CN117383595A - High-temperature evaporation return water recycling system for alumina production - Google Patents
High-temperature evaporation return water recycling system for alumina production Download PDFInfo
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- CN117383595A CN117383595A CN202311355206.1A CN202311355206A CN117383595A CN 117383595 A CN117383595 A CN 117383595A CN 202311355206 A CN202311355206 A CN 202311355206A CN 117383595 A CN117383595 A CN 117383595A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 195
- 238000004064 recycling Methods 0.000 title claims abstract description 21
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title claims abstract description 19
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 17
- 238000001704 evaporation Methods 0.000 title claims description 17
- 230000008020 evaporation Effects 0.000 title claims description 17
- 238000011084 recovery Methods 0.000 claims abstract description 13
- 238000011033 desalting Methods 0.000 claims description 53
- 239000011347 resin Substances 0.000 claims description 30
- 229920005989 resin Polymers 0.000 claims description 30
- 230000008929 regeneration Effects 0.000 claims description 5
- 238000011069 regeneration method Methods 0.000 claims description 5
- 230000001502 supplementing effect Effects 0.000 claims description 5
- 238000002955 isolation Methods 0.000 claims description 4
- 238000007789 sealing Methods 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 abstract description 12
- 238000000034 method Methods 0.000 abstract description 10
- 230000000694 effects Effects 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 238000004134 energy conservation Methods 0.000 abstract 1
- 239000007788 liquid Substances 0.000 description 10
- 150000001450 anions Chemical class 0.000 description 7
- 150000001768 cations Chemical class 0.000 description 6
- 238000010612 desalination reaction Methods 0.000 description 5
- 150000002500 ions Chemical class 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- 239000003513 alkali Substances 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- -1 hydrogen ions Chemical class 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000005342 ion exchange Methods 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 125000000129 anionic group Chemical group 0.000 description 2
- 125000002091 cationic group Chemical group 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 229910001570 bauxite Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003729 cation exchange resin Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 229910001388 sodium aluminate Inorganic materials 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000002344 surface layer Substances 0.000 description 1
- 239000012498 ultrapure water Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
- C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
- C01F7/0666—Process control or regulation
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Automation & Control Theory (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The invention relates to the technical field of evaporative water recycling systems, in particular to a high-temperature evaporative water recycling system for alumina production, which separates high-temperature condensed water from low-temperature condensed water, wherein the low-temperature condensed water is used for a low-temperature station, the high-temperature condensed water is conveyed to a deaerator and is used for carrying out auxiliary heating on the deaeration process of the deaerator, so that the deaeration water reaches a saturation temperature, the deaeration effect is maximized, heat of the condensed water is utilized to exchange heat with the deaerator, the heating power and energy of a heating calandria in the deaerator are reduced, the energy consumption of external heating is saved, the high-temperature condensed water is gradually cooled to meet the requirement of the high-pressure boiler on water recovery, the condensed water is recovered, and is used for all areas, so that the omnibearing recovery and utilization of the condensed water are realized, and the green energy conservation is realized.
Description
Technical Field
The invention relates to the technical field of evaporated water recovery systems, in particular to a high-temperature evaporated water recycling system for alumina production.
Background
Alumina is a white amorphous powdery inorganic substance, and is usually used as an analytical reagent, an adsorbent and the like, and is mainly extracted from equipment such as bauxite and the like, and the production processes such as raw material (raw ore pulp is prepared), dissolution (alumina components in the raw ore pulp are dissolved into sodium aluminate solution), sedimentation (coarse liquid in the slurry and red mud formed by adhering alkali and various impurities are separated), decomposition (the separated coarse liquid is filtered by a leaf filter to obtain refined liquid), mixing the refined liquid with seed crystal, gradually entering into decomposition tanks to cool and stir so as to fully separate aluminum hydroxide), roasting (the filtered coarse material is roasted at high temperature to finally obtain finished alumina) and the like are required, and in order to fully utilize mother liquid, an evaporation process workshop is further arranged for concentrating the circulating mother liquid so as to remove excessive moisture entering into the mother liquid in the process and achieve the mother liquid concentration required by the process.
