CN212039090U - Switchable two-effect evaporation concentration crystallizer - Google Patents
Switchable two-effect evaporation concentration crystallizer Download PDFInfo
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- CN212039090U CN212039090U CN202020396614.7U CN202020396614U CN212039090U CN 212039090 U CN212039090 U CN 212039090U CN 202020396614 U CN202020396614 U CN 202020396614U CN 212039090 U CN212039090 U CN 212039090U
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Abstract
The switchable two-effect evaporation concentration crystallizer comprises a switchable evaporation concentration crystallization tank group; the switchable evaporation concentration crystallization tank group consists of a crystallization tank X and a crystallization tank Y; a heat exchange coil X is arranged in the crystallizing tank X, a heat exchange coil Y is arranged in the crystallizing tank Y, the front ends of the heat exchange coil X and the heat exchange coil Y are connected with external steam through pipelines with valves, and the rear ends of the heat exchange coil X and the heat exchange coil Y are used for discharging water vapor after heat exchange; the inner cavity of the crystallizing tank X is connected with the front end of the heat exchange coil Y through a pipeline with a valve; the inner cavity of the crystallizing tank Y is connected with the front end of the heat exchange coil pipe X through a pipeline with a valve. The utility model is suitable for a production requirement of evaporative concentration crystallization workshop section of salts such as zinc sulfate monohydrate, manganese sulfate monohydrate, through the switching of an effect and two effects, utilize the method that raw materials liquid dissolved the crystallization scale deposit, can easily get rid of the inside crystallization scale deposit of crystallizer in turn, guarantee that equipment lasts normal operating.
Description
Technical Field
The utility model relates to a chemical industry equipment field, especially a changeable two-effect evaporation concentration crystallizer.
Background
The multi-effect evaporation concentration crystallizer is important unit operation equipment in the production of the chemical industry, has the advantages of energy conservation, environmental protection and the like, and is widely applied to the chemical industry.
However, the conventional multi-effect evaporation concentration crystallizer has the following defects:
1. in consideration of various factors, a tube type or plate type heat exchanger is mostly adopted in a general multi-effect evaporation crystallization process, when crystals are generated in an evaporated substance, an external heating forced circulation mode is generally adopted for preventing the heat exchanger from blocking the tubes and crystallizing, but in the evaporation, concentration and crystallization process of salts such as zinc sulfate monohydrate, manganese sulfate monohydrate and the like, a large amount of crystal solid is generated in a concentrated solution, and in order to meet the technical requirements of centrifugal dehydration of a later section, reduce the amount of mother liquor for centrifugal dehydration, reduce energy consumption and improve productivity, the higher the crystal solid content in the concentrated slurry is required to be, the better the crystal solid content is, and even the crystal solid content is required to reach 800-. Such high crystalline solids concentrate in tubes or plates can easily cause serious problems of crystallization, scaling, tube plugging and plate plugging.
2. The existing production of salts such as zinc sulfate monohydrate and manganese sulfate monohydrate can only adopt a single-effect normal-pressure evaporating pot, a heat exchanger of the single-effect normal-pressure evaporating pot is arranged in the pot, the heat exchange area is limited by the capacity of the pot body and cannot be greatly limited, if the certain scale capacity is reached, a large number of single-effect pots are needed, so that the equipment occupies more workshop space, and the equipment investment is increased.
Disclosure of Invention
The utility model aims at overcoming the not enough of prior art, and provide a changeable two-effect evaporation concentration crystallizer, it has solved current multiple-effect evaporation crystallizer and has appeared crystallization, scale deposit in the heat exchanger easily in the use, and then influences the problem of multiple-effect evaporation crystallizer normal use.
The technical scheme of the utility model is that: the switchable two-effect evaporation concentration crystallizer comprises a switchable evaporation concentration crystallization tank group; the switchable evaporation concentration crystallization tank group consists of a crystallization tank X and a crystallization tank Y; a heat exchange coil X is arranged in the crystallizing tank X, a heat exchange coil Y is arranged in the crystallizing tank Y, the front ends of the heat exchange coil X and the heat exchange coil Y are connected with external steam through pipelines with valves, and the rear ends of the heat exchange coil X and the heat exchange coil Y are used for discharging water vapor after heat exchange; the inner cavity of the crystallizing tank X is connected with the front end of the heat exchange coil Y through a pipeline with a valve; the inner cavity of the crystallizing tank Y is connected with the front end of the heat exchange coil pipe X through a pipeline with a valve.
