CN104477955A - Novel vapor condensate water temperature reduction and heat reclaim method in aluminum oxide production - Google Patents
Novel vapor condensate water temperature reduction and heat reclaim method in aluminum oxide production Download PDFInfo
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- CN104477955A CN104477955A CN201410839339.0A CN201410839339A CN104477955A CN 104477955 A CN104477955 A CN 104477955A CN 201410839339 A CN201410839339 A CN 201410839339A CN 104477955 A CN104477955 A CN 104477955A
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Abstract
The invention belongs to the technical field of aluminum oxide production in nonferrous metallurgical industry, and particularly relates to a novel vapor condensate water temperature reduction and heat reclaim method in aluminum oxide production. Novel vapor condensate water generated during indirect heat exchange among a dissolution workshop section, a resolving workshop section or other workshop sections and novel vapor condensate water generated in an evaporation workshop section in aluminum oxide production are mixed in a novel vapor condensate water tank; secondary vapor is flashed step by step in a negative pressure system, and enters a corresponding evaporator heating room; the novel vapor condensate water enters the next novel vapor condensate water tank until the secondary vapor flashed in the last novel vapor condensate water tank enters a water cooler; the finally generated novel vapor condensate water at 50 DEG C is sent to a power plant. Taking an aluminum oxide plant of which the vapor consumption is about 1000 thousand tons per year as example, the method can reclaim about 750-900 tons of novel vapor condensate water per year to the power plant; the requirements of green, environmental protection and energy conservation are met.
Description
Technical field
The invention belongs to technical field of alumina production in nonferrous metallurgy industry, be specifically related to the live steam condensed water cooling in a kind of alumina producing and heat recovery method.
Background technology
Alumina producing belongs to resource, the industry of energy dependent form, and the existing alumina producer of China has special supporting power plant substantially, and power plant is supplied to alumina producer power resource, comprises high pressure, low-pressure steam and electricity.At present, the production status of bayer's process alumina producer is not quite similar, during general process diaspore, and high pressure steam amount about 1.5 ~ 2.0t/t Al of consumption
2o
3, consume low-pressure steam about 0.5 ~ 1.0t/t Al
2o
3.During process gibbsite, high pressure steam amount about 1.0 ~ 1.05t/t Al of consumption
2o
3, consume low-pressure steam about 0.4 ~ 0.55t/t Al
2o
3.Like this, a steam consumption quantity producing the alumina producer of 500,000 tons per year is about 70 ~ 1,500,000 tons every year, and in order to produce steam, the consumption of the energy, cleaning water is huge.In order to reduce energy consumption, the water consumption of alumina producer, make full use of the clean steam condensate telegram in reply factory water treatment system that each workshop section of alumina producer produces, we develop the technique of the cooling of alumina producer live steam condensed water and heat recuperation according to design experiences for many years and on-the-spot running condition.
The boiler type of existing power plant of China is a lot, and existing alumina plant self-contained power station adopts circular fluid bed mostly.The power disposition of each alumina producer in the whole nation is different, has the situation suiting measures to local conditions to utilize neighbouring large power plant, also has the situation utilizing power plant for self-supply.The boiler of some power plant is very high to make up water quality requirements, require to the condensed water entering boiler carry out 100% except Ficus caricaL.The steam condensate of alumina producer, before telegram in reply factory continues utilization, needs to reduce the temperature to the Water Treatment that about 50 DEG C just can be carried out power plant's requirement.Because the live steam condensed water temperature of alumina producer is generally at about 158 DEG C, secondary steam water of condensation is at about 70 DEG C, and the alkalinity of secondary steam water of condensation is higher, can't reach the index request that telegram in reply factory completely continues to utilize at present.Therefore, the present invention can be adopted to lower the temperature to the live steam condensed water produced in alumina producing and reclaim heat.
Summary of the invention
For prior art Problems existing, the invention provides the live steam condensed water cooling in a kind of alumina producing and heat recovery method, object is that the live steam condensed water by alumina producer stripping Sum decomposition workshop section being produced is delivered in evaporation section, mix with evaporation live steam condensed water, the negative pressure system of evaporation system is utilized to carry out flash distillation, condensed water flash is lowered the temperature and reaches 50 DEG C, realize the live steam condensed water cooling of full factory, and recycle the heat of live steam condensed water.
