CN220877759U - Evaporation stoste temperature-raising system - Google Patents
Evaporation stoste temperature-raising system Download PDFInfo
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- CN220877759U CN220877759U CN202322486423.6U CN202322486423U CN220877759U CN 220877759 U CN220877759 U CN 220877759U CN 202322486423 U CN202322486423 U CN 202322486423U CN 220877759 U CN220877759 U CN 220877759U
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- tube bundle
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- 238000001704 evaporation Methods 0.000 title claims abstract description 47
- 230000008020 evaporation Effects 0.000 title claims abstract description 43
- 238000010438 heat treatment Methods 0.000 claims abstract description 87
- 239000012452 mother liquor Substances 0.000 claims abstract description 64
- 238000007599 discharging Methods 0.000 claims abstract description 46
- 239000007788 liquid Substances 0.000 claims abstract description 46
- 239000002893 slag Substances 0.000 claims abstract description 39
- 238000000926 separation method Methods 0.000 claims abstract description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 19
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 6
- 239000000463 material Substances 0.000 claims description 4
- 230000000630 rising effect Effects 0.000 claims description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 abstract description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 230000000149 penetrating effect Effects 0.000 abstract description 4
- 239000012535 impurity Substances 0.000 description 15
- 238000005265 energy consumption Methods 0.000 description 10
- 238000000034 method Methods 0.000 description 9
- 238000004062 sedimentation Methods 0.000 description 7
- 239000011550 stock solution Substances 0.000 description 7
- 238000007667 floating Methods 0.000 description 5
- 238000012544 monitoring process Methods 0.000 description 4
- 206010039509 Scab Diseases 0.000 description 3
- 239000010413 mother solution Substances 0.000 description 3
- 238000004364 calculation method Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000004131 Bayer process Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000002354 daily effect Effects 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to the technical field of alumina production, and discloses an evaporation raw liquid temperature raising system, wherein the upper part of a conical separation tank is connected with a liquid inlet pipe, the upper part of the conical separation tank is provided with a first heating pipe bundle, a liquid inlet of the first heating pipe bundle is connected with a low-pressure heat supply pipeline through a heat supply branch pipe, a slag discharging pipe is arranged at the bottom slag hole of the conical separation tank, the slag discharging pipe is connected with a decomposition unit, the upper liquid outlet of the conical separation tank is connected with a mother liquid heating tank through a first pipeline, a second heating pipe bundle is arranged in the mother liquid heating tank, the second heating pipe bundle is connected with the first heating pipe bundle through a second pipeline, the second heating pipe bundle is connected with a condensate water tank through a third pipeline, and a liquid outlet of the condensate water tank is connected with a thermoelectric unit; the edge of the mother liquor heating tank is provided with a lifting pipe penetrating into the tank bottom, the lifting pipe is connected with a discharging tank through a fourth pipeline, and the bottom of the discharging tank is provided with a discharging pipe connected with an evaporation unit. The system reduces the low-pressure gas consumption of the evaporation unit and synchronously reduces the low-pressure unit consumption of the whole alumina system.
Description
Technical Field
The utility model relates to the field of alumina production technology, in particular to an evaporation stock solution temperature raising system.
Background
In resource enterprises, along with the continuous rising of raw material cost, high-quality products are continuously low in price, enterprises face to the adjustment of severe cost control, and in the production of alumina, mother liquor subjected to plate heat exchange needs to enter an evaporation unit to be evaporated.
The mother liquor evaporation is an important process for maintaining the balance of the water quantity and the salt quantity of a production system in the production of alumina, and is a main energy-consuming process. In the pure Bayer process for producing alumina according to statistics, the steam energy consumption accounts for more than 60% of the total energy consumption, wherein the steam for evaporating the mother liquor accounts for about 25% of the total steam consumption, which is reduced to about 15% of the total energy consumption. In order to reduce the energy consumption of mother liquor evaporation, the technical personnel in the art research various aspects from the aspects of equipment selection, process selection, reference to other industries and the like, and aim to reduce the energy consumption of mother liquor evaporation through improvements in the aspects of equipment, process and the like. Most of the methods aim at the process of mother liquor evaporation, the mother liquor subjected to plate heat exchange needs to reach the boiling point of the solution through steam, water in the solution is converted into gas and stock solution to be separated, the mother liquor evaporation is realized, the problem of the work load of an evaporation unit is not solved from the source, enterprises need to reduce the energy consumption and simultaneously consider a series of problems of the time, the equipment cost, the operation stability and the like of the mother liquor evaporation, and the cost is reduced while the efficiency of the enterprises is improved.
