CN212581986U - Leachate cooling equipment - Google Patents
Leachate cooling equipment Download PDFInfo
- Publication number
- CN212581986U CN212581986U CN202021864326.6U CN202021864326U CN212581986U CN 212581986 U CN212581986 U CN 212581986U CN 202021864326 U CN202021864326 U CN 202021864326U CN 212581986 U CN212581986 U CN 212581986U
- Authority
- CN
- China
- Prior art keywords
- outlet
- inlet
- vacuum
- leachate
- vacuum cooling
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a leachate cooling arrangement, leachate cooling arrangement includes: a first vacuum cooling device, the first vacuum cooling device having a vacuum cooling cavity, a leachate inlet, a gas outlet, and a concentrate outlet, each of the leachate inlet, the gas outlet, and the concentrate outlet being in communication with the vacuum cooling cavity, at least a portion of a wall of the vacuum cooling cavity being a polished surface; the first vacuum generator is connected with the gas outlet; the first homogenizing device is matched with the first vacuum cooling device; the solid-liquid separation device is provided with a solid-liquid separation cavity, a concentrated solution inlet, a clear solution outlet and an underflow slurry outlet, each of the concentrated solution inlet, the clear solution outlet and the underflow slurry outlet is communicated with the solid-liquid separation cavity, and the concentrated solution inlet is communicated with the concentrated solution outlet. The utility model discloses a leachate cooling arrangement has the difficult scale deposit of calcium sulfate, can long-time steady operation's advantage.
Description
Technical Field
The utility model belongs to the technical field of the metal smelting, specifically relate to a leachate cooling arrangement.
Background
In the wet smelting process, because the feed liquid is recycled, and the raw and auxiliary materials contain a certain amount of calcium, a large amount of calcium ions are usually dissolved out in the sulfuric acid leaching process of valuable metals, and the condition of supersaturation of the calcium ions even occurs in partial working conditions. The temperature of the leaching solution is usually above 80 ℃ in the hydrometallurgical process of nickel, cobalt, copper and zinc, the subsequent processes such as extraction, electrodeposition and the like need to cool the material solution to be within 45 ℃, and the concentration of valuable metal ions in the cooled solution is improved as much as possible.
In the related technology, when leachate supersaturated with calcium ions is cooled by using an indirect heat exchanger, a large amount of calcium sulfate crystals are separated out on the inner wall of the heat exchanger and form dirt to block a flow channel due to rapid cooling of feed liquid. The indirect heat exchanger is frequently blocked and difficult to clean, a large amount of manpower is needed for disassembly and cleaning during large-scale continuous production, the labor intensity and the environment are severe, and the loss amount of valuable metals is large. When the leachate supersaturated with calcium ions is directly cooled by using the air cooling tower, although the cooling effect is better and the leachate has a certain concentration effect on feed liquid, the foam supplementing efficiency in the air cooling process cannot reach 100% of that of the first vacuum cooling device, a small amount of heavy metal foam inevitably overflows from the top of the tower, and a certain amount of acid mist is accompanied, so that the site environment is poor and the pollution is large.
SUMMERY OF THE UTILITY MODEL
The present invention aims at solving at least one of the technical problems in the related art to a certain extent. To this end, the embodiment of the utility model provides a leachate cooling arrangement.
According to the utility model discloses leachate cooling arrangement, include:
a first vacuum cooling device having a vacuum cooling chamber, a leachate inlet, a gas outlet, and a concentrate outlet, each of the leachate inlet, the gas outlet, and the concentrate outlet in communication with the vacuum cooling chamber, at least a portion of a wall of the vacuum cooling chamber being a polished surface;
a first vacuum generator connected to the gas outlet;
a first homogenizing device cooperating with the first vacuum cooling device; and
the solid-liquid separation device is provided with a solid-liquid separation cavity, a concentrated solution inlet, a clear solution outlet and an underflow slurry outlet, each of the concentrated solution inlet, the clear solution outlet and the underflow slurry outlet is communicated with the solid-liquid separation cavity, and the concentrated solution inlet is communicated with the concentrated solution outlet.
Therefore, according to the utility model discloses leachate cooling arrangement has the difficult scale deposit of calcium sulfate, can long-time steady operation's advantage.
In some embodiments, the leachate cooling apparatus according to embodiments of the present disclosure further includes:
a surface condenser having a condensing chamber, a gas inlet, a non-condensable gas outlet, and a first condensed water outlet, each of the gas inlet, the non-condensable gas outlet, and the condensed water outlet being in communication with the condensing chamber, the gas inlet being in communication with the gas outlet, the non-condensable gas outlet being in communication with the first vacuum generator;
the condensate tank is provided with a condensate inlet and a second condensate outlet, and the condensate inlet is communicated with the first condensate outlet; and
a water inlet of the delivery pump is communicated with a second condensate outlet of the condensate tank,
optionally, the surface condenser is one of a plate cooler, a spiral plate cooler, a tube and shell cooler.
In some embodiments, the leachate cooling apparatus according to embodiments of the present disclosure further includes:
the cyclone liquid-foam separator is provided with a separation cavity;
the foam supplementing device is detachably arranged at the gas outlet;
a first end of the steam collecting pipe is connected with the gas outlet, and a second end of the steam collecting pipe is communicated with the separation cavity;
a first end of the gas outlet pipe is communicated with the separation cavity, and a second end of the gas outlet pipe is communicated with the gas inlet; and
the upper end of the liquid outlet pipe is communicated with the separation cavity, the lower end of the liquid outlet pipe is communicated with the vacuum cooling cavity, and optionally, the liquid outlet pipe is obliquely arranged.
In some embodiments, the leachate cooling apparatus according to embodiments of the present disclosure further includes:
a second vacuum cooling device having a second vacuum cooling chamber, a second concentrate inlet, a second gas outlet, and a second concentrate outlet, each of the second concentrate inlet, the second gas outlet, and the second concentrate outlet in communication with the second vacuum cooling chamber, at least a portion of a wall of the second vacuum cooling chamber having a polished surface, the second concentrate inlet in communication with the concentrate outlet, the second concentrate outlet in communication with the concentrate inlet;
a second homogenizing device cooperating with the second vacuum cooling device;
optionally, the concentrate outlet of the first vacuum cooling device is at a higher elevation than the second concentrate inlet of the second vacuum cooling device.
