporator and is used for condensing and discharging steam; a vacuum control valve for controlling the on-off of the vacuumizing device is arranged between the vacuumizing device and the multi-effect forced circulation evaporation device; a feed valve is arranged on a feed pipeline of each effect of forced circulation evaporator and is used for controlling the feed liquid to enter and exit; the forced circulation evaporator of each effect is provided with an emptying pipeline communicated with the atmosphere, and the emptying pipeline is provided with an emptying valve for controlling the on-off of the pipeline. Adopt this evaporation plant on the one hand to have the problem that is not convenient for adjust the material in the adjacent evaporation unit, evaporation efficiency remains further optimization simultaneously.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a economic benefits and social benefits vaporization system convenient to adjust material and evaporation efficiency height in the adjacent evaporation unit.
In order to achieve the above purpose, the present invention adopts the following technical solution.
A double-effect evaporation system comprises a buffer tank, a preheater, an evaporation unit and a condenser which are sequentially connected, wherein the evaporation unit comprises a first-effect evaporation unit and a second-effect evaporation unit, the first-effect evaporation unit comprises a first-effect forced circulation heat exchanger, a first circulating pump and a first-effect separator, the top of the first-effect forced circulation heat exchanger is connected with the first-effect separator, and the bottom of the first-effect forced circulation heat exchanger is connected with the first-effect separator through the first circulating pump; the two-effect evaporation unit comprises a two-effect forced circulation heat exchanger, a second circulating pump and a second-effect separator, the top of the two-effect forced circulation heat exchanger is connected with the second-effect separator, the bottom of the two-effect forced circulation heat exchanger is connected with the second-effect separator through the second circulating pump, and the second-effect forced circulation heat exchanger is connected with the top of the first-effect separator; the top of the secondary effect separator is connected with a condenser, and the bottom of the secondary effect separator is also connected with a thick system; the first-effect separator and the second-effect separator are also communicated through a material transferring pipeline, an electric proportional control valve is arranged on the material transferring pipeline, a liquid level meter is also arranged on the second-effect separator, and the liquid level meter is simultaneously connected with the electric proportional control valve; the first-effect forced circulation heat exchanger and the second-effect forced circulation heat exchanger are respectively connected with a non-condensable gas pipeline, and an electric proportional control valve for controlling the steam quantity and a shell side pressure gauge interlocked with the electric proportional control valve are arranged on the non-condensable gas pipeline; the thickening system comprises a thickening device connected with the double-effect separator, the thickening device is sequentially connected with a crystallization buffer tank, a centrifugal machine and a mother liquid tank, the mother liquid tank is simultaneously connected with the double-effect separator in a return mode, the thickening device is connected with the double-effect forced circulation heat exchanger in a return mode, and the crystallization buffer tank is directly connected with the double-effect separator through another branch.
Furthermore, the bottoms of the first-effect forced circulation heat exchanger and the second-effect forced circulation heat exchanger are respectively connected with a condensate water tank, and the condensate water tank is connected with the preheater through a pump.
Further, the condenser is also connected with a vacuum system.
Further, the double-effect evaporation system also comprises a sewage discharge pipeline, and the sewage discharge point of each connecting pipeline is connected with the sewage discharge pipeline.
Due to the adoption of the technical scheme, the utility model can achieve the evaporation efficiency equivalent to the existing triple-effect or even four-effect evaporation system through the double-effect evaporation system, has better cost advantage and occupies smaller space; through being provided with electronic proportional control valve on changeing the material pipeline, the second-effect separator is connected with the level gauge, through the aperture of level gauge control electronic proportional control valve, can control the liquid level height of first-effect separator and second-effect separator more conveniently and keep in predetermineeing the within range. The utility model discloses a economic benefits and social benefits vaporization system can avoid heat exchanger shell side pressure too high, and the security is good.
Drawings
FIG. 1 is a flow chart of the double effect evaporation system in the embodiment.
Detailed Description
The present invention will be further described with reference to the accompanying drawings and specific embodiments, but the following description of the embodiments is only for the purpose of helping understanding the principle and the core idea of the present invention, and is not intended to limit the scope of the present invention. It should be noted that modifications to the present invention may occur to those skilled in the art without departing from the principles of the present invention and are intended to fall within the scope of the appended claims.