Disclosure of Invention
The utility model provides an evaporation raw liquid temperature raising system, which aims to solve a series of problems of high gas consumption, high load, high energy consumption, unfavorable cost control of enterprises and the like of a raw liquid evaporation unit in the existing mother liquid treatment in the production of aluminum oxide.
The utility model is realized by adopting the following technology: the device comprises a conical separation tank, wherein the upper part of the conical separation tank is connected with a liquid inlet pipe, the upper part of the conical separation tank is provided with a first heating pipe bundle, a liquid inlet of the first heating pipe bundle is connected with a low-pressure heat supply pipeline through a heat supply branch pipe, a slag outlet at the bottom of the conical separation tank is provided with a slag outlet pipe, the slag outlet pipe is connected with a decomposition unit, a liquid outlet at the upper part of the conical separation tank is connected with a mother liquor heating tank through a first pipeline, a second heating pipe bundle is arranged in the mother liquor heating tank, the second heating pipe bundle is connected with the first heating pipe bundle through a second pipeline, the second heating pipe bundle is connected with a condensate water tank through a third pipeline, and a liquid outlet of the condensate water tank is connected with a thermoelectric unit; the edge of the mother liquor heating tank is provided with a lifting pipe penetrating into the tank bottom, the lifting pipe is connected with a discharging tank through a fourth pipeline, the bottom of the discharging tank is provided with a discharging pipe connected with an evaporation unit, and a temperature measuring device is arranged on the discharging pipe.
When in implementation, the device comprises a conical separation tank, the upper part of the conical separation tank is connected with a liquid inlet pipe, mother liquid subjected to plate heat exchange is introduced into the liquid inlet pipe, a certain amount of suspended matters are contained in the mother liquid, the conical separation tank sinks a part of the suspended matters to the conical part, so that impurities in the mother liquid are effectively reduced, scabs in an evaporation tube bundle in an evaporation unit are reduced, the service life of the evaporation tube bundle is prolonged, the evaporation energy consumption is reduced, a first heating tube bundle is arranged at the upper part of the conical separation tank, the first heating tube bundle is an annular tube bundle encircling the upper part, the temperature of the mother liquor is raised, the natural sedimentation of impurities in the mother liquor is not affected, the liquid inlet of the first heating tube bundle is connected with a low-pressure heat supply pipeline through a heat supply branch pipe, the primary temperature rise of the mother liquor in the conical separation tank is carried out through the first heating tube bundle, the branch tube valve is arranged on the heat supply branch tube, the branch tube valve is controlled to be opened and closed according to feedback data of the temperature measuring device, the slag outlet at the bottom of the conical separation tank is provided with a slag discharging tube, the slag discharging tube is provided with a slag discharging valve, the slag discharging valve is normally closed, the slag discharging tube is connected with the decomposing unit, a certain amount of alumina contained in impurities is recovered through a decomposing unit, a liquid outlet at the upper part of the conical separating tank is connected with a mother liquor heating tank through a first pipeline, mother liquor subjected to separation slag discharge enters the mother liquor heating tank, a second heating tube bundle is arranged in the mother liquor heating tank and is in a symmetrical crotch shape or barreled shape, namely, a main pipeline is arranged, a plurality of branch heat exchange tube bundles are arranged on the main pipeline, the second heating tube bundle adopts the existing product, the heat exchange area of the second heating tube bundle is increased, heating the mother liquor in a mother liquor heating tank, connecting a second heating tube bundle with a first heating tube bundle through a second pipeline, connecting the second heating tube bundle with a condensing water tank through a third pipeline, and leading a liquid outlet of the condensing water tank to a thermoelectric unit; the edge of the mother liquor heating tank is provided with a lifting pipe penetrating into the tank bottom, the pipe orifice of the lifting pipe is higher than the liquid level in the mother liquor heating tank, the lifting pipe is connected with a discharging tank through a fourth pipeline, the bottom of the discharging tank is provided with a discharging pipe connected with an evaporation unit, and a temperature measuring device is arranged on the discharging pipe.