The utility model discloses further technical scheme is: a stirring device X is arranged in the crystallizing tank X, and a stirring device Y is arranged in the crystallizing tank Y.
The utility model discloses still further technical scheme is: the device also comprises a raw material liquid pool; the raw material liquid pool is connected with an X inner cavity of the crystallizing tank and a Y inner cavity of the crystallizing tank through pipelines with valves.
The utility model discloses a further technical scheme is: the device also comprises a condensed water gas-liquid separation device; the condensed water gas-liquid separation device comprises a vacuum gas-liquid separation tank A which is arranged at the rear end of the heat exchange coil X, Y.
The utility model discloses a further technical scheme is: the device also comprises a raw material liquid preheating assembly; the raw material liquid preheating assembly comprises a condensate water pool, a condensate water conveying pump and a preheater which are connected with each other; the condensation water tank is connected with the vacuum gas-liquid separation tank A; the preheater is arranged on a pipeline between the raw material liquid pool and the inner cavity of the crystallizing tank X and/or a pipeline between the raw material liquid pool and the inner cavity of the crystallizing tank Y.
The utility model discloses a further technical scheme is: it also includes a two-effect steam discharge treatment assembly; the secondary-effect steam discharging and treating component comprises a condenser, a cooling water pool, a circulating pump B, a water cooling tower, a circulating pump C, a vacuum gas-liquid separation tank B and a vacuum pump; the condenser is communicated with the inner cavity of the crystallizing tank X, Y through a pipeline with a valve, the condenser, the cooling water pool and the circulating pump A are communicated with each other to form a cooling water heating loop, the water cooling tower, the circulating pump C and the cooling water pool are communicated with each other to form a cooling water cooling loop, the vacuum gas-liquid separation tank B is communicated with the condenser, and the vacuum pump is communicated with the vacuum gas-liquid separation tank B.
Compared with the prior art, the utility model have following advantage:
1. the method is suitable for the production requirements of evaporation concentration crystallization sections of salts such as zinc sulfate monohydrate, manganese sulfate monohydrate and the like, and greatly saves the energy consumption of evaporation concentration crystallization of salts such as zinc sulfate monohydrate, manganese sulfate monohydrate and the like. Compared with the existing single-effect normal-pressure evaporation concentration crystallization equipment for salts such as zinc sulfate monohydrate, manganese sulfate monohydrate and the like, the equipment investment is saved, and the occupied area of the equipment is reduced.
2. Through the switching of the first effect and the second effect, the method for dissolving the crystallization scale by the raw material liquid can easily and alternately remove the crystallization scale in the crystallization tank, thereby ensuring the continuous and normal operation of the equipment; specifically, the method comprises the following steps: the evaporated liquor that is in the crystallizer flows outside heat exchange coil, and the crystallization scale deposit only can be attached to on crystallizer inner wall and heat exchange coil outer wall, only needs to switch one and imitate two effects, and the more rare stock solution of reintroduction concentration can dilute and dissolve the crystallization scale deposit, need not artifical clearance to, when diluting and dissolving the crystallization scale deposit, heat transfer evaporative concentration also goes on simultaneously, two are not wrong.
3. The number of the crystallizing tanks X, Y may be multiple, and when any crystallizing tank of the multiple crystallizing tanks introduces the raw material liquid to dilute, dissolve scale and crystallize, the rest crystallizing tanks can still work normally, and the whole production line can not be stopped.
The invention is further described below with reference to the figures and examples.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Detailed Description
Example 1:
as shown in fig. 1, the switchable two-effect evaporation concentration crystallizer includes a switchable evaporation concentration crystallization tank set and a raw material liquid pool 35.
The switchable evaporation concentration crystallizing tank group consists of a crystallizing tank X1 and a crystallizing tank Y2.