In some embodiments, the leachate cooling apparatus according to embodiments of the present disclosure further comprises
A second vacuum generator having a second gas inlet and a second gas outlet, the second gas inlet being in communication with the second end of the gas outlet tube, the second gas outlet being in communication with the gas inlet,
optionally, the first vacuum generator is a vacuum pump and the second vacuum generator is a vapor compressor or a vapor jet pump.
In some embodiments, the first homogenizing device comprises an agitator disposed within the vacuum cooling chamber;
in some embodiments, the first homogenizing device comprises a circulation pump, the first vacuum cooling device further has a circulation liquid inlet and a circulation liquid outlet, a liquid inlet of the circulation pump is communicated with the circulation liquid outlet of the first vacuum cooling device, a liquid outlet of the circulation pump is communicated with the circulation liquid outlet of the first vacuum cooling device, and optionally, the circulation liquid outlet and the leachate inlet are the same opening.
In some embodiments, the cooling apparatus further comprises an underflow pump and a backwash pump, wherein a water inlet of the underflow pump is connected to the underflow outlet, a water inlet of the backwash pump is connected to the underflow outlet, and a water outlet of the backwash pump is connected to the concentrate inlet.
In some embodiments, the solid-liquid separation device is a thickener or a settling tank.
Drawings
Fig. 1 is a structural schematic diagram of leachate cooling equipment according to an embodiment of the present invention.
Fig. 2 is a structural schematic diagram of leachate cooling equipment according to the embodiment of the utility model.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings. The embodiments described below with reference to the drawings are exemplary and intended to be used for explaining the present invention, and should not be construed as limiting the present invention.
A leachate cooling apparatus 1000 according to an embodiment of the present invention is described below with reference to the drawings. As shown in fig. 1 and 2, the leachate cooling apparatus 1000 includes a first vacuum cooling device 100, a first vacuum generator 200, a first homogenizing device, and a solid-liquid separating device 400.
The first vacuum cooling apparatus 100 has a vacuum cooling chamber 101, a leachate inlet 102, a gas outlet 103, and a concentrate outlet 104, each of the leachate inlet 102, the gas outlet 103, and the concentrate outlet 104 is in communication with the vacuum cooling chamber 101, and at least a portion of a wall of the vacuum cooling chamber 101 is a polishing surface. The first vacuum generator 200 is connected to the gas outlet 103 so as to make the first vacuum cooling apparatus 100 have a predetermined vacuum degree. The first homogenizing device cooperates with the first vacuum cooling device 100.
The solid-liquid separation device 400 has a solid-liquid separation chamber 401, a concentrate inlet 402, a clear liquid outlet 403, and an underflow outlet 404, each of the concentrate inlet 402, the clear liquid outlet 403, and the underflow outlet 404 is communicated with the solid-liquid separation chamber 401, and the concentrate inlet 402 is communicated with the concentrate outlet 104.
In the related technology, although the air cooling tower has a good cooling effect and has a certain concentration effect on the feed liquid, a small amount of heavy metal spray inevitably overflows from the top of the tower in the air cooling process, and a certain amount of acid mist is accompanied, so that valuable metal loss and environmental pollution are caused.
The leachate is subjected to vacuum flash cooling in the first vacuum cooling device 100 so as to achieve concentration and temperature reduction. During this vacuum flash cooling process, as the water in the leachate is evaporated, the calcium concentration in the leachate gradually increases, resulting in the precipitation of supersaturated calcium sulfate in the leachate (concentrate). Furthermore, the leachate may be fed substantially continuously to the first vacuum cooling apparatus 100 for vacuum flash cooling, i.e. fresh leachate may be fed to the first vacuum cooling apparatus 100.
According to the utility model discloses leachate cooling arrangement 1000 is through setting up first evener to can make the leachate misce bene in the first vacuum cooling device 100. Therefore, not only can the temperature distribution of the leachate in the first vacuum cooling device 100 be uniform, but also more importantly, the calcium ion concentration of the leachate in the first vacuum cooling device 100 can be uniformly distributed, so that the local calcium ion concentration of the leachate in the first vacuum cooling device 100 can be prevented from being too high, that is, the newly added leachate can dilute and reduce the calcium ion concentration of the leachate existing in the first vacuum cooling device 100, and the precipitation amount of supersaturated calcium sulfate can be reduced.
Because at least a portion of the wall of the vacuum cooling cavity 101 is polished, the precipitated supersaturated calcium sulfate does not scale up on the at least a portion of the wall of the vacuum cooling cavity 101. Therefore, after the vacuum flash evaporation cooling is finished, the precipitated supersaturated calcium sulfate leaves the first vacuum cooling device 100 along with the leaching solution (concentrated solution), so that the first vacuum cooling device 100 can normally operate for a long time, and further the leaching solution cooling device 1000 can normally operate for a long time. The leachate leaving the first vacuum cooling apparatus 100 enters a solid-liquid separation apparatus 400 to perform solid-liquid separation of the leachate, thereby obtaining a supernatant of decalcified concentrate containing no supersaturated calcium sulfate.
In addition, by providing the first vacuum cooling apparatus 100, the leachate may be concentrated while being cooled, so that the concentration of the valuable metal in the leachate is increased, which is advantageous for extraction and electrodeposition of the valuable metal.
Therefore, according to the utility model discloses leachate cooling arrangement 1000 has the difficult scale deposit of calcium sulfate, can long-time steady operation's advantage.
As shown in fig. 1 and 2, the leachate cooling apparatus 1000 includes a first vacuum cooling device 100, a first vacuum generator 200, a first homogenizing device, a solid-liquid separating device 400, a cyclone liquid-foam separator 600, and a surface condenser 500.
The first vacuum cooling apparatus 100 has a vacuum cooling chamber 101, a leachate inlet 102, a gas outlet 103, and a concentrate outlet 104, each of the leachate inlet 102, the gas outlet 103, and the concentrate outlet 104 is in communication with the vacuum cooling chamber 101, and at least a portion of a wall of the vacuum cooling chamber 101 is a polishing surface. The leachate may be introduced into the vacuum cooling chamber 101 through the leachate inlet 102, and the leachate is vacuum flash cooled in the first vacuum cooling apparatus 100 to obtain separated steam and concentrate. The steam carries away a large amount of heat from the leaching solution in order to lower the temperature of the leaching solution.
