CN102491385A - Method for using dissolved exhaust steam in alumina production - Google Patents
Method for using dissolved exhaust steam in alumina production Download PDFInfo
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- CN102491385A CN102491385A CN2011103667070A CN201110366707A CN102491385A CN 102491385 A CN102491385 A CN 102491385A CN 2011103667070 A CN2011103667070 A CN 2011103667070A CN 201110366707 A CN201110366707 A CN 201110366707A CN 102491385 A CN102491385 A CN 102491385A
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- exhaust steam
- stripping
- heat exchange
- steam
- alumina producing
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Abstract
A method for using dissolved exhaust steam in alumina production is especially relates to a method for recovering exhaust steam from a digesting diluted tank during the alumina production process by Bayer process. The method is characterized in that steam which is steamed out from the digesting diluted tank by flash evaporation and secondary exhaust steam generated after dam backwater mixing and heating undergo steam-water separation and then enter into a heat exchanger to exchange heat with an evaporation stock solution from a decomposition process, and the evaporation stock solution which has undergone heat exchange is sent into an evaporator by a pump. With the adoption of the method, the heat of the exhaust gas from the digesting diluted tank is fully utilized, and simultaneously the temperature of the evaporation stock solution is raised, thereby improving evaporative capacity of the evaporator and reducing steam consumption of the evaporator.
Description
Technical field
The method that the stripping exhaust steam utilizes in a kind of alumina producing particularly relates to the method that the exhaust steam of stripping dilution trap is recycled in a kind of process of alumina producing Bayer process.
Background technology
In the high pressure dissolving-out process of alumina producer, stripping slurry gets into dilution trap after through the flash distillation of final stage ore pulp flash-pot, and slip produces exhaust steam through self-evaporatint n. behind the dilatation release of pressure once more in dilution trap; But its weary temperature degree is relatively low; Have only 100-110 ℃, and owing to vapour amount, vapour pressure often fluctuate, so; On-the-spot not high to the utilization ratio of this part exhaust steam; Cause leaking in a large number of exhaust steam, particularly not enough to some extent or sleeve pipe scabs when serious when the sleeve pipe heat interchanging area, and situation is more serious.When exhaust steam leaked, band was expected easily on the one hand, and operating environment is brought certain danger, and the exhaust steam of band alkali enters in the atmosphere and can cause environmental pollution, can cause exhaust steam residual heat to fail to reclaim Direct Loss on the other hand, and alumina production cost is increased.
Evaporization process is the master operation of balance aluminium oxide production liquid measure, and the evaporative water capacity of vaporizer is one of key of raising of aluminum oxide output and index optimization.At present, the temperature of vaporizing raw liquor that obtains after the heat exchange of seed precipitation solution process plate-type heat exchanger has only 85～88 ℃, and temperature of vaporizing raw liquor is low, influences the conduction of system, causes steaming the water yield and reduces, and the steam consumption increases.
Summary of the invention
The object of the invention is exactly the deficiency that exists to above-mentioned prior art, provides a kind of and makes full use of the stripping exhaust steam and come heating evaporation stoste, improves the method that the stripping exhaust steam utilizes in the alumina producing of vaporizer evaporative water capacity.
The objective of the invention is to realize through following technical scheme.
The method that the stripping exhaust steam utilizes in a kind of alumina producing; It is characterized in that; After the secondary exhaust steam that produces after the steam that the flash distillation of stripping dilution trap is come out and the dam backwater Hybrid Heating separates through carbonated drink; Get into interchanger and carry out heat exchange with vaporizing raw liquor from decomposition process, the vaporizing raw liquor after the heat exchange is through being pumped into vaporizer; Water of condensation is from flowing into the ground sewage groove, then through being pumped into hot water tank.
The method that the stripping exhaust steam utilizes in a kind of alumina producing of the present invention, it is characterized in that the exhaust steam of described stripping dilution trap at first with dam backwater Hybrid Heating in the wash water well heater.
The method that the stripping exhaust steam utilizes in a kind of alumina producing of the present invention is characterized in that described interchanger is a kind of in falling film evaporation well heater, shell and tube heat exchanger, the fin interchanger.
The method that the stripping exhaust steam utilizes in a kind of alumina producing of the present invention, the former liquid temp of heat exchange front evaporator under it is characterized in that is 85～88 ℃, temperature of vaporizing raw liquor is 92～95 ℃ after the heat exchange;
The present invention has made full use of the heat of the weary gas of dilution trap, has improved the temperature of vaporizing raw liquor simultaneously, thereby has improved the vaporizer evaporative water capacity, has reduced the vaporizer ton and has steamed the steam consumption.
Description of drawings
Fig. 1 is a process flow diagram of the present invention.
