CN217220198U - Waste acid concentration recovery device - Google Patents
Waste acid concentration recovery device Download PDFInfo
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- CN217220198U CN217220198U CN202220798538.1U CN202220798538U CN217220198U CN 217220198 U CN217220198 U CN 217220198U CN 202220798538 U CN202220798538 U CN 202220798538U CN 217220198 U CN217220198 U CN 217220198U
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Abstract
The utility model provides a waste acid concentration recovery unit relates to chemical industry waste acid treatment technical field. A waste acid concentration recovery device comprises an evaporation tower, a heat exchange assembly, a regeneration acid tank and a fan; the evaporation tower comprises an evaporation tower body, a packing layer, a gas-liquid separator and a first water distribution system, wherein the packing layer, the gas-liquid separator and the first water distribution system are arranged in the evaporation tower body from bottom to top in sequence; the heat exchange assembly is connected with the first water distribution system; the regeneration acid tank and the fan are respectively connected with the evaporation tower. The utility model provides a pair of concentrated recovery unit of spent acid has adopted the mechanism of surface gasification evaporation, utilizes the saturated steam of hydrone in the air of different temperatures's difference to realize the moisture evaporation as mass transfer power promptly, can carry out spontaneous evaporation under the lower condition of temperature, has reduced the energy consumption.
Description
Technical Field
The utility model relates to a chemical industry waste acid processing technology field particularly, relates to a waste acid concentration recovery unit.
Background
In the field of anodic oxidation waste acid concentration, a graphite multi-effect evaporator is generally used for evaporating and concentrating waste acid, water is evaporated from acid liquor, and concentrated regenerated acid is recycled. The multi-effect evaporator is used in the field of salt chemical industry, but in the working condition of waste acid concentration, the graphite multi-effect evaporator is difficult to stably operate for a long time due to the complexity and high corrosivity of waste acid components. The existing waste acid recovery process mainly has the following problems: 1. the graphite multi-effect evaporation equipment is too heavy, and parts are more, so that the disassembly and the assembly are not facilitated; 2. the working principle of multi-effect evaporation is complex, and the temperature in the pipe needs to be observed at any time, so that a large amount of manpower is consumed; 3. the cost and the operation energy consumption are high; 3. the equipment is seriously corroded; 4. the investment of daily maintenance equipment is large, the concentration is limited and the exhaust gas is influenced. Therefore, it is very important to develop a waste acid recovery device which has simple process, saves cost and can reduce energy consumption.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a waste acid concentration recovery unit, it has advantages such as reduce the energy consumption, the suitability is strong, maintain simple, the easy-to-damage spare is few, the technology principle is simple.
The embodiment of the utility model is realized like this:
in a first aspect, an embodiment of the present application provides a waste acid concentration and recovery device, which includes an evaporation tower, a heat exchange assembly, a regeneration acid tank and a fan; the evaporation tower comprises an evaporation tower body, a packing layer, a gas-liquid separator and a first water distribution system, wherein the packing layer, the gas-liquid separator and the first water distribution system are arranged in the evaporation tower body from bottom to top in sequence; the heat exchange assembly is connected with the first water distribution system; the regeneration acid tank and the fan are respectively connected with the evaporation tower.
Waste acid enters the lower part of the evaporation tower, is preheated and heated through the heat exchange assembly device, then enters the evaporation tower through a connecting pipe at the top of the tower, and is scattered on the surface of the packing layer by utilizing the first water distribution system. Air is blown into the lower part of the evaporation tower by a fan, gas naturally rises, flows through the packing layer, and transfers heat and mass with waste acid on the surface of the packing, partial water is vaporized and enters the air, and the water in the waste acid is less evaporated by the gas-liquid separator until the waste acid reaches the target concentration. And the concentrated acid is conveyed to a regeneration acid tank through a pipeline, so that the waste acid is recycled.
The utility model discloses an in some embodiments, above-mentioned heat exchange assemblies is including the medium circulating pump that connects gradually, preheat heat exchanger and steam heat exchanger, and above-mentioned medium circulating pump is connected in above-mentioned evaporation tower body bottom, above-mentioned steam heat exchanger and the interconnect of above-mentioned first water distribution system.
