CN110624264A - Device for slowing down scale formation of anhydrous sodium sulphate evaporation system - Google Patents
Device for slowing down scale formation of anhydrous sodium sulphate evaporation system Download PDFInfo
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- CN110624264A CN110624264A CN201910904130.0A CN201910904130A CN110624264A CN 110624264 A CN110624264 A CN 110624264A CN 201910904130 A CN201910904130 A CN 201910904130A CN 110624264 A CN110624264 A CN 110624264A
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- Prior art keywords
- heat exchanger
- pipeline
- evaporation system
- sodium sulphate
- evaporator
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- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 title claims abstract description 70
- 238000001704 evaporation Methods 0.000 title claims abstract description 57
- 230000008020 evaporation Effects 0.000 title claims abstract description 57
- 229910052938 sodium sulfate Inorganic materials 0.000 title claims abstract description 41
- 235000011152 sodium sulphate Nutrition 0.000 title claims abstract description 41
- 230000015572 biosynthetic process Effects 0.000 title claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 38
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 claims abstract description 35
- 235000010333 potassium nitrate Nutrition 0.000 claims abstract description 35
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Inorganic materials [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 14
- 238000007738 vacuum evaporation Methods 0.000 claims abstract description 12
- 230000000694 effects Effects 0.000 claims description 26
- 239000012452 mother liquor Substances 0.000 claims description 10
- 238000004519 manufacturing process Methods 0.000 abstract description 16
- 239000012535 impurity Substances 0.000 abstract description 8
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract description 7
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 abstract description 7
- 239000011575 calcium Substances 0.000 abstract description 7
- 229910052791 calcium Inorganic materials 0.000 abstract description 7
- 239000011777 magnesium Substances 0.000 abstract description 7
- 229910052749 magnesium Inorganic materials 0.000 abstract description 7
- 238000005554 pickling Methods 0.000 abstract description 7
- 238000004140 cleaning Methods 0.000 abstract description 6
- 238000000034 method Methods 0.000 abstract description 4
- 230000002035 prolonged effect Effects 0.000 abstract description 2
- 239000000463 material Substances 0.000 description 10
- 239000013078 crystal Substances 0.000 description 7
- 229910002651 NO3 Inorganic materials 0.000 description 4
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 4
- 238000003825 pressing Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 235000010344 sodium nitrate Nutrition 0.000 description 2
- 239000004317 sodium nitrate Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000010446 mirabilite Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0064—Feeding of liquid into an evaporator
- B01D1/007—Feeding of liquid into an evaporator the liquid feed being split up in at least two streams before entering the evaporator
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0094—Evaporating with forced circulation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/26—Multiple-effect evaporating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/30—Accessories for evaporators ; Constructional details thereof
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/16—Purification
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to the technical field of anhydrous sodium sulphate evaporation, and discloses a device for slowing down the scaling of an anhydrous sodium sulphate evaporation system, which comprises a multiple-effect vacuum evaporation system and a refined saltpeter water pump, the multi-effect vacuum evaporation system comprises a plurality of evaporators connected in series through steam pipelines, the device also comprises a plurality of heat exchangers connected in series through pipelines, the process of sodium sulfate solution entering an evaporation system is changed by additionally arranging a heat exchanger, most of calcium and magnesium impurity scale layers in the sodium sulfate solution are formed in the newly added heat exchanger, when the scale layer in a certain heat exchanger needs to be cleaned, the liquid inlet and the liquid outlet of the heat exchanger are only required to be closed through the pipeline control valve, the online cleaning can be realized, so that the phenomenon that the production is influenced by the serious frequent shutdown treatment of the scaling of the evaporation system is avoided, the pickling period is prolonged by 1-2 times, and the newly added preheating component can also improve the evaporation intensity of the whole evaporation system, so that the production capacity of the anhydrous sodium sulphate evaporation system is improved by about 8 percent.
Description
Technical Field
The invention relates to the technical field of anhydrous sodium sulphate evaporation, in particular to a device for slowing down the scaling of an anhydrous sodium sulphate evaporation system.