As shown in fig. 1 and 2, the first vacuum generator 200 is connected to the gas outlet 103. The first vacuum generator 200 may draw gas from the vacuum cooling chamber 101 through the gas outlet 103 to create a low pressure environment for vacuum flash cooling of the leachate. Furthermore, the vacuum generator 200 may also draw the vapor out of the gas outlet 103. Optionally, the first vacuum generator 200 is a vacuum pump.
The first homogenizing device cooperates with the first vacuum cooling device 100.
As shown in FIG. 1, in some embodiments, the first homogenizing device comprises an agitator 300, and the agitator 300 is disposed within the vacuum cooling chamber 101. The stirrer 300 stirs the leachate (concentrated solution) in the vacuum cooling chamber 101 and the leachate which is continuously added, so that the temperature and concentration of the leachate (concentrated solution) and the leachate which is continuously added are uniformly distributed, and the condition that the precipitated supersaturated calcium sulfate is accumulated and scaled is reduced.
As shown in fig. 2, in some embodiments, the first homogenizing device includes a circulation pump 310, the first vacuum cooling device 100 further has a circulation liquid inlet 105 and a circulation liquid outlet 106, the circulation liquid inlet 105 and the circulation liquid outlet 106 are communicated with the vacuum cooling chamber 101, a liquid inlet of the circulation pump 310 is communicated with the circulation liquid outlet 106 of the first vacuum cooling device 100, and a liquid outlet of the circulation pump 310 is communicated with the circulation liquid outlet 106 of the first vacuum cooling device 100. The circulating pump 310 makes the leachate flow continuously, so that the temperature and concentration of the leachate in the vacuum cooling cavity 101 are distributed uniformly, and the condition that the precipitated supersaturated calcium sulfate is accumulated and scaled is reduced. Optionally, the recycle liquid outlet 106 is the same opening as the leachate inlet 102.
As shown in fig. 1 and 2, the leachate cooling apparatus 1000 further comprises a demister 610, a steam collecting pipe 620, a gas outlet pipe 630 and a liquid outlet pipe 640. A demister 610 is detachably provided in the gas outlet 103. The steam discharged from the gas outlet 103 passes through the foam compensating device 610, the foam compensating device 610 can liquefy heavy metal mist carried by the steam, and the liquefied heavy metal mist can flow back to the leachate in the vacuum cooling cavity 101, so as to prevent the loss of heavy metal. The foam supplement device 610 is set to be in a detachable mode, so that calcium sulfate scaling is convenient to replace and clean.
A first end of the manifold 620 is connected to the gas outlet 103 and a second end of the manifold 620 is in communication with the separation chamber. The steam discharged from the gas outlet 103 enters the separation cavity of the cyclone liquid-foam separator 600 through the steam collecting pipe 620, and heavy metal mist (heavy metal mist not liquefied by the mist compensator 610) in the steam is separated into recovery liquid in the separation cavity. The upper end of the liquid outlet pipe 640 is communicated with the separation cavity, and the lower end of the liquid outlet pipe 640 is communicated with the vacuum cooling cavity 101. The recovered liquid thus separated can be returned to the vacuum cooling chamber 101 through 640. Optionally, drain pipe 640 is disposed obliquely to facilitate heavy metal liquid to flow into vacuum cooling chamber 101 by itself.
A first end of the outlet pipe 630 is communicated with the separation chamber, and a second end of the outlet pipe 630 is communicated with the gas inlet of the surface condenser 500. The swirling steam leaving the separation chamber enters the surface condenser 500 through outlet pipe 630.
As shown in fig. 1 and 2, the surface condenser 500 has a condensation chamber, a gas inlet, a non-condensable gas outlet, and a first condensed water outlet, each of the gas inlet, the non-condensable gas outlet, and the condensed water outlet being communicated with the condensation chamber, the gas inlet being communicated with the gas outlet 103, and the non-condensable gas outlet being communicated with the first vacuum generator 200. The surface condenser 500 condenses the swirling steam leaving the separation chamber.
Alternatively, surface condenser 500 is one of a plate cooler, a spiral plate cooler, a tube and shell cooler, and a shell and tube cooler.
As shown in fig. 1 and 2, in some embodiments, the leachate cooling apparatus 1000 further comprises a condensate tank 510 and a transfer pump 520. The condensate tank 510 has a condensate inlet and a second condensate outlet, the condensate inlet communicating with the first condensate outlet. The water inlet of the transfer pump 520 is communicated with the second condensed water outlet of the condensed water tank 510. The swirling steam enters the condensing cavity from the gas inlet to be condensed, and condensed water and non-condensable gas are obtained. The non-condensable gas is discharged from the non-condensable gas outlet to the surface condenser 500, and then is discharged into the air through the first vacuum generator 200. The condensed water is discharged from the first condensed water outlet to the surface condenser 500, and then enters the condensed water tank 510, and the condensed water in the condensed water tank 510 is periodically discharged by the transfer pump 520.
As shown in fig. 1, in some embodiments, the leachate cooling apparatus 1000 further comprises a second vacuum cooling device 110 and a second homogenizing device.
The second vacuum cooling device 110 has a second vacuum cooling chamber 111, a second concentrated solution inlet 112, a second gas outlet 113 and a second concentrated solution outlet 114, each of the second concentrated solution inlet 112, the second gas outlet 113 and the second concentrated solution outlet 114 is communicated with the second vacuum cooling chamber 111, at least one part of the wall surface of the second vacuum cooling chamber 111 is a polished surface, the second concentrated solution inlet 112 is communicated with the concentrated solution outlet, and the second concentrated solution outlet 114 is communicated with the concentrated solution inlet 402. The second gas outlet 113 is connected to the first vacuum generator 200 so that the second vacuum cooling chamber 111 has the low pressure environment required for vacuum flash cooling to occur.
The concentrated solution from the first vacuum cooling device 100 enters the second vacuum cooling device 110 through the second concentrated solution inlet 112 to be vacuum flash-cooled again, and the concentrated solution is cooled and concentrated for the second time to obtain the second steam and the second concentrated solution. The second concentrate is at a lower temperature and a higher concentration than the concentrate exiting the first vacuum cooling apparatus 100.