In some embodiments of the present invention, the packing layer is provided with a spherical packing.
In some embodiments of the present invention, the waste acid concentrating and recycling apparatus further comprises a condensing tower and a condensing and recycling assembly connected to each other, wherein the condensing tower is connected to the evaporating tower through a pipeline.
In some embodiments of the present invention, the condensing tower includes a condensing tower body and a tray, and the tray is disposed in the condensing tower body.
In some embodiments of the present invention, the number of the trays is plural, and a plurality of the trays are layered and uniformly spaced in the condensing tower body. The utility model discloses an in some embodiments, above-mentioned condensing tower still includes second water distribution system and third water distribution system, and above-mentioned second water distribution system sets up in this internal top of above-mentioned condensing tower, and above-mentioned third water distribution system sets up in this internal middle part of above-mentioned condensing tower.
The utility model discloses an in some embodiments, above-mentioned condensation is retrieved the subassembly and is included a condensation recovery unit, and above-mentioned condensation recovery unit includes interconnect's condensate circulating pump and condensate cooler, and above-mentioned condensate circulating pump is connected in above-mentioned condensing tower body bottom, and above-mentioned condensate cooler and above-mentioned second water distribution system interconnect constitute a condensation circulation jointly with above-mentioned second water distribution system, above-mentioned condensate circulating pump, above-mentioned condensate cooler.
The utility model discloses an in some embodiments, above-mentioned condensation recovery subassembly still includes secondary condensation recovery unit, and above-mentioned secondary condensation recovery unit is including preheating the circulating pump, and the aforesaid is preheated the circulating pump respectively with above-mentioned condensing tower body bottom and the aforesaid and is preheated heat exchanger interconnect, and the aforesaid is preheated heat exchanger and above-mentioned third water distribution system interconnect, and the aforesaid is preheated the circulating pump, the aforesaid is preheated heat exchanger and is constituteed secondary condensation circulation jointly with above-mentioned third water distribution system.
In some embodiments of the present invention, the cooling circulation water inlet and the cooling circulation water outlet are provided in the above-mentioned condensate cooler.
Compared with the prior art, the embodiment of the utility model has following advantage or beneficial effect at least:
1. the utility model provides a pair of concentrated recovery unit of spent acid is with the evaporation of water in the spent acid under the state of not boiling, but utilizes the difference of the saturated vapor pressure of hydrone in the air under the different temperatures to realize the evaporation of water as mass transfer power, can control to carry out spontaneous evaporation under the lower condition of temperature, has reduced the energy consumption.
2. The utility model provides a pair of concentrated recovery unit of spent acid is because the operating temperature is low, and the phase transition interface does not have the heat transfer demand, and splitter's phase transition interface can adopt PPH non-metallic material and need not use and make the evaporimeter in the traditional evaporation technology and adopt various metal material, can greatly improve the suitability of device, especially the processing of corrosivity spent acid.
3. The utility model provides a pair of concentrated recovery unit of spent acid's engine equipment only adopts fan and water pump, has the advantage of maintaining simple, the fragile spare is few.
4. The utility model provides a pair of concentrated recovery unit of spent acid adopts the air as the extraction medium of vapor, and the process of whole technology evaporation and condensation all goes on under the ordinary pressure, need not use the sealed material and the structure of high specification like traditional evaporimeter (multi-effect evaporator) that use negative pressure or high pressure to evaporate, very big improvement system's reliability.
5. The utility model provides a pair of waste acid concentration recovery device not only can utilize steam as the heat source, can also regard waste heat more than 85 ℃ as the heat source, reaches the purpose with practicing thrift the energy consumption.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are required to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention, and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
FIG. 1 is a schematic structural view of a waste acid concentrating and recycling device in embodiment 1 of the present invention;
FIG. 2 is a schematic structural view of an evaporation tower in embodiment 1 of the present invention;
FIG. 3 is a schematic structural diagram of a condensing tower in embodiment 1 of the present invention;
fig. 4 is a schematic structural diagram of a waste acid concentrating and recycling device in embodiment 2 of the present invention.
