CN112125324A - New steam condensate water waste heat recovery device - Google Patents
New steam condensate water waste heat recovery device Download PDFInfo
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- CN112125324A CN112125324A CN202010810281.2A CN202010810281A CN112125324A CN 112125324 A CN112125324 A CN 112125324A CN 202010810281 A CN202010810281 A CN 202010810281A CN 112125324 A CN112125324 A CN 112125324A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 239000002918 waste heat Substances 0.000 title claims abstract description 17
- 238000011084 recovery Methods 0.000 title claims abstract description 16
- 230000029087 digestion Effects 0.000 claims abstract description 26
- 238000000034 method Methods 0.000 claims abstract description 19
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000004321 preservation Methods 0.000 claims abstract description 7
- 238000001704 evaporation Methods 0.000 claims description 18
- 230000008020 evaporation Effects 0.000 claims description 18
- 238000010438 heat treatment Methods 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 238000007865 diluting Methods 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 claims description 5
- 238000005406 washing Methods 0.000 claims description 5
- 238000004131 Bayer process Methods 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 3
- 238000004062 sedimentation Methods 0.000 claims 1
- 238000012423 maintenance Methods 0.000 abstract description 5
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 238000010790 dilution Methods 0.000 abstract description 2
- 239000012895 dilution Substances 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 238000004090 dissolution Methods 0.000 description 3
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
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Classifications
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- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Paper (AREA)
Abstract
The invention provides a new steam condensate waste heat recovery device, and mainly relates to the technical field of steam condensate waste heat recovery. The new steam condensate water waste heat recovery device comprises a digestion unit, wherein the digestion unit is an alumina low-temperature digestion unit, and the low-temperature digestion unit consists of a sleeve heat exchanger, a heat preservation tank, a flash tank, a dilution tank and a condensate water tank. The invention has the beneficial effects that: the new steam condensate water of the thermal power plant is recycled twice, the primary ore pulp can be preheated and heated in each cycle, the heat in the primary ore pulp is recovered, the temperature of the condensate water obtained by heat exchange is low, the temperature is generally 80-90 ℃, and the heat of the new steam can be fully utilized; the technical process is simple and easy to operate, does not need to invest new heat exchange equipment, can be well matched and connected with the dissolving-out unit, does not have extra manual maintenance workload, avoids cross-process linkage operation, avoids mutual interference among all processes, and realizes the self thermal cycle utilization of the dissolving-out unit.
Description
Technical Field
The invention mainly relates to the technical field of waste heat recovery of steam condensate water, in particular to a waste heat recovery device of fresh steam condensate water.
Background
In the existing Bayer process for producing alumina, the dissolution process is a core link. At present, in a dissolving-out process, a double-pipe heat exchanger is a mainstream heating technology, and flash evaporation exhaust steam preheating and new steam heating technologies are adopted in all alumina plants, so that the new steam consumption is reduced, and the alumina production cost is reduced. In the low-temperature (135-145 ℃) digestion process, the higher the utilization rate of the fresh steam in the heating section is, the lower the temperature of the condensed water after heat exchange is, the lower the digestion steam consumption is, and the lower the production cost of the alumina is. From the current situation of the alumina industry, the utilization rate of new steam is generally low, and the most intuitive performance is that the temperature of condensed water is higher, because the new steam condensed water is returned to a thermal power plant only by recycling once, still contains higher heat, and the heat with available value is not fully utilized.
In order to solve the above problems, the prior art discloses a method for dissolving new steam condensate and recycling the new steam condensate, such as chinese invention and invention patent with publication numbers CN105293544A and CN206069399U, respectively.
The above prior art solutions have the following drawbacks: the invention patent CN105293544A sends the dissolved new steam to an evaporation process for reuse, and a new steam condensate self-evaporator needs to be built, so that the technology has large investment and relates to cross-process operation; in order to recover the waste heat of the condensed water, the invention patent CN206069399U needs to pass through a plate type heat exchange device before being sent to a thermal power plant, and the technology also needs capital investment and manual maintenance.