Background
The raw material for producing anhydrous sodium sulphate is a sodium sulphate solution (commonly called crude sodium nitrate solution) prepared by exploiting mirabilite ores, the sodium sulphate solution needs to be purified because the sodium sulphate solution contains calcium, magnesium and other impurities, about 95% of the impurities can be removed through purification, the purified sodium sulphate solution (refined sodium nitrate solution) enters an end-effect evaporator when entering a multi-effect vacuum evaporation system, then enters a last-effect evaporator step by step through a material transfer pump, finally enters a first-effect evaporator, steam generates secondary steam through heat exchange of the first-effect evaporator, the secondary steam enters a next-effect evaporator, and is absorbed by circulating water through the end-effect evaporator finally, the concentrated sodium sulphate solution forms sodium sulphate crystals, the crystals are normally enriched to the first two effects under the common condition of a material taking process or are subjected to material returning and pressing to enrich the crystals to a low-temperature effect and then taken out, and finally the finished product is obtained through. Calcium and magnesium impurities can be attached to the surface of a heat exchanger to form a scale layer in the evaporation concentration process, so that the heat transfer efficiency of an evaporation system is influenced, the heat exchanger of the evaporation system needs to be stopped for pickling in 20-30 days under normal conditions, but the production efficiency and the economic benefit of a factory are influenced by frequent production stoppage.
Disclosure of Invention
The invention aims to: the device for slowing down the scale formation of the anhydrous sodium sulphate evaporation system is provided, and the problems that calcium and magnesium impurities can be attached to the surface of a heat exchanger to form a scale layer in the evaporation concentration process to influence the heat transfer efficiency of the evaporation system, the heat exchanger of the evaporation system needs to be stopped for acid washing in 20-30 days under normal conditions, but the production efficiency and the economic benefit of a factory are influenced due to frequent production stoppage are solved.
The technical scheme adopted by the invention is as follows:
the utility model provides a slow down device of sodium sulfate evaporation system scale deposit, includes multiple-effect vacuum evaporation system and refined saltpeter water pump, multiple-effect vacuum evaporation system includes that a plurality of platforms pass through the evaporimeter of steam conduit series connection, the device still includes a plurality of platforms and passes through the heat exchanger of pipeline series connection, the heat exchanger passes through the pipeline and is connected with the one to one pipeline of every other evaporimeter except that last effect evaporimeter, the output route of heat exchanger is firstly through the pipeline entering in the evaporimeter that links to each other with it, secondly through the pipeline entering next heat exchanger, the output route of refined saltpeter water pump is firstly through the pipeline entering last effect evaporimeter in, secondly through the pipeline entering first heat exchanger in, the device is still including the reserve pipeline of walking around the shut down heat exchanger when being used for the heat exchanger to shut down, equally divide on all pipelines that link to each other with heat.
The working principle of the invention is as follows: adding N-1 heat exchangers corresponding to N-effect evaporators, enabling the N-1 heat exchangers to be in one-to-one correspondence with other evaporators except for a last-effect evaporator and be communicated through a pipeline, when the system normally works, all control valves of a standby pipeline are in a closed state, fine saltpeter water enters a first heat exchanger after being pressurized by a fine saltpeter water pump, after being preheated to be close to the temperature of an evaporator connected with the heat exchangers by steam, opening the pipeline control valve to enable the fine saltpeter water to enter the effect evaporator for evaporation, simultaneously opening the pipeline control valve of a next heat exchanger to enable the fine saltpeter water to enter the next heat exchanger for heat exchange, after the heat exchange is close to the temperature of the evaporator connected with the heat exchangers, opening the pipeline control valve to enable the fine-effect evaporator to enter the effect evaporator for evaporation, simultaneously opening the pipeline control valve of the next heat exchanger, circulating the liquid of the last heat exchanger only enters the first-effect evaporator, the invention changes the flow of sodium sulfate solution entering into the evaporation system, so that most of calcium and magnesium impurities in the sodium sulfate solution form a scale layer in a newly added heat exchanger, when the scale layer in a certain heat exchanger needs to be cleaned, firstly, a pipeline control valve of an evaporator connected with the sodium sulfate solution and a pipeline control valve leading to a next heat exchanger are closed, then, a pipeline valve of a standby pipeline is properly adjusted, so that liquid directly enters into the next heat exchanger connected with the heat exchanger and the evaporator connected with the heat exchanger from a previous heat exchanger (a refined saltpeter water pump) connected with the heat exchanger without passing through the heat exchanger, and the online cleaning of the scale layer in the heat exchanger can be realized, thereby avoiding the influence on production caused by serious and frequent shutdown treatment of the evaporation system due to scale formation, prolonging the pickling period by 1-2 times, and the newly added heat exchanger can also improve the evaporation intensity of the whole evaporation system, the production capacity of the anhydrous sodium sulphate evaporation system is improved by about 8 percent.