An icon: 100. an evaporation tower; 100a, an evaporation tower A; 100B, an evaporation tower B; 101. an evaporation tower body; 102. a filler layer; 103. a gas-liquid separator; 104. a first water distribution system; 200. a condensing tower; 200a, a condensing tower A; 200B, a condensing tower B; 201. a condensing tower body; 202. a tray; 203. a second water distribution system; 204. a third water distribution system; 301. a medium circulation pump; 301a, medium circulation pump a; 301B, medium circulation pump B; 302. preheating a heat exchanger; 303. a steam heat exchanger; 304. a concentrated solution pump at the concentration section; 401. preheating a circulating pump; 402. a condensate circulating pump; 403. a condensate cooler; 4031. a cooling circulating water inlet; 4032. a cooling circulating water outlet; 404. a condensate pump; 405. an electric control cabinet; 500. a fan; 600. and (5) regenerating the acid tank.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of the embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the present invention, presented in the accompanying drawings, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
In the description of the embodiments of the present invention, it should be noted that, if the terms "upper", "lower", "left", "right", "inner", etc. indicate the position or positional relationship based on the position or positional relationship shown in the drawings, or the position or positional relationship that the products of the present invention are usually placed when in use, the description is only for convenience of description and simplification, but the indication or suggestion that the device or element to which the terms refer must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be interpreted as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance.
In the description of the embodiments of the present invention, "a plurality" means at least 2.
In the description of the embodiments of the present invention, it should be further noted that unless explicitly stated or limited otherwise, the terms "disposed," "connected," and "connected" should be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood according to specific situations by those skilled in the art.
Example 1
Referring to fig. 1 to fig. 3, the embodiment provides a waste acid concentrating and recycling apparatus, which may include an evaporation tower 100, a heat exchange assembly, a regeneration acid tank 600, and a fan 500; the evaporation tower 100 comprises an evaporation tower 100 body, a packing layer 102, a gas-liquid separator 103 and a first water distribution system 104, wherein the packing layer 102, the gas-liquid separator 103 and the first water distribution system 104 are arranged in the evaporation tower 100 body from bottom to top in sequence; the heat exchange component is connected with the first water distribution system 104; the regeneration acid tank 600 and the fan 500 are respectively interconnected with the evaporation tower 100. When in use, waste acid enters the lower part of the evaporation tower 100, is preheated and heated by the heat exchange component device, then enters the evaporation tower 100 through a connecting pipe at the top of the tower, and is scattered on the surface of a special filler by the first water distribution system 104. Air is blown into the lower part of the evaporation tower 100 by a fan 500 through a ventilation pipeline, gas is in countercurrent contact with waste acid liquid on the surface of a filler in the evaporation tower 100 from bottom to top to carry out heat and mass transfer, the formed warm and humid hot air is discharged from the top of the tower to the bottom of the evaporation tower 100, and the warm and humid hot air is in countercurrent contact with the heated waste acid to form high-temperature humid hot saturated air which is discharged from the top of the evaporation tower 100. Part of water is vaporized and enters the air, and the water in the waste acid is less evaporated through the gas-liquid separator 103 until the waste acid reaches the target concentration. The concentrated acid is sent to the regeneration acid tank 600 through a pipeline, so that the waste acid is recycled.
In this embodiment, the heat exchange assembly includes a medium circulation pump 301, a preheating heat exchanger 302 and a steam heat exchanger 303 that are connected in sequence, the medium circulation pump 301 is connected to the bottom of the body of the evaporation tower 100, and the steam heat exchanger 303 is connected to the first water distribution system 104. When the waste acid waste heat recovery device is used, the anodic oxidation waste acid is conveyed into the evaporation tower 100, the liquid at the bottom of the evaporation tower 100 is pumped to the preheating heat exchanger 302 by the medium circulating pump 301, the preheating heat exchanger 302 preheats the waste acid by the heat of the condensate in the condensation tower 200, the waste acid is heated to the temperature and flows to the steam heat exchanger 303, the waste acid is heated to 80-100 ℃ by the steam, then the waste acid enters the evaporation tower 100 through a connecting pipe at the top of the tower, the waste acid is uniformly dispersed on the surface of a special filler in the evaporation tower 100 by the first water distribution system 104 and contacts with the air flowing from bottom to top, and heat and mass transfer occurs. The medium circulating pump 301 pumps the liquid at the bottom of the evaporation tower 100 to the top of the evaporation tower 100, the first water distribution system 104 is used for spreading the waste acid on the surface of the special filler in the evaporation tower 100, and the waste acid is heated by the evaporation tower 100 and then contacts with air to generate heat transfer and mass transfer, so that the water is transferred from the waste acid to the hot air to form the concentrated liquid at the bottom of the tower. When the concentration of the concentrated solution reaches saturation, the system stops circulating evaporation and the concentrated solution is pumped out by a concentrated solution pump in the concentration section.
