CN102730879B - A kind of method of continuous preparation essence halogen - Google Patents
A kind of method of continuous preparation essence halogen Download PDFInfo
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Abstract
nullA kind of method that the invention discloses continuous preparation essence halogen，It includes that continuous raw material mixes、Demagging continuously、Deliming continuously、Continuous sedimentation and sedimentary naturally collection are discharged，Salt passes through successive reaction、Continuous sedimentation、Essence halogen is prepared after the continuous processing technology such as continuous clarification，Realize the novel technique of a kind of salt continuous purification，Ensure that under reactive state, the concentration of each composition is relative to stable equilibrium，Object wave moves，Be conducive to the carrying out of reaction，Decrease the response time,Ensure that material hybrid reaction has time enough and disclosure satisfy that the environment of reaction，Just reach the basic content requirement controlling to be issued to salt removing calcium and magnesium impurity within certain response time at this conditional,While successive reaction，Also there occurs that sedimentary part settles，It is not required to mechanical force，Flow velocity and fluidised form is relied on to realize the purpose of mixed flocculation，Alleviate the clarification load of defecator，Simultaneously precipitate by step by step share precipitation capacity，Be conducive to the smooth discharge of waste residue.
Description
Technical field
The present invention relates to a kind of water purification process, particularly to a kind of method preparing essence halogen.
Background technology
In raw brine in addition to Main Ingredients and Appearance NaCl, also Ca2+、Mg2+、SO4 2-Etc. plurality of impurity ions.The most purified raw brine directly goes salt manufacturing or carries nitre, has CaSO in preheating and evaporation process4、Ca(CO3)2、Mg(OH)2Generating Deng slightly solubility impurity, the enrichment of various compounds will result in equipment and tube wall incrustation, reduces heat transfer efficiency, increases energy consumption, affects salt manufacturing product quality.
Therefore first should purify salt before evaporating, be conducive to extending the cycle of operation of vacuum salt making facility, reduce operating cost, improve the effective rate of utilization of device, steady production, reduction consume, reduce labor strength, improve product quality and production capacity.
Bittern purifying includes the sport technique segment such as chemical technology and process unit, in terms of chemical process technology link: the mode of bittern purifying has a variety of, and wherein that conventional is two alkaline process, lime-soda method and Calx-Natrii Sulfas-CO2Method etc..Current domestic salt making enterprises uses two alkaline process or lime-soda method purified brine, and emerging Calx-Natrii Sulfas-CO mostly2Method, such as the Chinese patent of Application No. 200710057151.0.Caustic soda and the soda price added due to first two method are higher, and the calcium, the magnesium ion content that contain in salt are high, and the amount needing Caustic soda and soda is relatively big, causes purifying cost high.The latter then needs substantial amounts of CO2, the time of reaction is longer, and reaction rate waits deficiency more slowly.
For existing calcium and magnesium type bittern purifying treatment technology, mostly use Calx-Natrii Sulfas-CO2Method is as chemistry dominant response method.Using clearance-type reactive mode that salt is carried out purified treatment, the reactor of employing is intermittent reaction bucket (still).Its basic technology principle is raw brine and the solution rich in sulfate, load in sufficiently large reaction container according to certain ratio, and stirring is allowed to mix, Calx is passed into equipped with blended raw brine with rich in sulfate (mother solution after digestion, Natrii Sulfas) reaction container in, it is allowed to fully react, after question response certain time, add flocculant and carry out the sedimentary clarification of demagging, it is allowed to clarification and obtains primary salt, through pump, the supernatant primary salt in first order reaction bucket is rotated in secondary response bucket, then carbonated gas it is passed through, (using bubbling device bubbling) secondary response starts reaction, after certain time, a small amount of soda ash solution is added in the secondary response liquid that unreacted completes, again after secondary response, add flocculant, carry out the sedimentary clarification of deliming, just essence halogen is obtained after clarification.When the supernatant of I and II all flows into next operation, the discharge work of waste residue at different levels need to be carried out.Clearance-type mode essence is that several reactants are reacted as in different ratio successively loading reaction container, question response touches the mark and completes experiment when requiring, carry out flocculant interpolation again, it is followed by clarification process, its main reaction unit is the reaction container of batch (-type) running, specifically include that turning barrel in mother solution storage cylinder, primary response bucket, lime cream, turning barrel, (essence halogen bucket) etc. in slag.Clearance-type mode essence is that several reactants are reacted as in different ratio successively loading reaction container, and question response touches the mark and completes experiment when requiring, then carries out flocculant interpolation, is followed by clarification process.From the point of view of currently used news, although intermittent reaction mode has single treatment amount up to thousands of cubes, the advantages such as equipment is simple, but have that reaction vessel is more, course of reaction is longer, floor space is less compared with treating capacity in big, unit interval, feed time is compared with the deficiency such as long, instantaneous delivery is big, instantaneous load is big.