The technical scheme realizing the object of the invention is carried out according to following steps:
(1) the stripping workshop section in alumina producing, the live steam condensed water and the evaporation section that decompose generation when workshop section or other workshop sections carry out indirect heat exchange are produced live steam condensed water imitate in live steam condensed water tank I and mix, the non-condensable gases mixing generation afterwards enters the heating chamber of I single-effect evaporator;
(2) mixed live steam condensed water enters in II effect live steam condensed water tank and carries out flash distillation cooling, the secondary steam that flash distillation produces enters in the heating chamber of II single-effect evaporator as thermal source, live steam condensed water after flash distillation enters flash distillation cooling in III effect live steam condensed water tank, the secondary steam later flashed off step by step enters in corresponding evaporator heating chamber as thermal source, live steam condensed water after flash distillation enters in the live steam condensed water tank of next effect, until the secondary steam that final stage live steam condensed water flash tank flashes off enters in water cooler, the live steam condensed water of final 50 DEG C sends into live steam condensed water pump, power plant is pumped into by live steam condensed water, the heat that flash distillation temperature-fall period produces step by step all enters in corresponding vaporizer to be recycled.
The heating chamber of I described single-effect evaporator adopts 158 DEG C, absolute pressure is the saturated live steam of 0.6MPa, in I single-effect evaporator separate chamber containing Na
2the slip of O heats, slip boiling after heat exchange heats up produces the thermal source of secondary steam as II single-effect evaporator heating chamber, namely the water of condensation produced in I single-effect evaporator heating chamber is the live steam condensed water that the evaporation section described in step (1) produces, from flowing in I effect live steam condensed water mixing tank.Seething with excitement with I single-effect evaporator separate chamber slip, to produce secondary steam similar, and the secondary steam that each single-effect evaporator separate chamber produces all enters lower 1st effective evaporator heating chamber as thermal source.Until the secondary steam that last evaporator separate chamber produces enters in water cooler.
No matter vaporizer is following current or counter-current operation, and namely no matter material trend and steam are in the same way or oppositely, the secondary steam that in separate chamber, slip boiling produces all can as the thermal source of lower 1st effective evaporator.
I effect secondary steam in II single-effect evaporator heating chamber heat exchange condensation produce secondary steam water of condensation because of alkalinity larger, be separated with live steam condensed water, enter II effect vapor condensation water pot, its non-condensable gases produced enters in II single-effect evaporator heating chamber, II effect secondary steam water of condensation enters imitates secondary steam water of condensation with III in III effect secondary steam condensate water pot and mixes, the secondary steam flashed off enters III single-effect evaporator heating chamber, all carry out secondary steam water of condensation with front effect in this effect secondary steam water of condensation in-tank mixing by the secondary steam water of condensation produced in single-effect evaporator heating chamber later, flash distillation cooling is carried out in next effect secondary steam condensate water pot, the secondary steam that flash distillation cooling produces enters in corresponding evaporator heating chamber, until last evaporator produce secondary steam water of condensation with respectively imitate mixed flash boiling after, the secondary steam condensation water collection that each effect produces and energy recovery complete, deliver to alumina producer to recycle.
Described vaporizer effect number is not limit, and is the multiple-effect evaporator with negative pressure operating mode.
The present invention is also applicable to non-bauxitic method and produces alumina technology Zhong Ge workshop section and clean high-temperature water in the cooling of evaporation section and energy recovery.
Compared with prior art, feature of the present invention and beneficial effect are:
Live steam condensed water of the present invention is adopted to lower the temperature and heat recovery method, vaporizer is utilized to imitate the characteristic of successively decreasing step by step to end effect pressure from I, live steam condensed water temperature to 50 DEG C can be reduced, cryogenic condensation water is made directly to return Chemical Water Treatment System in Power Plant, wherein respectively imitate live steam condensed water to change thermogenetic secondary steam water of condensation with slip and do not mix mutually, ensure that the quality of live steam condensed water, and recycle the heat of live steam condensed water flash distillation.
For the alumina producer of annual about 1,000,000 tons of steam consumption quantity, adopt technical scheme of the present invention can save energy every year and be about 1.08x10
8kcal, is equivalent to save about 15428t every year and marks coal, can reclaim live steam condensed water about 75 ~ 900,000 tons/year to power plant, reach green, environmental protection, energy-conservation requirement.