However, a large amount of high-temperature condensed water is generated in the evaporation process, and the high-temperature condensed water is mixed with the acid-base components and is rich in oxygen, the components oxidize and corrode the high-pressure boiler, the quality standard (GB/T12145-2016) of the water supplement of the high-pressure boiler is not met, the mixed bed is required to be utilized to remove adverse components contained in the condensed water, but the temperature of the condensed water is up to 75 ℃ after preliminary recovery, and the water inlet temperature of the mixed bed is required to be regulated and controlled to be lower than 45 ℃, so that the condensed water needs to be cooled before being injected into the mixed bed, and the heat dissipation of the condensed water can not be fully utilized when the condensed water is cooled, so that heat loss is caused.
Therefore, the invention provides a high-temperature evaporation recycling system for alumina production, which improves the heat utilization rate of the condensation recycling water.
Disclosure of Invention
The invention aims to solve the problems in the prior art and provides a recycling system for high-temperature evaporation water in alumina production.
In order to achieve the above purpose, the present invention adopts the following technical scheme:
the high-temperature evaporation return water recycling system for alumina production is characterized by comprising five groups of exchangers which are connected in parallel, wherein the exchangers are connected in parallel with a high-temperature desalting water tank and a normal-temperature desalting water tank, the high-temperature desalting water tank and the normal-temperature desalting water tank are connected in parallel with a main pipe, a gate valve is arranged on the main pipe, a low-temperature desalting water pump and a high-temperature desalting water pump are respectively connected to two sides of the gate valve on the main pipe, the low-temperature desalting water pump is connected with a low-temperature water tank, the high-temperature desalting water pump is connected with a deaerator, and the deaerator is connected with a return water tank;
the side wall of the main pipe is communicated with a recovery pipe through an isolation valve, and the recovery pipe is communicated with a regeneration system.
Preferably, each group of exchangers comprises a primary mixed bed and a secondary mixed bed which are connected in series, and the water outlet end of the secondary mixed bed is respectively communicated with the high-temperature desalting water tank and the normal-temperature desalting water tank in parallel.
Preferably, the low-temperature desalted water in the low-temperature water tank is used for supplementing water for the condenser and sealing water for the high-pressure water supply pump.
Preferably, the water outlet of the secondary mixed bed is communicated with a high-temperature demineralized water tank through a DN250 pipeline.
Preferably, the low temperature desalination water pump and the high temperature desalination water pump are all provided with a plurality of groups, the water inlets of all the low temperature desalination water pumps are jointly communicated with a low temperature water inlet main pipe, and the water inlets of all the high temperature desalination water pumps are jointly communicated with a high Wen Jinshui main pipe.
Preferably, the outlet of the high-temperature desalting water tank is communicated with the high Wen Jinshui main pipe through a DN300 pipeline.
Preferably, all the primary mixed beds and the secondary mixed beds contain a positive resin and a negative resin, and the negative resin and the positive resin are high-temperature resistant resins.
Compared with the prior art, the invention provides a high-temperature evaporation return water recycling system for alumina production, which has the following beneficial effects.
1. The invention separates the high-temperature condensed water from the low-temperature condensed water, the low-temperature condensed water is used for low-temperature stations (the condenser is used for supplementing water and the high-pressure water supply pump is used for sealing water), the high-temperature condensed water is conveyed to the deaerator and is used for carrying out auxiliary heating on the deaeration process of the deaerator, the deaeration water is promoted to reach the saturation temperature, the deaeration effect is maximized, the heat of the condensed water is utilized for exchanging heat with the deaerator, the heating power and the energy of a heating calandria in the deaerator are reduced originally, the energy consumption of external heating is saved, the high-temperature condensed water is gradually cooled, the requirement of the high-pressure boiler for recovering the supplementing water is met, the high-temperature condensed water is recovered and utilized after the heat exchange, the high-temperature condensed water and the low-temperature condensed water can be applied to all areas, the omnibearing recovery and utilization of the condensed water are realized, the energy consumption and the water consumption are saved, and the environment is realized.
2. The invention utilizes an ion exchange method, improves water cyclic utilization, reduces heat loss, reduces coal consumption, and realizes green, clean and energy saving.
3. The anion-cation exchange resin in the mixed bed is made of high-temperature resistant resin, so that the heat resistance degree of the mixed bed is improved, condensed water does not need to be cooled before being input into the mixed bed, the process flow is reduced, and the operation steps are simplified.