The second vapor is drawn out by the first vacuum generator 200 through the second gas outlet 113. A cyclone liquid-foam separator 600 and a surface condenser 500 may be disposed between the second vacuum cooling device 110 and the first vacuum generator 200. Heavy metal mist in the second steam can be recovered by the cyclone liquid-foam separator 600, the second steam can be condensed by the surface condenser 500 to obtain second non-condensable gas, and the second non-condensable gas can be pumped out by the first vacuum generator 200.
The second concentrated liquid is discharged from the second concentrated liquid outlet 114 to the second vacuum cooling apparatus 110, and then enters the solid-liquid separation apparatus 400 through the concentrated liquid inlet 402.
The second homogenizing device is matched with the second vacuum cooling device 110, the second homogenizing device is a stirrer 300, concentrated liquid in the second vacuum cooling device 110 is stirred to enable the temperature and the concentration of the concentrated liquid to be uniformly distributed, and the situation that precipitated supersaturated calcium sulfate is accumulated and scaled is reduced.
Optionally, the height of the concentrate outlet 104 of the first vacuum cooling device 100 is higher than the height of the second concentrate inlet 112 of the second vacuum cooling device 110. So that the concentrate can flow into the second vacuum cooling device 110 by gravity.
As shown in fig. 2, in some embodiments, the leachate cooling apparatus 1000 further comprises a second vacuum generator 210 having a second gas inlet in communication with the second end of the gas outlet pipe 630 and a second gas outlet in communication with the gas inlet of the surface condenser 500.
The second vacuum generator 210 further vacuumizes the first vacuum cooling device 100, further reducing the pressure in the vacuum cooling cavity, thereby enhancing the effect of vacuum flash cooling, further reducing the temperature of the concentrated solution, and increasing the concentration of the concentrated solution.
Optionally, the second vacuum generator 210 is a vapor compressor or a vapor jet pump.
As shown in fig. 1 and 2, the solid-liquid separation device 400 has a solid-liquid separation chamber 401, a concentrate inlet 402, a clear liquid outlet 403, and an underflow outlet 404, each of the concentrate inlet 402, the clear liquid outlet 403, and the underflow outlet 404 is communicated with the solid-liquid separation chamber 401, and the concentrate inlet 402 is communicated with the concentrate outlet.
The leachate cooling apparatus 1000 further comprises an underflow pump 410 and a reflux pump (not shown), wherein a water inlet of the underflow pump 410 is connected to the underflow outlet 404, a water inlet of the reflux pump is connected to the underflow outlet 404, and a water outlet of the reflux pump is connected to the concentrate inlet 402.
The temperature of the concentrated solution entering the solid-liquid separation device 400 is less than or equal to 45 ℃, the retention time of the concentrated solution entering the solid-liquid separation device 400 is more than or equal to 12 hours, and the sufficient solid-liquid separation time and the solid-liquid separation effect of the concentrated solution are ensured. The concentrated solution is subjected to solid-liquid separation in the solid-liquid separation cavity 401 so as to obtain decalcified concentrated clear solution and underflow liquid. The supersaturated calcium sulfate precipitated from the concentrated solution is deposited to form underflow slurry, a part of the underflow slurry is pumped out by the backflow pump and then enters the solid-liquid separation device 400 from the concentrated solution inlet 402 again to be used as seed crystals, and a part of the underflow slurry is discharged from the underflow slurry outlet 404 by the underflow pump 410. The decalcified concentrate obtained by decalcifying the concentrate is discharged from the clear liquid outlet 403.
Alternatively, the solid-liquid separation device 400 is a thickener or a settling tank.
The application also provides a leachate cooling process implemented by using the leachate cooling apparatus 1000, which comprises the following steps:
A) performing primary vacuum flash evaporation cooling on the leachate by using a first vacuum cooling device 100 so as to obtain separated steam and concentrated solution, and uniformly treating the leachate in the primary vacuum flash evaporation cooling process; and
B) the concentrated solution is added into a solid-liquid separation device 400, and solid-liquid separation is performed on the concentrated solution, so that decalcified concentrated clear solution and underflow fluid are obtained.
C) Introducing the steam into the cyclone liquid-foam separator 600 to separate the steam into cyclone steam and recovered liquid, and introducing the recovered liquid into the first vacuum cooling device 100 as a return material; and
D) the swirling steam is introduced into the surface condenser 500 to be condensed, so that condensed water and non-condensable gas can be obtained, the non-condensable gas is extracted through the first vacuum generator 200, and the condensed water is conveyed into the water condensing tank 510.
According to the utility model discloses leachate cooling process carries out vacuum flash evaporation cooling through making the leachate in first vacuum cooling device 100 to realize concentrating and cooling. During this vacuum flash cooling process, as the water in the leachate is evaporated, the calcium concentration in the leachate gradually increases, resulting in the precipitation of supersaturated calcium sulfate in the leachate (concentrate). Furthermore, the leachate may be fed substantially continuously to the first vacuum cooling apparatus 100 for vacuum flash cooling, i.e. fresh leachate may be fed to the first vacuum cooling apparatus 100.
While the leachate is vacuum flash cooled in the first vacuum cooling device 100, the leachate in the first vacuum cooling device 100 is uniformly mixed by using a first homogenizing device. Therefore, not only can the temperature distribution of the leachate in the first vacuum cooling device 100 be uniform, but also more importantly, the calcium ion concentration of the leachate in the first vacuum cooling device 100 can be uniformly distributed, so that the local calcium ion concentration of the leachate in the first vacuum cooling device 100 can be prevented from being too high, that is, the newly added leachate can dilute and reduce the calcium ion concentration of the leachate existing in the first vacuum cooling device 100, and the precipitation amount of supersaturated calcium sulfate can be reduced.
The steam leaving the first vacuum cooling device 100 is separated into cyclone steam and recovery liquid by the cyclone liquid-foam separator, the recovery liquid returns to the first vacuum cooling device 100 again, loss of valuable metals is reduced, and the cyclone steam is condensed to obtain condensed water and non-condensable gas.
