CN1155521C - Directly heating and decomposing plate heat exchanging technology for alumina laterite washing - Google Patents
Directly heating and decomposing plate heat exchanging technology for alumina laterite washing Download PDFInfo
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- CN1155521C CN1155521C CNB001159291A CN00115929A CN1155521C CN 1155521 C CN1155521 C CN 1155521C CN B001159291 A CNB001159291 A CN B001159291A CN 00115929 A CN00115929 A CN 00115929A CN 1155521 C CN1155521 C CN 1155521C
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- 238000005406 washing Methods 0.000 title claims abstract description 57
- 238000010438 heat treatment Methods 0.000 title claims abstract description 27
- 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 12
- 238000005516 engineering process Methods 0.000 title claims abstract description 10
- 229910001710 laterite Inorganic materials 0.000 title claims description 11
- 239000011504 laterite Substances 0.000 title claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 53
- 238000000034 method Methods 0.000 claims abstract description 35
- 230000008569 process Effects 0.000 claims abstract description 20
- 238000001704 evaporation Methods 0.000 claims abstract description 17
- 230000008020 evaporation Effects 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 15
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 13
- 210000000582 semen Anatomy 0.000 claims description 21
- 230000000694 effects Effects 0.000 abstract description 10
- 230000008901 benefit Effects 0.000 abstract description 9
- 238000004062 sedimentation Methods 0.000 abstract description 9
- 238000004090 dissolution Methods 0.000 abstract 2
- 238000004140 cleaning Methods 0.000 description 12
- 238000001816 cooling Methods 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 8
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 8
- 239000003513 alkali Substances 0.000 description 7
- 239000012452 mother liquor Substances 0.000 description 7
- 230000008676 import Effects 0.000 description 6
- 238000004131 Bayer process Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000007701 flash-distillation Methods 0.000 description 4
- 230000008016 vaporization Effects 0.000 description 4
- 206010039509 Scab Diseases 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 229910021502 aluminium hydroxide Inorganic materials 0.000 description 2
- 229910001570 bauxite Inorganic materials 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 230000009191 jumping Effects 0.000 description 2
- 239000006210 lotion Substances 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 206010033799 Paralysis Diseases 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 229910001648 diaspore Inorganic materials 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 238000003780 insertion Methods 0.000 description 1
- 230000037431 insertion Effects 0.000 description 1
- 229910000765 intermetallic Inorganic materials 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000005432 seston Substances 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 239000008234 soft water Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 230000005619 thermoelectricity Effects 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
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- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention provides a direct heating and decomposing plate type heat exchanging technology for washing alumina red mud. The dissolution of secondary steam of new steam condensate is used for heating a red mud washing system and used as a heat source of evaporation, the method of the direct introduction of secondary steam into a washing and settling tank is used for heating a red mud sedimentation and washing system, and the technical scheme of the complete heat exchange among fine liquid, decomposition mother liquid and water is used. The implementation of the present invention fully utilizes the dissolution secondary steam of alumina, and the present invention has the advantages of energy resource saving, simplified technical process, improved operating condition and optimized technical index. The temperature of evaporation raw liquid is increased from 80 DEG C to 92 DEG C so that the highest international level at present is reached, and obvious effect of energy saving is offered.
Description
Technical field:
The present invention relates to a kind ofly from ore or concentrate, extract metallic compound with wet method, especially in inorganic alkali solution, alumina laterite washing direct heating and decomposing plate heat exchanging technology.
Background technology:
Alumina producing mainly contains two kinds of methods: Bayer process and sintering process.Wherein Bayer process is a main raw material with bauxite, caustic soda and lime, and bauxite is ground into qualified raw pulp with mother liquor through the raw material mill and sends into stripping, and under the effect of High Temperature High Pressure and high-alkalinity, the aluminum oxide in the ore enters solution, and its insolubles is a red mud.After dissolved mineral slurry separated, red mud effluxed behind washing, the attached alkali of filtered and recycled; Get seminal fluid behind the solution purification.Seminal fluid adds crystal seed and divides and parse aluminium hydroxide after lowering the temperature, aluminium hydroxide promptly gets aluminum oxide through roasting.Decomposition nut liquid returns feed circuit and recycles after evaporation concentration.