Further, the spare pipeline comprises a pipeline for connecting the refined saltpeter water pump and the second heat exchanger, and a pipeline for connecting the first heat exchanger with the corresponding evaporator and the refined saltpeter water pump.
Furthermore, the standby pipeline comprises a pipeline for connecting heat exchangers connected with two sides of the middle heat exchanger, and a pipeline for connecting the middle heat exchanger with a corresponding evaporator and a previous heat exchanger.
Further, the standby pipeline comprises a pipeline for connecting the first-effect evaporator and the last heat exchanger of the last heat exchanger.
Furthermore, except for the steam pipeline connected with the last-effect evaporator, branch pipes are respectively arranged on the rest steam pipelines, and the branch pipes are connected with the heat exchangers one by one.
Furthermore, a branch pipe of a steam pipeline at the air inlet end of the first-effect evaporator is connected with the last heat exchanger, and by analogy, the first heat exchanger is connected with the last-effect evaporator of the last-effect evaporator through the branch pipe.
Furthermore, the branch pipes are respectively provided with a control valve.
Further, the multi-effect vacuum evaporation system further comprises a centrifugal machine and a mother liquor pump, a liquid outlet of the centrifugal machine is connected with an input end of the mother liquor pump, and an output end of the mother liquor pump is communicated with each evaporator through a pipeline.
In summary, due to the adoption of the technical scheme, the invention has the beneficial effects that:
1. the invention changes the flow of sodium sulfate solution entering the evaporation system by arranging the additional heat exchanger, so that most of calcium and magnesium impurity scale layers in the sodium sulfate solution are formed in the newly added heat exchanger, and when the scale layers in a certain heat exchanger need to be cleaned, the online cleaning can be realized only by properly changing the liquid path through the standby pipeline, thereby avoiding the serious frequent shutdown treatment of the evaporation system to influence the production, and prolonging the pickling period by 1-2 times.
2. The invention can also improve the evaporation intensity of the whole evaporation system by arranging the preheating component, so that the production capacity of the anhydrous sodium sulphate evaporation system is improved by about 8 percent
3. The invention improves the prior material taking mode to carry out fractional effect material discharging, reduces the heat loss caused by higher material taking temperature or material returning and pressing, and reduces the steam energy consumption of an evaporation system by about 6 percent
Drawings
FIG. 1 is a schematic structural view of the present invention;
labeled as: the system comprises a 1-first-effect evaporator, a 2-second-effect evaporator, a 3-third-effect evaporator, a 4-fourth-effect evaporator, a 5-fifth-effect evaporator, a 6-last-effect evaporator, a 7-refined saltpeter water pump, an 8-first heat exchanger, a 9-second heat exchanger, a 10-third heat exchanger, an 11-fourth heat exchanger, a 12-fifth heat exchanger, a 13-branch pipe, a 14-standby pipeline, a 16-control valve, a 17-centrifuge, an 18-mother liquid pump and a 19-steam pipeline.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to fig. 1 in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
A device for slowing down scale formation of a sodium sulfate evaporation system comprises a multiple-effect vacuum evaporation system and a refined saltpeter water pump 7, as shown in figure 1, the multiple-effect vacuum evaporation system comprises six evaporators (namely six-effect evaporators) which are connected in series through a steam pipeline 19, the device also comprises five heat exchangers which are connected in series through pipelines, the heat exchangers are connected with every other evaporator except a last-effect evaporator 6 in a one-to-one pipeline mode through pipelines, specifically, a first-effect evaporator 1 is connected with a fifth-effect heat exchanger 12, a second-effect evaporator 2 is connected with a fourth-effect heat exchanger 11, a third-effect evaporator 3 is connected with a third-effect heat exchanger 10, a fourth-effect evaporator 4 is connected with a second-effect heat exchanger 9, and a fifth-effect evaporator 5 is connected with a first-effect heat exchanger 8;
except the fifth heat exchanger 12, the output paths of the other heat exchangers enter the connected evaporator through a pipeline and enter the next heat exchanger through a pipeline; the path of the fifth heat exchanger 12 is to enter the first-effect heat exchanger through a pipeline; the output path of the refined saltpeter water pump 7 enters the final-effect evaporator 6 through a pipeline and enters the first heat exchanger 8 through a pipeline;