The concentrate leaving the first vacuum cooling device 100 is fed to a separator 400 for solid-liquid separation of the leachate to obtain a decalcified concentrate clear and underflow slurry free of supersaturated calcium sulphate.
Therefore, according to the utility model discloses leachate cooling process has the difficult scale deposit of calcium sulfate, can long-time steady operation's advantage.
A leachate cooling apparatus 1000 according to some specific examples of the present invention will be described below with reference to the accompanying drawings.
As shown in fig. 1, a leachate cooling apparatus 1000 according to an embodiment of the present invention includes a first vacuum cooling device 100, a first vacuum generator 200, a first homogenizing device, a second vacuum cooling device 110, a second homogenizing device, a solid-liquid separating device 400, a cyclone liquid-foam separator 600, and a surface condenser 500.
The first vacuum cooling device 100 has a vacuum cooling chamber 101, a leachate inlet 102, a gas outlet 103, and a concentrate outlet 104, each of the leachate inlet 102, the gas outlet 103, and the concentrate outlet 104 is in communication with the vacuum cooling chamber 101, and a wall of the vacuum cooling chamber 101 is a polished surface. The leachate may be introduced into the vacuum cooling chamber 101 through the leachate inlet 102, and the leachate is vacuum flash cooled in the first vacuum cooling apparatus 100 to obtain separated steam and concentrate. The steam carries away a large amount of heat from the leaching solution in order to lower the temperature of the leaching solution.
The first vacuum generator 200 is a vacuum pump, and the first vacuum generator 200 is connected to the gas outlet 103. The first vacuum generator 200 may draw gas from the vacuum cooling chamber 101 through the gas outlet 103 to create a low pressure environment for vacuum flash cooling of the leachate. Furthermore, the vacuum generator 200 may also draw the vapor out of the gas outlet 103.
The first homogenizing device is a stirrer 300, and the stirrer 300 is disposed in the vacuum cooling chamber 101. The stirrer 300 stirs the leachate (concentrated solution) in the vacuum cooling chamber 101 and the leachate which is continuously added, so that the temperature and concentration of the leachate (concentrated solution) and the leachate which is continuously added are uniformly distributed, and the condition that the precipitated supersaturated calcium sulfate is accumulated and scaled is reduced.
As shown in fig. 1, the leachate cooling apparatus 1000 further comprises a demister 610, a steam collecting pipe 620, a gas outlet pipe 630 and a liquid outlet pipe 640. A demister 610 is detachably provided in the gas outlet 103. The steam discharged from the gas outlet 103 passes through the foam compensating device 610, the foam compensating device 610 can liquefy heavy metal mist carried by the steam, and the liquefied heavy metal mist can flow back to the leachate in the vacuum cooling cavity 101, so as to prevent the loss of heavy metal. The foam supplement device 610 is set to be in a detachable mode, so that calcium sulfate scaling is convenient to replace and clean.
A first end of the manifold 620 is connected to the gas outlet 103 and a second end of the manifold 620 is in communication with the separation chamber. The steam discharged from the gas outlet 103 enters the separation cavity of the cyclone liquid-foam separator 600 through the steam collecting pipe 620, and heavy metal mist (heavy metal mist not liquefied by the mist compensator 610) in the steam is separated into recovery liquid in the separation cavity. The upper end of the liquid outlet pipe 640 is communicated with the separation cavity, and the lower end of the liquid outlet pipe 640 is communicated with the vacuum cooling cavity 101. The recovered liquid thus separated can be returned to the vacuum cooling chamber 101 through 640. Optionally, drain pipe 640 is disposed obliquely to facilitate heavy metal liquid to flow into vacuum cooling chamber 101 by itself.
A first end of the outlet pipe 630 is communicated with the separation chamber, and a second end of the outlet pipe 630 is communicated with the gas inlet of the surface condenser 500. The swirling steam leaving the separation chamber enters the surface condenser 500 through outlet pipe 630.
As shown in fig. 1, the surface condenser 500 is a plate cooler, and the surface condenser 500 has a condensation chamber, a gas inlet, a non-condensable gas outlet, and a first condensed water outlet, each of the gas inlet, the non-condensable gas outlet, and the condensed water outlet is communicated with the condensation chamber, the gas inlet is communicated with the gas outlet 103, and the non-condensable gas outlet is communicated with the first vacuum generator 200. The surface condenser 500 condenses the swirling steam leaving the separation chamber.
The leachate cooling plant 1000 further comprises a condensate tank 510 and a transfer pump 520. The condensate tank 510 has a condensate inlet and a second condensate outlet, the condensate inlet communicating with the first condensate outlet. The water inlet of the transfer pump 520 is communicated with the second condensed water outlet of the condensed water tank 510. The swirling steam enters the condensing cavity from the gas inlet to be condensed, and condensed water and non-condensable gas are obtained. The non-condensable gas is discharged from the non-condensable gas outlet to the surface condenser 500, and then is discharged into the air through the first vacuum generator 200. The condensed water is discharged from the first condensed water outlet to the surface condenser 500, and then enters the condensed water tank 510, and the condensed water in the condensed water tank 510 is periodically discharged by the transfer pump 520.
The second vacuum cooling device 110 has a second vacuum cooling chamber 111, a second concentrated solution inlet 112, a second gas outlet 113, and a second concentrated solution outlet 114, each of the second concentrated solution inlet 112, the second gas outlet 113, and the second concentrated solution outlet 114 is communicated with the second vacuum cooling chamber 111, the wall surface of the second vacuum cooling chamber 111 is a polished surface, the second concentrated solution inlet 112 is communicated with the concentrated solution outlet, and the second concentrated solution outlet 114 is communicated with the concentrated solution inlet 402. The second gas outlet 113 is connected to the first vacuum generator 200 so that the second vacuum cooling chamber 111 has the low pressure environment required for vacuum flash cooling to occur.
The concentrated solution from the first vacuum cooling device 100 enters the second vacuum cooling device 110 through the second concentrated solution inlet 112 to be vacuum flash-cooled again, and the concentrated solution is cooled and concentrated for the second time to obtain the second steam and the second concentrated solution. The second concentrate is at a lower temperature and a higher concentration than the concentrate exiting the first vacuum cooling apparatus 100.
