CN103922529A - Low-energy-consumption device for recycling hydrochloric acid waste water and method for recycling hydrochloric acid waste water - Google Patents
Low-energy-consumption device for recycling hydrochloric acid waste water and method for recycling hydrochloric acid waste water Download PDFInfo
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- CN103922529A CN103922529A CN201410157059.1A CN201410157059A CN103922529A CN 103922529 A CN103922529 A CN 103922529A CN 201410157059 A CN201410157059 A CN 201410157059A CN 103922529 A CN103922529 A CN 103922529A
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Abstract
The invention relates to a low-energy consumption device for recycling hydrochloric acid waste water and a method for recycling hydrochloric acid waste water. The device comprises a cooling absorber 5, a water jet pump 6, a waste acid tank1, a triple effect evaporator 2, a twice effect evaporator 3, a once effect hydrochloric acid desorption tower 4, wherein the waste acid tank1, the triple effect evaporator 2, the twice effect evaporator 3 and the once effect hydrochloric acid desorption tower 4 are connected in sequence, the cooling absorber 5 is connected with the twice effect evaporator 3; the water jet pump 6 is connected with the triple effect evaporator 2. According to the invention, only 0.3MPa steam is introduced into a once effect heating room 42 of the once effect hydrochloric acid desorption tower 4, then water steam containing hydrogen chloride steamed out from the one effect hydrochloric acid desorption tower 4 is taken as a heat source of the twice effect evaporator 3, and similarly, the water steam containing hydrogen chloride of the twice effect evaporator 3 is taken as the heat source of the triple effect evaporator 2, so that the heat energy of the steam is utilized for three times repeatedly, and the energy consumption can be reduced. According to the invention, 22% hydrochloric acid and 31% hydrochloric acid can be obtained as required at the same time.
Description
Technical field
The present invention discloses a kind of method that less energy-consumption is reclaimed hydrochloric acid waste water device and reclaimed hydrochloric acid waste water.
Background technology
According to environmental requirement, originally the waste hydrochloric acid that enters sewerage can not at will be discharged again, this just makes the unit processing such as make metal material surface of hydrochloric acid, in production process, can produce the chemical industry of waste hydrochloric acid, as: the units such as epoxy chloropropane, Titanium Dioxide Produced by Chloride Procedure, are faced with the problem that how to solve waste hydrochloric acid.Under without a kind of apple, often adopt following two kinds of methods to process.
1, in waste water, add lime, neutralization generates calcium chloride, then pass through successively 1st effective evaporator, 2nd effect evaporator, triple-effect evaporator, climbing-film evaporator, falling-film evaporator, finally through fluidized bed dryer, dewater, require in process of production 1.1MPa steam, final dewatering will be with 300 ℃ of above warm airs, and energy consumption is very big, and technical process is long, investment is large, as Fig. 1.
If 2 waste hydrochloric acid concentration > 22%, adopt traditional hydrochloric acid desorption device 7 to carry out desorption, as Fig. 2, but final concentration of hydrochloric acid of discharging is at 22%(, this is because hydrochloric acid and water are azeotropic points when 22% left and right, cannot be separated by ordinary method), this concentration is that 22% hydrochloric acid still will be processed by neutralisation, makes calcium chloride as above-mentioned.
Summary of the invention
The object of the invention is to overcome the defect existing in prior art, provide that a kind of device flow process is short, less investment, energy consumption reduce, make hydrochloric acid again to utilize greatly, and the less energy-consumption that can stop defective discharge of wastewater is reclaimed hydrochloric acid waste water device and is reclaimed the method for hydrochloric acid waste water.
