CN103566621A - Evaporative crystallization device for extracting ammonium salt by utilizing vapor recompression technique - Google Patents
Evaporative crystallization device for extracting ammonium salt by utilizing vapor recompression technique Download PDFInfo
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- CN103566621A CN103566621A CN201310542273.4A CN201310542273A CN103566621A CN 103566621 A CN103566621 A CN 103566621A CN 201310542273 A CN201310542273 A CN 201310542273A CN 103566621 A CN103566621 A CN 103566621A
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Abstract
The invention relates to an evaporative crystallization device for extracting ammonium salt by a vapor recompression technique. The evaporative crystallization device comprises a charge pump, a preheater, a circulation pump, a crystallization tank, a crystal mush pump, a centrifuge and an evaporator; an outlet of the charge pump is connected with a solution inlet of the preheater; a solution outlet of the preheater is connected with an inlet of the circulation pump; an outlet of the circulation pump is connected with a solution inlet of the crystallization tank; a crystal mush outlet of the crystallization tank is connected with an inlet of the crystal mush pump; a crystal mush inlet of the crystallization tank is connected with an outlet of the crystal mush pump, and the outlet of the crystal mush pump is also connected with the centrifuge; the solution outlet of the crystallization tank is connected with a solution inlet of the evaporator; a solution outlet of the evaporator is connected with an inlet of the circulation pump. The evaporative crystallization device for extracting ammonium salt by utilizing the vapor recompression technique is characterized by also comprising a vapor compressor; an inlet of the vapor compressor is connected with a secondary vapor inlet of the crystallization tank; the outlet of the vapor compressor is connected with a vapor inlet of the evaporator; and the vapor outlet of the evaporator is connected with a vapor inlet of the preheater. Ammonium salt crystals are extracted by adopting the evaporative crystallization device, vapor is only required to be introduced at the initial running stage of the device; sufficient heat sources can be provided for the evaporator and the preheater during the subsequent evaporation process by utilizing secondary steam, and live vapor is not required to be introduced in again; the energy source consumption can be reduced effectively.
Description
Technical field
The present invention relates to a kind of ammonium salt production equipment, is to utilize steam recompression (MVR) to extract the evaporated crystallization device of ammonium salt specifically, and it can recycle fully to the indirect steam producing in ammonium salt solution crystallization process, thereby saves the energy.
Background technology
As everyone knows, evaporative crystallization is topmost a kind of ammonium salt extraction process, its main process is by heating (generally adopting steam) saturated ammonium salt solution, moisture in solution is evaporated in a large number, concentration supersaturation and produce ammonium salt crystallization, finally obtains the crystal product of ammonium salt by brilliant liquid separating apparatus.
Traditional ammonium salt evaporated crystallization device comprises feed pump, preheater, circulating pump, crystallizing tank, magma pump, centrifuge and evaporimeter.Solution inlet port and steam inlet are arranged at the top of preheater, and condensate outlet and taphole are arranged at bottom.Solution inlet port and steam (vapor) outlet are arranged at the top of crystallizing tank, and taphole and magma outlet are arranged at bottom.On evaporimeter, there are solution inlet port, taphole, steam inlet and steam (vapor) outlet.The taphole of described preheater is connected with the import of circulating pump, circulation delivery side of pump is connected with the solution inlet port of crystallizing tank, the magma outlet of crystallizing tank is connected with the import of magma pump, magma delivery side of pump is connected with centrifuge, the steam (vapor) outlet of crystallizing tank is connected with the steam inlet of evaporimeter, the taphole of crystallizing tank is connected with the solution inlet port of evaporimeter, and the taphole of evaporimeter is connected with the import of circulating pump, and the steam inlet of preheater is connected with raw jet chimney.It is in order to improve the utilization ratio of the energy that the steam (vapor) outlet of crystallizing tank is connected with the steam inlet of evaporimeter, and the indirect steam that utilizes a front evaporative crystallization to produce heats the ammonium salt solution flowing in evaporimeter again, and heat is utilized again.Yet, because the heat that indirect steam itself contains is less, after heating the solution in evaporimeter, it almost completely loses heat, so evaporimeter cannot be again for preheater provides steam source, need on the steam inlet of preheater, connect raw jet chimney, could provide the steam with enough heats for preheater.Therefore, this evaporated crystallization device, when operation, need to continuously pass into raw steam and just can make whole device normally move, and need to expend a large amount of energy.
