CN1358668A - Process for finely preparing salt water by tank type counter-flushing liquid filter made of balked polytetrafluorethylene film - Google Patents
Process for finely preparing salt water by tank type counter-flushing liquid filter made of balked polytetrafluorethylene film Download PDFInfo
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Abstract
The method for preparing refined salt water includes the following steps: dissolving salt to saturation, adding sodium hydroxide, and barium chloride, adding oxidant to make pretreatment, through the processes of adsorption, coprecipitation and air-floating action, regulating calcium-magnesium ratio and making it be greater than 1, adding sodium carbonate, feeding the salt water into bulk teflon film tank-type back-flushing liquid filter to make filtration so as to obtain pure refined salt water.
Description
The present invention relates to a kind of method of refined brine, the present invention especially relates to a kind of eptfe film pot type backflush liquid strainer that uses and is feed purification brinish method with sea salt, lake salt, rock salt, bittern water, purified salt.
Basic industry is that saturated brine is made in raw material salt (NaCl) dissolving, carries out electrolysis and produces products such as sodium hydroxide and chlorine.Contain impurity atom and water-fast mechanical impuritys such as a large amount of calcium, magnesium, sulfate radical, organism in the salt solution, must before electrolysis, remove, otherwise can in electrowinning process, cause resin tower resin caking, exchange capacity descends, ionic membrane efficient reduces, have a strong impact on the life-span of ionic membrane, destroy the ordinary production of electrolyzer, influence product quality.Therefore after salt solution needs with chemical process calcium, magnesium, the sulfate radical reaction of ionic state to be become solid, carry out solid-liquid separation.
The at present domestic brine rectification process that generally adopts comprises the following steps:
A) change salt: backflow salt solution and additional clear water enter from changing the salt trench bottom, by salt deposit, change salt to saturated, change the overflow of salt bath top certainly to reactive tank;
B) refining reaction: in reactive tank, add chemical agents such as caustic soda, soda ash, bariumchloride and make calcium ions and magnesium ions, sulfate radical in the salt solution fully react solid matters such as generating magnesium hydroxide, lime carbonate, calcium sulfate, flow out intake duct that settling tank from reactive tank top;
C) gravity settling: solid matter absorption and generation co-precipitation mutually in the Dao Er settling tank, the sedimentation through 20-30 hour, supernatant liquor flows out to the sand-bed filter filtration by settling tank top after the sedimentation, for quickening sedimentation, generally adds settling agents such as sodium polyacrylate;
D) sand filtration: the settling tank supernatant liquor enters from the sand-bed filter bottom, and by layer of sand, solid fine particle is intercepted, and salt solution overflows from sand-bed filter top, can obtain Ca in theory
2+≤ 6mg/l, Mg
2+≤ 2mg/l, the primary brine of SS (solid settlement thing)≤10mg/l, this salt solution is directly used in diaphragm electrolysis in the diaphragm process chlor-alkali, the primary brine secondary refining of still needing in ionic membrane method alkali-chloride;
E) smart filter: carbon pipe filter scribbles alpha-cellulose in advance; primary brine inherent filtration device bottom is squeezed into; solid matter in the salt solution mixes the formation filtering layer with precoated layer; salt solution is expelled to ion exchange resin by filtering layer inherent filtration device top; when filtering layer thickens pressure when excessive, strainer is shut down and is cleaned:
F) ion-exchange: salt solution enters from resin tower top after neutralizing, and flow out the bottom, and the calcium in the secondary brine, magnesium total amount can enter electrolyzer less than 0.02mg/l;
G) press filtration: clarification, sand filtration, smart filter equipment institute salt discharge mud are squeezed into filter press with pump, and mummification becomes mud cake, and liquid returns into system.
There is following shortcoming in this technology:
1. technology instability, it shows:
1) salt matter instability, enterprise is unfixing with the place of production of salt, and NaCl content all has from 85% to 95%, and Ca
2+/ Mg
2+Can＞1 all have to＜1;
2) water quality instability, enterprise water use has underground water, surface water, and is generally not treated, and inorganic in the water, organic impurity (comprising natural organic matters such as bacterium, algae) enriches, and with changing season;
3) operation control is unstable, power supply variations, salt qualitative changeization, crosses alkali number variation, temperature variation, fluctuations in discharge etc. and controls untimelyly, and it is muddy to cause settling tank to return, just insolubles particle diameter and state (as colloid) instability.