Disclosure of Invention
In order to solve the defects of the prior art, the invention provides a new steam condensate waste heat recovery device, wherein the new steam condensate of a thermal power plant is recycled twice, the original ore pulp can be preheated and heated in each cycle to recover the heat in the original ore pulp, the temperature of the condensate obtained by heat exchange is lower, the temperature is generally 80-90 ℃, and the heat of the new steam can be fully utilized; the invention has simple flow and easy operation, does not need to invest new heat exchange equipment, can be well matched and connected with the dissolving-out unit, has no extra manual maintenance workload, simultaneously avoids cross-process linkage operation, avoids mutual interference among various processes and realizes the self heat recycling of the dissolving-out unit.
In order to achieve the purpose, the invention is realized by the following technical scheme:
a new steam condensate waste heat recovery device comprises a stripping unit, wherein the stripping unit is an alumina low-temperature stripping unit, the low-temperature stripping unit is composed of a sleeve heat exchanger, a heat preservation tank, a flash tank, a dilution rear tank and a condensate water tank, the stripping unit is heated by an eight-stage sleeve heat exchanger, the first to fifth stages are preheating stages, the sixth to eighth stages are heating stages, the first stage sleeve heat exchanger is preheated by new steam condensate preheated by the fifth stage sleeve heat exchanger, the second to fourth stage sleeve heat exchangers are preheated by flash evaporation exhaust steam, the fifth stage sleeve heat exchanger is preheated by new steam condensate of the sixth to eighth stage sleeve heat exchangers, the sixth to eighth stage sleeve heat exchangers are heated by new steam of a thermal power plant, each stage of the stripping unit sleeve heat exchanger is provided with a corresponding condensate water tank for receiving condensate water after heat exchange, the first-stage condensed water tank is connected with an outward-feeding pump and is conveyed to a thermal power plant by a pump, the water outlet of the second-fourth-stage condensed water tank is collected into a header pipe, the header pipe is connected with the outward-feeding pump and is conveyed to a red mud washing procedure by the pump, and the water outlet of the sixth-eighth-stage condensed water tank is collected into a header pipe and then is preheated by a fifth-stage double-pipe heat exchanger.
Furthermore, the digestion unit adopts a Bayer process low-temperature digestion production process, and the digestion temperature is 135-145 ℃.
Further, the dissolving-out unit preheats the raw ore pulp by a sleeve heat exchanger, the raw ore pulp is heated to the dissolving-out temperature of 135-145 ℃, then the dissolving-out reaction is carried out in a heat preservation tank, the dissolved-out ore pulp after the reaction is cooled and depressurized by a three-stage flash tank, then the discharged material enters a diluting tank, and flash evaporation exhaust steam is used for preheating the raw ore pulp.
Furthermore, the preheating section of the sleeve of the digestion unit is preheated by adopting flash evaporation exhaust steam and new steam condensate water medium, the flash evaporation exhaust steam is obtained by flash evaporation of the digestion ore pulp, and the new steam condensate water is obtained by condensing the new steam heating raw ore pulp.
Furthermore, the heating section of the sleeve of the dissolution unit is heated by a new steam medium supplied by a thermal power plant, the new steam pressure is 0.7-0.9 Mpa, and the temperature is 210-220 ℃.
Furthermore, the heating medium of the double-pipe heat exchanger enters a corresponding condensate water tank for collection after heat exchange, flash evaporation exhaust steam condensate water is collected and then sent to a settling process to be used as red mud washing water, and new steam condensate water is collected and then sent to a thermal power plant for reuse.
Compared with the prior art, the invention has the beneficial effects that:
according to the invention, the new steam condensate water of the thermal power plant is recycled twice, the raw ore pulp can be preheated and heated to recover the heat in the raw ore pulp in each cycle, the temperature of the condensate water obtained by heat exchange is low, generally 80-90 ℃, and the heat of the new steam can be fully utilized; the invention has simple flow and easy operation, does not need to invest new heat exchange equipment, can be well matched and connected with the dissolving-out unit, has no extra manual maintenance workload, simultaneously avoids cross-process linkage operation, avoids mutual interference among various processes and realizes the self heat recycling of the dissolving-out unit.