In this embodiment, filler layer 102 is provided with spherical fillers. The mass transfer efficiency can be improved by arranging the spherical filler. When the device is used, air is blown into the lower part of the tower by the fan 500, the gas naturally rises, and flows through the spherical filler of the filler layer 102 to transfer heat and mass with waste acid on the surface of the spherical filler, and meanwhile, the spherical filler can also improve the mass transfer efficiency.
In this embodiment, a waste acid concentration and recovery device may further include a condensing tower 200 and a condensation recovery assembly connected to each other, and the condensing tower 200 is connected to the evaporation tower 100 through a pipe. The condensing tower 200 and the condensing recovery assembly realize the recycling of the condensate, and the energy consumption is saved.
In this embodiment, the condensing tower 200 includes a condensing tower 200 body and a tray 202, and the tray 202 is disposed in the condensing tower 200 body. The trays 202 are the primary components of the gas-liquid mass and heat transfer field. So that the two fluids closely exchange heat and mass between two phases to achieve the purpose of gas-liquid separation.
In this embodiment, the number of the trays 202 is plural, and the plural trays 202 are layered and uniformly spaced in the condensation tower 200 body. When the waste acid regeneration device is used, part of moisture flowing through the evaporation tower 100 is vaporized and enters air, the air passes through the gas-liquid separator 103, enters the condensation tower 200 together with the blown air, then enters different tower tray 202 layers, the moisture in the waste acid is reduced in evaporation until the waste acid reaches the target concentration, and the concentrated acid is sent to the regeneration acid tank 600 through a pipeline. In addition, the plurality of trays 202 are arranged in a layered and uniformly spaced manner, which is beneficial to better achieve the purpose of gas-liquid separation.
In this embodiment, the condensation tower 200 further includes a second water distribution system 203 and a third water distribution system 204, the second water distribution system 203 is disposed at the top of the condensation tower 200, and the third water distribution system 204 is disposed at the middle of the condensation tower 200. The first water distribution system 104, the second water distribution system 203 and the third water distribution system 204 are composed of a main water distribution pipe, branch water distribution pipes, nozzles and connecting pipes, and are used for atomizing liquid materials and then uniformly distributing the liquid materials on the surface layer of the filler, so that the function of uniform water distribution is achieved.
In this embodiment, the condensation recycling assembly includes a primary condensation recycling unit, the primary condensation recycling unit includes a condensate circulating pump 402 and a condensate cooler 403 that are connected to each other, the condensate circulating pump 402 is connected to the bottom of the condensation tower 200, the condensate cooler 403 is connected to the second water distribution system 203, and the condensate circulating pump 402, the condensate cooler 403 and the second water distribution system 203 form a primary condensation cycle together. When the air condensing device is used, air is blown into the lower portion of the evaporation tower 100 by the aid of the fan 500, the air naturally rises, flows through the packing layer 102, conducts heat and mass transfer with waste acid on the surface of the packing layer 102, part of water is vaporized and enters the air, the air passes through the gas-liquid separator 103 and enters the condensing tower 200 together with the blown air, damp and hot air condensed by the condensing tower 200 enters the bottom of the condensing tower 200 from the top of the condensing tower 200 through a connecting pipe, a condensate circulating pump 402 is arranged at the bottom of the condensing tower 200, the condensate is pumped into the condensing heat exchanger 404, the temperature is reduced to 30-35 ℃ by cooling circulating water, and then the damp and hot air enters the top of the condensing tower 200. The second water distribution system 203 at the top of the condensing tower 200 uniformly distributes the condensate into the tray 202 of the condensing tower 200, and the condensate is subjected to heat and mass transfer with the damp and hot air flowing from bottom to top, so that the damp and hot air is cooled and washed, the amount of water vapor carried by the damp and hot air is reduced, and the latent heat of the damp and hot air is recovered at the same time until high-temperature condensate at the bottom of the condensing tower 200 is formed, thereby realizing one-time recycling of the condensate.