The crystallization tank X1 is internally provided with a heat exchange coil X11, the front end of the heat exchange coil X11 is communicated to an external steam supply pipe 31 through a pipeline with an external steam supply inlet valve X12, and is communicated to a secondary steam pipe 32 through a pipeline with a secondary steam inlet valve X13. The rear end of the heat exchange coil X11 is communicated with the condensate pipe 34 through a pipeline to discharge the vapor after heat exchange. The upper end of the crystallizing tank X1 is provided with a steam outlet X14 communicated to the inner cavity of the crystallizing tank X1, and the steam outlet X14 is communicated to a secondary steam pipe 32 through a pipeline with a secondary steam discharge valve X15. The crystallizer X1 is provided with a feed inlet X16 communicated with the inner cavity of the crystallizer, a feed inlet X16 is communicated with the raw material liquid pipe 33 through a pipeline, and the lower end of the crystallizer X1 is provided with a discharge outlet X17 communicated with the inner cavity of the crystallizer.
The crystallization tank Y2 is internally provided with a heat exchange coil Y21, the front end of the heat exchange coil Y21 is communicated to an external steam supply pipe 31 through a pipeline with an external steam supply inlet valve Y22, and is communicated to a secondary steam pipe 32 through a pipeline with a secondary steam inlet valve Y23. The rear end of the heat exchange coil Y21 is communicated with the condensate pipe 34 through a pipeline to discharge the vapor after heat exchange. The upper end of the crystallizing tank Y2 is provided with a steam outlet Y24 communicated to the inner cavity of the crystallizing tank Y2, and the steam outlet Y24 is communicated to the secondary steam pipe 32 through a pipeline with a secondary steam discharge valve Y25. The crystallizer Y2 is provided with a feed inlet Y26 communicated with the inner cavity of the crystallizer, a feed inlet Y26 is communicated with the raw material liquid pipe 33 through a pipeline, and the lower end of the crystallizer Y2 is provided with a discharge outlet Y27 communicated with the inner cavity of the crystallizer.
The raw material liquid pool 35 is communicated with the raw material liquid pipe 33 through a pipeline with a valve.
Preferably, the crystallizer X1 includes a stirrer X18, and the crystallizer Y2 includes a stirrer Y28. The stirring device X18 and the stirring device Y28 allow the evaporated liquid to flow only in the corresponding tank, and can prevent the crystal from sinking and scaling to a certain extent.
Preferably, the device further comprises a condensed water gas-liquid separation device; the condensed water gas-liquid separation device comprises a vacuum gas-liquid separation tank A5, the vacuum gas-liquid separation tank A5 is arranged at the rear ends of the heat exchange coils X11 and Y21 and is used for performing gas-liquid separation treatment on the water vapor discharged by the heat exchange coils X11 and Y21, the treated gas is discharged outside, and the treated liquid is input into a condensed water pipe 34.
Preferably, it also comprises a two-effect steam emission treatment component; the double-effect steam discharge treatment component comprises a condenser 61, a cooling water pool 62, a circulating pump B63, a water cooling tower 64, a circulating pump C65, a vacuum gas-liquid separation tank B66 and a vacuum pump 67; the condenser 61 is communicated with inner cavities of crystallizing tanks X1 and Y2 through pipelines, the condenser 61, a cooling water pool 62 and a circulating pump A63 are communicated with each other to form a cooling water heating loop, a water cooling tower 64, a circulating pump C65 and a cooling water pool 62 are communicated with each other to form a cooling water cooling loop, a vacuum gas-liquid separation tank B66 is communicated with the condenser 61 and used for receiving heat-exchanged water vapor discharged by the condenser 61, and a vacuum pump 67 is communicated with the vacuum gas-liquid separation tank B66 and used for providing negative pressure to drive steam to flow. The circulation operation of the cooling water heating loop can continuously drive the cooling water in the cooling water pool 62 to flow through the condenser 61, so that the high-temperature steam in the condenser 61 exchanges heat with the cooling water to reduce the temperature and condense the cooling water. The circulation operation of the cooling water temperature reduction circuit can continuously drive the cooling water in the cooling water pool 62 to flow through the cooling water tower 64 for cooling and temperature reduction. Steam discharged from the crystallizing tank X1 or the crystallizing tank Y2 continuously enters the condenser 61 through a pipeline, the steam exchanges heat with cooling water in the condenser 61 to reduce the temperature, the steam which is discharged from the condenser 61 and is in a gas-liquid mixed state enters the vacuum gas-liquid separation tank B66 to be subjected to gas-liquid separation treatment, and the separated water and the separated steam are respectively discharged outside.