Stripping live steam condensed water secondary vapour utilizes present situation:
With the diaspore is that stripping is carried out under high temperature, high pressure and high-alkalinity in the Bayer process aluminum oxide production process of raw material, and pressure 60 * 10 is generally adopted in the indirect heating stripping
5Pa, temperature is the live steam heating stripping about 300 ℃.Live steam condensed water after the heating contains a large amount of waste heats, generally adopts its flash distillation at present, obtains 6 * 10
5Secondary vapour about pa, the way that is used then.Specifically have following several:
Incorporate the low-pressure steam pipe network into: this method is to incorporate the secondary steam that produces after the flash distillation of stripping live steam condensed water into the low-pressure steam pipe network, is sent to each then and uses the vapour point.This method is adopted in the our factory design just.Its advantage is to utilize this part secondary vapour more fully; Shortcoming is that the pressure surge of low-pressure steam pipe network impacts stripping live steam condensed water flash system, makes production hard to carry on.Alumina producer was gone into operation the initial stage in 95 years, after stripping live steam condensed water secondary vapour is incorporated full factory low-pressure steam pipe network into, just because the low-pressure steam pressure surge causes the live steam condensed water flash tank pressure higher, twice jumping of digestion series stops, simultaneously, condensed water flash jar serious vibration, the neat root drawing crack of wherein defective water flash tank vapor pipe, wall screw is shaken disconnected, makes a big impact to alumina producing.
Be directly used in pre-desiliconization or other uses the vapour point: the secondary steam that produces after the flash distillation of stripping live steam condensed water is directly used in a certain vapour point of using, as desiliconization.The advantage of this method is to have avoided secondary vapour to incorporate into behind the pipe network because the disadvantageous effect that pressure surge brings; Shortcoming is to necessarily require the secondary steam amount of live steam condensed water generation with in a basic balance with the required quantity of steam of vapour point, when stripping live steam condensed water secondary vapour is greater than or less than with the required quantity of steam of vapour point else if, will consider that second is replenished steam with vapour point or from other places, and can bring so again and incorporate the same problem of low-pressure steam pipe network into.
Also there is an identical shortcoming in above-mentioned two kinds of methods, are exactly when stripping autoclave heating tube bundle is damaged, and secondary steam is because the band material can only emptying, and both contaminate environment caused the waste of the energy again.
Red-mud settlement separating, washing system heating present situation:
In the settlement separate washing process of Bayer process red mud, because online liquid measure is big, the residence time is long, temperature reduces gradually, and solution is easy to take place hydrolysis and generates aluminum hydroxide precipitation, the low washing effect that also influences of simultaneous temperature, in order to reduce the alumina loss that causes because of hydrolysis as much as possible, reduce the attached alkali of red mud, generally will heat, particularly in the winter time, the wash water temperature is lower or stop under the situations such as the material time is long the red-mud settlement separation system.The heating of alumina producer sedimentation washing system has following several method both at home and abroad at present:
Heating red mud wash water: lower or when directly making wash water with industrial water, washing will feed live steam before or secondary steam heats the red mud wash water in red mud wash water temperature.This method has certain effect to keeping the subsider temperature, but because heating efficiency is limited, and the subsider temperature loss is big, and the last washing often has only about 70 ℃, so the aluminum oxide hydrolysising loss is big, laterite washing and poor filtration effect efflux the attached alkali height of red mud.
