CN221071046U - Sodium nitrate production system - Google Patents
Sodium nitrate production system Download PDFInfo
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- CN221071046U CN221071046U CN202322663084.4U CN202322663084U CN221071046U CN 221071046 U CN221071046 U CN 221071046U CN 202322663084 U CN202322663084 U CN 202322663084U CN 221071046 U CN221071046 U CN 221071046U
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- effect
- sodium nitrate
- production system
- evaporation device
- flash evaporator
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- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 title claims abstract description 87
- 235000010344 sodium nitrate Nutrition 0.000 title claims abstract description 44
- 239000004317 sodium nitrate Substances 0.000 title claims abstract description 44
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 32
- 238000001704 evaporation Methods 0.000 claims abstract description 82
- 230000008020 evaporation Effects 0.000 claims abstract description 73
- 239000000706 filtrate Substances 0.000 claims abstract description 24
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims abstract description 22
- 229910017604 nitric acid Inorganic materials 0.000 claims abstract description 22
- 239000002562 thickening agent Substances 0.000 claims abstract description 17
- 230000000694 effects Effects 0.000 claims description 43
- 238000004090 dissolution Methods 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 5
- 238000001035 drying Methods 0.000 claims description 4
- 239000012452 mother liquor Substances 0.000 description 10
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 6
- 238000009833 condensation Methods 0.000 description 6
- 230000005494 condensation Effects 0.000 description 6
- 239000011777 magnesium Substances 0.000 description 6
- 229910052749 magnesium Inorganic materials 0.000 description 6
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 description 4
- 239000013078 crystal Substances 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- ZFXVRMSLJDYJCH-UHFFFAOYSA-N calcium magnesium Chemical compound [Mg].[Ca] ZFXVRMSLJDYJCH-UHFFFAOYSA-N 0.000 description 2
- 239000012043 crude product Substances 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005338 heat storage Methods 0.000 description 2
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 229910000838 Al alloy Inorganic materials 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000012459 cleaning agent Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 210000003298 dental enamel Anatomy 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 150000008040 ionic compounds Chemical class 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- YPJKMVATUPSWOH-UHFFFAOYSA-N nitrooxidanyl Chemical compound [O][N+]([O-])=O YPJKMVATUPSWOH-UHFFFAOYSA-N 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000002367 phosphate rock Substances 0.000 description 1
- OJMIONKXNSYLSR-UHFFFAOYSA-N phosphorous acid Chemical compound OP(O)O OJMIONKXNSYLSR-UHFFFAOYSA-N 0.000 description 1
- OXNIZHLAWKMVMX-UHFFFAOYSA-N picric acid Chemical compound OC1=C([N+]([O-])=O)C=C([N+]([O-])=O)C=C1[N+]([O-])=O OXNIZHLAWKMVMX-UHFFFAOYSA-N 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 235000010333 potassium nitrate Nutrition 0.000 description 1
- 239000004323 potassium nitrate Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- -1 salt sodium nitrate Chemical class 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to the technical field of sodium nitrate processing systems, in particular to a sodium nitrate production system. The utility model discloses a sodium nitrate production system, which comprises a feed tank for receiving magnesium-removed filtrate, wherein the feed tank is connected to a first-effect evaporation device, the first-effect evaporation device is connected to a second-effect evaporation device, the second-effect evaporation device is connected to a third-effect evaporation device, the third-effect evaporation device is connected to a thickener, the thickener is connected to a first filter, and the first filter is connected to a dryer. According to the production system, through the arrangement of the multistage evaporation device, energy sources can be effectively utilized, the production efficiency is improved, and refined sodium nitrate is prepared and nitric acid solution is recovered.
Description
Technical Field
The utility model relates to the technical field of sodium nitrate processing systems, in particular to a sodium nitrate production system.