Drawings
FIG. 1 is a schematic structural view of the present invention;
Detailed Description
The invention is further described with reference to the accompanying drawings and specific embodiments. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. Further, it should be understood that various changes or modifications of the present invention may be made by those skilled in the art after reading the teaching of the present invention, and these equivalents also fall within the scope of the present application.
As shown in figure 1, the new steam condensate waste heat recovery device comprises a stripping unit, wherein the stripping unit is an alumina low-temperature stripping unit, the low-temperature stripping unit consists of a sleeve heat exchanger, a heat preservation tank, a flash tank, a diluted rear tank and a condensate water tank, the stripping unit is heated by eight stages of sleeve heat exchangers, wherein the first stage to the fifth stage are preheating stages, the sixth stage to the eighth stage are heating stages, the first stage sleeve heat exchanger is preheated by new steam condensate water preheated by the fifth stage sleeve heat exchanger, the second stage to the fourth stage sleeve heat exchangers are preheated by flash steam exhaust, the fifth stage sleeve heat exchanger is preheated by new steam condensate water by the sixth stage to the eighth stage sleeve heat exchangers, the sixth stage to the eighth stage sleeve heat exchangers are heated by new steam of a thermal power plant, and each stage of the sleeve heat exchangers of the stripping unit is provided with a corresponding condensate water tank, the first-stage condensed water tank is connected with an external pump and is pumped to a thermal power plant, the water outlet of the second-fourth-stage condensed water tank is collected into a header pipe, the header pipe is connected with the external pump and is pumped to the red mud washing procedure, the water outlet of the sixth-eighth-stage condensed water tank is collected into a header pipe, and then the header pipe is preheated by a fifth-stage double-pipe heat exchanger.
Specifically, the digestion unit adopts a Bayer process low-temperature digestion production process, and the digestion temperature is 135-145 ℃.
Specifically, the dissolving-out unit preheats raw ore pulp by a sleeve heat exchanger, the raw ore pulp is heated to the dissolving-out temperature of 135-145 ℃, then the dissolving-out reaction is carried out in a heat preservation tank, the dissolved-out ore pulp after the reaction is cooled and depressurized by a three-stage flash tank, then the discharged material enters a diluting tank, and flash evaporation exhaust steam is used for preheating the raw ore pulp.
Specifically, the preheating section of the sleeve of the digestion unit is preheated by adopting flash evaporation exhaust steam and new steam condensate water medium, the flash evaporation exhaust steam is obtained by flash evaporation of digestion ore pulp, and the new steam condensate water is obtained by condensing new steam heated raw ore pulp.
Specifically, the heating section of the sleeve of the dissolution unit is heated by a new steam medium supplied by a thermal power plant, the new steam pressure is 0.7-0.9 Mpa, and the temperature is 210-220 ℃.
Specifically, the heating medium of the double-pipe heat exchanger enters a corresponding condensate water tank for collection after heat exchange, flash evaporation exhaust steam condensate water is collected and then sent to a settling process to be used as red mud washing water, and new steam condensate water is collected and then sent to a thermal power plant for reuse.
Example (b):
when using this device, at first add the primary pulp to first order double-pipe heat exchanger in from the primary pulp import, the primary pulp is through the heat transfer after the heat transfer ejection of compact get into second level double-pipe heat exchanger that raises the temperature, through ejection of compact to the holding vessel after eighth level double-pipe heat exchanger raises the temperature in proper order, and the primary pulp dissolves out the reaction in the holding vessel, dissolves out the pulp and enters the flash tank cooling decompression after the reaction finishes, discharges to the back groove of diluting after tertiary flash distillation again.
According to the invention, the new steam condensate water of the thermal power plant is recycled twice, the raw ore pulp can be preheated and heated to recover the heat in the raw ore pulp in each cycle, the temperature of the condensate water obtained by heat exchange is low, generally 80-90 ℃, and the heat of the new steam can be fully utilized; the invention has simple flow and easy operation, does not need to invest new heat exchange equipment, can be well matched and connected with the dissolving-out unit, has no extra manual maintenance workload, simultaneously avoids cross-process linkage operation, avoids mutual interference among various processes and realizes the self heat recycling of the dissolving-out unit.