When the device is used, mother liquor at about 90 ℃ from plate heat exchange enters a conical separation tank through a liquid inlet pipe, natural sedimentation is started from the upper part of the conical separation tank, floating impurities fall into the conical part at the lower part of the conical separation tank, in the sedimentation process, the mother liquor is subjected to preliminary heating by a first heating tube bundle, the floating impurities are settled to the bottom, after accumulation for a period of time, the floating impurities are discharged into a slag discharge pipe through a slag outlet at the bottom, a slag discharge valve is opened when slag is discharged, the impurities settled at the bottom are sent to a decomposition unit from the slag discharge pipe, and the mother liquor subjected to preliminary heating and sedimentation separation impurities is connected with the mother liquor heating tank through a first pipeline from a liquid outlet at the upper part; the mother liquor heating tank is fully heated by a second heating tube bundle, the mother liquor is heated up, the mother liquor is heated uniformly, the mother liquor heating tank enters from the upper part, enters a lifting tube after passing through the second heating tube bundle, the mother liquor is extracted from the lower part and overflowed and discharged from the upper part, then the heated mother liquor enters a discharging tank through a fourth pipeline, is temporarily stored in the discharging tank and then is discharged to an evaporation unit through the discharging tube, a temperature measuring device in the discharging tube carries out real-time temperature monitoring, the temperature of the mother liquor conveyed to the evaporation unit is controlled to be about 95 ℃, the monitoring data are fed back to the central control, the central control regulates a branch valve on a heat supply branch tube, when the temperature is higher than 95 ℃, the branch valve is closed, the mother liquor at low temperature is introduced, the temperature is reduced, the raw liquor is prevented from being excessively high in lifting, when the temperature is lower than 95 ℃, the branch valve is opened to heat the raw liquor, low-pressure steam in a low-pressure heat supply pipeline is introduced into the first heating tube bundle through a heat supply branch tube, enters the second heating tube through a primary heat exchange, the heat exchange is carried out, the low-pressure steam and the condensate enters a condensate water tank, and then enters a condensate water tank.
Compared with the prior art, the utility model has the following beneficial effects: according to the evaporation stock solution temperature raising system provided by the utility model, the mother solution is preheated by utilizing 0.6Mpa low-pressure steam in the low-pressure heat supply pipeline, the temperature of the mother solution at 90 ℃ is raised to 95 ℃, and the preliminary concentration and the temperature raising of the mother solution at 5 ℃ are carried out while the prevention of scabbing in the pipe are ensured.
The specific heat of the material is 4.2 multiplied by 10 3 J/Kg DEG C, which means that the mass is 1000Kg of the material, the temperature is increased by 1 ℃, and the absorbed heat is 4.2 multiplied by 10 3 coke; the calculation was performed on a feed of 4000m 3/h as follows:
Heat required for temperature rise of 5 ℃: q 1=4.2×103J/（Kg·℃）×4000000Kg×5℃=8.652×109 J;
1000Kg of fresh steam release heat:
Q2=2748.59 kJ/kg×1000kg=2748590kJ=2.74859×109J；
The amount of fresh steam required per 4000m increase in feed temperature by 5 c is Q 1/Q2 = 3.15.
According to theoretical calculation, 3.15t of steam can be saved for every 4000m of feeding of the steam stock solution temperature raising system of the system, in actual operation, the higher the temperature is, the faster the heat dissipation is, meanwhile, the pipe loss and the heat exchange loss are considered, 10-12 t/h of new steam needs to be consumed in the actual operation process, 1.02t of new steam can be saved for evaporating the new steam consumption when the temperature is raised by 1 ℃, according to four evaporating units arranged in the factory, the stock solution temperature is raised by 5 ℃, the low-pressure steam can be saved by 1.02t/h multiplied by 5 ℃ multiplied by 4=20.4 t in each hour, and the new steam can be expected to be saved in each hour: 20.4t/h-12t/h = 8.4t/h; low pressure steam 201.6t can be saved every day.
The system utilizes the existing heat, reduces the energy consumption of the stock solution temperature raising system, ensures that the pipeline is not scarred through accurate temperature control, improves the production efficiency, is stable, is convenient to reform, greatly improves the operation efficiency after adopting the system, not only meets the daily production requirement, reduces the low-pressure gas consumption of the evaporation unit, reduces the low-pressure unit consumption of the whole alumina system, but also can wash the evaporation unit in stages, is favorable for the higher-efficiency long-term stable operation of the evaporation unit, and is suitable for wide popularization and use.
Drawings
Fig. 1 is a schematic structural view of the present utility model.
The figures are labeled as follows: 1-conical separation tank, 2-mother liquor heating tank, 3-discharge tank, 4-first heating tube bundle, 5-second heating tube bundle, 6-low pressure heat supply pipeline, 7-decomposition unit, 8-evaporation unit, 9-condensate tank, 10-thermoelectric unit, 11-temperature measuring device, 12-lifting tube, 13-liquid inlet, 14-slag outlet, 15-upper liquid outlet, 16-branch tube valve, 17-slag discharge valve,
L1-first pipeline, L2-second pipeline, L3-third pipeline, L4-fourth pipeline, L5-feed liquor pipe, L6-heat supply branch pipe, L7-slag discharge pipe, L8-discharging pipe.