The present invention is achieved in that a kind of less energy-consumption recovery hydrochloric acid waste water device, it is characterized in that: comprise spent acid tank 1, triple-effect evaporator 2,2nd effect evaporator 3, an effect hydrochloric acid desorption tower 4, cooling absorber 5, water jet pump 6; The material liquid outlet 11 of described spent acid tank 1 is connected with the triple effect heating chamber opening for feed 21 of described triple-effect evaporator 2, the triple effect gas-liquid separator liquid outlet 22 of described triple-effect evaporator 2 is connected with two effect heating chamber opening for feeds 31 of described 2nd effect evaporator 3, two effect gas-liquid separator liquid outlets 32 of described 2nd effect evaporator 3 are connected with an effect fluid inlet 41 of a described effect hydrochloric acid desorption tower 4, and an effect heating chamber 42 of a described effect hydrochloric acid desorption tower 4 is provided with steam-in 43;
One effect steam outlet 44 of a described effect hydrochloric acid desorption tower 4 is connected with two effect heating chamber steam inlets 33 of described 2nd effect evaporator 3, two effect non-condensable gas outlets 34 of described 2nd effect evaporator 3 are connected with described cooling absorber 5, two effect gas-liquid separator steam outlets 35 of described 2nd effect evaporator 3 are connected with the triple effect heating chamber steam inlet 23 of described triple-effect evaporator 2, and the triple effect gas-liquid separator steam outlet 24 of described triple-effect evaporator 2 is connected with described water jet pump 6;
Described 2nd effect evaporator 3 is provided with two effect condensation acid outlets 36.
The feed liquid fluid inlet 12 of described spent acid tank 1 is connected with discharge opeing outlet 45 at the bottom of the tower of triple effect condensation acid outlet 25, the one effect hydrochloric acid desorption tower 4 of described triple-effect evaporator 2 respectively.
The method of the recovery hydrochloric acid waste water of hydrochloric acid waste water device is reclaimed in a kind of less energy-consumption as above, it is characterized in that: in containing the described spent acid tank 1 of hydrochloride waste, add magnesium chloride to form mixed solution, in an effect heating chamber 42 of a described effect hydrochloric acid desorption tower 4, pass into 0.3MPa steam, the water vapour steaming in a described effect hydrochloric acid desorption tower 4 is as the thermal source of described 2nd effect evaporator 3 simultaneously;
Mixed solution in described spent acid tank 1 enter triple-effect evaporator 2 concentrated after, entering described 2nd effect evaporator 3 further evaporates, then enter a described effect hydrochloric acid desorption tower 4, the hydrochloride waste that enters a described effect hydrochloric acid desorption tower 4 under the effect of described magnesium chloride continues evaporation, steams the hydrochloric acid that hydrogenchloride and water vapour and concentration are less than 1%, and the hydrogenchloride steaming and water vapour enter described 2nd effect evaporator 3 by a described effect steam outlet 44; Because the existence of magnesium chloride has destroyed the azeotropic point of hydrochloric acid when 22% concentration, so the nearly all hydrogenchloride in an effect hydrochloric acid desorption tower 4 enters gas phase, all become gas, in liquid, only leave concentration less than 1% hydrochloric acid, this concentration be less than 1% hydrochloric acid by the tower of a described effect hydrochloric acid desorption tower 4 at the bottom of discharge opeing outlet 45 discharge.Wherein the consumption of magnesium chloride with enter an effect hydrochloric acid desorption tower 4 in the concentration hydrochloric acid that is 22% the mole number of containing hydrogen chloride identical.
The a part of condensation in described 2nd effect evaporator 3 of described hydrogenchloride and water vapour forms the salt acid condensation acid that concentration is 22% and discharges by described two effect condensation acid outlets 36; Another part of described hydrogenchloride and water vapour forms with the water vapour of hydrogenchloride and by described two effect gas-liquid separator steam outlets 35 and enters triple-effect evaporator 2 after described 2nd effect evaporator 3 evaporations; Hydrogenchloride non-condensable gas in described 2nd effect evaporator 4 enters described cooling absorber 5 by described two effect non-condensable gases outlets 34, and in described cooling absorber 5, adding concentration is that 22% hydrochloric acid makes the hydrochloric acid that the further concentrated cooling formation concentration of described hydrogenchloride non-condensable gas is 33%;
The described water vapour with hydrogenchloride from 2nd effect evaporator 33 provides thermal source for described triple-effect evaporator 2, it is 10% salt acid condensation acid by described triple effect condensation acid outlet 25 discharges that the part of the described water vapour with hydrogenchloride in triple-effect evaporator 2 is condensed into concentration, the further evaporation of another part of the described water vapour with hydrogenchloride by described triple-effect evaporator 2 forms the water vapour gas mixture that contains micro-hydrogenchloride or pure water vapour and by described triple effect gas-liquid separator steam outlet 24, enters that to form pH value after described water jet pump 6 condensations be 6 ~ 7 water of condensation, finally discharge,
Above process constantly circulates.
