CN102557090A - Method for recycling heat energy of new steam condensed water in whole plant during alumina production - Google Patents
Method for recycling heat energy of new steam condensed water in whole plant during alumina production Download PDFInfo
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- CN102557090A CN102557090A CN2010106050398A CN201010605039A CN102557090A CN 102557090 A CN102557090 A CN 102557090A CN 2010106050398 A CN2010106050398 A CN 2010106050398A CN 201010605039 A CN201010605039 A CN 201010605039A CN 102557090 A CN102557090 A CN 102557090A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 101
- PNEYBMLMFCGWSK-UHFFFAOYSA-N AI2O3 Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 238000004519 manufacturing process Methods 0.000 title abstract description 5
- 238000004064 recycling Methods 0.000 title abstract 3
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 238000001704 evaporation Methods 0.000 claims abstract description 10
- 230000001105 regulatory Effects 0.000 claims abstract description 6
- 238000001556 precipitation Methods 0.000 claims abstract description 4
- 238000009833 condensation Methods 0.000 claims description 37
- 230000005494 condensation Effects 0.000 claims description 37
- 238000001816 cooling Methods 0.000 claims description 11
- 239000012452 mother liquor Substances 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 6
- 238000000034 method Methods 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 6
- 238000005259 measurement Methods 0.000 claims description 5
- 238000003809 water extraction Methods 0.000 claims description 4
- 230000000694 effects Effects 0.000 claims description 3
- 238000010792 warming Methods 0.000 claims description 3
- 206010039509 Scab Diseases 0.000 claims description 2
- 239000003643 water by type Substances 0.000 claims description 2
- 238000004140 cleaning Methods 0.000 abstract description 2
- 239000011550 stock solution Substances 0.000 abstract 7
- 241000276425 Xiphophorus maculatus Species 0.000 abstract 2
- 230000001276 controlling effect Effects 0.000 abstract 1
- 239000010413 mother solution Substances 0.000 abstract 1
- 101700072563 POT1 Proteins 0.000 description 11
- 241000196324 Embryophyta Species 0.000 description 4
- 238000007599 discharging Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 241000893018 Armeria Species 0.000 description 2
- 210000000582 Semen Anatomy 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 1
- 239000008398 formation water Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Abstract
The invention discloses a method for recycling heat energy of new steam condensed water in the whole plant during alumina production. The method comprises the following steps of: collecting the new steam condensed water on each section of an alumina plant; feeding the collected new steam condensed water to a stock solution evaporating workshop and carrying out heat exchange on the collected new steam condensed water and a seed precipitation mother solution, namely an evaporated stock solution from a decomposing workshop, through a first platy heat exchanger (4) and a second heat exchanger (5); controlling the outlet temperature of the evaporated stock solution and the new stream condensed water according to the flow of a first speed regulating evaporated stock solution pump (7) and a second speed regulating evaporated stock solution pump (8); judging whether a plate is required to be cleaned or replaced or not according to a pressure difference value of a pressure gauge (11) on evaporated stock solution inlet-outlet pipes of the first platy heat exchanger (4) and the second heat exchanger (5); determining that the new stream condensed water is fed to a boiler room of a thermal power plant to be used as replenished water or is fed to a condensed water tank of the stock solution workshop to be used as hot water for the whole plant, according to a conductivity value of a conductivity meter (12); and measuring the liquid level of the condensed water in the tank by a liquid level meter (9). According to the method disclosed by the invention, the problem of recycling of the heat energy of the new stream condensed water is solved.
Description
Technical field
The present invention relates to the method for full factory live steam condensed water heat energy recycle in a kind of alumina producing.
Background technology
In whole alumina producing; Heating medium during low pressure live steam (the about 6bar of pressure, about 158 ℃ of the temperature) conduct that workshop sections such as evaporator station, desiliconization in advance, the heating of decompositionization clear liquid need adopt the thermal power plant boiler room is produced, the live steam heating medium forms live steam condensed water (the about 6bar of pressure after discharging the latent heat of vaporization after the heat exchange; About 158 ℃ of temperature); Directly send the thermal power plant boiler room then back to through behind the pressure and temperature reducing, remake the additional water into boiler, the partial heat energy of water of condensation is failed to obtain efficient recovery and is fallen with regard to Direct Loss like this; Thereby cause the thermal waste of steam condensate in the alumina producing, increased the production hear rate.