2. filter plant imperfection
If adopt natural subsidence, what then most enterprises used is settling tank-sand-bed filter in filtration procedure, and salt solution " whiting " phenomenon is arranged during owing to the technology instability, so even add the salt slurry circulation, also be difficult to avoid fully this phenomenon.If adopt PE pipe strainer, then some enterprise uses the forced filtration form, with further removal Ca
2+, Mg
2+Insolubles, thus satisfy the requirement of diaphram tank brine quality, and its life-span is generally 2-3, but its shortcoming is:
1) strainer easily stops up, and the tens of microns of mean pore size stop particulate by irregular long-channel, and micron-sized insolubles is difficult to stop that big slightly then may stop up the duct;
2) high pressure pulse cleaning, the blowback of 0.5MPa pressurized air causes the PE pipe to come off or damages, and untimely discovery can cause underproof salt solution to enter electrolyzer;
3) complicated operation, a switch one equipment or a few switch one equipment, and blowback troublesome poeration, replace tubes (come off, when damaging) then need be uncapped, and labor capacity is big.
If adopt sintering carbon element pipe, then the ion-exchange membrane electrolyzer more than 85% all can use, and just can satisfy processing requirement, and its operation life is 5-10, but its shortcoming is:
1) working cost height must help filtering layer with alpha-cellulose, nearly 5 yuan of 1 ton of alkali alpha-cellulose expense, and lose a certain amount of salt solution during regeneration, the average alpha-cellulose consumption of industry is 0.31kg/t100%NaOH;
2) complicated operation, precoating (equipment such as precoating jar, precoating pump should be arranged mutually) body feed and blowback complicated operation;
3) the high pressure blowback easily causes pipe loosening, and there is leakage phenomenon at the pad place, causes alpha-cellulose and unfiltered salt solution to enter electrolyzer.
3. large-area precipitation apparatus is huge, and process point control is complicated, influenced greatly by raw material, and labour intensity is big.
4. need special-purpose factory building, long flow path takes up an area of greatly, and the reorganization and expansion difficulty is big.
In addition, in prior art, also disclosed polytetrafluoroethylene film, as at Bacino, a kind of ptfe porous membrane is disclosed in the United States Patent (USP) 403232 of John, its aperture is the 0.05-0.4 micron, bubbling point is 10-60psi, and that polytetrafluoroethylene film is used for brinish was refining but this patent did not disclose.
At the problem that exists in the prior art, the method that the purpose of this invention is to provide a kind of refined brine of novelty, in the solid-liquid separation process of this method, use eptfe film pot type backflush liquid strainer, disposablely obtain purified refined brine, simplified traditional technology, save expense, obtained stable high-quality refined brine.
The objective of the invention is to realize that by method that a kind of refined brine is provided described method comprises the steps: successively
A) change salt to saturated;
B) add sodium hydroxide and bariumchloride, make magnesium ion, sulfate radical and its reaction in the salt solution generate magnesium hydroxide and barium sulfate, wherein the add-on of sodium hydroxide is for making brinish pH value for 10.5-12, the adding mole number of bariumchloride a little less than or equal the mole number of sulfate radical;
C) oxygenant that adds 1-10ppm carries out pre-treatment, through absorption, co-precipitation and air supporting effect, wherein calcium magnesium ratio is adjusted to greater than 1;
D) add yellow soda ash, make the calcium in the salt solution be transformed into lime carbonate;
E) salt solution is sent into eptfe film pot type backflush liquid strainer and filtered the acquisition refined brine.
Aforesaid method also is included in e) step after ion-exchange step.
Eptfe film pot type backflush liquid strainer in the inventive method comprises that cylindrical shell (1), the filter bag of being made by eptfe film are enclosed within filtering element (2), card (3), clear liquid chamber (4 of forming on the cage bone that is covered with aperture) and soiling solution chamber (5).
The mole number of the bariumchloride that adds in step b) in the aforesaid method can lack 0.01 to 0.02 mole than the mole number of sulfate radical.Because bariumchloride is relatively more expensive, concerning manufacturer, can save cost so its add-on is general less in practice.Moreover in salt solution, there be the quality did not influence of very a spot of sulfate radical to refined brine.
Used oxygenant is chlorinated lime, bleaching essence or hydrogen peroxide in the inventive method.
Absorption in the inventive method in the step c), co-precipitation and air supporting effect can adopt air flotation pool to realize.The pre-treatment of this step c) was controlled at 5-30 minute.
The reaction times of step d) is 30 minutes in the inventive method.
In the inventive method in step e) with 0.5-2.5 rice
3/ rice
2Hour speed salt solution is sent into strainer, and filter pressure is 0.02-0.4Mpa.The aperture of wherein said eptfe film is the 0.2-3.0 micron.
The inventive method also comprises step c) and e) in the body refuse that the produces step of carrying out press filtration.
In appended accompanying drawing:
Fig. 1 is the process flow sheet of traditional refined brine;
Fig. 2 is the process flow sheet that the present invention adopts eptfe film pot type backflush liquid strainer refined brine;
Fig. 3 is an eptfe film pot type backflush liquid structure of filter synoptic diagram of the present invention.
Describe the present invention in detail below with reference to above-mentioned accompanying drawing.
As shown in Figure 2, the method for refined brine provided by the invention comprises the steps: successively
A) backflow salt solution and additional clear water are added from changing the salt trench bottom, by salt deposit, change salt to saturated, certainly change the overflow of salt bath top to reactive tank I;
B) in reactive tank I, add NaOH (caustic soda) and barium chloride, make magnesium ion, sulfate radical in the salt solution fully react solid matters such as generating magnesium hydroxide and barium sulfate, its top outflow from reactive tank I is entered preprocessor;
C) because the raw material salt place of production is complicated, quality is unstable, calcium, magnesium are than low, need to carry out preliminary treatment to reacted salt solution, it is usually to add a certain amount of oxidant to realize such as bleaching powder, calcium hypochlorite or hydrogen peroxide in for the preprocessor of flotation tank, in this flotation tank, tentatively remove organic matter, mechanical admixture etc. through absorption, co-precipitation and air supporting effect, the calcium magnesium ratio of gained salt solution is adjusted to greater than 1, the pretreated time is controlled at 5-30 minute according to material quality is unusual, pretreated crude brine is directly squeezed into reactive tank II, this moment, the temperature of salt solution was 50-60 ℃, and solids content is 100-10000ppm, and calcium magnesium ratio is greater than 1;
D) in the salt solution of reactive tank II, add sodium carbonate (soda ash), reacted about 30 minutes, make the calcium in the salt solution be transformed into calcium carbonate fully, squeeze into filter with pump afterwards;
E) with salt solution with 0.5-2.5 rice3/ rice2The speed of hour (namely per hour have on the film of every square metre of area 0.5-2.5 cubic metre salt solution by) is sent salt solution into eptfe film pot type backflush liquid filter and is filtered, the aperture of film is the 0.2-3.0 micron, 0.5-1 micron preferably, this film can be available from W.L.Gore and Associated Inc.. Pressure during filtration is 0.02-0.4Mpa, the bottom of salt solution inherent filtration device enters, the filter bag surface of making by eptfe film afterwards whole solid matter is trapped in the filter bag surface, and as clear as crystal filtrate is from top outlet outflow, this moment, solids content was less than 1mg/l, when filtering time lengthening, when filter cake thickens to a certain degree, the recoil of filter automatic instantaneous, filter cake is pushed away film surface, because polytetrafluoroethylene (PTFE) does not have viscosity, and the filter membrane aperture is tiny, so filter cake can not pierce filter membrane, therefore filter cake can break away from the filter membrane surface fully, deposits to the bottom of filter, so this filter is called pot type backflush liquid filter, when filter cake runs up to when a certain amount of the filter automatic discharge.
Enter from the top of ion-exchanger after neutralization from filter salt solution out, flow out the bottom, and the calcium in the secondary brine, magnesium total amount are less than 0.02mg/l, and the used ion-exchanger of the present invention generally adopts common ion exchange resin. Can enter electrolytic cell from ion exchange resin refined brine out and carry out electrolysis, be used for alkaline.
As shown in Figure 2, method of the present invention also comprises at step c) and e) in the body refuse that the produces step of carrying out press filtration, this step is that the body refuse that will produce after preliminary treatment and filtration press dry in plate and frame type filter-press, and the liquid after the press filtration is back to initial change salt bath, and solid then abandons.
The structure of eptfe film pot type backflush liquid filter of the present invention is shown in Fig. 3, it comprises that cylindrical shell 1, the filter bag of being made by eptfe film are enclosed within filter element 2, card 3, clear liquid chamber 4 and the soiling solution chamber 5 that forms on the cage bone that is covered with aperture, certainly also has automatic control system and atmospheric control (not shown). As shown in Figure 3, the filter tank body is divided into up and down two chambeies, and epicoele is clear liquid chamber 4, cavity of resorption is soiling solution chamber 5, and the centre is separated by a card 3, has several holes on the card, hang a filter element 2 and sealing on each hole, upper and lower cavity can only be linked up by the aperture on the cage bone. During filter work, salt solution passes through 1 with certain speed#Valve enters filter, and through the filtration of film filter bag, clear liquid passes through on filter bag, the cage bone aperture to clear liquid chamber 4, by the outlet discharge. After filtering a period of time, when the filter cake of filter bag film reaches certain thickness, filter pressure raises, filtering traffic reduces, filter enters the backwash membrane stage automatically by automatic valve control, clear liquid in the clear liquid chamber 4 is towards soiling solution chamber 5 reverse flow, and the filter cake on filter bag surface is recoiled, and is deposited to the conical lower portion of filter. System reenters filtration condition. When the bottom filter cake runs up to when a certain amount of, system opens bottom 6 automatically#Valve, filter cake is discharged rapidly.
Fig. 1 is compared with Fig. 2, the difference that can find out technique of the present invention and traditional handicraft is, the present invention replaces sedimentation basin → sand filter → carbon pipe filter in the prior art with preprocessor → reactive tank II → pot type backflush liquid filter, as described in this paper foregoing, the sand filter in the prior art and carbon pipe filter have many unfavorable shortcomings. And eptfe film pot type backflush liquid filter of the present invention adopts the eptfe film filter bag to carry out surface filtration, this thin-film material has splendid chemical stability, splendid not viscosity and very little coefficient of friction and broad operating temperature range, and it is porous, the aperture is very little, be generally the 0.2-3.0 micron, this filter bag can not produce clogging basically, solid impurity nearly all in the liquid all is trapped within the filter bag surface, it is as clear as crystal that filtrate remains, filter efficiency can reach more than 99.5%, the solids content of refined brine is less than 1mg/l, one step was filtered the salt solution index that can reach after former flow process essence is filtered, greatly shorten rectification flow, simplified traditional handicraft. And used whole filter process is a kind of physical process in the inventive method, there is not chemical reaction, be not subjected to the impact of external factor, guaranteed that brine quality is stable, calcium content can be low to moderate 0 in the salt solution that the inventive method is made with extra care, and content of magnesium also can be low to moderate 0, and both total amounts can be lower than 1mg/L, greatly improved the quality of refined brine, for follow-up Electrolytic Alkali provides high-quality raw material. In addition, method of the present invention is simple to operate, and Automatic Control is compared with traditional handicraft and to have been saved cleaning settling tank, sand filter, accurate filter, greatly reduces hand labor power, has shortened flow process, has saved expense. Moreover, adopt preprocessor to eliminate the unsettled problem of material quality, slowed down the operation fluctuation to follow-up refining impact.
The present invention will be described further by following embodiment, but what should understand is that the present invention is not limited thereto.In described embodiment, the eptfe membrane that strainer adopted is all available from W.L.Gore andAssociated Inc., and remaining chemical is the product of buying on the general market.
Embodiment 1
With the about 290g/L bittern of saliferous aquation sea salt, the backflow salt aquation sea salt of the about 290g/L of saliferous, pH＞11, in changing the salt pond with these two kinds of saturated brines by the saturated brine that is mixed into 1L at 1: 1, wherein calcium contents is 546.6mg/L, Mg content is 16.7mg/L, SS content is 2895.03mg/L, and sulfate radical content is 5g/L.This saturated brine is sent into reactive tank I, add 0.26g caustic soda and 12g bariumchloride, make magnesium ion and sulfate radical in the salt solution fully react generation magnesium hydroxide and barium sulfate.This salt solution is entered from air flotation pool bottom inlet, add chlorinated lime 20mg, handle the pH value transferred to 10.5 in 5 minutes through absorption, co-precipitation and air supporting, calcium magnesium ratio is 1.5, and salt solution overflows from air flotation pool top, and 80% solid matter particle diameter is greater than 1.0 microns in the salt solution.Salt solution enters reactive tank II, and add 1.6g soda ash this moment, made the calcium in the salt solution be transformed into lime carbonate in about 30 minutes.Selecting the aperture is 1.0 microns eptfe film (with trade(brand)name TS 611 available from W.L.Gore and Associated Inc.), and salt solution is with 0.5 meter
3/ rice
2Hour enter from the tank filter fluid inlet, filter pressure is 0.02Mpa, and the clear liquid after the filtration is expelled to follow-up ion-exchange from top.With ICP method (plasma emission spectrometry) salt solution after filtering is tested, calcium does not detect, and Mg content is 1.5mg/L, and SS does not detect, and the results are shown in Table 1.
Press the identical mode refined brine of embodiment 1, different is to replenish backflow salt solution salt with service water, and the calcium contents of crude brine is 813.2mg/L, and Mg content is 778.2mg/L, and SS content is 6812.57mg/L, and sulfate radical content is 15g/L.This saturated brine of 1L is sent into reactive tank I, add 2.8g caustic soda and 34g bariumchloride, make magnesium ion and sulfate radical in the salt solution fully react generation magnesium hydroxide and barium sulfate.This salt solution is entered from air flotation pool bottom inlet, add the smart 30mg of bleaching, handle the pH value transferred to 11.36 in 15 minutes through absorption, co-precipitation and air supporting, calcium magnesium ratio is 1.8, salt solution overflows from air flotation pool top, and 80% solid matter particle diameter is greater than 0.5 micron in the salt solution.Salt solution enters reactive tank II, and add 2.2g soda ash this moment, made the calcium in the salt solution be transformed into lime carbonate in about 30 minutes.Selecting the aperture is 0.5 micron eptfe film (with trade(brand)name TN 611 available from W.L.Gore and AssociatedInc.), and salt solution is with 0.87 meter
3/ rice
2Hour enter from the tank filter fluid inlet, filter pressure is 0.12Mpa, and the clear liquid after the filtration is expelled to follow-up ion-exchange from top.With the ICP method salt solution after filtering is tested, calcium does not detect, and Mg content is 1.7mg/L, and SS content is 0.16mg/L, and the results are shown in Table 1.
Press the identical mode refined brine of embodiment 1, different is to replenish backflow salt aquation lake salt with underground water, and the calcium contents of crude brine is 539.9mg/L, and Mg content is 545.3mg/L, and SS content is 5098.21mg/L, and sulfate radical content is 10g/L.This saturated brine of 1L is sent into reactive tank I, add 2.0g caustic soda and 23g bariumchloride, make magnesium ion and sulfate radical in the salt solution fully react generation magnesium hydroxide and barium sulfate.This salt solution is entered from air flotation pool bottom inlet, add the smart 20mg of bleaching, handle the pH value transferred to 11.08 in 30 minutes through absorption, co-precipitation and air supporting, calcium magnesium ratio is 1.3, salt solution overflows from air flotation pool top, and 80% solid matter particle diameter is greater than 1.0 microns in the salt solution.Salt solution enters reactive tank II, and add 1.6g soda ash this moment, made the calcium in the salt solution be transformed into lime carbonate in about 30 minutes.Selecting the aperture is 1.0 microns eptfe film (with trade(brand)name TS 611 available from W.L.Gore and AssociatedInc.), and salt solution is with 2.01 meters
3/ rice
2Hour enter from the tank filter fluid inlet, filter pressure is 0.09Mpa, and the clear liquid after the filtration is expelled to follow-up ion-exchange from top.With the ICP method salt solution after filtering is tested, calcium does not detect, and Mg content is 0.56mg/L, and SS does not detect, and the results are shown in Table 1.
Embodiment 4
Press the identical mode refined brine of embodiment 1, different is to use the halogen hydratable salt, and the calcium contents of crude brine is 114.8mg/L, and Mg content is 21.3mg/L, and SS content is 712.02mg/L, and sulfate radical content is 5g/L.This saturated brine of 1L is sent into reactive tank I, add 0.27g caustic soda and 12g bariumchloride, make magnesium ion and sulfate radical in the salt solution fully react generation magnesium hydroxide and barium sulfate.This salt solution is entered from air flotation pool bottom inlet, add hydrogen peroxide 5mg, handle the pH value transferred to 11.2 in 10 minutes through absorption, co-precipitation and air supporting, calcium magnesium ratio is 1.2, and salt solution overflows from air flotation pool top, and 80% solid matter particle diameter is greater than 3.0 microns in the salt solution.Salt solution enters reactive tank II, and add 0.7g soda ash this moment, made the calcium in the salt solution be transformed into lime carbonate in about 30 minutes.Selecting the aperture is 3.0 microns eptfe film (with trade(brand)name TX 611 available from W.L.Gore and Associated Inc.), and salt solution is with 2.5 meters
3/ rice
2Hour enter from the tank filter fluid inlet, filter pressure is 0.4Mpa, and the clear liquid after the filtration is expelled to follow-up ion-exchange from top.With the ICP method salt solution after filtering is tested, calcium, magnesium and SS all do not detect, and the results are shown in Table 1.
Press the identical mode refined brine of embodiment 1, different is with aquation rock salt from the beginning, and the calcium contents of crude brine is 623.4mg/L, and Mg content is 1116.3mg/L, and SS content is 6996.78mg/L, and sulfate radical content is 5g/L.This saturated brine of 1L is sent into reactive tank I, add 3.9g caustic soda and 12g bariumchloride, make magnesium ion and sulfate radical in the salt solution fully react generation magnesium hydroxide and barium sulfate.This salt solution is entered from air flotation pool bottom inlet, add chlorinated lime 50mg, handle the pH value transferred to 12 in 10 minutes through absorption, co-precipitation and air supporting, calcium magnesium ratio is 1.6, and salt solution overflows from air flotation pool top, and 80% solid matter particle diameter is greater than 0.2 micron in the salt solution.Salt solution enters reactive tank II, and add 1.8g soda ash this moment, made the calcium in the salt solution be transformed into lime carbonate in about 30 minutes.Selecting the aperture is 0.2 micron eptfe film (with trade(brand)name TK 611 available from W.L.Gore and Associated Inc.), and salt solution is with 0.53 meter
3/ rice
2Hour enter from the tank filter fluid inlet, filter pressure is 0.38Mpa, and the clear liquid after the filtration is expelled to follow-up ion-exchange from top.With the ICP method salt solution after filtering is tested, calcium does not detect, and Mg content is 2.04mg/L, and SS content is 0.23mg/L, and the results are shown in Table 1.
Comparative Examples 1
Salt solution is identical with embodiment 1, adopts traditional process for refining, enters settling tank after promptly salt solution reacts completely, sedimentation 16 hours, clear liquid are flowed out from settling tank top and are primary brine, and wherein calcium contents is 6.6mg/L, Mg content is 1.35mg/L, and SS content is 6.92mg/L.Primary brine enters carbon fibre pipe strainer and filters, and cleaner liquid is a secondary brine, and wherein calcium contents is 0.81mg/L, and Mg content is 1.25mg/L, and SS content is 1.12mg/L.
To handle 50 tons of/hour salt solution is example, and relatively the inventive method and traditional method will reach the required investment of same refined brine quality, running cost etc., and the results are shown in Table 2.In table 2, as 1, embodiment 2 and Comparative Examples 1 and 2 are compared with it with the required investment of alkaline purification salt solution per ton among the embodiment 1.In like manner, " ton alkali equipment take up an area of than ", " ton alkali working cost than " all with embodiment 1 required as 1, remaining embodiment is by comparison.
Comparative Examples 2
Salt solution is identical with embodiment 2, adopts traditional process for refining, enters settling tank after promptly salt solution reacts completely, sedimentation 10-20 hour, clear liquid flowed out from settling tank top and is primary brine, and wherein calcium contents is 2.11mg/L, Mg content is 7.13mg/L, and SS content is 8.25mg/L.Primary brine enters carbon pipe filter and filters, and cleaner liquid is a secondary brine, and wherein calcium contents is 0.15mg/L, and Mg content is 2.57mg/L, and SS content is 1.44mg/L.
To handle 10 tons of/hour salt solution is example, and relatively the inventive method and traditional method will reach the required investment of same refined brine quality, running cost etc., and the results are shown in Table 2.
The data of embodiment 1-5 are compared with the data of Comparative Examples 1-2, can clearly be seen that the method that adopts refined brine of the present invention can disposable acquisition calcium, the magnesium total amount is less than 3mg/L, SS content is less than the salt solution of 1mg/L, and if embodiment 1 required investment cost is counted 1, Comparative Examples 1 and 2 is respectively 3.20 and 3.41, that is to say that the required investment cost of traditional method is more than 3 times of the inventive method, same equipment occupation of land of the present invention and working cost are all more much smaller than the traditional method.
Table 1
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 | |||
| The salt solution source | Bittern adds backflow salt solution | Service water adds backflow salt solution | Underground water adds backflow salt solution | Bittern | Tap water | ||
| The crude brine quality | Calcium (mg/L) | ????546.6 | ?????813.2 | ????539.9 | ????114.8 | ????623.4 | |
| Magnesium (mg/L) | ????16.7 | ?????778.2 | ????545.3 | ????21.3 | ???1116.3 | ||
| SS(mg/L) | ???2895.03 | ????6812.57 | ???5098.21 | ???712.02 | ???6996.78 | ||
| Solids plasmid particle diameter (80% particle) (micron) | ????＞1.0 | ????＞0.5 | ???＞1.0 | ???＞3.0 | ????＞0.2 | ||
| The dosage of oxygenant (mg/L) | ?????20 | ??????30 | ????20 | ?????5 | ?????50 | ||
| The pH value of crude brine | ????10.5 | ????11.36 | ???11.08 | ????11.2 | ?????12 | ||
| Eptfe film aperture (micron) | ????1.0 | ?????0.5 | ????1.0 | ????3.0 | ????0.2 | ||
| Salt solution enters the speed (rice of strainer 3/ rice 2Hour) | ????0.5 | ?????0.87 | ????2.01 | ????2.5 | ????0.53 | ||
| Filter pressure (Mpa) | ????0.02 | ?????0.12 | ????0.09 | ????0.4 | ????0.38 | ||
| The refined brine quality | Calcium (mg/L) | ?????0 | ??????0 | ?????0 | ?????0 | ?????0 | |
| Magnesium (mg/L) | ????1.5 | ?????1.7 | ????0.56 | ?????0 | ????2.04 | ||
| SS(mg/L) | ?????0 | ?????0.16 | ?????0 | ?????0 | ????0.23 | ||
Table 2
| Embodiment 1 | Embodiment 2 | Comparative Examples 1 | Comparative Examples 2 | ||
| The salt solution source | Bittern adds backflow salt solution | Service water adds backflow salt solution | Bittern adds backflow salt solution | Service water adds backflow salt solution | |
| The crude brine quality | Calcium (mg/L) | ?????546.6 | ?????813.2 | ?????546.6 | ?????813.2 |
| Magnesium (mg/L) | ?????16.7 | ?????778.2 | ?????16.7 | ?????778.2 | |
| SS(mg/L) | ????2895.03 | ????6812.57 | ????2895.03 | ????6812.57 | |
| The salt water yield (m 3/h) | ??????50 | ??????100 | ??????50 | ??????100 | |
| The refined brine quality | Calcium (mg/L) | ??????0 | ???????0 | ?????0.81 | ??????0.15 |
| Magnesium (mg/L) | ?????1.5 | ??????1.7 | ?????1.25 | ??????2.57 | |
| SS(mg/L) | ??????0 | ?????0.16 | ?????1.12 | ??????1.44 | |
| Ton alkali output investment ratio | ??????1 | ?????1.09 | ?????1.45 | ??????1.54 | |
| Ton alkali equipment takes up an area of ratio | ??????1 | ?????1.02 | ?????3.20 | ??????3.41 | |
| Ton alkali working cost ratio | Medicament expense | ??????1 | ?????1.16 | ?????4.33 | ??????4.67 |
| Upkeep cost | ??????1 | ?????1.12 | ?????1.20 | ??????1.34 | |
Claims (11)
1. the method for a refined brine, it comprises the steps: successively
A) change salt to saturated;
B) add sodium hydroxide and bariumchloride, make magnesium ion, sulfate radical and its reaction in the salt solution generate magnesium hydroxide and barium sulfate, wherein the add-on of sodium hydroxide is for making brinish pH value for 10.5-12, the adding mole number of bariumchloride a little less than or equal the mole number of sulfate radical;
C) oxygenant that adds 1-10ppm carries out pre-treatment, through absorption, co-precipitation and air supporting effect, wherein calcium magnesium ratio is adjusted to greater than 1;
D) add yellow soda ash, make the calcium in the salt solution be transformed into lime carbonate;
E) salt solution is sent into eptfe film pot type backflush liquid strainer and filtered the acquisition refined brine.
2. the method for claim 1, it also is included in e) ion-exchange step after the step.
3. the method for claim 1, wherein eptfe film pot type backflush liquid strainer comprises that cylindrical shell (1), the filter bag of being made by eptfe film are enclosed within filtering element (2), card (3), clear liquid chamber (4 of forming on the cage bone that is covered with aperture) and soiling solution chamber (5).
4. the method for claim 1, few 0.01 to 0.02 mole of the mole number of the mole ratio sulfate radical of the bariumchloride that wherein in step b), adds.
5. as claim 1 or 3 described methods, wherein said oxygenant is chlorinated lime, bleaching essence or hydrogen peroxide.
6. as claim 1 or 3 described methods, the wherein absorption in the step c), co-precipitation and air supporting effect adopt air flotation pool to reach.
7. as claim 1 or 3 described methods, wherein the pre-treatment of step c) was controlled at 5-30 minute.
8. as claim 1 or 3 described methods, wherein the reaction times of step d) is 30 minutes.
9. as claim 1 or 3 described methods, wherein in step e) with 0.5-2.5 rice
3/ rice
2Hour speed salt solution is sent into strainer, and filter pressure is 0.02-0.4Mpa.
10. as claim 1 or 3 described methods, the aperture of wherein said eptfe film is the 0.2-3.0 micron.
11. the method for claim 1, it also comprises step c) and e) in the body refuse that the produces step of carrying out press filtration.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001278533A CN1147429C (en) | 2000-12-12 | 2000-12-12 | Process for finely preparing salt water by tank type counter-flushing liquid filter made of balked polytetrafluorethylene film |
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| Application Number | Priority Date | Filing Date | Title |
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| CNB001278533A CN1147429C (en) | 2000-12-12 | 2000-12-12 | Process for finely preparing salt water by tank type counter-flushing liquid filter made of balked polytetrafluorethylene film |
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| CN1358668A true CN1358668A (en) | 2002-07-17 |
| CN1147429C CN1147429C (en) | 2004-04-28 |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102070160A (en) * | 2009-11-20 | 2011-05-25 | 天津渤天化工有限责任公司 | Device for producing alkali by using purified salt |
| CN102923736A (en) * | 2012-10-22 | 2013-02-13 | 戈尔工业品贸易（上海）有限公司 | Processing method for refining industrial brine |
| CN103274550A (en) * | 2013-06-17 | 2013-09-04 | 广西大学 | Brine impurity removal method in sodium chlorate production technology |
| CN103288104A (en) * | 2013-06-26 | 2013-09-11 | 河南城建学院 | Method for removing odor of refined salt through ferric salt |
| WO2017049467A1 (en) * | 2015-09-21 | 2017-03-30 | 江苏久吾高科技股份有限公司 | Brine refining method and device based on membrane technology |
| CN113699542A (en) * | 2021-08-05 | 2021-11-26 | 苏州清缘环保科技有限公司 | H2O2Continuous electrochemical synthesis system |
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Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100460326C (en) * | 2006-03-15 | 2009-02-11 | 南京九思高科技有限公司 | Method of refining salt by membrane filtration |
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2000
- 2000-12-12 CN CNB001278533A patent/CN1147429C/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102070160A (en) * | 2009-11-20 | 2011-05-25 | 天津渤天化工有限责任公司 | Device for producing alkali by using purified salt |
| CN102923736A (en) * | 2012-10-22 | 2013-02-13 | 戈尔工业品贸易（上海）有限公司 | Processing method for refining industrial brine |
| CN103274550A (en) * | 2013-06-17 | 2013-09-04 | 广西大学 | Brine impurity removal method in sodium chlorate production technology |
| CN103288104A (en) * | 2013-06-26 | 2013-09-11 | 河南城建学院 | Method for removing odor of refined salt through ferric salt |
| CN103288104B (en) * | 2013-06-26 | 2014-12-03 | 河南城建学院 | Method for removing odor of refined salt through ferric salt |
| WO2017049467A1 (en) * | 2015-09-21 | 2017-03-30 | 江苏久吾高科技股份有限公司 | Brine refining method and device based on membrane technology |
| CN113699542A (en) * | 2021-08-05 | 2021-11-26 | 苏州清缘环保科技有限公司 | H2O2Continuous electrochemical synthesis system |
| CN113699541A (en) * | 2021-08-05 | 2021-11-26 | 苏州清缘环保科技有限公司 | H2O2Continuous electrochemical synthesis method |
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|---|---|
| CN1147429C (en) | 2004-04-28 |
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