Summary of the invention
The problem to be solved in the present invention is to provide a kind of evaporated crystallization device that utilizes both vapor compression technology to extract ammonium salt, adopt this evaporated crystallization device to extract ammonium salt crystal, only need to it, pass into steam at device initial operating stage, subsequent evaporation process utilizes indirect steam to can be evaporimeter and preheater provides enough thermals source, without passing into again raw steam, can effectively reduce the consumption of the energy.
For addressing the above problem, take following scheme:
The evaporated crystallization device that utilizes steam recompression to extract ammonium salt of the present invention comprises feed pump, preheater, circulating pump, crystallizing tank, magma pump, centrifuge and evaporimeter.The first solution inlet port and the first steam inlet are arranged at the top of preheater, and the first taphole and condensate outlet are arranged at bottom.The second solution inlet port and indirect steam outlet are arranged at the top of crystallizing tank, and the second taphole, magma outlet and magma import are arranged at bottom.On evaporimeter, there are the 3rd solution inlet port, the 3rd taphole, the 3rd steam inlet and the 3rd steam (vapor) outlet.Described feed pump outlet is connected with the first solution inlet port of preheater, the first taphole of preheater is connected with the import of circulating pump, circulation delivery side of pump is connected with the second solution inlet port of crystallizing tank, the magma outlet of crystallizing tank is connected with the import of magma pump, the magma import of crystallizing tank is connected with magma delivery side of pump, magma delivery side of pump is also connected with centrifuge, the second taphole of crystallizing tank is connected with the 3rd solution inlet port of evaporimeter, and the 3rd taphole of evaporimeter is connected with the import of circulating pump.Be characterized in there is vapour compression machine between described crystallizing tank and evaporimeter, the import of vapour compression machine is connected with the outlet of the indirect steam of crystallizing tank, the outlet of vapour compression machine is connected with the 3rd steam inlet of evaporimeter, and the 3rd steam (vapor) outlet of evaporimeter is connected with the first steam inlet of preheater.
Further improvement of the present invention scheme is that described evaporimeter is lateral arrangement, and its 3rd steam inlet and the 3rd steam (vapor) outlet are all positioned at the top of evaporimeter, and its 3rd solution inlet port and the 3rd taphole lay respectively at the transverse ends of evaporimeter.
Wherein, in described crystallizing tank, have baffle plate, baffle plate is cylindrical shape and both ends open, and the upper end of baffle plate is connected with crystallizing tank inner chamber top.The guide shell that has concentric layout in baffle plate, there is screw crystallizing tank bottom corresponding to guide shell lower end, and the turning cylinder of screw is connected with drive unit.The indirect steam outlet of crystallizing tank is positioned at crystallizing tank top corresponding to guide shell upper end, the second solution inlet port of crystallizing tank is positioned on crystallizing tank sidewall corresponding to baffle plate top, the second taphole of crystallizing tank is positioned on crystallizing tank sidewall corresponding to guide shell bottom, the relative position place that the magma outlet of crystallizing tank and magma import lay respectively at crystallizing tank internal propeller below.