In a described effect hydrochloric acid desorption tower 4 concentration be less than 1% hydrochloric acid by described tower at the bottom of discharge opeing outlet 45 enter in described spent acid tank 1 and reclaim.
In described triple-effect evaporator 2, be condensed into concentration and be 10% salt acid condensation acid, by described triple effect condensation acid outlet 25, enter in described spent acid tank 1 and reclaim.
Under the effect of described water jet pump 6, described triple-effect evaporator 2 is worked under temperature is 55 ℃, vacuum 0.08MPa condition.
The invention has the beneficial effects as follows: the moisture content after concentration and evaporation is discharged through water jet pump 6 by triple-effect evaporator 2, and because temperature is low, material concentration is low, therefore it is very micro-to steam the hydrogen chloride content of moisture content, reaching PH6~7 can discharge; The present invention only passes into 0.3MPa steam in an effect heating chamber 42 of an effect hydrochloric acid desorption tower 4, then the water vapor (containing hydrogen chloride) steaming in an effect hydrochloric acid desorption tower 4 is as the thermal source of 2nd effect evaporator 3, the water vapor (containing hydrogen chloride) of same 2nd effect evaporator 3 is again as the thermal source of three vaporizers 2, the heat energy of steam has been recycled three times, therefore reduced energy consumption; Can obtain as required in the present invention concentration simultaneously and be the hydrochloric acid that 22% hydrochloric acid and concentration are 31%.
Accompanying drawing explanation
Fig. 1 is the frame structure schematic diagram of a kind of common structure in prior art.
Fig. 2 is another kind of conventional structural representation in prior art.
Fig. 3 is structural representation of the present invention.
Wherein: 1, spent acid tank; 2, triple-effect evaporator; 3,2nd effect evaporator; 4, an effect hydrochloric acid desorption tower; 5, cooling absorber; 6, water jet pump; 11, material liquid outlet; 12, feed liquid fluid inlet; 21, triple effect heating chamber opening for feed; 22, triple effect gas-liquid separator liquid outlet; 23, triple effect heating chamber steam inlet; 24, triple effect gas-liquid separator steam outlet; 25, triple effect condensation acid outlet; 31, two effect heating chamber opening for feeds; 32, two effect gas-liquid separator liquid outlets; 33, two effect heating chamber steam inlets; 34, two effect non-condensable gas outlets; 35, two effect gas-liquid separator steam outlets; 36, two effect condensation acid outlets; 41, an effect fluid inlet; 4, an effect heating chamber; 43, steam-in; 44, an effect steam outlet; 45, discharge opeing outlet at the bottom of tower.
Embodiment
According to Fig. 3, hydrochloric acid waste water device is reclaimed in less energy-consumption of the present invention, comprises spent acid tank 1, triple-effect evaporator 2,2nd effect evaporator 3, an effect hydrochloric acid desorption tower 4, cooling absorber 5, water jet pump 6.The material liquid outlet 11 of described spent acid tank 1 is connected with the triple effect heating chamber opening for feed 21 of described triple-effect evaporator 2, the triple effect gas-liquid separator liquid outlet 22 of described triple-effect evaporator 2 is connected with two effect heating chamber opening for feeds 31 of described 2nd effect evaporator 3, two effect gas-liquid separator liquid outlets 32 of described 2nd effect evaporator 3 are connected with an effect fluid inlet 41 of a described effect hydrochloric acid desorption tower 4, and an effect heating chamber 42 of a described effect hydrochloric acid desorption tower 4 is provided with steam-in 43.