Background
Sodium nitrate is a raw material for manufacturing mine explosives, is widely used for glass manufacturing industry and enamel production, is used as a metal cleaning agent in the mechanical industry, is used as a heat treatment agent for steelmaking and aluminum alloy in the metallurgical industry, is also used as a decoloring agent for molten caustic soda, is used as a raw material for manufacturing potassium nitrate and picric acid, and is gradually used as a fracturing agent instead of other chemical raw materials in petroleum exploitation. In recent years, with the rapid rise of the emerging solar energy industry, the usage of molten salt sodium nitrate as a heat storage medium in solar heat storage power generation has been in an increasing trend year by year.
In phosphorite and chemical fertilizer processing enterprises, chemical mineral separation byproducts such as calcium-magnesium concentrated solution and crude calcium nitrate solution contain a large amount of calcium, magnesium, potassium and other ionic compounds; after the calcium-magnesium concentrate and the crude calcium nitrate solution are treated, magnesium-removed filtrate is obtained, and nitrate radical and sodium ions are contained in the magnesium-removed filtrate, so that the magnesium-removed filtrate can not be directly discharged.
For this reason, it is necessary to provide a system for sodium nitrate production using the demagging filtrate.
Disclosure of utility model
In order to overcome the defects of the prior art, the sodium nitrate production system provided by the utility model can more effectively utilize energy sources through the arrangement of the multistage evaporation device, improve the production efficiency, prepare refined sodium nitrate and recycle nitric acid solution.
The technical scheme adopted for solving the technical problems is as follows:
a sodium nitrate production system comprising a feed tank receiving a demagging filtrate, the feed tank being connected to a first effect evaporation device, the first effect evaporation device being connected to a second effect evaporation device, the second effect evaporation device being connected to a third effect evaporation device, the third effect evaporation device being connected to a thickener, the thickener being connected to a first filter, the first filter being connected to a dryer.
Further, the first-effect evaporation device comprises a first-effect flash evaporator and a first-effect condenser, wherein the first-effect flash evaporator is connected to the feed tank, and the first-effect condenser is connected to the nitric acid collector.
Still further, the two-effect evaporation device comprises a two-effect flash evaporator and a two-effect condenser, wherein the two-effect flash evaporator is connected to the one-effect evaporator, and the two-effect condenser is connected to the nitric acid collector.
Still further, triple effect evaporation plant includes triple effect flash vessel and triple effect condenser, triple effect flash vessel's feed inlet is connected to the discharge gate of double effect flash vessel, triple effect flash vessel's discharge gate is connected to the thickener, triple effect condenser is connected to the nitric acid collector.
Still further, the system also includes a preheater for preheating the demagnetized filtrate introduced into the first-effect flash vessel from the feed tank.
Further, the system also comprises a redissolution tank, wherein the redissolution tank is used for redissolving sodium nitrate after being dried by the dryer.
Still further, the system further comprises an evaporative crystallizer connected to the redissolution tank.
Still further, the system further comprises a second filter connected to the evaporative crystallizer.
Further, the preheating temperature of the preheater is 60-70 ℃.
Further, the evaporating temperature of the evaporating crystallizer is 85-90 ℃.
The beneficial effects of the utility model are as follows:
According to the production system, through the arrangement of the multistage evaporation device, energy sources can be effectively utilized, the production efficiency is improved, and refined sodium nitrate is prepared and nitric acid solution is recovered.
The production system can produce sodium nitrate products with high quality and high purity through the steps of multi-effect evaporation, redissolution, evaporation crystallization and the like.
Drawings
The utility model will be further described with reference to the drawings and examples.
FIG. 1 is a schematic diagram of a sodium nitrate production system according to the present application;
FIG. 2 is a schematic flow diagram of a product of a sodium nitrate production system of the present application in operation;
In the figure: 1. a feed chute; 2. a first-effect evaporation device; 3. a double-effect evaporation device; 4. a triple effect evaporation device; 5. a thickener; 6. a first filter; 7. a dryer; 8. a nitric acid collector; 9. a preheater; 10. a redissolving tank; 11. an evaporative crystallizer; 12. a second filter; 1101. a one-effect flash evaporator; 1102. a first effect condenser; 2101. a two-effect flash evaporator; 2102. a double-effect condenser; 3101. a triple effect flash evaporator; 3102. a three-effect condenser.