Take such scheme, have the following advantages:
Owing to having vapour compression machine between the crystallizing tank that utilizes the evaporated crystallization device that steam recompression extracts ammonium salt of the present invention and evaporimeter, the import of vapour compression machine is connected with the outlet of the indirect steam of crystallizing tank, the outlet of vapour compression machine is connected with the 3rd steam inlet of evaporimeter, and the 3rd steam (vapor) outlet of evaporimeter is connected with the first steam inlet of preheater.Like this, the indirect steam flowing out from crystallizing tank is when through vapour compression machine, its pressure and temperature will obviously raise, heat content increases greatly, being imported evaporimeter heats the ammonium salt solution flowing out from crystallizing tank again, all the other vapour also have enough heats, and it can flow into preheater by the pipeline between the 3rd steam (vapor) outlet of evaporimeter and the first steam inlet of preheater, and the ammonium salt solution in preheater is heated.Therefore, the initial stage of only moving at this evaporated crystallization device, need to pass into a small amount of raw steam or adopt Electric heating that steam is provided it, once complete evaporative crystallization for the first time, device itself just can produce enough thermals source evaporimeter and preheater are heated, without passing into again raw steam, get final product the normal operation of assurance device, thereby can greatly reduce the consumption of the energy.
Accompanying drawing explanation
Fig. 1 is the structural representation that utilizes steam recompression to extract the evaporated crystallization device of ammonium salt of the present invention.
The specific embodiment
Below in conjunction with accompanying drawing, the present invention is described in further detail.
As shown in Figure 1, the evaporated crystallization device that utilizes steam recompression to extract ammonium salt of the present invention comprises feed pump 1, preheater 2, circulating pump 13, crystallizing tank 24, magma pump 14, centrifuge 15, evaporimeter 10 and vapour compression machine 8.The first solution inlet port 5 and the first steam inlet 6 are arranged at the top of preheater 2, and the first taphole 4 and condensate outlet 3 are arranged at bottom.The second solution inlet port 23 and indirect steam outlet 25 are arranged at the top of crystallizing tank 24, and the second taphole 16, magma outlet 17 and magma import 19 are arranged at bottom.Evaporimeter 10 is lateral arrangement, on it, there are the 3rd solution inlet port 12, the 3rd taphole 7, the 3rd steam inlet 11 and the 3rd steam (vapor) outlet 9, the 3rd steam inlet 11 and the 3rd steam (vapor) outlet 9 are all positioned at the top of evaporimeter 10, and the 3rd solution inlet port 12 and the 3rd taphole 7 lay respectively at the transverse ends of evaporimeter 10.Described feed pump 1 outlet is connected with the first solution inlet port 5 of preheater 2, the first taphole 4 of preheater 2 is connected with the import of circulating pump 13, the outlet of circulating pump 13 is connected with the second solution inlet port 23 of crystallizing tank 24, the magma outlet 17 of crystallizing tank 24 is connected with the import of magma pump 14, the magma import 19 of crystallizing tank 24 is connected with the outlet of magma pump 14, the outlet of magma pump 14 is also connected with centrifuge 15, the indirect steam outlet 25 of crystallizing tank 24 is connected with the import of vapour compression machine 8, the outlet of vapour compression machine 8 is connected with the 3rd steam inlet 11 of evaporimeter 10, the 3rd steam (vapor) outlet 9 of evaporimeter 10 is connected with the first steam inlet 6 of preheater 2, the second taphole 16 of crystallizing tank 24 is connected with the 3rd solution inlet port 12 of evaporimeter 10, the 3rd taphole 7 of evaporimeter 10 is connected with the import of circulating pump 13.
Wherein, in described crystallizing tank 24, have baffle plate 22, baffle plate 22 is cylindrical shape and both ends open, and the upper end of baffle plate 22 is connected with crystallizing tank 24 inner chamber tops.The guide shell 21 that has concentric layout in baffle plate 22, there is screw 20 crystallizing tank 24 bottoms corresponding to guide shell 21 lower ends, and the turning cylinder of screw 20 is connected with drive unit 18.The indirect steam outlet 25 of crystallizing tank 24 is positioned at crystallizing tank 24 tops corresponding to guide shell 21 upper ends, the second solution inlet port 23 of crystallizing tank 24 is positioned on crystallizing tank 24 sidewalls corresponding to baffle plate 22 tops, the second taphole 16 of crystallizing tank 24 is positioned on crystallizing tank 24 sidewalls of guide shell 21 bottom correspondences, and the outlet 17 of the magma of crystallizing tank 24 and magma import 19 lay respectively at the relative position place of crystallizing tank 24 internal propeller 20 belows.