In this embodiment, the condensation recycling assembly further includes a secondary condensation recycling unit, the secondary condensation recycling unit includes a preheating circulation pump 401, the preheating circulation pump 401 is respectively connected to the bottom of the condensation tower 200 and the preheating heat exchanger 302, the preheating heat exchanger 302 is connected to the third water distribution system 204, and the preheating circulation pump 401, the preheating heat exchanger 302 and the third water distribution system 204 jointly form a secondary condensation circulation. When the waste acid heat recovery system is used, air is blown into the lower part of the evaporation tower 100 through the ventilation pipeline by the fan 500, gas is in countercurrent contact with waste acid liquid on the surface of a filler in the evaporation tower 100 from bottom to top to carry out heat transfer and mass transfer, the formed warm and humid air is discharged from the top of the evaporation tower 100 to the bottom of the evaporation tower 100, and is in countercurrent contact with the heated waste acid to form high-temperature humid and hot saturated air which is discharged from the top of the evaporation tower 100, and then enters high-temperature condensed water formed in the condensation tower 200, the high-temperature condensed water is conveyed to the preheating heat exchanger 302 by the preheating circulating pump 401, is subjected to heat exchange with concentrated circulating liquid and is cooled, and then enters the third water distribution system 204 in the middle of the condensation tower 200, the latent heat energy of secondary steam is evaporated by the recovery system, and secondary recycling of the condensed liquid is realized.
In this embodiment, the condensate cooler 403 is provided with a cooling circulation water inlet and a cooling circulation water outlet 4032. When the cooling device is used, the condensate circulating pump 402 pumps part of condensate into the condensate cooler 403, and the connected cooling circulating water is used for cooling the condensate to 30-35 ℃.
Example 2
In this embodiment, as shown in fig. 4, the numbers of the evaporation tower 100, the condensation tower 200, and the medium circulation pump 301 are two, which are respectively expressed as an evaporation tower a 100a, an evaporation tower B100B, a condensation tower a200a, a condensation tower B200B, a medium circulation pump a 301a, and a medium circulation pump B301B, other parts are the same as those in embodiment 1, and are not described herein again, and the working principle thereof is as follows:
conveying the anodic oxidation waste acid into an evaporation tower A100 a, pumping liquid at the bottom of the evaporation tower A100 a to a preheating heat exchanger 302 by using a medium circulating pump A301 a, preheating the waste acid by using the heat of condensate in a condensation tower A200a by using the preheating heat exchanger 302, then flowing to a steam heat exchanger 303, raising the temperature of the waste acid to 80-100 ℃ by using steam, then entering into an evaporation tower B100B through a connecting pipe at the top of the tower, uniformly spreading the waste acid on the surface of a special filler in the evaporation tower B100B by using a liquid distributor, and contacting with air flowing from bottom to top to generate heat and mass transfer. The medium circulating pump B301B pumps the liquid at the bottom of the evaporation tower B100B to the top of the evaporation tower A100 a, the liquid distributor is utilized to disperse waste acid on the surface of a special filler in the evaporation tower A100 a, and the heated waste acid in the tower contacts with air to generate heat transfer and mass transfer, so that the water is transferred from the waste acid to hot air to form the concentrated liquid at the bottom of the tower. When the concentration of the concentrated solution reaches saturation, the system stops circulating evaporation and the concentrated solution is pumped out by a concentrated solution pump in the concentration section.