Preferably, the device also comprises a raw material liquid preheating assembly; the raw material liquid preheating assembly comprises a condensate water tank 41, a condensate water conveying pump 42 and a preheater 43 which are connected with each other; the condensed water tank 41 is communicated with a vacuum gas-liquid separation tank A5 through a condensed water pipe 34; the preheater 43 is provided on the piping between the raw material liquid pool 35 and the raw material liquid pipe 33. The raw material liquid preheating assembly is used for preheating raw material liquid discharged from the raw material liquid pool 35 at a normal temperature, the heat source of the preheater 43 is water vapor discharged from the rear end of the heat exchange coil X11 and the rear end of the heat exchange coil Y21 after heat exchange, when the raw material liquid discharged from the raw material liquid pool 35 passes through the preheater 43, the raw material liquid exchanges heat with the water vapor with relatively high temperature in the preheater 43 to rise in temperature, the raw material liquid is discharged from the preheater 43 and then is input into the raw material liquid pipe 33, and finally the raw material liquid pipe 33 is respectively conveyed into inner cavities of the crystallizing tanks X1 and Y2.
Brief description the utility model discloses a work flow:
1. the discharge port X17 and the discharge port Y27 were closed, and the corresponding valves and pumps were opened to feed the raw material liquid in the raw material liquid tank 35 into the crystallizing tank X1 and the crystallizing tank Y2. After the crystallizer X1 and the crystallizer Y2 both reached the predetermined capacity, the pumps and valves were closed to stop the supply of the raw material liquid, and when the raw material liquid was supplied, the stirring devices X18 and Y28 were started to stir the raw material liquid.
2. The external steam inlet valve X12 and the secondary steam outlet valve X15 on the crystallizing tank X1 are opened, and the secondary steam inlet valve X13 is closed. And opening a secondary steam inlet valve Y23 and a secondary steam outlet valve Y25 on the crystallizing tank Y2, and closing an external supply steam inlet valve Y22. At the moment, externally supplied steam enters the heat exchange coil X11 from the front end of the heat exchange coil X11 to heat the raw material liquid in the crystallizing tank X1, the steam generated by evaporation of the raw material liquid in the inner cavity of the crystallizing tank X1 enters the heat exchange coil Y21 through the steam outlet X14, the secondary steam pipe 32 and the front end of the heat exchange coil Y21 in sequence to heat the raw material liquid in the crystallizing tank Y2, and the steam generated by evaporation of the raw material liquid in the inner cavity of the crystallizing tank Y2 is discharged into the secondary steam pipe 32.
3. And starting the two-effect steam discharge processing assembly to cool the steam in the secondary steam pipe 32 and separate the steam from the gas and the liquid, and then respectively discharging the steam outside. And starting a vacuum gas-liquid separation tank A5 to perform gas-liquid separation treatment on the water vapor discharged from the rear ends of the heat exchange coils X11 and Y21. The raw material liquid preheating assembly is started to preheat the raw material liquid discharged from the raw material liquid pool 35.
4. When the solid content of the crystal in the crystallizing tank X1 reaches the required concentration, switching between the first effect and the second effect, wherein the switching method comprises the following steps: closing an external steam inlet valve X12 on a crystallizing tank X1, opening a secondary steam inlet valve X13, opening an external steam inlet method Y22 on a crystallizing tank Y2, and closing a secondary steam inlet valve Y23; before switching, the crystallizers X1 and Y2 are respectively one-effect and two-effect, and after switching, the crystallizers X, Y are respectively two-effect and one-effect.
5. Opening bin outlet X17, discharging the crystallization material and carrying out centrifugal dehydration, after the material in crystallizer X1 is discharged, closing bin outlet X17, opening corresponding valve and pump, making the raw material liquid in raw material liquid pool 35 enter crystallizer X1, utilizing the characteristic that the raw material liquid concentration is more dilute, dissolving the crystallization scale on the inner wall of crystallizer X1 and the crystallization scale on the outer wall of heat exchange coil X11.