Examples
A double-effect evaporation system is shown in figure 1 and comprises a buffer tank 201, a preheater 203, an evaporation unit and a condenser 210 which are sequentially connected, wherein the evaporation unit comprises a first-effect evaporation unit and a second-effect evaporation unit, the first-effect evaporation unit comprises a first-effect forced circulation heat exchanger 204, a first circulating pump 205 and a first-effect separator 206, the top of the first-effect forced circulation heat exchanger 204 is connected with the first-effect separator 206, and the bottom of the first-effect forced circulation heat exchanger is connected with the first-effect separator 206 through the first circulating pump 205; the two-effect evaporation unit comprises a two-effect forced circulation heat exchanger 207, a second circulating pump 208 and a two-effect separator 209, the top of the two-effect forced circulation heat exchanger 207 is connected with the two-effect separator 209, the bottom of the two-effect forced circulation heat exchanger is connected with the two-effect separator 209 through the second circulating pump 208, and the two-effect forced circulation heat exchanger 207 is simultaneously connected with the top of the first-effect separator 206; the top of the secondary effect separator 209 is connected with a condenser 210, and the bottom is also connected with a thick system; the first-effect separator 206 is communicated with the second-effect separator 209 through a material transferring pipeline 211, an electric proportional control valve is arranged on the material transferring pipeline 211, a liquid level meter 212 is also arranged on the second-effect separator 209, and the liquid level meter 212 is connected with the electric proportional control valve; the first-effect forced circulation heat exchanger 204 and the second-effect forced circulation heat exchanger 207 are respectively connected with a non-condensable gas pipeline 215, and an electric proportional control valve for controlling the steam quantity and a shell side pressure gauge interlocked with the electric proportional control valve are arranged on the pipeline of the non-condensable gas pipeline 215; the thickening system comprises a thickening device 213 connected with the double-effect separator 209, the thickening device 213 is sequentially connected with a crystallization buffer tank 218, a centrifuge 220 and a mother liquid tank 221, the mother liquid tank 221 is simultaneously connected with the double-effect separator 209, the thickening device 213 is connected with the double-effect forced circulation heat exchanger 207, and the crystallization buffer tank 218 is also directly connected with the double-effect separator 209 through another branch. The bottoms of the first-effect forced circulation heat exchanger 204 and the second-effect forced circulation heat exchanger 207 are respectively connected with a condensed water tank 224, and the condensed water tank 224 is connected with the preheater 203 through a pump; the condenser 210 is also connected to a vacuum system 223; the dual effect evaporation system further comprises a blowdown line 225, the blowdown points of each connecting line being connected to the blowdown line 225. The double-effect evaporation system adopts vacuum negative pressure operation, can improve evaporation efficiency and reduce liquid phase temperature, thereby prolonging the service life of the evaporation equipment, the vacuum of the system can be provided by a water ring vacuum pump, most of working liquid can be recycled, and the discharged part can be utilized together with condensed water. The double-effect evaporation system can achieve the evaporation efficiency equivalent to that of the existing triple-effect or even four-effect evaporation system, has better cost advantage and occupies smaller space.
In the operation process, the raw materials enter a buffer tank 201 and enter a preheater 203 (plate heat exchanger) through a feed pump 202 for preheating, the preheated raw materials enter a first-effect forced circulation heat exchanger 204, and then the raw materials reaching the evaporation temperature are conveyed to a first-effect separator 206 connected with the first-effect forced circulation heat exchanger through a first circulation pump 205; the steam separated by the first-effect separator 206 enters the second-effect forced circulation heat exchanger 207 from the top end, then the raw material reaching the evaporation temperature is conveyed to the second-effect separator 209 connected with the second-effect separator for gas-liquid separation by the second circulating pump 208, and the separated steam enters the final-effect condenser 210 from the top end of the second-effect separator 209 for condensation; a material transferring pipeline 211 is further arranged between the first-effect separator 206 and the second-effect separator 209, an electric proportional control valve is arranged on the material transferring pipeline 211, the second-effect separator 209 is connected with a liquid level meter 212, and the opening degree of the electric proportional control valve is controlled by the liquid level meter 212, so that the liquid level heights of the first-effect separator 206 and the second-effect separator 209 are kept within a preset range; the bottom of the two-effect separator 209 is connected with a thickener 213 through a pipeline, part of the concentrated solution enters the thickener 213 from the two-effect separator 209 and precipitates crystals, and the other part of the concentrated solution further enters a crystallization buffer tank 218 and precipitates crystals.
Wherein, the tube side of the first-effect forced circulation heat exchanger 204 is filled with materials, the shell side is filled with fresh steam (in the figure, fresh steam is filled in a fresh steam conveying pipeline 214), heat exchange is carried out between the raw materials and the fresh steam to provide a heat source for evaporation, the solution reaching the evaporation temperature is provided with a dynamic head by a forced circulation pump 205 and conveyed into the first-effect separator 206 through the first-effect forced circulation heat exchanger 3, flash evaporation is carried out in the first-effect separator 206 for gas-liquid separation, the separated steam enters the shell side of the second-effect forced circulation heat exchanger 207 from the top end of the first-effect separator 206, the separated liquid enters a large pipeline from the bottom of the first-effect separator 206 and continues to circulate through the forced circulation pump, the secondary steam of the first-effect evaporation enters the shell side of the second-effect forced circulation heat exchanger 205 to exchange heat with the materials in the tube side of the second-effect forced circulation heat exchanger 207 to provide a heat source for the evaporation of the solution in the second-effect forced circulation heat exchanger 207, a communicating pipeline line 211 (namely, a material transferring pipeline 211) is arranged between the first-liquid separating device 206 and the second-separating device 209, the solution in the first-effect separator 206 is transferred to the second-effect separator 209 through an electric proportional control valve on the pipeline 211, the liquid level is supplied to the second-effect separator 209, the solution reaching the evaporation temperature is provided with dynamic pressure through a forced circulation pump and is conveyed to the second-effect separator 209 through the second-effect forced circulation heat exchanger 207 to be flashed and separated into gas and liquid, the separated steam enters a last-effect condenser 210 from the top end of the second-effect separator 209 in a shell pass and exchanges heat with circulating cooling water in a tube pass to be condensed, the condensed distilled water is discharged out of a system, the liquid separated in the second-effect separator 209 enters a large pipeline from the bottom of the separator and continues to circulate through the forced circulation pump 208, and the concentrated solution reaches a certain concentration and enters thick precipitated crystals in the thick system.