Additional advantages, objects, and features of the invention will be set forth in part in the description which follows; and will be apparent to those skilled in the art in part based upon a review of the following; alternatively, the teachings may be directed to practice of the present invention.
Drawings
Fig. 1 is a schematic diagram of a basic condensate recovery system according to embodiment 1 of the present invention.
Fig. 2 is a schematic diagram of an improved condensate recovery system of embodiment 2 of the present invention.
Fig. 3 is a schematic diagram of a combined condensate recovery system according to embodiment 3 of the present invention.
In the figure: 1. a first-stage mixed bed; 2. a second-stage mixed bed; 3. a high temperature desalination tank; 4. normal temperature desalting water tank; 5. a first parent pipe; 6. a second gate valve; 7. low temperature desalting water pump; 8. high-temperature desalting water pump; 9. a deaerator; 10. a low temperature water tank; 11. DN250 line; 12. DN300 pipeline.
Detailed Description
The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to fig. 1 to 3 of the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, but not all embodiments.
In order to improve the heat utilization rate of high-temperature condensed water, the embodiment provides a high-temperature evaporation water recycling system for alumina production, which comprises five groups of exchangers connected in parallel, wherein each group of exchangers comprises a primary mixed bed 1 and a secondary mixed bed 2 (the mixed beds are short for mixed ion exchangers) which are connected in series, and water inlet and outlet of the primary mixed bed 1 and the secondary mixed bed 2 of a first group are isolated to form a single set of system;
referring to fig. 1, the water outlet end of the second-stage mixed bed 2 is respectively communicated with a high-temperature desalting water tank 3 and a normal-temperature desalting water tank 4 through water supply pipes, the inlets and outlets of the high-temperature desalting water tank 3 and the normal-temperature desalting water tank 4 are respectively provided with a first gate valve, the high-temperature desalting water tank 3 is communicated with the normal-temperature desalting water tank 4 in parallel with a first main pipe 5, the first main pipe 5 is provided with a second gate valve 6, the two sides of the gate valve on the first main pipe 5 are respectively communicated with a low-temperature desalting water pump 7 and a high-temperature desalting water pump 8, the low-temperature desalting water pump 7 and the high-temperature desalting water pump 8 are jointly communicated with a second main pipe, an isolation valve is arranged between the low-temperature desalting water pump 7 and the high-temperature desalting water pump 8 on the second main pipe, and the end part of the communication part of the low-temperature desalting water pump 7 on the second main pipe is communicated with a deaerator 9.
In this embodiment, all the primary mixed beds 1 and the secondary mixed beds 2 contain renewable cationic resin and anionic resin, and after the anions and cations of salts contained in the condensed water pass through the mixed beds, the condensed water is exchanged by the resin to obtain high-purity water, and when the condensed water is initially recovered, the recovery temperature is about 75 ℃, and according to the specification, the water inlet temperature of the mixed beds can only be controlled at 40 ℃, so that the anionic resin and the cationic resin both adopt high-temperature resistant resins, and the heat resistance degree of the mixed beds is improved.
In the embodiment, a water return tank is arranged for gathering all high-temperature condensed water, and the water return tank is communicated with the primary mixed bed 1 through a water return pump.
In this embodiment, the low-temperature desalting water pump 7 and the high-temperature desalting water pump 8 are provided with a plurality of groups for improving the pipeline conveying efficiency.