Finally, it should be noted that: the above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (6)
1. The utility model provides a new steam condensate water waste heat recovery device, includes dissolves out the unit, its characterized in that: the digestion unit is an alumina low-temperature digestion unit, the low-temperature digestion unit consists of a sleeve heat exchanger, a heat preservation tank, a flash tank, a diluting rear tank and a condensed water tank, the digestion unit is heated by an eight-stage sleeve heat exchanger, wherein the first to the fifth stages are preheating stages, the sixth to the eighth stages are heating stages, the first stage sleeve heat exchanger is preheated by new steam condensed water preheated by the fifth stage sleeve heat exchanger, the second to the fourth stage sleeve heat exchangers are preheated by flash exhausted steam, the fifth stage sleeve heat exchanger is preheated by new steam condensed water of the sixth to the eighth stage sleeve heat exchangers, the sixth to the eighth stage sleeve heat exchangers are heated by new steam of a thermal power plant, each stage of the sleeve heat exchanger of the digestion unit is provided with a corresponding condensed water tank for receiving the condensed water after heat exchange, and the first stage condensed water tank is connected with an outward-feeding pump, and the water from the sixth-eighth stage condensed water tanks is collected into a header pipe and then sent to a fifth-stage double-pipe heat exchanger for preheating.
2. The fresh steam condensate waste heat recovery device of claim 1, wherein: the digestion unit adopts a Bayer process low-temperature digestion production process, and the digestion temperature is 135-145 ℃.
3. The fresh steam condensate waste heat recovery device of claim 1, wherein: the dissolving-out unit preheats the raw ore pulp by adopting a sleeve heat exchanger, the raw ore pulp is heated to reach the dissolving-out temperature of 135-145 ℃, then the dissolving-out reaction is carried out in a heat preservation tank, the dissolved-out ore pulp after the reaction is cooled and depressurized by a three-stage flash tank, then the discharged material enters a diluting rear tank, and flash evaporation exhaust steam is used for preheating the raw ore pulp.
4. The fresh steam condensate waste heat recovery device of claim 1, wherein: the preheating section of the digestion unit sleeve is preheated by adopting flash evaporation exhaust steam and a new steam condensate water medium, the flash evaporation exhaust steam is obtained by flash evaporation of digestion ore pulp, and the new steam condensate water is obtained by condensing the new steam heated original ore pulp.
5. The fresh steam condensate waste heat recovery device of claim 1, wherein: the heating section of the dissolving-out unit sleeve is heated by a new steam medium supplied by a thermal power plant, the new steam pressure is 0.7-0.9 Mpa, and the temperature is 210-220 ℃.
6. The fresh steam condensate waste heat recovery device of claim 1, wherein: the heating medium of the double-pipe heat exchanger enters a corresponding condensate water tank for collection after heat exchange, flash evaporation exhaust steam condensate water is collected and then sent to a sedimentation process to be used as red mud washing water, and new steam condensate water is collected and then sent to a thermal power plant for reuse.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010810281.2A CN112125324A (en) | 2020-08-13 | 2020-08-13 | New steam condensate water waste heat recovery device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010810281.2A CN112125324A (en) | 2020-08-13 | 2020-08-13 | New steam condensate water waste heat recovery device |
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| CN112125324A true CN112125324A (en) | 2020-12-25 |
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| CN202010810281.2A Pending CN112125324A (en) | 2020-08-13 | 2020-08-13 | New steam condensate water waste heat recovery device |