Mother liquor (vaporizing raw liquor) after decomposing in the alumina producing is delivered to evaporation section after seminal fluid heat exchange workshop section is warming up to about 85 ℃; Vaporizing raw liquor passes through low pressure live steam (the about 6bar of pressure in evaporator station; About 158 ℃ of temperature) more than the heat temperature raising to 120 ℃ and through becoming mother liquid evaporation after the flash concentration, delivers to the circulating mother liquor allotment workshop section incoming stock grinder section in the good back of allotment again and prepare burden.Because the steam consumption of evaporation section accounts for whole alumina producing energy consumption about 30%; Therefore low if get into the temperature of vaporizing raw liquor of evaporation section; Can cause required live steam consumption increasing in the evaporative process; Thereby increased the steam-water ratio of evaporation, caused the alumina producing energy consumption to increase, strengthened production cost and working cost.
Summary of the invention
The technical problem that the present invention will solve is: the method that full factory live steam condensed water heat energy recycle in a kind of alumina producing is provided; Thereby this method can improve temperature of vaporizing raw liquor practices thrift the evaporator station steam consumption; Thereby the heat energy that can recycle live steam condensed water again reduces the water of condensation thermosteresis, to overcome the deficiencies such as thermal waste that prior art exists.
The present invention is achieved in that its employing plate-type heat exchanger is with live steam condensed water and vaporizing raw liquor heat exchange; The temperature that full factory is come everywhere is that 155 ℃～160 ℃ live steam condensed waters compile into condensation water pot 1; Through cold first water extraction pump 2, second water extraction pump 3 live steam condensed water is delivered to respectively in first plate-type heat exchanger 4, second plate-type heat exchanger 5 and be that vaporizing raw liquor the vaporizing raw liquor storage tank 6 carries out heat exchange from decomposing the seed precipitation solution that comes; Live steam condensed water temperature (from about 158 ℃) heat exchange is cooled to below 95 ℃, and temperature of vaporizing raw liquor is warming up to more than 92 ℃ from about 85 ℃.
Compile after first plate-type heat exchanger 4,5 heat exchange of second plate-type heat exchanger are delivered to after lowering the temperature in the deoxygenator of boiler house of heat power plant from the live steam condensed water of evaporator station, in advance desiliconization, the heating of decompositionizations clear liquid, the water of condensation after the cooling is directly as boiler replenishing water.
Part vaporizing raw liquor is delivered to evaporator station as the evaporation charging after delivering to first plate-type heat exchanger, 4 heat exchange intensification through the first vaporizing raw liquor pump 7, and a part of vaporizing raw liquor is delivered to second plate-type heat exchanger, 5 heat exchange intensification backs (more than 90 ℃) through the second vaporizing raw liquor pump 8 and delivered to the circulating mother liquor storage tank as circulating mother liquor allotment usefulness.
On the water of condensation import and export of first plate-type heat exchanger 4, second plate-type heat exchanger 5 and vaporizing raw liquor import and export pipeline, TM 10 is set, measures water of condensation and temperature of vaporizing raw liquor before and after the heat exchange; And judge the heat exchange effect of plate-type heat exchanger, the temperature out of regulating vaporizing raw liquor flow control water of condensation and vaporizing raw liquor according to the import and export temperature of heat transferring medium.
On the vaporizing raw liquor pipeline of first plate-type heat exchanger 4, second plate-type heat exchanger 5, pressure warning unit 11 is being set; Measure the pressure reduction that vaporizing raw liquor gets into first plate-type heat exchanger 4, second plate-type heat exchanger, 5 front and back; Judge the situation that scabs of first plate-type heat exchanger 4, the inner plate of second plate-type heat exchanger (5), confirm whether plate cleans or change.