Description of the embodiments
Specific embodiments of the present utility model will be described below with reference to the accompanying drawings.
An evaporation stock solution temperature raising system is shown in fig. 1: comprises a conical separation tank 1, a liquid inlet pipe L5 is connected to the upper part of the conical separation tank 1, mother liquid subjected to plate heat exchange is introduced into the liquid inlet pipe L5, a certain suspended matters are contained in the mother liquid, the conical separation tank 1 settles a part of the suspended matters to the conical part, impurities in the mother liquid are effectively reduced, scabbing in an evaporation tube bundle in an evaporation unit 8 is reduced, the service life of the evaporation tube bundle is prolonged, the energy consumption of evaporation is reduced, a first heating tube bundle 4 is arranged at the upper part of the conical separation tank 1, the first heating tube bundle 4 is an annular tube bundle encircling the upper part, the natural settlement of impurities in the mother liquid is not influenced when the temperature of the mother liquid is raised, a liquid inlet 13 of the first heating tube bundle 4 is connected with a low-pressure heat supply pipeline 6 through a heat supply branch pipe L6, the primary temperature of the mother liquid in the conical separation tank 1 is raised through the first heating tube bundle 4, a branch pipe valve 16 is arranged on the heat supply branch pipe L6, the branch pipe valve 16 is controlled to open and close according to feedback data of the temperature measuring device 11, a slag discharging pipe L7 is arranged at a slag discharging hole 14 at the bottom of the conical separation tank 1, a slag discharging valve 17 is arranged on the slag discharging pipe L7, the slag discharging valve 17 is closed normally, the slag discharging pipe L7 is connected with the decomposing unit 7, a certain amount of alumina contained in impurities is recovered through the decomposing unit 7, an upper liquid outlet 15 of the conical separation tank 1 is connected with the mother liquor heating tank 2 through a first pipeline L1, mother liquor subjected to slag separation enters the mother liquor heating tank 2, a second heating tube bundle 5 is arranged in the mother liquor heating tank 2, the second heating tube bundle 5 is in a symmetrical crotch shape or is in a barrel shape, namely, a main pipeline is arranged, a plurality of branch heat exchange tube bundles are arranged on the main pipeline, the second heating tube bundle 5 is selected as an existing product, the heat exchange area of the second heating tube bundle 5 is increased, the mother liquor in the mother liquor heating tank 2 is heated, the second heating tube bundle 5 is connected with the first heating tube bundle 4 through the second pipeline L2, the second heating tube bundle 5 is connected with a condensate water tank 9 through a third pipeline L3, and a liquid outlet of the condensate water tank 9 is communicated with a thermoelectric unit 10; the edge of the mother liquor heating tank 2 is provided with a lifting pipe 12 penetrating into the tank bottom, the pipe opening of the lifting pipe 12 is higher than the liquid level in the mother liquor heating tank 2, the lifting pipe 12 is connected with a discharging tank 3 through a fourth pipeline L4, the bottom of the discharging tank 3 is provided with a discharging pipe L8 connected with an evaporation unit 8, and a temperature measuring device 11 is arranged on the discharging pipe L8.
When the device is used, mother liquor at the temperature of about 90 ℃ from plate heat exchange enters the conical separation tank 1 through the liquid inlet pipe L5, natural sedimentation starts from the upper part of the conical separation tank 1, floating impurities fall into the conical part at the lower part of the conical separation tank 1, in the sedimentation process, the mother liquor is subjected to preliminary temperature rise of the first heating tube bundle 4, the floating impurities are settled to the bottom, are discharged into the slag discharge pipe L7 through the bottom slag hole 14 after accumulating for a period of time, when slag is discharged, the slag discharge valve 17 is opened, the impurities settled at the bottom go to the decomposition unit 7 from the slag discharge pipe L7, and the mother liquor subjected to preliminary temperature rise and sedimentation separation impurities is connected with the mother liquor heating tank 2 through the first pipeline L1 from the upper liquid outlet 15; the mother liquor heating tank 2 is fully heated by the second heating tube bundle 5, the temperature of the mother liquor is raised, in order to ensure that the mother liquor is heated uniformly, the mother liquor heating tank 2 enters from the upper part, enters the lifting tube 12 after passing through the second heating tube bundle 5, the lifting tube 12 extracts the mother liquor from the lower part and overflows and is discharged from the upper part, then the raised mother liquor enters the discharging tank 3 through the fourth pipeline L4, the mother liquor is temporarily stored in the discharging tank 3 and then is discharged to the evaporation unit 8 through the discharging pipe L8, the temperature measuring device in the discharging pipe L8 carries out real-time temperature monitoring, the temperature of the mother liquor conveyed to the evaporation unit 8 is controlled to be about 95 ℃, after the monitoring data is fed back to the central control, the central control regulates the branch valve 16 on the heat supply branch tube L6, when the temperature is higher than 95 ℃, the branch valve 16 is closed, the mother liquor at low temperature is introduced, the temperature is reduced, the system scaling is avoided, when the temperature is lower than 95 ℃, the branch valve 16 is opened to raise the temperature of the mother liquor, the low-pressure steam of 0.6Mpa in the low-pressure pipeline 6 is introduced into the first heating tube bundle 4, the low-pressure steam is subjected to heat exchange tube bundle 9, the condensate enters the heat exchange water tank through the second heat exchange pipeline L2, and the condensate water tank 9, the condensate is fully condensed from the heat exchange water tank 9, and the condensate water is fully fed into the heat water after passing through the heat exchange tube 9.