Accompanying drawing explanation
Fig. 1 is live steam condensed water cooling in the alumina producing of the embodiment of the present invention 1 and the device schematic diagram of heat recuperation;
Wherein: 1-1: I effect live steam condensed water mixing tank; 1-2: II effect live steam condensed water tank; 1-3: III effect live steam condensed water tank; 1-4: IV effect live steam condensed water tank; 1-5: V effect live steam condensed water tank; 1-6: VI effect live steam condensed water tank; 1-7: final stage live steam condensed water flash tank;
2-1: I single-effect evaporator; 2-2: II single-effect evaporator; 2-3: III single-effect evaporator; 2-4: IV single-effect evaporator; 2-5: V single-effect evaporator; 2-6: VI single-effect evaporator;
3-1: I single-effect evaporator heating chamber; 3-2: II single-effect evaporator heating chamber; 3-3: III single-effect evaporator heating chamber; 3-4: IV single-effect evaporator heating chamber; 3-5: V single-effect evaporator heating chamber; 3-6: VI single-effect evaporator heating chamber;
4-1: I single-effect evaporator separate chamber; 4-2: II single-effect evaporator separate chamber; 4-3: III single-effect evaporator separate chamber; 4-4: IV single-effect evaporator separate chamber; 4-5: V single-effect evaporator separate chamber; 4-6: VI single-effect evaporator separate chamber;
5-1: II effect secondary steam condensate water pot; 5-2: III effect secondary steam condensate water pot; 5-3: IV effect secondary steam condensate water pot; 5-4: V effect secondary steam condensate water pot; 5-5: VI effect secondary steam condensate water pot;
6: water cooler; 7: live steam condensed water pump;
represent the flow direction of live steam condensed water;
represent the flow direction of secondary steam water of condensation;
represent the flow direction of secondary steam and non-condensable gases;
represent 158 DEG C, the live steam of 0.6MPa.
Embodiment
Embodiment 1
The embodiment of the present invention adopts sextuple-effect evaporator, its schematic diagram as shown in Figure 1, I effect live steam condensed water mixing tank 1-1, II effect live steam condensed water tank 1-2 ..., VI effect vapor condensation water pot 1-6, final stage live steam condensed water flash tank 1-7 be connected step by step, be connected with live steam condensed water pump 7 bottom final stage live steam condensed water flash tank 1-7, the live steam condensed water of 50 DEG C final stage live steam condensed water tank 1-7 flash distillation produced sends into power plant, top is connected with water cooler 6, and secondary steam enters water cooler 6;
I effect live steam condensed water mixing tank 1-1 is also connected with I single-effect evaporator heating chamber 3-1, the non-condensable gases of generation is sent in I single-effect evaporator heating chamber 3-1, simultaneously I single-effect evaporator heating chamber 4-1 is also imitated live steam condensed water tank 1-1 and is connected with I, the live steam condensed water produced that slip heat exchange heated up sends into I effect live steam condensed water tank 1-1, by that analogy, each effect live steam condensed water tank is connected with the evaporator heating chamber that it imitates number corresponding, with the secondary steam carrying non-condensable gases He flash off;
I single-effect evaporator separate chamber 4-1 is connected with II single-effect evaporator heating chamber 3-2, the secondary steam that slip boiling in I single-effect evaporator separate chamber 4-1 produces is sent in II single-effect evaporator heating chamber 3-2, by that analogy, all lower with it 1st effective evaporator heating chamber in each single-effect evaporator separate chamber is connected, and VI single-effect evaporator separate chamber 4-6 is connected with water cooler 6;
II single-effect evaporator heating chamber 4-2 is also imitated secondary steam condensate water pot 5-1 and is connected with II, II effect secondary steam condensate water pot 5-1 top is connected with II single-effect evaporator heating chamber 3-2, bottom and III is imitated secondary steam condensate water pot 5-2 and is connected, by that analogy, each single-effect evaporator heating chamber and the secondary steam condensate water pot corresponding with its effect number are connected, each effect secondary steam condensate water pot top is connected with the evaporator heating chamber that it imitates number corresponding, and bottom is imitated secondary steam condensate water pot with next and is connected.
Adopt the sextuple-effect evaporator in Fig. 1 to carry out live steam condensed water cooling and heat recuperation, carry out according to following steps:
(1) alumina producer stripping workshop section 158 DEG C of live steam condensed waters are about 110t/h, and the temperature produced with evaporation section is that the 50t/h live steam condensed water of 158 DEG C is imitated in live steam condensed water mixing tank 1-1 mixed I;
(2) non-condensable gases produced enters in the heating chamber 3-1 of I single-effect evaporator, live steam condensed water enters flash distillation in II effect live steam condensed water tank 1-2 and is cooled to 135 DEG C, the secondary steam that flash distillation produces enters the heating chamber 3-2 of II single-effect evaporator, the 135 DEG C of live steam condensed waters produced enter flash distillation in III effect live steam condensed water tank 1-3 and are cooled to 115 DEG C, the secondary steam that flash distillation produces enters the heating chamber 3-3 of III single-effect evaporator, 115 DEG C of live steam condensed waters after flash distillation enter IV effect live steam condensed water tank 1-4 flash distillation and are cooled to 97 DEG C, the secondary steam that flash distillation produces enters IV single-effect evaporator heating chamber 3-4, 97 DEG C of live steam condensed waters after flash distillation enter V effect live steam condensed water tank 1-5 flash distillation and are cooled to 79 DEG C, the secondary steam produced enters V single-effect evaporator heating chamber 3-5, 79 DEG C of live steam condensed waters after flash distillation enter VI effect live steam condensed water tank 1-6 flash distillation and are cooled to 65 DEG C, the secondary steam produced enters VI single-effect evaporator heating chamber 3-6, 65 DEG C of live steam condensed waters after flash distillation enter final stage live steam condensed water flash tank 1-7 flash distillation and are cooled to 50 DEG C, secondary steam enters water cooler 6, live steam condensed water after flash distillation enters live steam condensed water pump 7, by pump delivery to power plant.