The specific use process of the embodiment comprises the following steps:
starting a water return pump, pumping high-temperature condensed water in a water return tank into the first-stage mixed bed 1, carrying out ion exchange on the high-temperature condensed water to remove unfavorable components contained in the high-temperature condensed water, and injecting the condensed water filtered from the first-stage mixed bed 1 into the second-stage mixed bed 2 again for secondary filtration to improve the purification effect of the condensed water;
if the purified condensate water is lower than normal temperature (less than 30 ℃), a first gate valve of a water inlet of the normal temperature desalting water tank 4 is opened, low-temperature condensate water is injected into the normal temperature desalting water tank 4, impurities and salt in the water are removed by using a specific chemical reagent, the purifying effect of the condensate water is improved again, so that the treated condensate water can meet the qualified requirements, after desalting, the first gate valve of an outlet of the normal temperature desalting water tank 4 is opened, a low-temperature desalting water pump 7 is started, the treated condensate water is injected into the low-temperature water tank 10, and low-temperature desalting water in the low-temperature water tank 10 is used for low-temperature stations such as condenser water supplementing and sealing water of a high-pressure water feeding pump;
if the purified condensed water exceeds normal temperature, a first gate valve of a water inlet of the high-temperature desalting water tank 3 is opened, the high-temperature condensed water is injected into the high-temperature desalting water tank 3 for impurity removal and salt removal treatment, then the first gate valve of an outlet of the high-temperature desalting water tank 3 is opened, the high-temperature desalting water pump 8 is started, the treated high-temperature condensed water is sent to the deaerator 9 and is used for carrying out auxiliary heating on the deaeration process of the deaerator 9, the deaeration water is promoted to reach saturation temperature, the deaeration effect is maximized, heat of the condensed water is utilized for exchanging heat with the deaerator 9, the heating power and energy of an original heating calandria in the deaerator 9 are reduced, the energy consumption of external heating is saved, such as coal consumption is reduced when a boiler is heated, the electric consumption is reduced when the boiler is heated, according to estimation, 50t evaporation backwater is used for calculation every hour, the original use temperature is increased by 31 ℃, the annual income is 50×24×30×12×1000× 4.2/29270 =1921 ton standard coal, and the high-temperature condensed water is gradually cooled, so that the requirement of the high-pressure boiler is met, and the environment-friendly energy saving is realized.
In embodiment 2, the pipeline is optimized based on embodiment 1, as shown in fig. 2, DN250 pipelines are opened on the side wall of the water supply pipe, a third gate valve is arranged between the DN250 pipelines and the conveying pipe, the water supply pipe is only communicated with the normal-temperature desalting water tank 4, the first main pipe 5 is divided into a low-temperature water inlet main pipe and a high Wen Jinshui main pipe at the second gate valve 6, the water inlets of all low-temperature desalting water pumps 7 are jointly communicated with the low-temperature water inlet main pipe, the water inlets of all high-temperature desalting water pumps 8 are jointly communicated with the high-Wen Jinshui main pipe, the high-Wen Jinshui main pipe is communicated with the high-temperature desalting water tank 3 through the DN300 pipelines, and the second main pipe is respectively communicated with the low-temperature water tank 10 and the deaerator 9 at the second gate valve 6, so that the low-temperature condensed water and the high-temperature condensed water are completely separated, the high-temperature condensed water is exclusively used by the deaerator 9, heat is directly utilized, the original low-temperature condensed water is still used by the low-temperature stations, the two pipelines are separated, the pipelines with different materials for conveying different temperatures, the pipelines with different prices, the conveying pipelines with different prices, the high-temperature pipelines are also different, the pipelines are simultaneously separated by the high-temperature pipelines, the pipelines are more convenient to separate the pipelines, the pipeline has high cost and the pipeline has better compression performance, and high cost.
In example 3, the basic pipeline of example 1 is still reserved in example 2, so that the two pipelines can be used in emergency when any pipeline has a problem.
In the embodiment 4, in order to further improve the recycling rate of the condensed water, in the embodiment, the side wall of the first main pipe 5 is communicated with a recycling pipe through an isolation valve, the recycling pipe is communicated with a mixed bed regeneration system, after the mixed bed is used for a certain time, the ion adsorption in the anion and cation resin in the mixed bed is saturated, and the ion exchange with the ion in the condensed water can not be continued, so that the purification effect of the mixed bed is greatly reduced, in order to restore the mixed bed, acid and alkali solution are required to be alternately injected into the mixed bed, and hydrogen ions and hydroxyl ions in the acid and alkali solution are respectively exchanged with the anion and cation ions adsorbed on the anion and cation resin, so that the saturated state of the anion and cation resin is consumed, and the anion and cation resin of the mixed bed is restored to the original state, so that the mixed bed function is restored;
regeneration step of yin-yang resin of mixed bed:
1. backwash layering: the female and male resins were delaminated by repeated washing.
2. Closing a mixed bed backwashing water inlet door, and checking whether the mixed bed resin is completely layered;
3. and (3) water discharge: after the positive and negative resins are completely layered, the positive washing drainage door is opened, water in the mixed bed is discharged, and the water is placed at a position about 10cm away from the surface of the resin surface layer.