In the accompanying drawing: 1, dilution trap; 2, wash water well heater; 3, hot water tank; 4, steam separator; 5, interchanger.
Embodiment
The method that the stripping exhaust steam utilizes in a kind of alumina producing; It is characterized in that; Exhaust steam that 1 flash distillation of stripping dilution trap is come out and dam backwater Hybrid Heating in wash water well heater 2, heated hot water send hot water tank 3 to be used for the red mud wash water, and the secondary exhaust steam that the heating back produces is through behind the steam separator 4; Get into interchanger 5 and carry out heat exchange with vaporizing raw liquor from decomposition process, the vaporizing raw liquor after the heat exchange is through being pumped into vaporizer.Water of condensation is from flowing into the ground sewage groove, then through being pumped into hot water tank.
Below in conjunction with instance the present invention is described further.
Embodiment 1
110 ℃ of exhaust steam of the temperature that the flash distillation of stripping dilution trap is come out and dam backwater Hybrid Heating in the wash water well heater; 97 ℃ of hot water of heated temperatures send hot water tank to be used for the red mud wash water; The secondary exhaust steam that the heating back produces is through behind the steam separator; Get into the falling film evaporation well heater and carry out heat exchange, obtain 92 ℃ of vaporizing raw liquors of temperature after the heat exchange through being pumped into vaporizer with 85 ℃ of vaporizing raw liquors of temperature from decomposition process.Water of condensation is from flowing into the ground sewage groove, then through being pumped into hot water tank.
Embodiment 2
110 ℃ of exhaust steam of the temperature that the flash distillation of stripping dilution trap is come out and dam backwater Hybrid Heating in the wash water well heater; 97 ℃ of hot water of heated temperatures send hot water tank to be used for the red mud wash water; The secondary exhaust steam that the heating back produces is through behind the steam separator; Get into shell and tube heat exchanger and carry out heat exchange, obtain 95 ℃ of vaporizing raw liquors of temperature after the heat exchange through being pumped into vaporizer with 87 ℃ of vaporizing raw liquors of temperature from the self-decomposition operation.Water of condensation is from flowing into the ground sewage groove, then through being pumped into hot water tank.
Embodiment 3
110 ℃ of exhaust steam of the temperature that the flash distillation of stripping dilution trap is come out and dam backwater Hybrid Heating in the wash water well heater; 97 ℃ of hot water of heated temperatures send hot water tank to be used for the red mud wash water; The secondary exhaust steam that the heating back produces is through behind the steam separator; The 88 ℃ of vaporizing raw liquors of temperature that get into the fin interchanger and the self-decomposition operation of evaluating oneself carry out heat exchange, obtain 94 ℃ of vaporizing raw liquors of temperature after the heat exchange through being pumped into vaporizer.Water of condensation is from flowing into the ground sewage groove, then through being pumped into hot water tank.
Claims (4)
1. the method that the stripping exhaust steam utilizes in the alumina producing; It is characterized in that; After the secondary exhaust steam that produces after the steam that the flash distillation of stripping dilution trap is come out and the dam backwater Hybrid Heating separates through carbonated drink; Get into interchanger and carry out heat exchange with vaporizing raw liquor from decomposition process, the vaporizing raw liquor after the heat exchange is through being pumped into vaporizer; Water of condensation is from flowing into the ground sewage groove, then through being pumped into hot water tank.
2. the method that the stripping exhaust steam utilizes in a kind of alumina producing according to claim 1, it is characterized in that the exhaust steam of described stripping dilution trap at first with dam backwater Hybrid Heating in the wash water well heater.
3. the method that the stripping exhaust steam utilizes in a kind of alumina producing according to claim 1 is characterized in that described interchanger is a kind of in falling film evaporation well heater, shell and tube heat exchanger, the fin interchanger.