Air is blown into the lower part of an evaporation tower A100 a by a fan 500 through a ventilation pipeline, gas is in countercurrent contact with waste acid liquid on the surface of a filler in the evaporation tower A100 a from bottom to top to carry out heat transfer and mass transfer, the formed warm and humid air is discharged from the top of the evaporation tower B100B to the bottom of the evaporation tower B100B, and is in countercurrent contact with the heated waste acid to form high-temperature humid and hot saturated air which is discharged from the top of the evaporation tower B100B, and then enters a high-temperature condensation water formed in a condensation tower A200a, and the high-temperature condensation water is conveyed to a preheating heat exchanger 302 by a preheating circulating pump 401, then is subjected to heat exchange with a concentrated circulating liquid and is cooled and then enters a top water distribution system of the condensation tower A200a, and latent heat energy of secondary steam evaporated by the recovery system is obtained.
The damp and hot air condensed by the condensing tower A200a enters the bottom of the condensing tower B200B from the top of the condensing tower A200a through a connecting pipe, a condensate circulating pump 402 is arranged at the bottom of the condensing tower B200B, the condensate is pumped into a condensing heat exchanger 404, the temperature is reduced to 30-35 ℃ by utilizing cooling circulating water, and then the damp and hot air enters the top of the condensing tower B200B. The water distribution system at the top of the condensing tower B200B uniformly distributes the condensate into a tray 202 of the condensing tower B200B, the condensate and the moist and hot air flowing from bottom to top carry out heat and mass transfer, the condensate is condensed to form liquid drops to enter the condensate, the low-temperature dry air formed by countercurrent contact is discharged out of the system from the top of the tower. After the liquid level in the condensing tower B200B rises to the overflow height, part of the condensate is discharged out of the condensing tower B200B to a condensate tank and is pumped out by a condensate pump 404.
The automatic control of the whole device system is completed by the electric control cabinet 405, and one-key start-stop and remote control can be realized.
To sum up, the embodiment of the utility model provides a waste acid concentration recovery unit, waste acid get into 100 lower parts of evaporating tower, utilize medium circulating pump 301 with the liquid pump in the bottom of the tower to preheat heat exchanger 302, utilize the condensate heat to flow to steam heat exchanger 303 after rising the temperature as the heat medium, rise the temperature to 80 ~ 100 ℃, then in the connecting pipe entering evaporating tower 100 through the top of the tower, utilize first water distribution system 104 to spread the waste acid on special packing layer 102 surface. Air is blown into the lower part of the evaporation tower 100 by the fan 500, gas naturally rises, flows through the packing layer 102, and performs heat and mass transfer with waste acid on the surface of the spherical packing, partial water is vaporized and enters the air, and the air and the blown air enter the condensation tower 200 through the gas-liquid separator 103, so that the water in the waste acid is less evaporated until the waste acid reaches the target concentration, and concentrated acid is sent to the regenerated acid tank 600 through a pipeline. The preheating circulating pump 401 sends the high-temperature condensate at the bottom of the condensing tower 200 to the preheating heat exchanger 302, and the heat of the high-temperature condensate is transferred to the medium side for preheating, so that the raw steam consumption of temperature rise of the medium side is saved. The condensate after heat exchange and temperature reduction returns to the third water distribution system 204 at the high temperature section at the middle lower part of the condensing tower 200, and the latent heat of the secondary steam evaporated by the recovery system. The bottom of the condensing tower 200 is provided with a condensate circulating pump 402, a part of condensate is pumped into a condensate cooler 403 by a condensate pump 404, the condensate is cooled to 30-35 ℃ by using the accessed cooling circulating water, and then is sent to a second water distribution system 203 at the top of the condensing tower 200 to cool and wash the damp and hot air, so that the amount of water vapor carried by the damp and hot air is reduced, and meanwhile, the latent heat of the damp and hot air is recovered until the high-temperature condensate at the bottom of the condensing tower 200 is formed. The whole process realizes the recycling of the condensate, can also utilize the latent heat of the condensate as a heat source, saves energy consumption and simultaneously realizes the concentration and recycling of waste acid. The preheating heat exchanger 302, the steam heat exchanger 303 and the condensate cooler 403 of the system all adopt corrosion-resistant detachable plate heat exchangers, so that the heat transfer efficiency of the system is greatly improved, the investment is saved, the occupied area is small, and the operation, the maintenance and the like are convenient.