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Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1994003396A1 (en) * | 1992-07-29 | 1994-02-17 | Alcan International Limited | Improved process and apparatus for digestion of bauxite |
| CN102249271A (en) * | 2011-05-27 | 2011-11-23 | 东北大学设计研究院（有限公司） | Tube array and remaining tank dissolving-out system and method for gibbsite bauxite |
| CN202099075U (en) * | 2011-05-27 | 2012-01-04 | 东北大学设计研究院（有限公司） | Tubulation and staying tank dissolving-out system of gibbsite bauxite |
| CN102515225A (en) * | 2011-12-22 | 2012-06-27 | 东北大学设计研究院（有限公司） | Double-sleeve preheating stirring-free retention insulation dissolution method for alumina |
| CN102531011A (en) * | 2011-12-22 | 2012-07-04 | 东北大学设计研究院（有限公司） | Aluminum oxide dissolving device capable of realizing both high-temperature and low-temperature dissolving ways and method thereof |
| CN102583461A (en) * | 2011-12-22 | 2012-07-18 | 东北大学设计研究院（有限公司） | Device and method for preheating by utilizing steam condensate water for aluminum oxide high-pressure digestion process |
| CN105293544A (en) * | 2014-06-27 | 2016-02-03 | 沈阳铝镁设计研究院有限公司 | Dissolution live steam condensate water evaporation secondary utilization method |
| CN105692665A (en) * | 2016-03-17 | 2016-06-22 | 东北大学设计研究院（有限公司） | Parallel row tube and remaining tank dissolving-out system and method for gibbsite bauxite |
| CN106276999A (en) * | 2016-08-24 | 2017-01-04 | 东北大学设计研究院（有限公司） | A kind of method recycling dissolution flash distillation exhaust steam in alumina producing |
| CN206069399U (en) * | 2016-08-29 | 2017-04-05 | 广西田东锦鑫化工有限公司 | Water reutilization system of dissolution |
| CN107497128A (en) * | 2017-09-30 | 2017-12-22 | 山东南山铝业股份有限公司 | The method for evaporating unit and solution evaporation |
| CN212450664U (en) * | 2020-08-13 | 2021-02-02 | 山东南山铝业股份有限公司 | New steam condensate water waste heat recovery device |
-
2020
- 2020-08-13 CN CN202010810281.2A patent/CN112125324A/en active Pending
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1994003396A1 (en) * | 1992-07-29 | 1994-02-17 | Alcan International Limited | Improved process and apparatus for digestion of bauxite |
| CN102249271A (en) * | 2011-05-27 | 2011-11-23 | 东北大学设计研究院（有限公司） | Tube array and remaining tank dissolving-out system and method for gibbsite bauxite |
| CN202099075U (en) * | 2011-05-27 | 2012-01-04 | 东北大学设计研究院（有限公司） | Tubulation and staying tank dissolving-out system of gibbsite bauxite |
| CN102515225A (en) * | 2011-12-22 | 2012-06-27 | 东北大学设计研究院（有限公司） | Double-sleeve preheating stirring-free retention insulation dissolution method for alumina |
| CN102531011A (en) * | 2011-12-22 | 2012-07-04 | 东北大学设计研究院（有限公司） | Aluminum oxide dissolving device capable of realizing both high-temperature and low-temperature dissolving ways and method thereof |
| CN102583461A (en) * | 2011-12-22 | 2012-07-18 | 东北大学设计研究院（有限公司） | Device and method for preheating by utilizing steam condensate water for aluminum oxide high-pressure digestion process |
| CN105293544A (en) * | 2014-06-27 | 2016-02-03 | 沈阳铝镁设计研究院有限公司 | Dissolution live steam condensate water evaporation secondary utilization method |
| CN105692665A (en) * | 2016-03-17 | 2016-06-22 | 东北大学设计研究院（有限公司） | Parallel row tube and remaining tank dissolving-out system and method for gibbsite bauxite |
| CN106276999A (en) * | 2016-08-24 | 2017-01-04 | 东北大学设计研究院（有限公司） | A kind of method recycling dissolution flash distillation exhaust steam in alumina producing |
| CN206069399U (en) * | 2016-08-29 | 2017-04-05 | 广西田东锦鑫化工有限公司 | Water reutilization system of dissolution |
| CN107497128A (en) * | 2017-09-30 | 2017-12-22 | 山东南山铝业股份有限公司 | The method for evaporating unit and solution evaporation |
| CN212450664U (en) * | 2020-08-13 | 2021-02-02 | 山东南山铝业股份有限公司 | New steam condensate water waste heat recovery device |
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