One effect steam outlet 44 of a described effect hydrochloric acid desorption tower 4 is connected with two effect heating chamber steam inlets 33 of described 2nd effect evaporator 3, two effect non-condensable gas outlets 34 of described 2nd effect evaporator 3 are connected with described cooling absorber 5, two effect gas-liquid separator steam outlets 35 of described 2nd effect evaporator 3 are connected with the triple effect heating chamber steam inlet 23 of described triple-effect evaporator 2, and the triple effect gas-liquid separator steam outlet 24 of described triple-effect evaporator 2 is connected with described water jet pump 6; Described 2nd effect evaporator 3 is provided with two effect condensation acid outlets 36.Under the effect of described water jet pump 6, described triple-effect evaporator 2 is worked under temperature is 55 ℃, vacuum 0.08MPa condition.
The feed liquid fluid inlet 12 of described spent acid tank 1 is connected with discharge opeing outlet 45 at the bottom of the tower of triple effect condensation acid outlet 25, the one effect hydrochloric acid desorption tower 4 of described triple-effect evaporator 2 respectively.
The method of the recovery hydrochloric acid waste water of hydrochloric acid waste water device is reclaimed in a kind of less energy-consumption as above: in containing the described spent acid tank 1 of hydrochloride waste, add magnesium chloride to form mixed solution, in an effect heating chamber 42 of a described effect hydrochloric acid desorption tower 4, pass into 0.3MPa steam, the water vapour steaming in a described effect hydrochloric acid desorption tower 4 is as the thermal source of described 2nd effect evaporator 3 simultaneously.
Under the effect of described water jet pump 6, described triple-effect evaporator 2 is worked under temperature is 55 ℃, vacuum 0.08MPa condition.
Mixed solution in described spent acid tank 1 enter triple-effect evaporator 2 concentrated after, entering described 2nd effect evaporator 3 further evaporates, then enter a described effect hydrochloric acid desorption tower 4, the hydrochloride waste that enters a described effect hydrochloric acid desorption tower 4 under the effect of described magnesium chloride continues evaporation, steams the hydrochloric acid that hydrogenchloride and water vapour and concentration are less than 1%, and the hydrogenchloride steaming and water vapour enter described 2nd effect evaporator 3 by a described effect steam outlet 44; Because the existence of magnesium chloride has destroyed the azeotropic point of hydrochloric acid when 22% concentration, so the nearly all hydrogenchloride in an effect hydrochloric acid desorption tower 4 enters gas phase, all become gas, in liquid, only leave the hydrochloric acid that concentration is less than 1%; Wherein the consumption of magnesium chloride with enter an effect hydrochloric acid desorption tower 4 in the concentration hydrochloric acid that is 22% the mole number of containing hydrogen chloride identical.In a described effect hydrochloric acid desorption tower 4, concentration is less than 1% the direct recovery of hydrochloric acid or is entered in described spent acid tank 1 and reclaimed by discharge opeing outlet 45 at the bottom of described tower.
The a part of condensation in described 2nd effect evaporator 3 of described hydrogenchloride and water vapour forms the salt acid condensation acid that concentration is 22% and discharges by described two effect condensation acid outlets 36; Another part of described hydrogenchloride and water vapour forms with the water vapour of hydrogenchloride and by described two effect gas-liquid separator steam outlets 35 and enters triple-effect evaporator 2 after described 2nd effect evaporator 3 evaporations; Hydrogenchloride non-condensable gas in described 2nd effect evaporator 4 enters described cooling absorber 5 by described two effect non-condensable gases outlets 34, and in described cooling absorber 5, adding concentration is that 22% hydrochloric acid makes the hydrochloric acid that the further concentrated cooling formation concentration of described hydrogenchloride non-condensable gas is 33%;
The described water vapour with hydrogenchloride from 2nd effect evaporator 33 provides thermal source for described triple-effect evaporator 2, it is 10% salt acid condensation acid by described triple effect condensation acid outlet 25 discharges that the part of the described water vapour with hydrogenchloride in triple-effect evaporator 2 is condensed into concentration, and it is directly reclaimed or entered in described spent acid tank 1 and reclaim, the further evaporation of another part of the described water vapour with hydrogenchloride by described triple-effect evaporator 2 forms the water vapour gas mixture that contains micro-hydrogenchloride or pure water vapour and by described triple effect gas-liquid separator steam outlet 24, enters that to form pH value after described water jet pump 6 condensations be 6 ~ 7 water of condensation, finally discharge, above process constantly circulates.