6. And repeating the steps 2-5 to realize the continuous operation of the double-effect evaporation concentration crystallizer.
This embodiment utilizes the method that the more rare stock solution of concentration dissolves the crystallization scale deposit through the switching of an effect and two effects, can easily get rid of the inside crystallization scale deposit of crystallizer X, Y in turn, need not manual cleaning to, when diluting and dissolving the crystallization scale deposit, heat transfer evaporative concentration also goes on simultaneously, two unmistakable.
Claims (6)
1. Switchable two-effect evaporation concentration crystallizer, which is characterized in that: comprises a switchable evaporation concentration crystallization tank group; the switchable evaporation concentration crystallization tank group consists of a crystallization tank X and a crystallization tank Y; a heat exchange coil X is arranged in the crystallizing tank X, a heat exchange coil Y is arranged in the crystallizing tank Y, the front ends of the heat exchange coil X and the heat exchange coil Y are connected with external steam through pipelines with valves, and the rear ends of the heat exchange coil X and the heat exchange coil Y are used for discharging water vapor after heat exchange; the inner cavity of the crystallizing tank X is connected with the front end of the heat exchange coil Y through a pipeline with a valve; the inner cavity of the crystallizing tank Y is connected with the front end of the heat exchange coil pipe X through a pipeline with a valve.
2. The switchable two-effect evaporative concentration crystallizer of claim 1, wherein: a stirring device X is arranged in the crystallizing tank X, and a stirring device Y is arranged in the crystallizing tank Y.
3. The switchable two-effect evaporative concentration crystallizer of claim 2, wherein: the device also comprises a raw material liquid pool; the raw material liquid pool is connected with an X inner cavity of the crystallizing tank and a Y inner cavity of the crystallizing tank through pipelines with valves.
4. A switchable two-effect evaporative concentration crystallizer as claimed in claim 3, wherein: the device also comprises a condensed water gas-liquid separation device; the condensed water gas-liquid separation device comprises a vacuum gas-liquid separation tank A which is arranged at the rear end of the heat exchange coil X, Y.
5. The switchable two-effect evaporative concentration crystallizer of claim 4, wherein: the device also comprises a raw material liquid preheating assembly; the raw material liquid preheating assembly comprises a condensate water pool, a condensate water conveying pump and a preheater which are connected with each other; the condensation water tank is connected with the vacuum gas-liquid separation tank A; the preheater is arranged on a pipeline between the raw material liquid pool and the inner cavity of the crystallizing tank X and/or a pipeline between the raw material liquid pool and the inner cavity of the crystallizing tank Y.
6. The switchable two-effect evaporative concentration crystallizer of claim 5, wherein: it also includes a two-effect steam discharge treatment assembly; the secondary-effect steam discharging and treating component comprises a condenser, a cooling water pool, a circulating pump B, a water cooling tower, a circulating pump C, a vacuum gas-liquid separation tank B and a vacuum pump; the condenser is communicated with the inner cavity of the crystallizing tank X, Y through a pipeline with a valve, the condenser, the cooling water pool and the circulating pump A are communicated with each other to form a cooling water heating loop, the water cooling tower, the circulating pump C and the cooling water pool are communicated with each other to form a cooling water cooling loop, the vacuum gas-liquid separation tank B is respectively communicated with the condenser, and the vacuum pump is communicated with the vacuum gas-liquid separation tank B.
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| CN202020396614.7U CN212039090U (en) | 2020-03-25 | 2020-03-25 | Switchable two-effect evaporation concentration crystallizer |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115006857A (en) * | 2022-06-30 | 2022-09-06 | 广西埃索凯循环科技有限公司 | Intermittent evaporative crystallization device and process adopting two-effect parallel evaporation |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115006857A (en) * | 2022-06-30 | 2022-09-06 | 广西埃索凯循环科技有限公司 | Intermittent evaporative crystallization device and process adopting two-effect parallel evaporation |
| CN115006857B (en) * | 2022-06-30 | 2024-02-13 | 广西埃索凯循环科技有限公司 | Intermittent evaporation crystallization device and process adopting two-effect parallel evaporation |
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