Detailed Description
The utility model will be further illustrated by the following examples, which are not intended to limit the scope of the utility model, in order to facilitate the understanding of those skilled in the art.
As used herein, "and/or" includes any and all combinations of one or more of the associated listed items. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the utility model. As used herein, the singular forms "a", "an", and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise. It will be further understood that the terms "comprises" and/or "comprising," when used in this specification, specify the presence of stated features, integers, steps, operations, elements, and/or components, but do not preclude the presence or addition of one or more other features, integers, steps, operations, elements, components, and/or groups thereof.
A sodium nitrate production system as claimed in figures 1-2 comprising a feed tank 1 receiving a demagnetized filtrate, the feed tank 1 being connected to a one-effect evaporation device 2, the one-effect evaporation device 2 being connected to a two-effect evaporation device 3, the two-effect evaporation device 3 being connected to a three-effect evaporation device 4, the three-effect evaporation device 4 being connected to a thickener 5, the thickener 5 being connected to a first filter 6, the first filter 6 being connected to a dryer 7.
Specifically, the feed tank 1 is used for receiving a magnesium removal filtrate, and the magnesium removal filtrate contains sodium nitrate.
And the one-effect evaporation device 2 is used for evaporating and condensing the introduced magnesium-removed filtrate.
And the second-effect evaporation device 3 is used for evaporating and condensing the first-effect evaporation mother liquor led in by the first-effect evaporation device 2.
And the three-effect evaporation device 4 is used for evaporating and condensing the two-effect evaporation mother liquor led in by the two-effect evaporation device 3.
And the thickener 5 is used for collecting the sodium nitrate crystal slurry obtained after the evaporation of the three-effect evaporation device 4.
And a filter for filtering the sodium nitrate crystal slurry collected by the thickener 5.
And a dryer 7 for filtering the filter to obtain sodium nitrate filter cake.
In one embodiment, the first effect evaporation device 2 comprises a first effect flash evaporator 1101 and a first effect condenser 1102, the first effect flash evaporator 1101 is connected to the feed tank 1, and the first effect condenser 1102 is connected to the nitric acid collector 8.
Specifically, the feed inlet of the one-effect flash evaporator 1101 is connected to the discharge outlet of the feed tank 1, the exhaust outlet of the one-effect flash evaporator 1101 is connected to the condensation inlet of the one-effect condenser 1102, and the condensation outlet of the one-effect condenser 1102 is connected to the feed inlet of the nitric acid collector 8. Heating the magnesium-removed filtrate to 120-130 ℃ in a first-effect evaporator, condensing steam in a first-effect condenser 1102 through an exhaust port of a first-effect flash evaporator 1101, and introducing the first-effect condensate into a nitric acid collector 8; after the evaporation is finished, the first-effect mother liquor in the first-effect evaporator is led into the second-effect evaporation device 3.
In one embodiment, the two-effect evaporation device 3 comprises a two-effect flash evaporator 2101 and a two-effect condenser 2102, wherein the two-effect flash evaporator 2101 is connected to a one-effect evaporator, and the two-effect condenser 2102 is connected to a nitric acid collector 8.
Specifically, the feed inlet of the two-effect flash evaporator 2101 is connected to the discharge outlet of the one-effect evaporator, the exhaust outlet of the two-effect flash evaporator 2101 is connected to the condensation inlet of the two-effect condenser 2102, and the condensation outlet of the two-effect condenser 2102 is connected to the feed inlet of the nitric acid collector 8. Heating the magnesium-removed filtrate to 110-120 ℃ in a double-effect evaporator, condensing steam in a double-effect condenser 2102 through an exhaust port of a double-effect flash evaporator 2101, and introducing the double-effect condensate into a nitric acid collector 8; after the evaporation is finished, the two-effect mother liquor in the two-effect evaporator is led into the three-effect evaporation device 4.