1, the present invention enters the steam heating evaporation of the containing hydrogen chloride that triple-effect evaporator 2 sends here via 2nd effect evaporator 3 add magnesium chloride in spent acid tank 1 after, the water vapor producing is due to low-temperature evaporation (55 ℃), institute's containing hydrogen chloride is atomic, and its PH is discharged by water jet pump 6 suctions 6~7.Because of water jet pump 6 effect, triple-effect evaporator 2 is worked under 55 ℃, vacuum 0.08MPa condition, and the heating chamber inner condensat liquid concentration of hydrochloric acid of triple-effect evaporator 2 is 10%, can return to spent acid tank 1 by triple effect condensation acid outlet 25.
2, the spent acid solution after concentrated via triple-effect evaporator 2 enters 2nd effect evaporator 3, the steam heating evaporation of the containing hydrogen chloride that the spent acid solution after concentrated in 2nd effect evaporator 3 is sent here via an effect hydrochloric acid desorption tower 4, the water vapor producing in 2nd effect evaporator 3 is done thermal source for triple-effect evaporator 2, in 2nd effect evaporator 3 heating chambers, condensation hydrochlorate acid concentration is 22%, and the condensation hydrochlorate acid that this concentration is 22% is discharged and reclaimed by two effect condensation acid outlet 36.Non-condensable gas (being mainly hydrogenchloride) in described 2nd effect evaporator 3 heating chambers removes the hydrochloric acid that hydrochloric acid cooling and absorbing that cooling absorber 5 use concentration are 22% is 31% to desired concn.
3, the concentration of hydrochloric acid after 2nd effect evaporator 3 is concentrated is 22%, and the hydrochloric acid of this concentration and water form azeotrope in the prior art, cannot be separated.And the present invention is owing to having added magnesium chloride in spent acid tank 1, destroy its azeotropic point, thereby the hydrochloric acid that concentration is 22% can continue to steam hydrogenchloride an effect hydrochloric acid desorption tower 4 is interior, nearly all hydrogenchloride in an effect hydrochloric acid desorption tower 4 enters gas phase, all become gas, thereby make liquid effluent content of hydrochloric acid < 1% at the bottom of the tower of an effect hydrochloric acid desorption tower 4, and return to spent acid tank 1 by discharge opeing outlet 45 at the bottom of tower.The consumption of described magnesium chloride with enter an effect hydrochloric acid desorption tower 4 in the concentration hydrochloric acid that is 22% the mole number of containing hydrogen chloride identical.
The moisture content of concentration and evaporation of the present invention (water vapour) is discharged through the suction of described water jet pump 6 by the triple effect gas-liquid separator steam outlet 24 of triple-effect evaporator 2, and because temperature is low, material concentration is low, therefore it is very micro-to steam moisture content hydrogen chloride content, PH6~7 can be discharged.
The present invention only passes into 0.3MPa steam in an effect heating chamber 42 of an effect hydrochloric acid desorption tower 4, then the water vapor (containing hydrogen chloride) steaming in an effect hydrochloric acid desorption tower 4 is as the thermal source of 2nd effect evaporator 3, the water vapor (containing hydrogen chloride) of same 2nd effect evaporator 3 is again as the thermal source of three vaporizers 2, the heat energy of steam has been recycled three times, therefore reduced energy consumption; Can obtain as required in the present invention concentration simultaneously and be the hydrochloric acid that 22% hydrochloric acid and concentration are 31%.