During work, utilize feed pump 1 that ammonium salt solution is introduced from the first solution inlet port 5 of preheater 2, ammonium salt solution is subject to Steam Heating in preheater 2, and moisture content volatilization, becomes saturated ammonium salt solution.By circulating pump 13, act on again, the saturated ammonium salt solution in preheater 2 is continuously flowed in crystallizing tank 24.Saturated ammonium salt solution flows into crystallizing tank 24 bottoms from the passage between crystallizing tank 24 Internal baffles 22 and inwall, under the promotion of its bottom screw 20, saturated ammonium salt solution is by guide shell 21 fast rise, because crystallizing tank 24 is interior, it is negative pressure, make the part instant water evaporation in saturated ammonium salt solution produce indirect steam, and got rid of by the indirect steam outlet 25 of crystallizing tank 24.After the evaporation of part water in saturated ammonium salt solution, will produce ammonium salt crystallization, these ammonium salt crystallizations fall to crystallizing tank 24 bottoms from the passage of 22, guide shell 21 and baffle plate.Then, by magma pump 14, the mixture of the ammonium salt crystallization of crystallizing tank 24 bottoms and solution is drawn to centrifuge 15, and by centrifuge 15, liquid is deviate from, thereby form ammonium salt crystallization.The indirect steam of getting rid of from crystallizing tank 24 top indirect steam outlets 25 flow in vapour compression machine 8, and after vapour compression machine 8 compressions, the pressure and temperature of indirect steam will obviously raise, and heat content increases greatly.Indirect steam after overcompression enters evaporimeter 10 through the 3rd steam inlet 11 of evaporimeter 10, this indirect steam can heat flow into the ammonium salt solution of evaporimeters 10 from crystallizing tank 24 bottoms, makes it again become saturated ammonium salt solution and is again pumped into and in crystallizing tank 24, carried out evaporative crystallization by circulating pump 13.Indirect steam in evaporimeter 10 again via the 3rd steam (vapor) outlet 9 of evaporimeter 10, enter preheater 2 after the first steam inlet 6 of preheater 2, thereby the ammonium salt solution that can be follow-up introducing preheater 2 carries out Steam Heating.
Claims (3)
1. utilize steam recompression to extract the evaporated crystallization device of ammonium salt, comprise feed pump (1), preheater (2), circulating pump (13), crystallizing tank (24), magma pump (14), centrifuge (15) and evaporimeter (10), the first solution inlet port (5) and the first steam inlet (6) are arranged at the top of preheater (2), and the first taphole (4) and condensate outlet (3) are arranged at bottom, the second solution inlet port (23) and indirect steam outlet (25) are arranged at the top of crystallizing tank (24), and the second taphole (16), magma outlet (17) and magma import (19) are arranged at bottom, on evaporimeter (10), there are the 3rd solution inlet port (12), the 3rd taphole (7), the 3rd steam inlet (11) and the 3rd steam (vapor) outlet (9), described feed pump (1) outlet is connected with first solution inlet port (5) of preheater (2), first taphole (4) of preheater (2) is connected with the import of circulating pump (13), the outlet of circulating pump (13) is connected with second solution inlet port (23) of crystallizing tank (24), the magma outlet (17) of crystallizing tank (24) is connected with the import of magma pump (14), the magma import (19) of crystallizing tank (24) is connected with the outlet of magma pump (14), the outlet of magma pump (14) is also connected with centrifuge (15), second taphole (16) of crystallizing tank (24) is connected with the 3rd solution inlet port (12) of evaporimeter (10), the 3rd taphole (7) of evaporimeter (10) is connected with the import of circulating pump (13), it is characterized in that there is vapour compression machine (8) between described crystallizing tank (24) and evaporimeter (10), the import of vapour compression machine (8) is connected with the indirect steam outlet (25) of crystallizing tank (24), the outlet of vapour compression machine (8) is connected with the 3rd steam inlet (11) of evaporimeter (10), and the 3rd steam (vapor) outlet (9) of evaporimeter (10) is connected with first steam inlet (6) of preheater (2).