The second vapor is drawn out by the first vacuum generator 200 through the second gas outlet 113. A cyclone liquid-foam separator 600 and a surface condenser 500 may be disposed between the second vacuum cooling device 110 and the first vacuum generator 200. Heavy metal mist in the second steam can be recovered by the cyclone liquid-foam separator 600, the second steam can be condensed by the surface condenser 500 to obtain second non-condensable gas, and the second non-condensable gas can be pumped out by the first vacuum generator 200.
The second concentrated liquid is discharged from the second concentrated liquid outlet 114 to the second vacuum cooling apparatus 110, and then enters the solid-liquid separation apparatus 400 through the concentrated liquid inlet 402.
The second homogenizing device is a stirrer 300, and the second homogenizing device is matched with the second vacuum cooling device 110, so that the concentrated solution in the second vacuum cooling device 110 is stirred to enable the temperature and the concentration of the concentrated solution to be uniformly distributed, and the condition that precipitated supersaturated calcium sulfate is accumulated and scaled is reduced.
The height of the concentrate outlet 104 of the first vacuum cooling device 100 is higher than the height of the second concentrate inlet 112 of the second vacuum cooling device 110. So that the concentrate can flow into the second vacuum cooling device 110 by gravity.
The solid-liquid separation device 400 is a thickener, the solid-liquid separation device 400 has a solid-liquid separation chamber 401, a concentrate inlet 402, a clear liquid outlet 403 and an underflow slurry outlet 404, each of the concentrate inlet 402, the clear liquid outlet 403 and the underflow slurry outlet 404 is communicated with the solid-liquid separation chamber 401, and the concentrate inlet 402 is communicated with the concentrate outlet.
The leachate cooling apparatus 1000 further comprises an underflow pump 410 and a reflux pump (not shown), wherein a water inlet of the underflow pump 410 is connected to the underflow outlet 404, a water inlet of the reflux pump is connected to the underflow outlet 404, and a water outlet of the reflux pump is connected to the concentrate inlet 402.
The temperature of the concentrated solution entering the solid-liquid separation device 400 is less than or equal to 45 ℃, the retention time of the concentrated solution entering the solid-liquid separation device 400 is more than or equal to 12 hours, and the sufficient solid-liquid separation time and the solid-liquid separation effect of the concentrated solution are ensured. The concentrated solution is subjected to solid-liquid separation in the solid-liquid separation cavity 401 so as to obtain decalcified concentrated clear solution and underflow liquid. The supersaturated calcium sulfate precipitated from the concentrated solution is deposited to form underflow slurry, a part of the underflow slurry is pumped out by the backflow pump and then enters the solid-liquid separation device 400 from the concentrated solution inlet 402 again to be used as seed crystals, and a part of the underflow slurry is discharged from the underflow slurry outlet 404 by the underflow pump 410. The decalcified concentrate obtained by decalcifying the concentrate is discharged from the clear liquid outlet 403.
As shown in fig. 2, the leachate cooling apparatus 1000 according to another embodiment of the present invention includes a first vacuum cooling device 100, a first vacuum generator 200, a first homogenizing device, a second vacuum generator 210, a solid-liquid separating device 400, a cyclone liquid-foam separator 600, and a surface condenser 500.
The first vacuum cooling device 100 has a vacuum cooling chamber 101, a leachate inlet 102, a gas outlet 103, and a concentrate outlet 104, each of the leachate inlet 102, the gas outlet 103, and the concentrate outlet 104 is in communication with the vacuum cooling chamber 101, and a wall of the vacuum cooling chamber 101 is a polished surface. The leachate may be introduced into the vacuum cooling chamber 101 through the leachate inlet 102, and the leachate is vacuum flash cooled in the first vacuum cooling apparatus 100 to obtain separated steam and concentrate. The steam carries away a large amount of heat from the leaching solution in order to lower the temperature of the leaching solution.
The first vacuum generator 200 is a vacuum pump, and the first vacuum generator 200 is connected to the gas outlet 103. The first vacuum generator 200 may draw gas from the vacuum cooling chamber 101 through the gas outlet 103 to create a low pressure environment for vacuum flash cooling of the leachate. Furthermore, the vacuum generator 200 may also draw the vapor out of the gas outlet 103.
The first homogenizing device is a circulating pump 310, the first vacuum cooling device 100 further comprises a circulating liquid inlet 105 and a circulating liquid outlet 106, the circulating liquid inlet 105 and the circulating liquid outlet 106 are communicated with the vacuum cooling cavity 101, a liquid inlet of the circulating pump 310 is communicated with the circulating liquid outlet 106 of the first vacuum cooling device 100, and a liquid outlet of the circulating pump 310 is communicated with the circulating liquid outlet 106 of the first vacuum cooling device 100. The circulating pump 310 makes the leachate flow continuously, so that the temperature and concentration of the leachate in the vacuum cooling cavity 101 are distributed uniformly, and the condition that the precipitated supersaturated calcium sulfate is accumulated and scaled is reduced. The circulating liquid outlet 106 and the leaching liquid inlet 102 are the same opening
As shown in fig. 2, the leachate cooling apparatus 1000 further comprises a demister 610, a steam collecting pipe 620, a gas outlet pipe 630 and a liquid outlet pipe 640. A demister 610 is detachably provided in the gas outlet 103. The steam discharged from the gas outlet 103 passes through the foam compensating device 610, the foam compensating device 610 can liquefy heavy metal mist carried by the steam, and the liquefied heavy metal mist can flow back to the leachate in the vacuum cooling cavity 101, so as to prevent the loss of heavy metal. The foam supplement device 610 is set to be in a detachable mode, so that calcium sulfate scaling is convenient to replace and clean.
A first end of the manifold 620 is connected to the gas outlet 103 and a second end of the manifold 620 is in communication with the separation chamber. The steam discharged from the gas outlet 103 enters the separation cavity of the cyclone liquid-foam separator 600 through the steam collecting pipe 620, and heavy metal mist (heavy metal mist not liquefied by the mist compensator 610) in the steam is separated into recovery liquid in the separation cavity. The upper end of the liquid outlet pipe 640 is communicated with the separation cavity, and the lower end of the liquid outlet pipe 640 is communicated with the vacuum cooling cavity 101. The recovered liquid thus separated can be returned to the vacuum cooling chamber 101 through 640. Optionally, drain pipe 640 is disposed obliquely to facilitate heavy metal liquid to flow into vacuum cooling chamber 101 by itself.