The heating chamber 3-1 of I described single-effect evaporator adopts 158 DEG C, absolute pressure is the saturated live steam of 0.6MPa, in I single-effect evaporator separate chamber 4-1 containing Na
2the slip of O heats, and the slip after heat exchange heats up produces the thermal source of secondary steam as II single-effect evaporator heating chamber 3-2.The water of condensation produced in I effect heating chamber is the live steam condensed water described in step (1), imitate in live steam condensed water mixing tank 1-1 from inflow I, seething with excitement with I single-effect evaporator separate chamber slip, to produce secondary steam similar, the secondary steam that each single-effect evaporator separate chamber produces all enters lower 1st effective evaporator heating chamber as thermal source, until the secondary steam that VI single-effect evaporator separate chamber 4-6 produces enters in water cooler 6.
The secondary steam secondary steam water of condensation that heat exchange condensation produces in II single-effect evaporator heating chamber 3-2 of I effect enters II effect vapor condensation water pot 5-1, its non-condensable gases produced enters II single-effect evaporator heating chamber 3-2, II effect secondary steam water of condensation enters III effect secondary steam condensate water pot 5-2 and III and imitates secondary steam water of condensation and mix, and flash off secondary steam, enter III single-effect evaporator heating chamber 3-3.All carry out secondary steam water of condensation with front effect in this effect secondary steam water of condensation in-tank mixing by the secondary steam water of condensation produced in single-effect evaporator heating chamber later, flash distillation cooling is carried out in next effect secondary steam condensate water pot, the secondary steam that flash distillation cooling produces enters in corresponding evaporator heating chamber, until the secondary steam water of condensation of II effect-V effect is after the VI secondary steam water of condensation mixed flash boiling that produce of effect secondary steam condensate water pot 5-5 and VI single-effect evaporator heating chamber 3-6, secondary steam condensation water collection and energy recovery complete, and deliver to alumina producer and recycle.
Embodiment 2
The present embodiment adopts quintuple effect evaporator, carries out live steam condensed water cooling and heat recuperation, carries out according to following steps:
(1) alumina producer decomposes workshop section 158 DEG C of live steam condensed waters and is about 80t/h, and the temperature produced with evaporation section is that the 50t/h live steam condensed water of 158 DEG C is imitated in live steam condensed water mixing tank I and mixed and carry out flash distillation cooling;
(2) non-condensable gases produced enters in the heating chamber of I single-effect evaporator, live steam condensed water enters flash distillation in II effect live steam condensed water tank and is cooled to 127 DEG C, the secondary steam that flash distillation produces enters the heating chamber of II single-effect evaporator, 127 DEG C of live steam condensed waters after flash distillation enter flash distillation in III effect live steam condensed water tank and are cooled to 98 DEG C, the secondary steam that flash distillation produces enters the heating chamber of III single-effect evaporator, 98 DEG C of live steam condensed waters after flash distillation enter IV effect live steam condensed water tank flash distillation and are cooled to 83 DEG C, the secondary steam that flash distillation produces enters IV single-effect evaporator heating chamber, 83 DEG C of live steam condensed waters after flash distillation enter V effect live steam condensed water tank flash distillation and are cooled to 66 DEG C, the secondary steam produced enters V single-effect evaporator heating chamber, 66 DEG C of live steam condensed waters after flash distillation enter the flash distillation of final stage live steam condensed water flash tank and are cooled to 50 DEG C, secondary steam enters water cooler, live steam condensed water after flash distillation enters live steam condensed water pump, by pump delivery to power plant, the heat that flash distillation cooling produces step by step enters vapo(u)rization system and recycles.