Subsider directly feeds live steam: when the red mud wash water can not satisfy red mud separating, washing to the requiring of temperature, can adopt the way that directly feeds live steam in the subsider.Its advantage is: can improve the temperature of laterite washing, improve washing and filter effect; Shortcoming is to use thermal source one time, increases boiler load.Therefore directly feed the general of live steam, only stop just use under the situations such as material or winter temperature are low for a long time at subsider only as a kind of boosting means.
Plate-type heat exchanger heating washing lotion: lateral flow causticization or subsider causticization are higher to the secondary cleaning water temperature requirement, generally more than 95 ℃.And the seminal fluid temperature is 100～105 ℃, needs cooling before the decomposition.Adopt plate-type heat exchanger, make seminal fluid and secondary cleaning water carry out heat exchange, the secondary cleaning water temperature can be brought up to 95 ℃ by about 80 ℃, satisfy the requirement of lateral flow causticization or subsider causticization.Its advantage is the heat that has utilized seminal fluid preferably; Shortcoming is object height because secondary cleaning water swims, and plate-type heat exchanger scabs seriously, and the cleaning difficulty is big, facility investment and working cost height.
Seminal fluid cooling present situation:
The temperature general requirement that bayer process seed decomposes is about 60 ℃, and the seminal fluid temperature after the smart filter is 100～105 ℃, so will lower the temperature to seminal fluid before decomposing.It is several that cool-down method mainly contains plate-type heat exchanger cooling, vacuum cool-down, spray water cooling etc., adopts simultaneously sometimes, specifically decides on the technological process of production.What our factory design was adopted is the board-like cooling flow process of level Four, and wherein the I level is board-like with the cooling of red mud secondary cleaning water, and II, III level are board-like with decomposition nut liquid cooling, the board-like cooling water temperature of using of last step.The heat utilization efficiency of this cooling flow process seminal fluid is higher, and board-like temperature out can be regulated, and can satisfy the requirement of decomposition technique.Shortcoming is that the board-like secondary cleaning water side of I level scabs seriously, and the mother liquor temperature is not very high in addition.
Summary of the invention:
Purpose of the present invention mainly is to solve because stripping autoclave heating tube bundle leaks to cause live steam condensed water secondary vapour band material and this part steam to incorporate full factory 6 * 10 into
5Condensed water flash jar serious vibration, a jar internal pressure fluctuation cause the jumping of stripping unit to stop greatly during the pa steam pipe system, make intrinsic stripping live steam condensed water secondary steam incorporate full factory 6 * 10 into
5The problem that the scheme of pa steam pipe system can't realize.Seek a kind of alumina red-mud settlement washing direct heating and decomposing plate heat exchanging novel process simultaneously, this method had both been simplified technical process, had rationally utilized stripping live steam water coolant secondary steam again, and made temperature of vaporizing raw liquor bring up to 92 ℃ by 80 ℃.
The technical scheme that the present invention takes is: stripping live steam condensed water secondary steam is used to heat the laterite washing system and is used as the evaporation thermal source; The employing of red-mud settlement washing system type of heating is heated the red-mud settlement washing system to the method that washing settling groove directly feeds secondary steam; Board-like heat exchange process flow process adopt seminal fluid all with decomposition nut liquid and water heat exchange.
Positively effect of the present invention and benefit:
Coming into effect live steam condensed water secondary steam heating red-mud settlement washing and board-like system flow in January, 1996 improves, at first send the sedimentation rinse bath with stripping secondary vapour, it is board-like to have cancelled decomposition I level, and the red mud secondary cleaning water directly advances to wash subsider, and the back of coming into operation is respond well.Again secondary vapour is introduced evaporization process later on, make the utilization of stripping secondary vapour more reasonable, through updating, it is perfect that the present invention more becomes.Operation obtained remarkable economic efficiency and social benefit 4 years more.