the device also comprises a standby pipeline 14 which is used for bypassing the shutdown heat exchanger when the heat exchanger is shut down, wherein the standby pipeline 14 comprises a pipeline for connecting the refined saltpeter water pump 7 and the second heat exchanger 9, and a pipeline for connecting the fifth effect evaporator 5 and the refined saltpeter water pump 7; the standby pipeline 14 comprises a pipeline for connecting the first heat exchanger 8 with the third heat exchanger 10 and also comprises a pipeline for connecting the fourth-effect evaporator 4 with the first heat exchanger 8; the standby pipeline 14 comprises a pipeline for connecting the second heat exchanger 9 with the fourth heat exchanger 11, and also comprises a pipeline for connecting the third-effect evaporator 3 with the second heat exchanger 9; the standby pipeline 14 comprises a pipeline for connecting the third heat exchanger 10 with the fifth heat exchanger 12, and also comprises a pipeline for connecting the second-effect evaporator 2 with the third heat exchanger 10; the standby pipeline 14 also comprises a pipeline for connecting the first-effect evaporator 1 and the fourth heat exchanger 11;
except for the steam pipeline 19 connected with the last-effect evaporator 6, branch pipes 13 are respectively arranged on the other steam pipelines 19, the branch pipes 13 are connected with the heat exchangers one by one, the direction of steam is that air is fed from the first-effect evaporator 1, and the last-effect evaporator 6 is discharged and connected with an atmospheric condenser;
a branch pipe 13 of a steam pipeline 19 at the air inlet end of the first-effect evaporator 1 is connected with a fifth heat exchanger 12, a branch pipe 13 of the steam pipeline 19 between the first-effect evaporator 1 and the second-effect evaporator 2 is connected with a fourth heat exchanger 11, a branch pipe 13 of the steam pipeline 19 between the second-effect evaporator 2 and the third-effect evaporator 3 is connected with a third heat exchanger 10, a branch pipe 13 of the steam pipeline 19 between the third-effect evaporator 3 and the fourth-effect evaporator 4 is connected with a second heat exchanger 9, and a branch pipe 13 of the steam pipeline 19 between the fourth-effect evaporator 4 and the fifth-effect evaporator 5 is connected with a first heat exchanger 8;
all pipelines connected with the heat exchanger and the branch pipe 13 are respectively provided with a control valve 16, and all pipelines connected with the refined saltpeter water pump 7 are respectively provided with a control valve 16.
When all the heat exchangers work, all the control valves 16 of the standby pipeline 14 are in a closed state, after the refined saltpeter water is pressurized by the refined saltpeter water pump 7, one part of the refined saltpeter water enters the first heat exchanger 8, the other part of the refined saltpeter water enters the last effect evaporator 6, after the refined saltpeter water in the first heat exchanger 8 is preheated to the temperature close to the fifth effect evaporator 5 connected with the first heat exchanger, one part of the refined saltpeter water enters the evaporator, the other part of the refined saltpeter water enters the second heat exchanger 9 for heat exchange, after the refined saltpeter water in the second heat exchanger 9 is preheated to the temperature close to the fourth effect evaporator 4 connected with the second heat exchanger, one part of the refined saltpeter water enters the evaporator, the other part of the refined saltpeter water enters the third heat exchanger 10 and the fourth heat exchanger 11 by analogy, the refined saltpeter water enters the fifth heat exchanger 12 and only enters the first effect evaporator, most of calcium and magnesium impurities in the sodium sulfate solution form a scale layer in the newly-added heat exchanger;
when the scale layer in a certain heat exchanger needs to be cleaned, firstly, the pipeline control valve 16 of the evaporator connected with the heat exchanger and the pipeline control valve 16 leading to the next heat exchanger are closed, then the pipeline valve of the spare pipeline 14 is properly adjusted, so that the liquid does not pass through the heat exchanger, directly enters the next heat exchanger connected with the heat exchanger and the evaporator connected with the heat exchanger from the last heat exchanger (the refined saltpeter water pump 7) connected with the heat exchanger,