A first end of the outlet pipe 630 is communicated with the separation chamber, and a second end of the outlet pipe 630 is communicated with the gas inlet of the surface condenser 500. The swirling steam leaving the separation chamber enters the surface condenser 500 through outlet pipe 630.
As shown in fig. 2, the surface condenser 500 is a plate cooler, and the surface condenser 500 has a condensation chamber, a gas inlet, a non-condensable gas outlet, and a first condensed water outlet, each of the gas inlet, the non-condensable gas outlet, and the condensed water outlet is communicated with the condensation chamber, the gas inlet is communicated with the gas outlet 103, and the non-condensable gas outlet is communicated with the first vacuum generator 200. The surface condenser 500 condenses the swirling steam leaving the separation chamber.
The leachate cooling plant 1000 further comprises a condensate tank 510 and a transfer pump 520. The condensate tank 510 has a condensate inlet and a second condensate outlet, the condensate inlet communicating with the first condensate outlet. The water inlet of the transfer pump 520 is communicated with the second condensed water outlet of the condensed water tank 510. The swirling steam enters the condensing cavity from the gas inlet to be condensed, and condensed water and non-condensable gas are obtained. The non-condensable gas is discharged from the non-condensable gas outlet to the surface condenser 500, and then is discharged into the air through the first vacuum generator 200. The condensed water is discharged from the first condensed water outlet to the surface condenser 500, and then enters the condensed water tank 510, and the condensed water in the condensed water tank 510 is periodically discharged by the transfer pump 520.
The second vacuum generator 210 is a vapor compressor, and the second vacuum generator has a second gas inlet and a second gas outlet, the second gas inlet is communicated with the second end of the gas outlet pipe 630, and the second gas outlet is communicated with the gas inlet of the surface condenser 500. The second vacuum generator 210 further vacuumizes the first vacuum cooling device 100, further reducing the pressure in the vacuum cooling cavity, thereby enhancing the effect of vacuum flash cooling, further reducing the temperature of the concentrated solution, and increasing the concentration of the concentrated solution.
The solid-liquid separation device 400 is a thickener, the solid-liquid separation device 400 has a solid-liquid separation chamber 401, a concentrate inlet 402, a clear liquid outlet 403 and an underflow slurry outlet 404, each of the concentrate inlet 402, the clear liquid outlet 403 and the underflow slurry outlet 404 is communicated with the solid-liquid separation chamber 401, and the concentrate inlet 402 is communicated with the concentrate outlet.
The leachate cooling apparatus 1000 further comprises an underflow pump 410, a material dumping pump 405 and a reflux pump (not shown), wherein the inlet of the underflow pump 410 is connected to the underflow outlet 404. The water inlet of the material pouring pump 405 is connected with the concentrate outlet 104. The outlet of the material pouring pump 405 is connected with the concentrate inlet 402. The inlet of the reverse flow pump is connected to the underflow outlet 404 and the outlet of the reverse flow pump is connected to the concentrate inlet 402.
The temperature of the concentrated solution entering the solid-liquid separation device 400 is less than or equal to 45 ℃, the retention time of the concentrated solution entering the solid-liquid separation device 400 is more than or equal to 12 hours, and the sufficient solid-liquid separation time and the solid-liquid separation effect of the concentrated solution are ensured. The concentrated solution enters a solid-liquid separation cavity 401 through a material pouring pump 405 to carry out solid-liquid separation so as to obtain decalcified concentrated clear solution and underflow liquid. The supersaturated calcium sulfate precipitated from the concentrated solution is deposited to form underflow slurry, a part of the underflow slurry is pumped out by the backflow pump and then enters the solid-liquid separation device 400 from the concentrated solution inlet 402 again to be used as seed crystals, and a part of the underflow slurry is discharged from the underflow slurry outlet 404 by the underflow pump 410. The decalcified concentrate obtained by decalcifying the concentrate is discharged from the clear liquid outlet 403.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", and the like, indicate the orientation or positional relationship indicated based on the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," and "fixed" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally formed; may be mechanically coupled, may be electrically coupled or may be in communication with each other; they may be directly connected or indirectly connected through intervening media, or they may be connected internally or in any other suitable relationship, unless expressly stated otherwise. The specific meaning of the above terms in the present invention can be understood according to specific situations by those skilled in the art.
In the present application, unless expressly stated or limited otherwise, the first feature may be directly on or directly under the second feature or indirectly via intermediate members. Also, a first feature "on," "over," and "above" a second feature may be directly or diagonally above the second feature, or may simply indicate that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature may be directly under or obliquely under the first feature, or may simply mean that the first feature is at a lesser elevation than the second feature.
In the present disclosure, the terms "one embodiment," "some embodiments," "an example," "a specific example," or "some examples" or the like mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present disclosure. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.
Although embodiments of the present invention have been shown and described, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art without departing from the scope of the present invention.
Claims (9)
1. A leachate cooling apparatus, comprising:
a first vacuum cooling device having a vacuum cooling chamber, a leachate inlet, a gas outlet, and a concentrate outlet, each of the leachate inlet, the gas outlet, and the concentrate outlet in communication with the vacuum cooling chamber, at least a portion of a wall of the vacuum cooling chamber being a polished surface;
a first vacuum generator connected to the gas outlet;
a first homogenizing device cooperating with the first vacuum cooling device; and
the solid-liquid separation device is provided with a solid-liquid separation cavity, a concentrated solution inlet, a clear solution outlet and an underflow slurry outlet, each of the concentrated solution inlet, the clear solution outlet and the underflow slurry outlet is communicated with the solid-liquid separation cavity, and the concentrated solution inlet is communicated with the concentrated solution outlet.
2. The leachate cooling apparatus of claim 1, further comprising:
a surface condenser having a condensing chamber, a gas inlet, a non-condensable gas outlet, and a first condensed water outlet, each of the gas inlet, the non-condensable gas outlet, and the condensed water outlet being in communication with the condensing chamber, the gas inlet being in communication with the gas outlet, the non-condensable gas outlet being in communication with the first vacuum generator;
the condensate tank is provided with a condensate inlet and a second condensate outlet, and the condensate inlet is communicated with the first condensate outlet; and
a water inlet of the delivery pump is communicated with a second condensate outlet of the condensate tank,
optionally, the surface condenser is one of a plate cooler, a spiral plate cooler, a tube and shell cooler.