The utility model provides a pair of concentrated recovery unit of spent acid has adopted the mechanism of surface gasification evaporation, utilizes the saturated steam of hydrone in the air of different temperatures's difference to realize the moisture evaporation as mass transfer power promptly, can carry out spontaneous evaporation under the lower condition of temperature, has reduced the energy consumption. In addition, because the waste acid concentration and recovery device has low operation temperature and no heat transfer requirement on a phase change interface, the phase change interface of the separation equipment can be made of PPH (pentatricopeptide hydrogen) non-metallic materials instead of various metallic materials for manufacturing an evaporator in the traditional evaporation technology, and the applicability of the device, particularly the treatment of corrosive waste acid, can be greatly improved.
The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and various modifications and changes will occur to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A waste acid concentration recovery device is characterized by comprising an evaporation tower, a heat exchange assembly, a regeneration acid tank and a fan; the evaporation tower comprises an evaporation tower body, a packing layer, a gas-liquid separator and a first water distribution system, wherein the packing layer, the gas-liquid separator and the first water distribution system are sequentially arranged in the evaporation tower body from bottom to top; the heat exchange assembly is connected with the first water distribution system; the regeneration acid tank and the fan are respectively connected with the evaporation tower.
2. The waste acid concentrating and recycling device according to claim 1, wherein the heat exchange assembly comprises a medium circulating pump, a preheating heat exchanger and a steam heat exchanger which are connected in sequence, the medium circulating pump is connected to the bottom of the evaporation tower body, and the steam heat exchanger is connected with the first water distribution system.
3. A waste acid concentrating and recycling device according to claim 1, wherein the packing layer is provided with spherical packing.
4. A spent acid concentration recovery device according to claim 2, further comprising a condensing tower and a condensation recovery assembly connected to each other, the condensing tower being interconnected to the evaporation tower by a conduit.
5. A waste acid concentrating and recycling device according to claim 4, wherein the condensing tower comprises a condensing tower body and a tray, and the tray is arranged in the condensing tower body.
6. A waste acid concentrating and recycling device as claimed in claim 5, wherein said number of said trays is plural, and a plurality of said trays are arranged in said condensing tower body in a layered and evenly spaced manner.
7. The waste acid concentrating and recycling device of claim 4, wherein the condensing tower further comprises a second water distribution system and a third water distribution system, the second water distribution system is arranged at the top of the condensing tower body, and the third water distribution system is arranged in the middle of the condensing tower body.
8. The waste acid concentrating and recycling device according to claim 7, wherein the condensing and recycling assembly comprises a primary condensing and recycling unit, the primary condensing and recycling unit comprises a condensate circulating pump and a condensate cooler which are connected with each other, the condensate circulating pump is connected to the bottom of the condensing tower body, the condensate cooler is connected with the second water distribution system, and the condensate circulating pump, the condensate cooler and the second water distribution system together form a primary condensing cycle.
9. The waste acid concentrating and recycling device according to claim 8, wherein the condensing and recycling assembly further comprises a secondary condensing and recycling unit, the secondary condensing and recycling unit comprises a preheating circulating pump, the preheating circulating pump is respectively interconnected with the bottom of the condensing tower body and the preheating heat exchanger, the preheating heat exchanger is interconnected with the third water distribution system, and the preheating circulating pump, the preheating heat exchanger and the third water distribution system jointly form a secondary condensing cycle.
10. A waste acid concentrating and recycling device as claimed in claim 8, wherein the condensate cooler is provided with a cooling circulating water inlet and a cooling circulating water outlet.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202220798538.1U CN217220198U (en) | 2022-04-07 | 2022-04-07 | Waste acid concentration recovery device |
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| CN202220798538.1U CN217220198U (en) | 2022-04-07 | 2022-04-07 | Waste acid concentration recovery device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116617686A (en) * | 2023-07-24 | 2023-08-22 | 瑞燃(上海)环境工程技术有限公司 | Foam evaporation concentration crystallization system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116617686A (en) * | 2023-07-24 | 2023-08-22 | 瑞燃(上海)环境工程技术有限公司 | Foam evaporation concentration crystallization system |
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