if the first heat exchanger 8 needs to be cleaned, firstly, the control valve 16 of the pipeline connected with the fifth effect evaporator 5, the control valve 16 of the pipeline connected with the refined saltpeter water pump 7, the control valve 16 of the pipeline leading to the second heat exchanger 9 and the control valve 16 of the branch pipe 13 connected with the steam pipeline 19 are closed, then the control valve 16 of the pipeline between the refined saltpeter water pump 7 and the second heat exchanger 9 is opened, the control valve 16 of the pipeline between the refined saltpeter water pump 7 and the fifth effect evaporator 5 is opened, so that liquid does not pass through the first heat exchanger 8 and directly enters the second heat exchanger 9 and the fifth effect evaporator 5 from the refined saltpeter water pump 7, the first heat exchanger 8 can be shut down and cleaned without influencing the normal work of the whole evaporation system to realize on-line cleaning, thereby avoiding the serious scaling of the evaporation system from frequent shutdown treatment to influence production, prolonging the pickling period by 1-2 times, and the newly added heat exchanger can also improve the evaporation intensity of the, the production capacity of the anhydrous sodium sulphate evaporation system is improved by about 8 percent;
if the third heat exchanger 10 needs to be cleaned, firstly, the control valve 16 of the pipeline connected with the third effect evaporator 3, the control valve 16 of the pipeline connected with the second heat exchanger 9, the control valve 16 of the pipeline leading to the fourth heat exchanger 11 and the control valve 16 of the branch pipe 13 connected with the steam pipeline 19 are closed, then the control valve 16 of the pipeline between the second heat exchanger 9 and the fourth heat exchanger 11 is opened, the control valve 16 of the pipeline between the second heat exchanger 9 and the third effect evaporator 3 is opened, so that liquid does not pass through the third heat exchanger 10 and directly enters the fourth heat exchanger 11 and the third effect evaporator 3 from the second heat exchanger 9, the first heat exchanger 8 can be shut down and cleaned without influencing the normal work of the whole evaporation system to realize online cleaning, thereby avoiding the serious scale formation of the evaporation system from frequent shutdown treatment to influence production, prolonging the pickling period by 1-2 times, the newly added heat exchanger can also improve the evaporation intensity of the whole evaporation system, so that the production capacity of the anhydrous sodium sulphate evaporation system is improved by about 8 percent;
if the fifth heat exchanger 12 needs to be cleaned, the control valve 16 of the pipeline connected with the first effect evaporator 1, the control valve 16 of the pipeline connected with the fourth heat exchanger 11 and the control valve 16 of the branch pipe 13 connected with the steam pipeline 19 are firstly closed, then the control valve 16 of the pipeline between the fourth heat exchanger 11 and the first effect evaporator 1 is opened, so that liquid does not pass through the fifth heat exchanger 12 and directly enters the first effect evaporator 1 from the fourth heat exchanger 11, the fifth heat exchanger 12 can be stopped and cleaned, the normal work of the whole evaporation system is not affected, the online cleaning is realized, the serious frequent stopping treatment of the scaling of the evaporation system is avoided, the production is prevented from being influenced, the pickling period is prolonged by 1-2 times, the newly added heat exchanger can also improve the evaporation intensity of the whole evaporation system, and the production capacity of the anhydrous sodium sulphate evaporation system is improved by about 8%.
Example 2
In this embodiment, on the basis of embodiment 1, further, the multiple-effect vacuum evaporation system further includes a centrifuge 17 and a mother liquor pump 18, each effect evaporator is provided with a crystallizer, crystals are placed into a nitrate slurry barrel through the crystallizer after the crystals are formed, the nitrate slurry barrel is connected with an inlet of the centrifuge 17 through a pump, a liquid outlet of the centrifuge 17 is connected with an input end of the mother liquor pump 18, an output end of the mother liquor pump 18 is communicated with each evaporator through a pipeline, sodium sulfate crystals appear after evaporation and concentration of each effect evaporator, the crystallizer is taken out from the crystallizer of each effect evaporator and placed into the nitrate slurry barrel, the pump between the nitrate slurry barrel and the centrifuge 17 is started, the crystals are sent into the centrifuge 17 for centrifugal separation, the separated liquid is sent into each effect evaporator through the mother liquor pump 18, the effect-separation discharge of the existing material taking mode is improved, the heat loss caused by higher material taking temperature or material returning and pressing is reduced, and the steam energy consumption of the evaporation system is reduced by about 6 percent.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that various changes in the embodiments and/or modifications of the embodiments and/or portions thereof may be made, and all changes, equivalents, and modifications which fall within the spirit and scope of the invention are therefore intended to be embraced by the appended claims.