4. the method that the stripping exhaust steam utilizes in a kind of alumina producing according to claim 1, the former liquid temp of heat exchange front evaporator under it is characterized in that is 85～88 ℃, temperature of vaporizing raw liquor is 92～95 ℃ after the heat exchange.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011103667070A CN102491385A (en) | 2011-11-18 | 2011-11-18 | Method for using dissolved exhaust steam in alumina production |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011103667070A CN102491385A (en) | 2011-11-18 | 2011-11-18 | Method for using dissolved exhaust steam in alumina production |
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| CN102491385A true CN102491385A (en) | 2012-06-13 |
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| CN2011103667070A Pending CN102491385A (en) | 2011-11-18 | 2011-11-18 | Method for using dissolved exhaust steam in alumina production |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102992363A (en) * | 2012-10-24 | 2013-03-27 | 广西华银铝业有限公司 | Steam waste heat recovery of dissolved and diluted slurry |
| CN102997692A (en) * | 2012-10-24 | 2013-03-27 | 广西华银铝业有限公司 | Method for utilizing residual heat of roasting furnace smoke to heat evaporated raw liquid |
| CN103288109A (en) * | 2013-06-24 | 2013-09-11 | 中国铝业股份有限公司 | Alumina high pressure dissolution dilution ore slurry exhaust steam recovery method |
| CN104436716A (en) * | 2013-09-17 | 2015-03-25 | 贵阳铝镁设计研究院有限公司 | Ore pulp spontaneous-evaporation steam-liquid separation device |
| CN104692425A (en) * | 2013-12-10 | 2015-06-10 | 沈阳铝镁设计研究院有限公司 | Method for reducing smoking of dissolution dilution tank |
| CN105271324A (en) * | 2014-06-26 | 2016-01-27 | 沈阳铝镁设计研究院有限公司 | Low-pressure exhausted steam recycling system |
| CN105271326A (en) * | 2014-06-27 | 2016-01-27 | 沈阳铝镁设计研究院有限公司 | Method for improving water-return ratio of primary water in evaporation system |
| CN106051738A (en) * | 2016-07-20 | 2016-10-26 | 广西田东锦鑫化工有限公司 | Steam recycling and reusing device of high-temperature slurry tank |
| CN106115749A (en) * | 2016-08-09 | 2016-11-16 | 中国铝业股份有限公司 | A kind of dissolved exhaust steam in alumina production utilize system and method |
| CN107954457A (en) * | 2018-01-11 | 2018-04-24 | 杨蕊鸿 | A kind of non-level dead steam recovery system of dissolution and technique |
| CN108529657A (en) * | 2018-04-18 | 2018-09-14 | 太原理工大学 | Multi-effect evaporating device and technique applied to alumina refinery |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201610380U (en) * | 2009-12-22 | 2010-10-20 | 杭州锦江集团有限公司 | System heating and evaporating secondary qualified water by utilizing dissolved afterheat |
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2011
- 2011-11-18 CN CN2011103667070A patent/CN102491385A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201610380U (en) * | 2009-12-22 | 2010-10-20 | 杭州锦江集团有限公司 | System heating and evaporating secondary qualified water by utilizing dissolved afterheat |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102992363A (en) * | 2012-10-24 | 2013-03-27 | 广西华银铝业有限公司 | Steam waste heat recovery of dissolved and diluted slurry |
| CN102997692A (en) * | 2012-10-24 | 2013-03-27 | 广西华银铝业有限公司 | Method for utilizing residual heat of roasting furnace smoke to heat evaporated raw liquid |
| CN103288109A (en) * | 2013-06-24 | 2013-09-11 | 中国铝业股份有限公司 | Alumina high pressure dissolution dilution ore slurry exhaust steam recovery method |
| CN104436716A (en) * | 2013-09-17 | 2015-03-25 | 贵阳铝镁设计研究院有限公司 | Ore pulp spontaneous-evaporation steam-liquid separation device |
| CN104692425A (en) * | 2013-12-10 | 2015-06-10 | 沈阳铝镁设计研究院有限公司 | Method for reducing smoking of dissolution dilution tank |
| CN105271324B (en) * | 2014-06-26 | 2017-08-15 | 沈阳铝镁设计研究院有限公司 | A kind of low pressure exhaust steam recycling system |
| CN105271324A (en) * | 2014-06-26 | 2016-01-27 | 沈阳铝镁设计研究院有限公司 | Low-pressure exhausted steam recycling system |
| CN105271326A (en) * | 2014-06-27 | 2016-01-27 | 沈阳铝镁设计研究院有限公司 | Method for improving water-return ratio of primary water in evaporation system |
| CN106051738A (en) * | 2016-07-20 | 2016-10-26 | 广西田东锦鑫化工有限公司 | Steam recycling and reusing device of high-temperature slurry tank |
| CN106115749A (en) * | 2016-08-09 | 2016-11-16 | 中国铝业股份有限公司 | A kind of dissolved exhaust steam in alumina production utilize system and method |
| CN106115749B (en) * | 2016-08-09 | 2018-04-20 | 中国铝业股份有限公司 | A kind of dissolved exhaust steam in alumina production utilizes system and method |
| CN107954457A (en) * | 2018-01-11 | 2018-04-24 | 杨蕊鸿 | A kind of non-level dead steam recovery system of dissolution and technique |
| CN108529657A (en) * | 2018-04-18 | 2018-09-14 | 太原理工大学 | Multi-effect evaporating device and technique applied to alumina refinery |
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Application publication date: 20120613 |