---make full use of stripping water of condensation secondary vapour, saved the energy, reduced environmental noise, prevented the alkali steam contamination;
---the stripping secondary steam send laterite washing and vapo(u)rization system, has solved vibration of live steam condensed water flash tank and pressure surge problem, has guaranteed the reliability service of digestion series, has improved the unit operation factor;
---stripping secondary vapour heating sedimentation washing system, improved the sedimenting system process conditions.Because wash temperature improves, the washing lotion seston takes a turn for the better, and the red mud filter production capacity increases, and abandons the attached alkali of red mud and reduces, and the loss of aluminum oxide in the sedimentation washing process greatly reduces, and the aluminum oxide total yield is improved;
---increased the reliability of washing system.Add in the rinse bath as can directly going up water, also can not run muddy with production.In July, 1997 is because littoral landslide, the Youjiang River, the river silt content is big, power plant's water treatment capacity reduces greatly, cause heat power plant's soft water treatment system almost to be paralysed, the stripping water of condensation all send thermoelectricity, sedimentation does not have washing and uses hot water, have to introduce a large amount of muddy waters from hydrant and directly add to the washing settling groove, has still guaranteed the normal operation of producing;
---secondary cleaning water do not walk board-like after, the I plate-type heat exchanger changes seminal fluid into and all carries out heat exchange with mother liquor, has both simplified flow process, has improved the decomposition nut liquid preheating temperature again;
---because secondary cleaning water do not carry out heat exchange with seminal fluid, board-like can the cancellation of I level and what is board-like standby as other avoided the board-like white residue of this level problem that scabs simultaneously, prolonged the board-like soak cleaning cycle, the longer service life of plate-type heat exchanger;
---decomposition nut liquid (vaporizing raw liquor) temperature had both alleviated evaporation load after improving, and had saved a large amount of energy again;
---stripping secondary vapour advances evaporation, the evaporation steam consumption is reduced greatly, and owing to force to imitate the independent vapour source of using, the evaporation operation is more stable.
Technico-economical comparison before and after improving is as shown in table 1.
The economic benefit that obtains every year:
1, stripping live steam condensed water secondary steam is energy-conservation
Design conditions: secondary steam flow rate: 22t/h plant operation rate: 95%
Steam utilization: 90% steam unit price: 70 yuan/t
Calculation result: the quantity of steam of saving is: 8760 * 22 * 0.95 * 0.90=164775.6 (t)
Be worth: 164775.6 * 70=11534292 (unit)
2, improve the steam that mother liquor temperature and evaporation are saved with the stripping secondary steam
Because the improvement of decomposing plate flow process, temperature of vaporizing raw liquor is brought up to 92 ℃ by 78 ℃, and simultaneously, the stripping secondary steam is used in evaporation, makes the evaporation steam consumption reduce significantly, and the low-pressure steam unit consumption is reduced to present 1.14t/t by the 1.5t/t of design.In 400,000 tons/year
The quantity of steam of saving is: 400000 * 0.36=144000 (t)
Be worth: 144000 * 70=10080000 (unit)
3, total economic benefit: the steam total amount of year saving: 164775.6+144000=308775.6 (t)
Total value: 11534292+10080000=21614292 (unit).
Description of drawings:
Elaborate below in conjunction with accompanying drawing.
Fig. 1 is a flow process before red mud washing of precipitate system and decomposing plate heat exchanging technology improve.
Fig. 2 is red mud washing of precipitate system and decomposing plate heat exchanging technology flow process of the present invention.
Embodiment:
The present invention mainly comprises three contents: 1, the reasonable utilization of stripping live steam condensed water secondary steam; 2, the change of red-mud settlement washing system type of heating; 3, the improvement of board-like heat exchange process flow process.
Technology of the present invention is: the water of condensation after the heating of stripping live steam contains a large amount of waste heats, this part water of condensation produces the secondary steam of about 22t/h after flash distillation, wherein major part is sent evaporation, accounts for 60% (13t/h) of total amount, and all the other advance the red-mud settlement washing system.Send under the stripping secondary steam normal circumstances of evaporation as the heating steam of pump feed evaporator, when forcing to imitate not open, advance the II single-effect evaporator.