The heating chamber of I single-effect evaporator adopts 158 DEG C, the live steam of 0.6MPa, in I single-effect evaporator separate chamber containing Na
2the slip of O heats, and the slip after heat exchange heats up produces the thermal source of secondary steam as II single-effect evaporator heating chamber, and the water of condensation of generation is the live steam condensed water described in step (1), from flowing in I effect live steam condensed water mixing tank; Seething with excitement with I single-effect evaporator separate chamber slip, to produce secondary steam similar, and the secondary steam that each single-effect evaporator separate chamber produces all enters lower 1st effective evaporator heating chamber as thermal source, until the secondary steam that V single-effect evaporator separate chamber produces enters in water cooler.
The secondary steam secondary steam water of condensation that heat exchange condensation produces in II single-effect evaporator heating chamber of I effect enters II effect vapor condensation water pot, its non-condensable gases produced enters II single-effect evaporator heating chamber, II effect secondary steam water of condensation enters III effect secondary steam condensate water pot and III and imitates secondary steam water of condensation and mix, and flash off secondary steam, enter III single-effect evaporator heating chamber.All carry out secondary steam water of condensation with front effect in this effect secondary steam water of condensation in-tank mixing by the secondary steam water of condensation produced in single-effect evaporator heating chamber later, flash distillation cooling is carried out in next effect secondary steam condensate water pot, the secondary steam that flash distillation cooling produces enters in corresponding evaporator heating chamber, until the secondary steam water of condensation of II effect-IV effect is after V effect secondary steam condensate water pot and the secondary steam water of condensation mixed flash boiling that produces of V single-effect evaporator heating chamber, secondary steam condensation water collection and energy recovery complete, and deliver to alumina producer and recycle.
Claims (2)
1. the live steam condensed water cooling in alumina producing and a heat recovery method, is characterized in that carrying out according to following steps:
(1) the temperature live steam condensed water stripping workshop section in alumina producing, the live steam condensed water and the evaporation section that decompose generation when workshop section or other workshop sections carry out indirect heat exchange produced imitate in live steam condensed water tank I and is mixed, and the non-condensable gases mixing generation afterwards enters the heating chamber of I single-effect evaporator;
(2) mixed live steam condensed water enters in II effect live steam condensed water tank and carries out flash distillation cooling, the secondary steam that flash distillation produces enters in the heating chamber of II single-effect evaporator as thermal source, live steam condensed water after flash distillation enters flash distillation cooling in III effect live steam condensed water tank, the secondary steam later flashed off step by step enters in corresponding evaporator heating chamber as thermal source, live steam condensed water after flash distillation enters in the live steam condensed water tank of next effect, until the secondary steam that final stage live steam condensed water flash tank flashes off enters in water cooler, the live steam condensed water of final 50 DEG C sends into live steam condensed water pump, power plant is pumped into by live steam condensed water, the heat that flash distillation temperature-fall period produces step by step all enters in corresponding vaporizer to be recycled.
2. the live steam condensed water cooling in a kind of alumina producing according to claim 1 and heat recovery method, it is characterized in that described vaporizer effect number is not limit, is the multiple-effect evaporator with negative pressure operating mode.
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|---|---|---|---|
| CN201410839339.0A CN104477955B (en) | 2014-12-30 | 2014-12-30 | Live steam condensed water cooling in a kind of alumina producing and heat recovery method |
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|---|---|---|---|
| CN201410839339.0A CN104477955B (en) | 2014-12-30 | 2014-12-30 | Live steam condensed water cooling in a kind of alumina producing and heat recovery method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107754363A (en) * | 2016-08-23 | 2018-03-06 | 沈阳铝镁设计研究院有限公司 | A kind of method that raising system evaporation volume reduces the steam consumption |
| CN108211392A (en) * | 2016-12-10 | 2018-06-29 | 沈阳铝镁设计研究院有限公司 | Split type falling film evaporation method |
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| CN101671045A (en) * | 2009-10-13 | 2010-03-17 | 杭州锦江集团有限公司 | Pressure digestion system and recycling method of live steam condensed water |
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2014
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| CN101671045A (en) * | 2009-10-13 | 2010-03-17 | 杭州锦江集团有限公司 | Pressure digestion system and recycling method of live steam condensed water |
Non-Patent Citations (1)
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| 吉林化学工业公司化肥厂: "《硝酸铵生产工艺与操作》", 31 January 1980 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107754363A (en) * | 2016-08-23 | 2018-03-06 | 沈阳铝镁设计研究院有限公司 | A kind of method that raising system evaporation volume reduces the steam consumption |
| CN108211392A (en) * | 2016-12-10 | 2018-06-29 | 沈阳铝镁设计研究院有限公司 | Split type falling film evaporation method |
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