On condensation water pot 1 outlet conduit, conductivity meter 12 is set; Whether its specific conductivity of live steam condensed water that measurement comes from full factory reaches the water quality requirement of oiler feed; The water of condensation of specific conductivity qualified (specific conductivity≤5 μ S/cm, 25 ℃) is directly delivered to the boiler house as boiler replenishing water, the defective (specific conductivity＞5 μ S/cm of specific conductivity after the heat exchange cooling; 25 ℃) water of condensation in the good condensate draining that is pumped to the vaporizing raw liquor workshop, use hot water, formation water quality safety bypass flow process as each workshop of full factory.
On the first vaporizing raw liquor pump 7, the second vaporizing raw liquor pump 8, frequency transformer is set; Vaporizing raw liquor flow to getting into first plate-type heat exchanger 4, second plate-type heat exchanger 5 is regulated; With the live steam condensed water flow matches, make temperature after the live steam condensed water heat exchange cooling below 95 ℃.
Liquidometer 9 is set on condensation water pot 1; Water of condensation liquid level in the condensation water pot 1 is monitored measurement; During high liquid level warning valve opening on the inlet pipe of condensation water pot 1 is turned down; During low liquid level warning valve opening on the outlet pipe of first condensate pump 2, second condensate pump 3 is turned down, make liquid level in the condensation water pot 1 in normal range.
Do not reclaim the flow process of heat energy compares with the direct back boiler of general live steam condensed water room cooling decompression; Flow process of the present invention is simple; Though increased heat-exchanger rig, reduced the reducing-and-cooling plant of the former usefulness of boiler systems, so facility investment be few; And heat energy can be recycled effectively, its energy-saving effect and remarkable in economical benefits.The present invention has not only solved each workshop live steam condensed water heat energy recycle problem of alumina producer; Live steam condensed water cooling decompression and heat-energy losses of causing before getting into the boiler house have been avoided; Simultaneously; The present invention can improve temperature of vaporizing raw liquor effectively, has practiced thrift the required live steam consumption of evaporator station heating evaporation stoste, thereby has reduced the production energy consumption of aluminum oxide.
Description of drawings
Fig. 1 is a schematic flow sheet of the present invention.
Among the figure, A representes to add thermalization stillness of night live steam condensed water pipe by decomposing tubular heat exchanger, and B representes to come the live steam condensed water pipe by evaporator station; C representes to come the live steam condensed water pipe by preparatory desiliconization; D representes the allotment of circulating mother liquor storage tank with pipe, and E representes the boiler house with pipe, and F representes the good water of condensation barrel of devaporation stoste and washing; G representes the devaporation station with pipe, and H representes to come the mother liquor pipe by decomposing the seminal fluid heat exchange.
Embodiment
Embodiments of the invention: as shown in Figure 1; It is that the live steam condensed water and the heat-exchange equipment of vaporizing raw liquor that first plate-type heat exchanger 4, second interchanger 5 come as each workshop section of alumina producer (comprise evaporator station, desiliconization in advance, decompose tubular heat exchanger etc.) is set in the vaporizing raw liquor workshop, thereby realization is with the heat energy recycle of live steam condensed water.The live steam condensed water (about 158 ℃) that comes from each workshop section of full factory is delivered to first plate-type heat exchanger 4, second interchanger 5 through first condensate pump 2, second condensate pump 3 and is that vaporizing raw liquor carries out heat exchange from the seed precipitation solution that decomposes through condensation water pot 1 compiles after, the live steam condensed water after the cooling is delivered to the boiler house as boiler replenishing water.Part vaporizing raw liquor is delivered to through the first vaporizing raw liquor pump 7 and is directly delivered to evaporator station after 4 heat exchange of first plate-type heat exchanger heat up as the evaporation charging; Part vaporizing raw liquor is delivered to deliver to after 5 heat exchange of second plate-type heat exchanger heat up through the second vaporizing raw liquor pump 8 and is joined mining mother liquor as raw material after the circulating mother liquor storage tank is allocated.On first plate-type heat exchanger 4, second interchanger, 5 charging and discharging pipes, TM 10 is set, controls the drop temperature of vaporizing raw liquor and live steam condensed water through the flow of the first speed control by frequency variation vaporizing raw liquor pump 7, the second speed control by frequency variation vaporizing raw liquor pump 8.On the vaporizing raw liquor charging and discharging pipe of first plate-type heat exchanger 4, second interchanger 5, pressure warning unit 11 is set, judges whether to clean or change plate through input and output material pressure reduction.On condensation water pot 1 outlet pipe, conductivity meter 12 is set; Qualified (the specific conductivity≤5 μ S/cm of specific conductivity; 25 ℃) water of condensation after first plate-type heat exchanger 4, second interchanger, 5 heat exchange cooling, deliver to the boiler house as boiler replenishing water; The water of condensation of specific conductivity defective (specific conductivity＞5 μ S/cm, 25 ℃) directly send the good condensate draining in vaporizing raw liquor workshop as full station-service hot water, forms water quality safety bypass flow process.Liquidometer 9 is set on condensation water pot 1; Water of condensation liquid level in the condensation water pot 1 is monitored measurement; During high liquid level warning valve opening on the inlet pipe of condensation water pot 1 is turned down, during low liquid level warning valve opening on the outlet pipe of first condensate pump 2, second condensate pump 3 is turned down.