The secondary steam that advances the red-mud settlement washing system feeds in each time washing settling groove by vapour pipe, with the heating red mud wash liquor,, avoid liquid level to be stired and make muddy simultaneously by steam in order to guarantee heats, the degree of depth in the vapour pipe insertion groove is suitable, and generally 1.5m is advisable under the liquid level to insert.After feeding secondary vapour, the temperature of first and second rinse bath can be mentioned below 95 ℃, and the temperature of No. three rinse baths is (can be higher, but the too high meeting of temperature is to the inconvenience of filtering red mud machine operation) more than 85 ℃.
When stripping heating tube bundle occurs and leaks situations such as causing secondary steam band material, the evaporation of not bothering to see me out of secondary vapour, but all advance the sedimentation washing system.
Because secondary cleaning water is by more than the temperature raising to 95 ℃, can satisfy the temperature requirement of causticization, needn't be through decomposing plate and seminal fluid heat exchange and directly send the once washing groove, therefore it is board-like to cancel intrinsic I level, the seminal fluid heat exchange changes three grades into by the level Four plate-type heat-exchange, that is: II, III level still are seminal fluid and decomposition nut liquid heat exchange, and the IV level is seminal fluid and water coolant heat exchange, and the seminal fluid temperature is by the board-like adjusting of IV level.The I level that spares is board-like as standby.After changing three grades of board-like heat exchange into, the temperature of decomposition nut liquid can be brought up to more than 92 ℃ for 80 ℃ by original less than.This technology is world's initiative, and the decomposition nut liquid temperature after the heat exchange is present international highest level.
Main technique condition of the present invention is:
1, stripping live steam condensed water secondary vapour: 145～165 ℃ of pressure 3～6 * 10 of temperature
5Pa flow 20～25t/h
Wherein send evaporation 12～15t/h, sedimentation washing 8～10t/h
2, each groove temperature of red-mud settlement washing system: one washes 95～100 ℃ two washes 95～98 ℃ three and washes 85～90 ℃
3, plate-type heat exchanger: seminal fluid: 65～75 ℃ of 105～108 ℃ of III level outlets of board-like import
58～62 ℃ of board-like outlets
Mother liquor: 90～95 ℃ of 50～56 ℃ of board-like outlets of board-like import.
Embodiment:
Production instance 1:
Stripping live steam condensed water secondary steam: 165 ℃ of temperature, pressure 6 * 10
5Pa, flow 25t/h
Wherein send evaporation 15t/h, send sedimentation washing 10t/h
Laterite washing subsider temperature: 100 ℃ of once washings
98 ℃ of secondary washing
90 ℃ of three washings
Plate-type heat-exchange: seminal fluid temperature: 62 ℃ of 75 ℃ of board-like outlets of 108 ℃ of III level outlets of board-like import
Mother liquor temperature: board-like import: 55 ℃
Board-like outlet: 95 ℃
Production instance 2:
Stripping live steam condensed water secondary steam: 145 ℃ of pressure 3 * 10 of temperature
5Pa flow 20t/h
Laterite washing subsider temperature: 95 ℃ of once washings
95 ℃ of secondary washing
85 ℃ of three washings
Plate-type heat-exchange: seminal fluid temperature: 105 ℃ of board-like imports, 65 ℃ of III level outlets, 58 ℃ of board-like outlets
Mother liquor temperature: board-like import: 50 ℃
Board-like outlet: 92 ℃
Enforcement of the present invention has not only made full use of aluminum oxide stripping secondary steam, saved the energy, and found the novel process of red-mud settlement washing and decomposing plate heat exchanging, simplified the technical process of these operations simultaneously, improved operational condition, technical indicator is optimized, and makes temperature of vaporizing raw liquor bring up to 92 ℃ by 80 ℃, reach present international highest level, energy conservation and consumption reduction effects is remarkable.