In one embodiment, the triple effect evaporation device 4 comprises a triple effect flash evaporator 3101 and a triple effect condenser 3102, wherein the feed inlet of the triple effect flash evaporator 3101 is connected to the discharge outlet of the double effect flash evaporator 2101, the discharge outlet of the triple effect flash evaporator 3101 is connected to the thickener 5, and the triple effect condenser 3102 is connected to the nitric acid collector 8.
Specifically, the feed inlet of the three-effect flash evaporator 3101 is connected to the discharge outlet of the two-effect flash evaporator 2101, the exhaust outlet of the three-effect flash evaporator 3101 is connected to the condensation inlet of the three-effect condenser 3102, and the condensation outlet of the three-effect condenser 3102 is connected to the feed inlet of the nitric acid collector 8. Heating the magnesium-removed filtrate to 105-110 ℃ in a three-effect evaporator, condensing steam in a three-effect condenser 3102 through an exhaust port of the three-effect flash evaporator 3101, and introducing the three-effect condensate into a nitric acid collector 8; after the evaporation is finished, the three-effect mother liquor in the three-effect evaporator is led into the thickener 5.
In one embodiment, the system further comprises a preheater 9, the preheater 9 being used to preheat the demagnetized filtrate introduced into the first-effect flash vessel 1101 from the feed tank 1. The preheating temperature of the preheater 9 is 60-70 c and the demagnetized filtrate may be preheated to about 50 c.
In one embodiment, the system further comprises a re-dissolution tank 10, wherein the re-dissolution tank 10 is used for re-dissolving sodium nitrate after drying by the dryer 7. Also included is an evaporative crystallizer 11, said evaporative crystallizer 11 being connected to a redissolution tank 10. The system further comprises a second filter 12, said second filter 12 being connected to the evaporative crystallizer 11. The evaporating temperature of the evaporating crystallizer 11 is 85-90 ℃.
Specifically, the discharge port of the redissolution tank 10 is connected to the feed port of the evaporation crystallizer 11, the discharge port of the evaporation crystallizer 11 is connected to the feed port of the filter, and after the redissolution tank 10 dissolves sodium nitrate, the sodium nitrate is evaporated in the evaporation crystallizer 11, and after the evaporation is finished, the sodium nitrate crystals are crystallized at 30-40 ℃. After the crystallization, the solution was filtered by a second filter 12 and dried to obtain purified sodium nitrate.
The production system of the application has the following specific operation processes:
introducing the magnesium-removed filtrate into a feed tank, and conveying the received magnesium-removed filtrate to a one-effect evaporation device by the feed tank;
in a one-effect evaporation device, the magnesium-removed filtrate is heated to a specific temperature (for example, 120-130 ℃), and then enters a one-effect flash evaporator for flash evaporation to generate steam; the steam enters a first-effect condenser through an exhaust port of the first-effect flash evaporator to be condensed, and the generated condensate is led into a nitric acid collector; the mother liquor treated by the first-effect evaporation device (i.e. the non-evaporated magnesium removal filtrate) is led into the second-effect evaporation device.
In a two-effect evaporation device, the mother liquor is heated to a specific temperature (for example, 110-120 ℃), and then enters a two-effect flash evaporator for flash evaporation to generate steam; the steam enters a double-effect condenser through an exhaust port of the double-effect flash evaporator to be condensed, and the generated condensate is led into a nitric acid collector; the mother liquor treated by the two-effect evaporation device (namely, the non-evaporated magnesium removal filtrate) is led into the three-effect evaporation device.