The first-effect forced circulation heat exchanger 204 and the second-effect forced circulation heat exchanger 207 are connected with a non-condensable gas pipeline 215, an electric proportional control valve for controlling the steam quantity and a first-effect shell-side pressure gauge interlocked with the electric proportional control valve are arranged on the non-condensable gas pipeline connected with the first-effect forced circulation heat exchanger 204, and a non-condensable gas pipeline connected with the second-effect forced circulation heat exchanger 207 is provided with a pressure gauge for controlling the steam quantity
The electric proportional control valve of the amount and the two-effect shell pass pressure gauge interlocked with the electric proportional control valve are controlled by a program to control the opening of the electric proportional control valve by the one-effect shell pass pressure gauge and the two-effect shell pass pressure gauge, thereby controlling the input amount of fresh steam and avoiding the danger caused by overhigh shell pass pressure.
Claims (4)
1. The utility model provides a economic benefits and social benefits vaporization system, includes buffer tank (201), pre-heater (203), evaporation unit and condenser (210) that connect gradually, its characterized in that: the evaporation unit comprises a first-effect evaporation unit and a second-effect evaporation unit, the first-effect evaporation unit comprises a first-effect forced circulation heat exchanger (204), a first circulation pump (205) and a first-effect separator (206), the top of the first-effect forced circulation heat exchanger (204) is connected with the first-effect separator (206), and the bottom of the first-effect forced circulation heat exchanger is connected with the first-effect separator (206) through the first circulation pump (205); the two-effect evaporation unit comprises a two-effect forced circulation heat exchanger (207), a second circulating pump (208) and a two-effect separator (209), the top of the two-effect forced circulation heat exchanger (207) is connected with the two-effect separator (209), the bottom of the two-effect forced circulation heat exchanger is connected with the two-effect separator (209) through the second circulating pump (208), and the two-effect forced circulation heat exchanger (207) is simultaneously connected with the top of the first-effect separator (206); the top of the two-effect separator (209) is connected with a condenser (210), and the bottom is also connected with a thick system; the first-effect separator (206) is communicated with the second-effect separator (209) through a material transferring pipeline (211), an electric proportional control valve is arranged on the material transferring pipeline (211), a liquid level meter (212) is also arranged on the second-effect separator (209), and the liquid level meter (212) is connected with the electric proportional control valve at the same time; the first-effect forced circulation heat exchanger (204) and the second-effect forced circulation heat exchanger (207) are respectively connected with a non-condensable gas pipeline (215), and an electric proportional control valve for controlling the steam quantity and a shell side pressure gauge interlocked with the electric proportional control valve are arranged on the pipeline of the non-condensable gas pipeline (215); the thickening system comprises a thickening device (213) connected with the double-effect separator (209), the thickening device (213) is sequentially connected with a crystallization buffer tank (218), a centrifuge (220) and a mother liquor tank (221) in sequence, the mother liquor tank (221) is simultaneously connected with the double-effect separator (209) in a return mode, the thickening device (213) is connected with the double-effect forced circulation heat exchanger (207) in a return mode, and the crystallization buffer tank (218) is directly connected with the double-effect separator (209) through another branch.
2. The dual effect evaporation system of claim 1, wherein: the bottoms of the first-effect forced circulation heat exchanger (204) and the second-effect forced circulation heat exchanger (207) are respectively connected with a condensed water tank (224), and the condensed water tank (224) is connected with the preheater (203) through a pump.
3. The dual effect evaporation system of claim 2, wherein: the condenser (210) is also connected to a vacuum system (223).
4. The dual effect evaporation system of claim 3, wherein: the double-effect evaporation system also comprises a sewage discharge pipeline (225), and the sewage discharge point of each connecting pipeline is connected with the sewage discharge pipeline (225).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121391229.4U CN215136953U (en) | 2021-06-22 | 2021-06-22 | Double-effect evaporation system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121391229.4U CN215136953U (en) | 2021-06-22 | 2021-06-22 | Double-effect evaporation system |
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| CN215136953U true CN215136953U (en) | 2021-12-14 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114797137A (en) * | 2022-05-09 | 2022-07-29 | 四川永祥股份有限公司 | System for retrieve salt and nitre among nitre centrifugation mother liquor |
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2021
- 2021-06-22 CN CN202121391229.4U patent/CN215136953U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114797137A (en) * | 2022-05-09 | 2022-07-29 | 四川永祥股份有限公司 | System for retrieve salt and nitre among nitre centrifugation mother liquor |
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