Table 1: technico-economical comparison relatively before and after improving
1996 1999 nineteen ninety-five of index name design load
The 9-12 month
The primary wash liquor seston---246 176 126
(mg/l)
Red mud filter cake water ratio 47 27.54 30.55 32.37
(％)
Efflux the attached alkali 5 6.74 7.90 3.16 of red mud
(the dried red mud of kg/t-)
Sedimenting system AO loss---20.15 16.93 15.23
(kg/t-AO)
Aluminum oxide total yield 81.5 71.86 78.89 82.16
(％)
Steam consumption (t/t) 4.0 4.34 4.06 3.45
Wherein: high pressure steam 2.5 2.60 2.58 2.31
Low-pressure steam 1.5 1.74 1.48 1.14
Comprehensive energy consumption 590.0---633.8 515.9
(kg mark coal/t-AO)
Red mud filter production capacity 200 143.2 172.5 200.9
(kg/m
2·h)
Claims (1)
1, a kind of alumina laterite washing direct heating and decomposing plate heat exchanging technology is characterized in that:
A, stripping live steam condensed water secondary steam are used to heat the laterite washing system and are used as the evaporation thermal source;
B, the employing of red-mud settlement washing system type of heating are heated the red-mud settlement washing system to the method that washing settling groove directly feeds secondary steam;
C, board-like heat exchange process flow process adopt seminal fluid all with decomposition nut liquid and water heat exchange.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001159291A CN1155521C (en) | 2000-07-26 | 2000-07-26 | Directly heating and decomposing plate heat exchanging technology for alumina laterite washing |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001159291A CN1155521C (en) | 2000-07-26 | 2000-07-26 | Directly heating and decomposing plate heat exchanging technology for alumina laterite washing |
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| CN1280100A CN1280100A (en) | 2001-01-17 |
| CN1155521C true CN1155521C (en) | 2004-06-30 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1329297C (en) * | 2005-09-28 | 2007-08-01 | 中国铝业股份有限公司 | Red mud slurry heating method and apparatus for alumina production |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100408479C (en) * | 2004-12-29 | 2008-08-06 | 贵阳铝镁设计研究院 | Method for raising temperature of vaporizing raw liquor |
| CN100381359C (en) * | 2006-03-17 | 2008-04-16 | 沈阳铝镁设计研究院 | Heat exchange technology for producing sand like aluminium oxide by two stage decomposition and its equipment |
| CN101575107B (en) * | 2008-05-08 | 2011-06-29 | 沈阳铝镁设计研究院有限公司 | Respective self-evaporation technology of new steam condensate and secondary steam condensate |
| CN101659450B (en) * | 2008-08-28 | 2011-05-11 | 中铝国际技术发展有限公司 | Process for combined spontaneous evaporation of new steam condensate and secondary steam condensate |
| CN101691235B (en) * | 2009-10-16 | 2011-06-15 | 中国铝业股份有限公司 | Method for reducing energy consumption of mother liquor evaporation processes |
| CN103723747A (en) * | 2012-10-15 | 2014-04-16 | 沈阳铝镁设计研究院有限公司 | Method used for reducing steam used for heating red mud washing water |
| CN103539176B (en) * | 2013-10-24 | 2015-03-04 | 满永国 | Aluminum oxide production method capable of optimizing process sequence |
| CN107814402A (en) * | 2017-11-13 | 2018-03-20 | 中国铝业股份有限公司 | One kind decomposes seminal fluid plate-type heat-exchange and falls to organize an apparatus and method online |
-
2000
- 2000-07-26 CN CNB001159291A patent/CN1155521C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1329297C (en) * | 2005-09-28 | 2007-08-01 | 中国铝业股份有限公司 | Red mud slurry heating method and apparatus for alumina production |
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| CN1280100A (en) | 2001-01-17 |
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