2. the evaporated crystallization device that utilizes both vapor compression technology to extract ammonium salt as claimed in claim 1, it is characterized in that described evaporimeter (10) is lateral arrangement, its the 3rd steam inlet (11) and the 3rd steam (vapor) outlet (9) are all positioned at the top of evaporimeter (10), and its 3rd solution inlet port (12) and the 3rd taphole (7) lay respectively at the transverse ends of evaporimeter (10).
3. the evaporated crystallization device that utilizes both vapor compression technology to extract ammonium salt as claimed in claim 1 or 2, it is characterized in that in described crystallizing tank (24), there is baffle plate (22), baffle plate (22) is cylindrical shape and both ends open, and the upper end of baffle plate (22) is connected with crystallizing tank (24) inner chamber top; The guide shell (21) that has concentric layout in baffle plate (22), there is screw (20) crystallizing tank (24) bottom corresponding to guide shell (21) lower end, and the turning cylinder of screw (20) is connected with drive unit (18); The indirect steam outlet (25) of crystallizing tank (24) is positioned at crystallizing tank (24) top corresponding to guide shell (21) upper end, second solution inlet port (23) of crystallizing tank (24) is positioned on crystallizing tank (24) sidewall corresponding to baffle plate (22) top, second taphole (16) of crystallizing tank (24) is positioned on crystallizing tank (24) sidewall corresponding to guide shell (21) bottom, and the magma outlet (17) of crystallizing tank (24) and magma import (19) lay respectively at the relative position place of crystallizing tank (24) internal propeller (20) below.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201310542273.4A CN103566621A (en) | 2013-11-06 | 2013-11-06 | Evaporative crystallization device for extracting ammonium salt by utilizing vapor recompression technique |
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| CN201310542273.4A CN103566621A (en) | 2013-11-06 | 2013-11-06 | Evaporative crystallization device for extracting ammonium salt by utilizing vapor recompression technique |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104355322A (en) * | 2014-12-02 | 2015-02-18 | 成都华西堂投资有限公司 | System for preparing ammonium salt from fume cleaning waste liquid |
| CN107128988A (en) * | 2017-04-13 | 2017-09-05 | 江苏瑞升华能源科技有限公司 | A kind of waste water crystal system containing sodium sulphate |
| CN108910997A (en) * | 2018-09-17 | 2018-11-30 | 山东天力能源股份有限公司 | A kind of high-salt wastewater energy conservation evaporation and crystallization system and technique |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104355322A (en) * | 2014-12-02 | 2015-02-18 | 成都华西堂投资有限公司 | System for preparing ammonium salt from fume cleaning waste liquid |
| CN107128988A (en) * | 2017-04-13 | 2017-09-05 | 江苏瑞升华能源科技有限公司 | A kind of waste water crystal system containing sodium sulphate |
| CN107128988B (en) * | 2017-04-13 | 2019-08-06 | 江苏瑞升华能源科技有限公司 | A kind of waste water crystal system containing sodium sulphate |
| CN108910997A (en) * | 2018-09-17 | 2018-11-30 | 山东天力能源股份有限公司 | A kind of high-salt wastewater energy conservation evaporation and crystallization system and technique |
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Application publication date: 20140212 |