Claims (8)
1. the method for full factory live steam condensed water heat energy recycle in the alumina producing; It is characterized in that: the temperature that full factory is come everywhere is that 150 ℃～160 ℃ live steam condensed waters compile into condensation water pot (1); Through cold first water extraction pump (2), second water extraction pump (3) live steam condensed water is delivered to respectively in first plate-type heat exchanger (4), second plate-type heat exchanger (5) and be that vaporizing raw liquor the vaporizing raw liquor storage tank (6) carries out heat exchange from decomposing the seed precipitation solution that comes; The heat exchange of live steam condensed water temperature is cooled to below 95 ℃, and temperature of vaporizing raw liquor is warming up to more than 92 ℃.
2. the method for full factory live steam condensed water heat energy recycle in the alumina producing according to claim 1; It is characterized in that: compile after first plate-type heat exchanger (4), second plate-type heat exchanger (5) heat exchange are delivered to after lowering the temperature in the deoxygenator of boiler house of heat power plant from the live steam condensed water of evaporator station, in advance desiliconization, the heating of decompositionizations clear liquid, the water of condensation after the cooling is directly as boiler replenishing water.
3. the method for full factory live steam condensed water heat energy recycle in the alumina producing according to claim 1; It is characterized in that: a part of vaporizing raw liquor is delivered to through the first vaporizing raw liquor pump (7) and is delivered to evaporator station after first plate-type heat exchanger (4) heat exchange heats up as the evaporation charging, and a part of vaporizing raw liquor is delivered to through the second vaporizing raw liquor pump (8) and delivered to the circulating mother liquor storage tank after second plate-type heat exchanger (5) heat exchange heats up as circulating mother liquor allotment usefulness.
4. the method for full factory live steam condensed water heat energy recycle in the alumina producing according to claim 1; It is characterized in that: on the water of condensation import and export of first plate-type heat exchanger (4), second plate-type heat exchanger (5) and vaporizing raw liquor import and export pipeline, TM (10) is set, measures water of condensation and temperature of vaporizing raw liquor before and after the heat exchange; And judge the heat exchange effect of plate-type heat exchanger, the temperature out of regulating vaporizing raw liquor flow control water of condensation and vaporizing raw liquor according to the import and export temperature of heat transferring medium.
5. the method for full factory live steam condensed water heat energy recycle in the alumina producing according to claim 1; It is characterized in that: on the vaporizing raw liquor pipeline of first plate-type heat exchanger (4), second plate-type heat exchanger (5), pressure warning unit (11) is being set; Measure the pressure reduction that vaporizing raw liquor gets into first plate-type heat exchanger (4), second plate-type heat exchanger (5) front and back; Judge the situation that scabs of first plate-type heat exchanger (4), the inner plate of second plate-type heat exchanger (5), confirm whether plate cleans or change.