4. Feeding a regeneration liquid: placing the regenerated liquid to promote cation and anion replacement of the mixed bed resin;
5. replacement: the ion saturation state of the mixed resin is eased by displacement;
6. mixing of yin and yang resins: and (5) remixing the replaced ions to produce the regenerated resin.
7. Forward washing: the water can be used for standby or put into operation after washing until the water is qualified.
In the embodiment, the middle row main pipe flange of the middle row device in the mixed bed is moved to the outer side of the tank body of the mixed bed, so that the assembly and the replacement are convenient.
The present invention is not limited to the above-mentioned embodiments, and any person skilled in the art, based on the technical solution of the present invention and the inventive concept thereof, can be replaced or changed within the scope of the present invention.
In the description of the present specification, a description referring to terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.
While embodiments of the present invention have been shown and described above, it will be understood that the above embodiments are illustrative and not to be construed as limiting the invention, and that variations, modifications, alternatives and variations may be made to the above embodiments by one of ordinary skill in the art within the scope of the invention.
Claims (7)
1. The utility model provides an alumina production high temperature evaporation return water recycling system which is characterized in that the system comprises five groups of exchangers which are connected in parallel, wherein the exchangers are connected in parallel and are provided with a high temperature desalting water tank (3) and a normal temperature desalting water tank (4), the high temperature desalting water tank (3) is connected in parallel and is provided with a main pipe with the normal temperature desalting water tank (4), a gate valve is arranged on the main pipe, two sides of the gate valve on the main pipe are respectively connected with a low temperature desalting water pump (7) and a high temperature desalting water pump (8), the low temperature desalting water pump (7) is connected with a low temperature water tank (10), the high temperature desalting water pump (8) is connected with a deaerator (9), and the deaerator (9) is connected with a return water tank;
the side wall of the main pipe is communicated with a recovery pipe through an isolation valve, and the recovery pipe is communicated with a regeneration system.
2. The recycling system for high-temperature evaporation for alumina production according to claim 1, wherein each group of exchangers comprises a primary mixed bed (1) and a secondary mixed bed (2) which are connected in series, and the water outlet end of the secondary mixed bed (2) is respectively communicated with a high-temperature desalting water tank (3) and a normal-temperature desalting water tank (4) in parallel.
3. The alumina production high-temperature evaporation return water recycling system according to claim 1, wherein low-temperature desalted water in the low-temperature water tank (10) is used for water supplementing of a condenser and sealing of a high-pressure water feeding pump.
4. The recycling system for high-temperature evaporation of alumina production according to claim 2, wherein the water outlet of the secondary mixed bed (2) is communicated with the high-temperature demineralized water tank (3) through a DN250 pipeline (11).
5. The recycling system for high-temperature evaporation of alumina production according to claim 2, wherein the low-temperature demineralized water pumps (7) and the high-temperature demineralized water pumps (8) are all provided with a plurality of groups, the water inlets of all the low-temperature demineralized water pumps (7) are commonly communicated with a low-temperature water inlet main pipe, and the water inlets of all the high-temperature demineralized water pumps (8) are commonly communicated with a high Wen Jinshui main pipe.
6. The recycling system for high-temperature evaporation for alumina production according to claim 5, wherein the outlet of the high-temperature demineralized water tank (3) is communicated with a Gao Wenjin water main through a DN300 pipeline (12).
7. The recycling system for high-temperature evaporation for alumina production according to claim 5, wherein all the primary mixed beds (1) and the secondary mixed beds (2) comprise a positive resin and a negative resin, and the negative resin and the positive resin are high-temperature resistant resins.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311355206.1A CN117383595A (en) | 2023-10-19 | 2023-10-19 | High-temperature evaporation return water recycling system for alumina production |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202311355206.1A CN117383595A (en) | 2023-10-19 | 2023-10-19 | High-temperature evaporation return water recycling system for alumina production |
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| CN117383595A true CN117383595A (en) | 2024-01-12 |
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| CN202311355206.1A Pending CN117383595A (en) | 2023-10-19 | 2023-10-19 | High-temperature evaporation return water recycling system for alumina production |
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