Claims (8)
1. A device for slowing down the scaling of a sodium sulfate evaporation system, which comprises a multi-effect vacuum evaporation system and a refined saltpeter water pump (7), the multi-effect vacuum evaporation system comprises a plurality of evaporators connected in series through steam pipelines (19), it is characterized in that the device also comprises a plurality of heat exchangers connected in series through pipelines, the heat exchangers are connected with each other evaporator except the last-effect evaporator (6) in a one-to-one pipeline way through pipelines, the output path of the heat exchanger enters the evaporator connected with the heat exchanger through a pipeline and enters the next heat exchanger through a pipeline, the output path of the refined saltpeter water pump (7) enters the last effect evaporator (6) through a pipeline and enters the first heat exchanger through a pipeline, the device also comprises a backup line (14) for bypassing the shutdown heat exchanger when the heat exchanger is shutdown, all pipelines connected with the heat exchanger and the refined saltpeter water pump (7) are respectively provided with a control valve (16).
2. The device for slowing down the scale formation of the anhydrous sodium sulphate evaporation system according to claim 1, wherein the spare pipeline (14) comprises a pipeline for connecting the refined sodium sulphate water pump (7) and the second heat exchanger, and a pipeline for connecting the first heat exchanger with the corresponding evaporator and the refined sodium sulphate water pump (7).
3. The device for slowing down the scaling of the anhydrous sodium sulphate evaporation system as claimed in claim 2, wherein the spare pipeline (14) comprises a pipeline for connecting the heat exchangers connected at two sides of the middle heat exchanger, and a pipeline for connecting the corresponding evaporator of the middle heat exchanger with the previous heat exchanger.
4. The apparatus for slowing down the scaling of a sodium sulfate evaporation system according to claim 3, wherein the spare pipeline (14) comprises a pipeline for connecting the first-effect evaporator (1) and the last heat exchanger of the last heat exchangers.
5. The device for slowing down the scaling of the anhydrous sodium sulphate evaporation system according to claim 1, wherein the steam pipelines (19) are provided with branch pipes (13) except for the steam pipelines (19) connected with the last-effect evaporator (6), and the branch pipes (13) are connected with the heat exchangers one by one.
6. The device for slowing down the scaling of the anhydrous sodium sulphate evaporation system according to claim 5, characterized in that a branch pipe (13) of a steam pipeline (19) at the air inlet end of the first-effect evaporator (1) is connected with a last-effect heat exchanger, and so on, and the first-effect heat exchanger is connected with a last-effect evaporator of the last-effect evaporator (6) through the branch pipe (13).
7. The device for slowing down the scaling of the anhydrous sodium sulphate evaporation system according to claim 5, wherein the branch pipes (13) are respectively provided with a control valve (16).
8. The device for slowing down the scaling of the anhydrous sodium sulphate evaporation system according to claim 1, wherein the multi-effect vacuum evaporation system further comprises a centrifuge (17) and a mother liquor pump (18), a liquid outlet of the centrifuge (17) is connected with an input end of the mother liquor pump (18), and an output end of the mother liquor pump (18) is respectively communicated with each evaporator through a pipeline.
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| CN204824500U (en) * | 2015-06-24 | 2015-12-02 | 中国石油天然气集团公司 | Crystal system is evaporated in succession in ultrasonic wave scale control scale removal |
| CN105399168A (en) * | 2015-12-18 | 2016-03-16 | 许达人 | Multi-effect evaporation and concentration device and technology thereof for solution containing sulfuric acid and salts thereof |
| CN211411015U (en) * | 2019-09-24 | 2020-09-04 | 四川同庆南风有限责任公司 | Device for slowing down scale formation of anhydrous sodium sulphate evaporation system |
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