3. The leachate cooling apparatus of claim 2, further comprising:
the cyclone liquid-foam separator is provided with a separation cavity;
the foam supplementing device is detachably arranged at the gas outlet;
a first end of the steam collecting pipe is connected with the gas outlet, and a second end of the steam collecting pipe is communicated with the separation cavity;
a first end of the gas outlet pipe is communicated with the separation cavity, and a second end of the gas outlet pipe is communicated with the gas inlet; and
the upper end of the liquid outlet pipe is communicated with the separation cavity, the lower end of the liquid outlet pipe is communicated with the vacuum cooling cavity, and optionally, the liquid outlet pipe is obliquely arranged.
4. The leachate cooling apparatus of claim 3, further comprising:
a second vacuum cooling device having a second vacuum cooling chamber, a second concentrate inlet, a second gas outlet, and a second concentrate outlet, each of the second concentrate inlet, the second gas outlet, and the second concentrate outlet in communication with the second vacuum cooling chamber, at least a portion of a wall of the second vacuum cooling chamber having a polished surface, the second concentrate inlet in communication with the concentrate outlet, the second concentrate outlet in communication with the concentrate inlet;
a second homogenizing device cooperating with the second vacuum cooling device;
optionally, the concentrate outlet of the first vacuum cooling device is at a higher elevation than the second concentrate inlet of the second vacuum cooling device.
5. The leachate cooling plant of claim 3, further comprising
A second vacuum generator having a second gas inlet and a second gas outlet, the second gas inlet being in communication with the second end of the gas outlet tube, the second gas outlet being in communication with the gas inlet,
optionally, the first vacuum generator is a vacuum pump and the second vacuum generator is a vapor compressor or a vapor jet pump.
6. The leachate cooling apparatus of claim 1, wherein the first homogenizing means comprises an agitator disposed within the vacuum cooling chamber.
7. The leachate cooling apparatus of claim 1, wherein the first homogenizing device comprises a circulation pump, the first vacuum cooling device further having a circulation fluid inlet and a circulation fluid outlet, a fluid inlet of the circulation pump being in communication with the circulation fluid outlet of the first vacuum cooling device, and a fluid outlet of the circulation pump being in communication with the circulation fluid outlet of the first vacuum cooling device, optionally the circulation fluid outlet being the same opening as the leachate inlet.
8. The leachate cooling apparatus of claim 1, wherein the cooling apparatus further comprises an underflow pump and a backwash pump, wherein the underflow pump has a water inlet connected to the underflow outlet, the backwash pump has a water inlet connected to the underflow outlet, and the backwash pump has a water outlet connected to the concentrate inlet.
9. The leachate cooling apparatus of claim 1, wherein the solid-liquid separation device is a thickener or a settler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021864326.6U CN212581986U (en) | 2020-08-31 | 2020-08-31 | Leachate cooling equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021864326.6U CN212581986U (en) | 2020-08-31 | 2020-08-31 | Leachate cooling equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212581986U true CN212581986U (en) | 2021-02-23 |
Family
ID=74652716
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202021864326.6U Active CN212581986U (en) | 2020-08-31 | 2020-08-31 | Leachate cooling equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN212581986U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112029993A (en) * | 2020-08-31 | 2020-12-04 | 中国恩菲工程技术有限公司 | Leachate cooling equipment and cooling process |
-
2020
- 2020-08-31 CN CN202021864326.6U patent/CN212581986U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112029993A (en) * | 2020-08-31 | 2020-12-04 | 中国恩菲工程技术有限公司 | Leachate cooling equipment and cooling process |
| CN112029993B (en) * | 2020-08-31 | 2024-03-19 | 中国恩菲工程技术有限公司 | Leachate cooling equipment and cooling process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP5642987B2 (en) | Method for recovering nickel from copper electrolyte | |
| CN108359813B (en) | A kind of energy-saving and environment-friendly salt lake bittern proposes lithium technique | |
| CN212581986U (en) | Leachate cooling equipment | |
| CN105540626A (en) | Alumina mother liquor MVR circulation evaporation device and process | |
| CN106430787A (en) | APT (ammonium paratungstate) production wastewater recycling method | |
| CN207175684U (en) | The system that hydrochloric acid and metallic compound are reclaimed from hydrochloric acid pickling waste liquor | |
| CN112516619B (en) | Forced circulation evaporation device and method for slurry with crystals | |
| CN115872406A (en) | Hydrogen fluoride wastewater resource utilization system device and method in photovoltaic industry | |
| CN214050523U (en) | Cooling crystallization device for recovering metal ions from waste acid solution | |
| CN112029993B (en) | Leachate cooling equipment and cooling process | |
| CN108341429A (en) | A kind of post-processing approach of black titanium liquid and its device used | |
| CN210973888U (en) | Wet process phosphoric acid production system | |
| CN218665442U (en) | Device for extracting high-purity lithium chloride and sodium chloride from lithium-rich salt lake | |
| CN216986365U (en) | Bisphenol A adduct crystallization separation device | |
| CN104524806A (en) | Urotropin complete continuous crystallization production technology and equipment | |
| CN115448523A (en) | Device for recovering lithium in lithium precipitation mother liquor | |
| CN208292675U (en) | A kind of black titanium liquid continuously post-processes process units | |
| CN204428875U (en) | The complete continuous crystallisation production process equipment of a kind of methenamine | |
| CN106517123A (en) | Sodium phosphate dibasic dodecahydrate continuous production device and method | |
| CN209974349U (en) | Waste water concentration evaporation crystallizer | |
| CN209778705U (en) | calcium gluconate continuous crystallization system | |
| CN105177622A (en) | Novel energy-saving consumption-reduction process for producing electrolytic manganese | |
| CN104047009B (en) | The recovery process device of ferrous chloride in acid washing rolled steel liquid | |
| CN217613030U (en) | Battery-grade manganese sulfate production system | |
| CN109399853A (en) | The processing unit of ammonia nitrogen waste water |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |