CN201762103U - Separating system for inorganic acid and inorganic acid salt in waste acid - Google Patents
Separating system for inorganic acid and inorganic acid salt in waste acid Download PDFInfo
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- CN201762103U CN201762103U CN2010205068417U CN201020506841U CN201762103U CN 201762103 U CN201762103 U CN 201762103U CN 2010205068417 U CN2010205068417 U CN 2010205068417U CN 201020506841 U CN201020506841 U CN 201020506841U CN 201762103 U CN201762103 U CN 201762103U
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Abstract
The utility model relates to a separating system for inorganic acid and inorganic acid salt in waste acid, which comprises a raw acid groove, a resin desalter, a middle groove, a cartridge filter, a high-pressure pump, a nanofiltration membrane filter and an acid cleaning groove. A resin exchanging bed is arranged in the resin desalter. The separating system adopts the resin desalter to remove the salt and other dissolved substances in the waste acid; the raw acid with reduced salinity is separated into clear acid and salt concentration acid through the nanofiltration membrane, and the salt concentration acid returns to the resin desalter to circularly separate salty substances. The separating system avoids resource waste caused by neutralization through adding alkali or evaporation concentration processing method, and effectively solves the problems caused by the resin separating technology that the clear acid volume is expanded and the nanofiltration membrane technology can not be suitable for processing the acid solution with high salt concentration. The separating system is suitable for processing sulfuric acid solution with high salt concentration generated by the sulfuric acid industry, the smelting industry and the sulfuric acid downstream industry, and is suitable for separating the nitric acid and the nitrate, as well as separating the hydrochloric acid and the chloride.
Description
Technical field
The utility model relates to the separation system of mineral acid and inorganic acid salt in a kind of spent acid, specifically relates to a kind of separation sulfuric acid and vitriol, nitric acid and nitrate, hydrochloric acid and muriatic separation system.
Background technology
In the gas cleaning process of gas washing in SA production, can produce a certain amount of spent acid; In the sulfuric acid method titanium pigment production process, also can produce a large amount of dense spent acid; When metals such as hydrometallurgy electrolysis (or electrodeposition) copper, nickel, cobalt, can produce a certain amount of high salt spent acid.At present, the common method of handling these spent acid is to add lime neutralization or evaporation concentration.The former causes the sulfuric acid wasting of resources, produces the secondary pollution that contains the heavy metal gypsum tailings in a large number.Evaporation concentration is handled the energy consumption height, and the sulfuric acid that obtains is impure, can influence secondary and use.At sulfuric acid with aspect vitriol separates, development abroad two kinds of technology, a kind of is resin method, another kind is acidproof Nanofiltering membrane.Resin method adopts the resins exchange bed, is full of the resin that can adsorb strong acid in the exchange bed.When saliferous sulfuric acid when the resin layer, sulfuric acid can be by the temporary transient absorption of resin and the aqueous solution of vitriol and other salt is not crossed resin layer by resin absorption (or absorption is seldom).Be about to be released when flowing out when the sulfuric acid of resin absorption reaches capacity, oppositely enter resin layer, wash sulfuric acid with clear water.This separation method, guarantee sulfuric acid concentration descend be not more than 15% and the sulfuric acid loss be not higher than under 15% the prerequisite, its sulfuric acid and vitriol separation efficiency are 50-70%.Its shortcoming is to add water to cause the volume of brine waste and clear acid to expand.Advantage is that separating effect is not influenced by sulfate concentration.Often sulfate concentration is high more, and the resin isolation effect is good more.Adopt separately resin method to handle above-mentioned several spent acid, be subjected to that separation efficiency is not high to influence the reuse requirement that can't satisfy spent acid.
Acid proof nanofiltration membrane, its acidproof concentration can anti-sulfuric acid 25%, and the separation rate of sulfuric acid and vitriol is at 95-98%, the normal running conditions of nanofiltration membrane be vitriol can not be saturated in concentration process, fouling or crystallization.The concentration of simultaneously treated vitriol can not be too high, can not make nanofiltration membrane osmotic pressure be higher than the maximum working pressure (MWP) of this film of 4.5MPa.Be subjected to the influence of nanofiltration membrane to the feed liquor requirement, many spent acid do not satisfy the working conditions of nanofiltration membrane and can not handle with nanofiltration.
The utility model content
The purpose of this utility model is to overcome the defective of above-mentioned prior art, and a kind of separation system of handling complicated component, salt concentration than higher spent acid is provided, and can use as resource after making sulfuric acid purification, reduces three waste discharge.
For achieving the above object, the technical solution adopted in the utility model is:
The separation system of mineral acid and inorganic acid salt in a kind of spent acid is characterized in that: comprise former acid tank, resin desalination device, medial launder, security personnel's strainer, high-pressure pump, nanofiltration membrane strainer and clear acid tank; Be provided with the resins exchange bed in the resin desalination device, its top is provided with backwashing water import and filtered liquid outlet, and its bottom is provided with ortho acid fluid inlet and elutriant outlet; The outlet of former acid tank is connected through pipeline with the ortho acid fluid inlet of resin desalination device, and the elutriant outlet of resin desalination device is connected through pipeline with medial launder; The outlet of medial launder is connected through pipeline with the inlet of high-pressure pump with the nanofiltration membrane strainer by security personnel's strainer successively; The penetrating fluid outlet of nanofiltration membrane strainer is connected through pipeline with clear acid tank, and the concentrated solution outlet of nanofiltration membrane strainer is connected through pipeline with former acid tank.
Preferable, the outlet of former acid tank is connected through pipeline by the ortho acid fluid inlet of water pump with resin desalination device.
Further, described separation system also comprises the ortho acid input duct, and described former acid tank all is connected with the ortho acid input duct with medial launder.
The spent acid that described spent acid produces in the time of can being metal such as the spent acid that produces in the spent acid, sulfuric acid method titanium pigment production process of the discharging of vitriol works flue gas washing or hydrometallurgy electrolysis (or electrodeposition) copper, nickel, cobalt.Contain mineral acid, inorganic acid salt and other dissolved matters in the described spent acid.According to the source difference of spent acid, wherein contained mineral acid and inorganic acid salt are also inequality.
Described mineral acid is strong acid such as sulfuric acid, nitric acid or hydrochloric acid, and described inorganic acid salt is vitriol, nitrate and muriate.Positively charged ion in the described inorganic acid salt comprises and is not limited in iron ion, magnesium ion, calcium ion, aluminum ion, cupric ion, cadmium ion, nickel ion, the cobalt ion etc. one or more.
The resin of filling in the described resins exchange bed is an adsorbable mineral acid and adsorb the resin of inorganic acid salt and other dissolved matters hardly; And the mineral acid of its absorption can be washed out.When the saliferous spent acid when the resin layer, mineral acid can be by the temporary transient absorption of resin and the aqueous solution of inorganic acid salt and other salt is not crossed resin layer by resin absorption (or absorption is seldom); When the mineral acid of resin absorption reaches full, oppositely enter resin layer with clear water, wash mineral acid.
The nanofiltration membrane of loading in the described nanofiltration membrane strainer is vitriolic nanofiltration membrane that can anti-concentration expressed in percentage by weight 20%, and for example the GE company model of producing is the nanofiltration membrane of NF4040, NF8080 etc.
Described filtration adopts security personnel's strainer also to claim accurate filter, and effect is to prevent that fine particles (as the resin of fragmentation) from entering downstream unit.
The above-mentioned separation system that the utility model provides can be separated the spent acid that contains high salt concentration, can obtain the salts solution of purified acid solution and low acidity respectively, make isolated mineral acid and the salt can be respectively as the utilization of resources, avoided existing and traditional wasting of resources that alkali neutralizes or the evaporation concentration treatment process is caused that adds, and the useless admittedly pollution of the secondary that produces.In addition, separation system of the present utility model is that the resin method isolation technique is combined and improve, develops into a kind of brand new technical with the nanofiltration membrane technology, solved effectively that clear sour volume that the resin isolation technology produces expands and the nanofiltration membrane technology can not be applicable to the problems such as processing of high hydrochloric solution.The utility model is applicable to the processing of the high saliferous sulphuric acid soln of handling sulfuric acid industry, metallurgy industry and the generation of sulfuric acid downstream industry, is applicable to that also nitric acid separates with muriatic with nitrate, hydrochloric acid simultaneously.Sulfuric acid and vitriol, nitric acid and nitrate, hydrochloric acid and muriatic separation efficiency are all greater than 90%.
Description of drawings
Fig. 1 is a process flow sheet of the present utility model.
Embodiment
Embodiment 1:
As shown in Figure 1, the mineral acid that the utility model provides and the separation system of inorganic acid salt comprise former acid tank 2, resin desalination device 6, medial launder 11, security personnel's strainer 13, high-pressure pump 15, nanofiltration membrane strainer 17 and clear acid tank 19; Be provided with the resins exchange bed in the resin desalination device 6, its top is provided with backwashing water import and filtered liquid outlet, and its bottom is provided with ortho acid fluid inlet and elutriant outlet; The outlet of former acid tank 2 is connected through pipeline by the ortho acid fluid inlet of water pump 4 with resin desalination device 6, and the outlet of the elutriant of resin desalination device 6 and medial launder 11 are connected through pipeline; The outlet of medial launder 11 is connected through pipeline with the inlet of high-pressure pump 15 with nanofiltration membrane strainer 17 by security personnel's strainer 13 successively; The outlet of the penetrating fluid of nanofiltration membrane strainer 17 and acid tank clearly 19 are connected through pipeline, and the concentrated solution outlet of nanofiltration membrane strainer 17 and former acid tank 2 are connected through pipeline.
Further, above-mentioned separation system also comprises the ortho acid input duct, and former acid tank 2 all is connected with the ortho acid input duct with medial launder 11.
The separating technology process of above-mentioned separation system is: ortho acid 1 basis is the concentration of contained solvability salt wherein, can all enter in the former acid tank 2, also can enter medial launder 11 by by-passing portions, perhaps all enters medial launder 11.The ortho acid that directly enters medial launder 11 is controlled at and guarantees not have salt crystallization (or fouling) in the nanofiltration membrane concentration process, and osmolality is less than 4.5MPa, otherwise by valve 3 controls, reduces the ortho acid flow that enters medial launder 11, guarantees non-crystallizable.Liquid in the former acid tank 2 is the mixed solution of being made up of ortho acid and nanofiltration membrane concentrated solution.Ejector priming 4 when advancing acid in the resin desalination device 6, open valve 5 and 8, when acid enters resin layer in the desalination device 6 by resin absorption, salt and other dissolved matters pass through resin layer fast, and in the low acid salt solution groove 10 of valve 8 inflows, this salts solution can further be purified and be produced various salt, also can discharge with in the lime and back.When acid is adsorbed when saturated, when promptly detecting acid and passing resin layer and flow out concentration from the top near the 20-40% of ortho acid, valve 5 and 8 is closed in termination of pumping 4, opens valve 7 and 9, and clear water is imported from desalination device top through valve 7, clear acid in the extrusion resin enters medial launder 11, close valve 7 and 9 when the concentration of the acid of discharging when valve 9 is lower than the 20-40% of former acid concentration, restart pump 4, open valve 5 and 8, the desalination device advances ortho acid, so circular flow.
The nanofiltration membrane filtering system is made up of security personnel's strainer 13, high-pressure pump 15, film device 17 and by-pass cock 16,18.Acid after the desalination device is handled and part ortho acid are used to control concentrated solution (salt gelled acid) quantity discharged (control concentrated solution quantity discharged is the 40-60% of high-pressure pump feed liquor amount) with high-pressure pump 15 input nanofiltration membrane strainers 17, valve 18.Nanofiltration membrane sees through liquid and advances acid tank 19 clearly, obtains more purified clear acid (sulfuric acid, nitric acid or hydrochloric acid).
Embodiment 2: certain vitriol works's flue gas washing discharging spent acid.
Adopt embodiment 1 described separation system.
Ortho acid main component: H
2SO
4130g/L, Fe
Always3.2g/L vitriol total amounts such as other metals Ca, Al, Cu, Cd are at 2-4g/L.Ortho acid treatment capacity 100M
3/ D wherein advances former acid tank 60M
3, directly advance medial launder 40M
3Resin method sulfuric acid and vitriol separating device adopt CNIII-2000, and processing power is 160M
3/ D, regeneration clear water 150M
3, the low sour sulfate liquor 150M of row
3, less salt sulphuric acid soln (elutriant) 160M
3The nanofiltration membrane strainer adopts 10 NF8040 series operations, water inlet 200M
3/ D produces clear sour 100M
3/ D; Salt concentrated vitriol solution returns former acid tank.
Operation result: clear acid yield 100M
3/ D, composition H
2SO
4115g/L, Fe
Always51mg/L, other vitriol 38mg/L.Low sour sulfate liquor 150M
3/ D, composition H
2SO
410g/L, Fe
Always20.5g/L, other vitriol 18g/L.
Embodiment 3: certain sulfuric acid method titanium pigment production discharging spent acid
Adopt embodiment 1 described separation system.
Ortho acid main component: H
2SO
4230g/L, Fe
Always27g/L, other Me
Always9.5g/L.Ortho acid treatment capacity 6M
3/ D.Resin method sulfuric acid and vitriol separating device adopt CNIII-500, and a day maximum processing capability is 10M
3/ D.The nanofiltration membrane strainer adopts 2 NF4040 series operations, produces clear sour 6M
3/ D.
Operation result: day clear sour 6M of processing
3/ D, clear acid yield 6M
3/ D, main component H
2SO
4195g/L, Fe
Always442mg/L, other metal M e
Always181mg/L.The low sour sulfate liquor 9M of discharging
3/ D, its composition are H
2SO
423g/L, Fe
Always17.7g/L, other Me
Always6.2g/L.
Claims (3)
1. the separation system of mineral acid and inorganic acid salt in the spent acid is characterized in that: comprise former acid tank, resin desalination device, medial launder, security personnel's strainer, high-pressure pump, nanofiltration membrane strainer and clear acid tank; Be provided with the resins exchange bed in the resin desalination device, its top is provided with backwashing water import and filtered liquid outlet, and its bottom is provided with ortho acid fluid inlet and elutriant outlet; The outlet of former acid tank is connected through pipeline with the ortho acid fluid inlet of resin desalination device, and the elutriant outlet of resin desalination device is connected through pipeline with medial launder; The outlet of medial launder is connected through pipeline with the inlet of high-pressure pump with the nanofiltration membrane strainer by security personnel's strainer successively; The penetrating fluid outlet of nanofiltration membrane strainer is connected through pipeline with clear acid tank, and the concentrated solution outlet of nanofiltration membrane strainer is connected through pipeline with former acid tank.
2. the separation system of mineral acid and inorganic acid salt in the spent acid as claimed in claim 1 is characterized in that: the outlet of described former acid tank is connected through pipeline by the ortho acid fluid inlet of water pump with resin desalination device.
3. the separation system of mineral acid and inorganic acid salt in the spent acid as claimed in claim 1 or 2, it is characterized in that: described separation system also comprises the ortho acid input duct, described former acid tank all is connected with the ortho acid input duct with medial launder.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205068417U CN201762103U (en) | 2010-08-24 | 2010-08-24 | Separating system for inorganic acid and inorganic acid salt in waste acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205068417U CN201762103U (en) | 2010-08-24 | 2010-08-24 | Separating system for inorganic acid and inorganic acid salt in waste acid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201762103U true CN201762103U (en) | 2011-03-16 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010205068417U Expired - Lifetime CN201762103U (en) | 2010-08-24 | 2010-08-24 | Separating system for inorganic acid and inorganic acid salt in waste acid |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101966400A (en) * | 2010-08-24 | 2011-02-09 | 上海西恩化工设备有限公司 | Method for separating inorganic acid and inorganic acid salt in waste acid |
| CN104876362A (en) * | 2015-05-19 | 2015-09-02 | 武汉飞博乐环保工程有限公司 | Acid purification recycling system |
| CN106744721A (en) * | 2016-12-20 | 2017-05-31 | 攀枝花市精研科技有限公司 | The recovery separation method and application of sulfuric acid and dissolubility titanium in titanium white waste acid |
-
2010
- 2010-08-24 CN CN2010205068417U patent/CN201762103U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101966400A (en) * | 2010-08-24 | 2011-02-09 | 上海西恩化工设备有限公司 | Method for separating inorganic acid and inorganic acid salt in waste acid |
| CN104876362A (en) * | 2015-05-19 | 2015-09-02 | 武汉飞博乐环保工程有限公司 | Acid purification recycling system |
| CN104876362B (en) * | 2015-05-19 | 2017-02-01 | 武汉飞博乐环保工程有限公司 | Acid purification recycling system |
| CN106744721A (en) * | 2016-12-20 | 2017-05-31 | 攀枝花市精研科技有限公司 | The recovery separation method and application of sulfuric acid and dissolubility titanium in titanium white waste acid |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: SHANGHAI CN TECHNOLOGY CO., LTD. Free format text: FORMER NAME: XIEN CHEMICAL EQUIPMENT CO., LTD., SHANGHAI |
|
| CP01 | Change in the name or title of a patent holder |
Address after: 201501 Shanghai city Jinshan District Fengjing Industrial Park No. 165 east two ring road Patentee after: Shanghai Xien Technology Co.,Ltd. Address before: 201501 Shanghai city Jinshan District Fengjing Industrial Park No. 165 east two ring road Patentee before: Xien Chemical Equipment Co., Ltd., Shanghai |
|
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Chizhou CN New Material Technology Co., Ltd. Assignor: Shanghai Xien Technology Co.,Ltd. Contract record no.: 2014340000005 Denomination of utility model: Separating system for inorganic acid and inorganic acid salt in waste acid Granted publication date: 20110316 License type: Exclusive License Record date: 20140102 |
|
| LICC | Enforcement, change and cancellation of record of contracts on the licence for exploitation of a patent or utility model | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Chizhou CN New Material Technology Co., Ltd. Assignor: Shanghai Xien Technology Co.,Ltd. Contract record no.: 2014340000005 Denomination of utility model: Separating system for inorganic acid and inorganic acid salt in waste acid Granted publication date: 20110316 License type: Exclusive License Record date: 20140102 |
|
| LICC | Enforcement, change and cancellation of record of contracts on the licence for exploitation of a patent or utility model | ||
| C56 | Change in the name or address of the patentee |
Owner name: SHANGHAI XI'EN TECHNOLOGY CO., LTD. Free format text: FORMER NAME: SHANGHAI CN TECHNOLOGY CO., LTD. |
|
| CP01 | Change in the name or title of a patent holder |
Address after: 201501 Shanghai city Jinshan District Fengjing Industrial Park No. 165 east two ring road Patentee after: Shanghai Sean Polytron Technologies Inc Address before: 201501 Shanghai city Jinshan District Fengjing Industrial Park No. 165 east two ring road Patentee before: Shanghai Xien Technology Co.,Ltd. |
|
| CX01 | Expiry of patent term |
Granted publication date: 20110316 |
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| CX01 | Expiry of patent term |