Claims (6)
1. a hydrochloric acid waste water device is reclaimed in less energy-consumption, it is characterized in that: comprise spent acid tank (1), triple-effect evaporator (2), 2nd effect evaporator (3), an effect hydrochloric acid desorption tower (4), cooling absorber (5), water jet pump (6); The material liquid outlet (11) of described spent acid tank (1) is connected with the triple effect heating chamber opening for feed (21) of described triple-effect evaporator (2), the triple effect gas-liquid separator liquid outlet (22) of described triple-effect evaporator (2) is connected with two effect heating chamber opening for feeds (31) of described 2nd effect evaporator (3), two effect gas-liquid separator liquid outlets (32) of described 2nd effect evaporator (3) are connected with an effect fluid inlet (41) of a described effect hydrochloric acid desorption tower (4), and an effect heating chamber (42) of a described effect hydrochloric acid desorption tower (4) is provided with steam-in (43);
One effect steam outlet (44) of a described effect hydrochloric acid desorption tower (4) is connected with two effect heating chamber steam inlets (33) of described 2nd effect evaporator (3), two effect non-condensable gas outlets (34) of described 2nd effect evaporator (3) are connected with described cooling absorber (5), two effect gas-liquid separator steam outlets (35) of described 2nd effect evaporator (3) are connected with the triple effect heating chamber steam inlet (23) of described triple-effect evaporator (2), and the triple effect gas-liquid separator steam outlet (24) of described triple-effect evaporator (2) is connected with described water jet pump (6);
Described 2nd effect evaporator (3) is provided with two effect condensation acid outlets (36).
2. according to less energy-consumption described in claim 1, reclaim hydrochloric acid waste water device, it is characterized in that: the feed liquid fluid inlet (12) of described spent acid tank (1) respectively with the triple effect condensation acid outlet (25) of described triple-effect evaporator (2), at the bottom of the tower of an effect hydrochloric acid desorption tower (4) discharge opeing outlet (45) be connected.
3. the method for the recovery hydrochloric acid waste water of hydrochloric acid waste water device is reclaimed in a less energy-consumption as described in claim 1, it is characterized in that: in containing the described spent acid tank (1) of hydrochloride waste, add magnesium chloride to form mixed solution, in an effect heating chamber (42) of a described effect hydrochloric acid desorption tower (4), pass into 0.3MPa steam, the water vapour steaming in a described effect hydrochloric acid desorption tower (4) is as the thermal source of described 2nd effect evaporator (3) simultaneously;
Mixed solution in described spent acid tank (1) enter triple-effect evaporator (2) concentrated after, entering described 2nd effect evaporator (3) further evaporates, then enter a described effect hydrochloric acid desorption tower (4), the hydrochloride waste that enters a described effect hydrochloric acid desorption tower (4) under the effect of described magnesium chloride continues evaporation, steams the hydrochloric acid that hydrogenchloride and water vapour and concentration are less than 1%, and the hydrogenchloride steaming and water vapour enter described 2nd effect evaporator (3) by a described effect steam outlet (44); Described concentration be less than 1% hydrochloric acid by the tower of a described effect hydrochloric acid desorption tower 4 at the bottom of discharge opeing outlet 45 discharge;
The a part of condensation in described 2nd effect evaporator (3) of described hydrogenchloride and water vapour forms the salt acid condensation acid that concentration is 22% and discharges by described two effect condensation acid outlets (36); Another part of described hydrogenchloride and water vapour forms with the water vapour of hydrogenchloride and by described two effect gas-liquid separator steam outlets (35) and enters triple-effect evaporator (2) after described 2nd effect evaporator (3) evaporation; Hydrogenchloride non-condensable gas in described 2nd effect evaporator (4) enters described cooling absorber (5) by described two effect non-condensable gases outlets (34), and in described cooling absorber (5), adding concentration is that 22% hydrochloric acid makes the hydrochloric acid that the further concentrated cooling formation concentration of described hydrogenchloride non-condensable gas is 33%;
The described water vapour with hydrogenchloride from 2nd effect evaporator (33) is that described triple-effect evaporator (2) provides thermal source, it is 10% salt acid condensation acid by described triple effect condensation acid outlet (25) discharge that the part of the described water vapour with hydrogenchloride in triple-effect evaporator (2) is condensed into concentration, the further evaporation of another part of the described water vapour with hydrogenchloride by described triple-effect evaporator (2) forms the water vapour gas mixture that contains micro-hydrogenchloride or pure water vapour and by described triple effect gas-liquid separator steam outlet (24), enters that to form pH value after described water jet pump (6) condensation be 6 ~ 7 water of condensation, finally discharge,
Above process constantly circulates.
4. the method for the recovery hydrochloric acid waste water of hydrochloric acid waste water device is reclaimed in less energy-consumption according to claim 3, it is characterized in that: in a described effect hydrochloric acid desorption tower (4) concentration be less than 1% hydrochloric acid by described tower at the bottom of discharge opeing outlet (45) enter recovery in described spent acid tank (1).
5. the method for the recovery hydrochloric acid waste water of hydrochloric acid waste water device is reclaimed in less energy-consumption according to claim 3, it is characterized in that: in described triple-effect evaporator (2), be condensed into concentration and be 10% salt acid condensation acid, by described triple effect condensation acid outlet (25), enter in described spent acid tank (1) and reclaim.
6. the method for the recovery hydrochloric acid waste water of hydrochloric acid waste water device is reclaimed in less energy-consumption according to claim 3, it is characterized in that: under the effect of described water jet pump (6), described triple-effect evaporator (2) is worked under temperature is 55 ℃, vacuum 0.08MPa condition.
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Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104711617A (en) * | 2015-04-09 | 2015-06-17 | 南通晨光石墨设备有限公司 | Regeneration method of acid washing waste acids |
CN106966365A (en) * | 2017-03-29 | 2017-07-21 | 天津富友创新环保科技有限公司 | A kind of triple effect evaporation spent acid processing system |
CN108862196A (en) * | 2018-07-03 | 2018-11-23 | 青海盐湖工业股份有限公司 | A kind of method and system parsing hydrogen chloride from containing hydrogen chloride solution |
CN109052323A (en) * | 2018-09-10 | 2018-12-21 | 李晓垚 | A kind of HCl recovery concentrating regenerative method |
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Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102285641A (en) * | 2010-06-21 | 2011-12-21 | 南通星球石墨设备有限公司 | Recycling process of waste hydrochloric acid |
CN102502500A (en) * | 2011-11-07 | 2012-06-20 | 韩扶军 | Device for producing hydrogen chloride by resolving hydrochloric acid |
CN203436836U (en) * | 2013-08-13 | 2014-02-19 | 常州泰特环境设备工程有限公司 | Efficient and energy-saving type three-effect negative-pressure graphite evaporative crystallization device of hydrochloric acid pickling waste liquid |
CN203668169U (en) * | 2014-04-19 | 2014-06-25 | 上海亿华科技有限公司 | Low energy consumption hydrochloric acid wastewater recycling device |
-
2014
- 2014-04-19 CN CN201410157059.1A patent/CN103922529B/en active Active
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102285641A (en) * | 2010-06-21 | 2011-12-21 | 南通星球石墨设备有限公司 | Recycling process of waste hydrochloric acid |
CN102502500A (en) * | 2011-11-07 | 2012-06-20 | 韩扶军 | Device for producing hydrogen chloride by resolving hydrochloric acid |
CN203436836U (en) * | 2013-08-13 | 2014-02-19 | 常州泰特环境设备工程有限公司 | Efficient and energy-saving type three-effect negative-pressure graphite evaporative crystallization device of hydrochloric acid pickling waste liquid |
CN203668169U (en) * | 2014-04-19 | 2014-06-25 | 上海亿华科技有限公司 | Low energy consumption hydrochloric acid wastewater recycling device |
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Publication number | Priority date | Publication date | Assignee | Title |
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CN104711617A (en) * | 2015-04-09 | 2015-06-17 | 南通晨光石墨设备有限公司 | Regeneration method of acid washing waste acids |
CN106966365A (en) * | 2017-03-29 | 2017-07-21 | 天津富友创新环保科技有限公司 | A kind of triple effect evaporation spent acid processing system |
CN108862196A (en) * | 2018-07-03 | 2018-11-23 | 青海盐湖工业股份有限公司 | A kind of method and system parsing hydrogen chloride from containing hydrogen chloride solution |
CN108862196B (en) * | 2018-07-03 | 2021-12-21 | 青海盐湖工业股份有限公司 | Method and system for resolving hydrogen chloride from solution containing hydrogen chloride |
CN109052323A (en) * | 2018-09-10 | 2018-12-21 | 李晓垚 | A kind of HCl recovery concentrating regenerative method |
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CN109231167B (en) * | 2018-09-10 | 2020-08-04 | 绍兴玖越智能装备有限公司 | Concentrated regenerating unit of hydrochloric acid |
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