The scope of the present utility model is not limited to the above embodiments, and various modifications and alterations of the present utility model will become apparent to those skilled in the art, and any modifications, improvements and equivalents within the spirit and principle of the present utility model are intended to be included in the scope of the present utility model.
Claims (6)
1. An evaporation stoste temperature rising system which is characterized in that: the device comprises a conical separation tank (1), wherein a liquid inlet pipe (L5) is connected to the upper part of the conical separation tank (1), a first heating tube bundle (4) is arranged on the upper part of the conical separation tank (1), a liquid inlet (13) of the first heating tube bundle (4) is connected with a low-pressure heating pipeline (6) through a heating branch pipe (L6), a slag outlet (L7) is arranged at the bottom slag outlet (14) of the conical separation tank (1), the slag outlet (L7) is connected with a decomposition unit (7), a mother liquor heating tank (2) is connected to an upper liquid outlet (15) of the conical separation tank (1) through a first pipeline (L1), a second heating tube bundle (5) is arranged in the mother liquor heating tank (2), the second heating tube bundle (5) is connected with the first heating tube bundle (4) through a second pipeline (L2), the second heating tube bundle (5) is connected with a condensing water tank (9) through a third pipeline (L3), and a liquid outlet (10) of the condensing water tank (9) is connected to the thermoelectric unit (10); the utility model discloses a temperature measuring device, including mother liquor heating tank (2), discharging groove (3), discharging pipe (L8), temperature measuring device (11) are installed on discharging pipe (L8), mother liquor heating tank (2) edge is equipped with carries material pipe (12) of deep tank bottom, carry material pipe (12) and connect discharging groove (3) through fourth pipeline (L4), the bottom of discharging groove (3) is equipped with discharging pipe (L8) of connecting evaporation unit (8).
2. The evaporation stock temperature raising system according to claim 1, wherein: the pipe orifice of the lifting pipe (12) is higher than the liquid level in the mother liquor heating tank (2).
3. The evaporation stock temperature raising system according to claim 1, wherein: and a branch pipe valve (16) is arranged on the heat supply branch pipe (L6), and the branch pipe valve (16) is controlled to be opened and closed according to feedback data of the temperature measuring device (11).
4. The evaporation stock temperature raising system according to claim 1, wherein: the first heating tube bundle (4) is an annular tube bundle encircling the upper part.
5. The evaporation stock temperature raising system according to claim 1, wherein: the second heating tube bundle (5) is in a symmetrical crotch shape or a cylindrical shape.
6. The evaporation stock temperature raising system according to claim 1, wherein: the slag discharging pipe (L7) is provided with a slag discharging valve (17), and the slag discharging valve (17) is normally closed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322486423.6U CN220877759U (en) | 2023-09-13 | 2023-09-13 | Evaporation stoste temperature-raising system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322486423.6U CN220877759U (en) | 2023-09-13 | 2023-09-13 | Evaporation stoste temperature-raising system |
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| Publication Number | Publication Date |
|---|---|
| CN220877759U true CN220877759U (en) | 2024-05-03 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202322486423.6U Active CN220877759U (en) | 2023-09-13 | 2023-09-13 | Evaporation stoste temperature-raising system |
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| Country | Link |
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| CN (1) | CN220877759U (en) |
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2023
- 2023-09-13 CN CN202322486423.6U patent/CN220877759U/en active Active
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