6. the method for full factory live steam condensed water heat energy recycle in the alumina producing according to claim 1; It is characterized in that: on condensation water pot (1) outlet conduit, conductivity meter (12) is set; Whether its specific conductivity of live steam condensed water that measurement comes from full factory reaches the water quality requirement of oiler feed; The water of condensation that specific conductivity is qualified is directly delivered to the boiler house as boiler replenishing water after the heat exchange cooling; The underproof water of condensation of specific conductivity is used hot water as each workshop of full factory in the good condensate draining that is pumped to the vaporizing raw liquor workshop, form water quality safety bypass flow process.
7. the method for full factory live steam condensed water heat energy recycle in the alumina producing according to claim 3; It is characterized in that: on the first vaporizing raw liquor pump (7), the second vaporizing raw liquor pump (8), frequency transformer is set; Vaporizing raw liquor flow to getting into first plate-type heat exchanger (4), second plate-type heat exchanger (5) is regulated; With the live steam condensed water flow matches, make temperature after the live steam condensed water heat exchange cooling below 95 ℃.
8. the method for full factory live steam condensed water heat energy recycle in the alumina producing according to claim 1; It is characterized in that: liquidometer (9) is set on condensation water pot (1); Water of condensation liquid level in the condensation water pot (1) is monitored measurement; During high liquid level warning valve opening on the inlet pipe of condensation water pot (1) is turned down; When hanging down liquid level warning valve opening on the outlet pipe of first condensate pump (2), second condensate pump (3) is turned down, make the interior liquid level of condensation water pot (1) in normal range.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010106050398A CN102557090A (en) | 2010-12-26 | 2010-12-26 | Method for recycling heat energy of new steam condensed water in whole plant during alumina production |
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| CN2010106050398A CN102557090A (en) | 2010-12-26 | 2010-12-26 | Method for recycling heat energy of new steam condensed water in whole plant during alumina production |
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| CN102557090A true CN102557090A (en) | 2012-07-11 |
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Cited By (4)
| 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 |
| CN112344756A (en) * | 2020-09-24 | 2021-02-09 | 靖西天桂铝业有限公司 | Unqualified new steam condensate water waste heat utilization and secondary recovery method |
| CN112429756A (en) * | 2020-12-17 | 2021-03-02 | 中铝国际工程股份有限公司 | Method and device for controlling temperature of first decomposition tank |
| CN114754600A (en) * | 2022-03-21 | 2022-07-15 | 三江化工有限公司 | Steam condensate water heat recycling system in storage and transportation system |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040107835A1 (en) * | 2002-12-04 | 2004-06-10 | Malatak William A | Method and apparatus for treating synthesis gas and recovering a clean liquid condensate |
| CN1796281A (en) * | 2004-12-29 | 2006-07-05 | 贵阳铝镁设计研究院 | Method for raising temperature of vaporizing raw liquor |
| CN2805873Y (en) * | 2005-04-26 | 2006-08-16 | 贵阳铝镁设计研究院 | Apparatus for improving raw liquor evaporation temperature |
-
2010
- 2010-12-26 CN CN2010106050398A patent/CN102557090A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040107835A1 (en) * | 2002-12-04 | 2004-06-10 | Malatak William A | Method and apparatus for treating synthesis gas and recovering a clean liquid condensate |
| CN1796281A (en) * | 2004-12-29 | 2006-07-05 | 贵阳铝镁设计研究院 | Method for raising temperature of vaporizing raw liquor |
| CN2805873Y (en) * | 2005-04-26 | 2006-08-16 | 贵阳铝镁设计研究院 | Apparatus for improving raw liquor evaporation temperature |
Cited By (5)
| 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 |
| CN112344756A (en) * | 2020-09-24 | 2021-02-09 | 靖西天桂铝业有限公司 | Unqualified new steam condensate water waste heat utilization and secondary recovery method |
| CN112429756A (en) * | 2020-12-17 | 2021-03-02 | 中铝国际工程股份有限公司 | Method and device for controlling temperature of first decomposition tank |
| CN114754600A (en) * | 2022-03-21 | 2022-07-15 | 三江化工有限公司 | Steam condensate water heat recycling system in storage and transportation system |
| CN114754600B (en) * | 2022-03-21 | 2022-12-09 | 三江化工有限公司 | Steam condensate water heat recycling system in storage and transportation system |
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Application publication date: 20120711 |