In a three-effect evaporation device, the mother liquor is heated to a specific temperature (for example, 105-110 ℃), and then enters a three-effect flash evaporator for flash evaporation to generate steam; the steam enters a three-effect condenser through an exhaust port of the three-effect flash evaporator to be condensed, and the generated condensate is led into a nitric acid collector; the mother liquor treated by the triple effect evaporation device (i.e. the non-evaporated magnesium removal filtrate) is led into a thickener.
And sending the sodium nitrate crystal slurry collected by the thickener into a first filter for filtering, and drying by a dryer to obtain a sodium nitrate crude product.
Dissolving the sodium nitrate crude product in a redissolving tank, evaporating and crystallizing in an evaporating crystallizer, filtering in a second filter, and drying to obtain refined sodium nitrate.
The above embodiments are preferred embodiments of the present utility model, and besides, the present utility model may be implemented in other ways, and any obvious substitution is within the scope of the present utility model without departing from the concept of the present utility model.
Claims (10)
1. Sodium nitrate production system, characterized by, including receiving feed chute (1) of demagging filtrate, feed chute (1) is connected to one effect evaporation plant (2), one effect evaporation plant (2) are connected to two effect evaporation plant (3), two effect evaporation plant (3) are connected to three effect evaporation plant (4), three effect evaporation plant (4) are connected to thickener (5), thickener (5) are connected to first filter (6), first filter (6) are connected to desicator (7).
2. A sodium nitrate production system according to claim 1, characterized in that the one-effect evaporation device (2) comprises one-effect flash evaporator (1101) and one-effect condenser (1102), the one-effect flash evaporator (1101) being connected to the feed tank (1), the one-effect condenser (1102) being connected to the nitric acid collector (8).
3. A sodium nitrate production system according to claim 2, wherein the two-effect evaporation device (3) comprises a two-effect flash evaporator (2101) and a two-effect condenser (2102), the two-effect flash evaporator (2101) being connected to a one-effect evaporator, the two-effect condenser (2102) being connected to a nitric acid collector (8).
4. A sodium nitrate production system according to claim 3, characterized in that the triple effect evaporation device (4) comprises a triple effect flash evaporator (3101) and a triple effect condenser (3102), wherein the feed inlet of the triple effect flash evaporator (3101) is connected to the discharge outlet of the double effect flash evaporator (2101), wherein the discharge outlet of the triple effect flash evaporator (3101) is connected to the thickener (5), and wherein the triple effect condenser (3102) is connected to the nitric acid collector (8).
5. A sodium nitrate production system according to claim 2, further comprising a preheater (9), the preheater (9) being adapted to preheat the demagnetized filtrate introduced into the first effect flash vessel (1101) from the feed tank (1).
6. A sodium nitrate production system according to claim 1, characterized in that the system further comprises a re-dissolution tank (10), the re-dissolution tank (10) being adapted to re-dissolve sodium nitrate after drying in the dryer (7).
7. A sodium nitrate production system according to claim 6, characterized in that the system further comprises an evaporative crystallizer (11), the evaporative crystallizer (11) being connected to the re-dissolution tank (10).
8. A sodium nitrate production system according to claim 6, characterized in that the system further comprises a second filter (12), the second filter (12) being connected to the evaporative crystallizer (11).
9. A sodium nitrate production system according to claim 5, characterized in that the pre-heating temperature of the pre-heater (9) is 60-70 ℃.
10. A sodium nitrate production system according to claim 7, characterized in that the evaporation temperature of the evaporation crystallizer (11) is 85-90 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322663084.4U CN221071046U (en) | 2023-09-28 | 2023-09-28 | Sodium nitrate production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322663084.4U CN221071046U (en) | 2023-09-28 | 2023-09-28 | Sodium nitrate production system |
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| Publication Number | Publication Date |
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| CN221071046U true CN221071046U (en) | 2024-06-04 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202322663084.4U Active CN221071046U (en) | 2023-09-28 | 2023-09-28 | Sodium nitrate production system |
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| Country | Link |
|---|---|
| CN (1) | CN221071046U (en) |
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