External vacuum salt production produces, and major part carries out Ca to raw brine2+、Mg2+Purified treatment.As Rumanian Buddhist comes just, the saltworks such as the Ying Yan company limited of Britain, the Stade of Germany, Dutch Heng Geluo are owing to salt is through purified treatment, significantly enhance the using effect of heat transmission equipment, reduce preheater and the scavenging period of evaporator, reduce salt, nitre product energy consumption, improve the quality of product, extend effective production time.Domestic salt making enterprises is provided without bittern purifying technique mostly, and (the most existing many families take bittern purifying, but it is step), China is from the external sal prunella coproduction vacuum salt making facility introduced, all using bittern purifying production technology, salt making technology economic indicator is markedly superior to the enterprise level that domestic salt is non-purified.
Present bittern purifying never uses continuous way to purify technique, and its reason has:
First, the reaction environment fluctuation of concentration that the feeding manner of clearance-type technique is easily caused mixed liquor is relatively big, air-teturning mixed phenomenon occurs, causes reaction rate to decline, and the hybrid reaction time is long；So-called back-mixing, also known as backmixing.In a broad sense, refer to the mixing between the material of different time entrance system, including material against the flowing of flow direction, such as: circulation and spread the axial backmixing caused by turbulent flow and molecule, and short circuit, stagnant wake or " dead band ", channel etc. caused by uneven VELOCITY DISTRIBUTION make the material time of staying in systems discrepant all factors.Back-mixing makes the uneven of the material time of staying in equipment, causes the distribution of the time of staying.Imperfect flow can cause the distribution of the time of staying equally.Narrowly understanding, back-mixing refers to the material mixing that motion contrary with main flow direction in continuous process is caused, the existence of this mixing, have impact on the concentration distribution along main flow direction and Temperature Distribution, makes concentration trend towards exit concentration.For mass transport process, such concentration change makes concentration motive force reduce, thus reduces transmission speed.For course of reaction, such concentration change makes reactant concentration reduce, and production concentration increases, so that primary response speed reduces and series winding side reaction speed increases, reaction selectivity declines.Clearance-type reaction method, owing to being to be separately added into according to certain stoichiometry when storeroom feeds, there is the relatively large unbalance of local in the concentration making each chemical substance, chemical molecular or ion collision between material is made to absorb the ambient concentration instability of reaction, the most axial diffusion concentration is unstable, cause the main cause that the response time is slower, thus easily cause the appearance of air-teturning mixed phenomenon；
Second, the pH value of the reactant liquor of course of reaction is long because of fluctuation and response time, and PH monitoring controls difficulty, and the addition causing lime cream is wayward, easily causes the requirement that the pH value of reactant liquor can not meet the salt process conditions of secondary response deliming technique；
3rd, the single-stage production cycle is long, and because using batch process, various operations all need interval to carry out, and carry out one by one, and whole production process is the longest；
4th, between reactant, chemical reaction amount is than instability, and undulatory property is big, causes reaction response slow, and the time is long；
5th, waste sludge discharge is difficult, and single treatment amount is big, and the quantity of slag is many, and sedimentation tapping equipment load is big, and the time is long；
These all factors are exactly some technical bottlenecks using now clearance-type technique, but by actual motion for many years, the clearance-type purification technique at salt exists operation, management, technologic problem and is difficult to support the development further of bittern purifying.
Summary of the invention
One of goal of the invention of the present invention: for the problem of above-mentioned existence, it is provided that a kind of method that can realize continuous purification gypsum mould salt thus prepare essence halogen.
The technical solution used in the present invention is such that a kind of method of continuous preparation essence halogen, it is characterised in that: it includes that the mixing of continuous raw material, continuous demagging, continuous deliming, continuous sedimentation and sedimentary naturally collection are discharged, wherein,
A: raw material mixing continuously: by raw brine and salt-making mother liquor flow-rate ratio meter, raw brine: salt-making mother liquor=(3-5): 1 is continuously added to, and lime cream is continuously added in the lump by the concentration of 50-100ml/L after adding, utilize fluid nature flow velocity in premixing device and mix in conveyance conduit, obtain successive reaction liquid, carry out continuous multi-stage reaction subsequently into reaction of high order generator；
B: demagging continuously: use lime cream regulation successive reaction liquid, make successive reaction liquid pH >=12, (inlet velocity) of every order reaction generator of reaction of high order generator: (exit velocity) is (2.5-1.5): 1, and the successive reaction flow velocity entering first order reaction generator is 0.8-2.0m/s, and reduce the successive reaction liquid flow velocity at reaction generators at different levels step by step, control magnesium ion content≤5PPM, i.e. complete demagging step, obtain one-level salt；
C: one-level continuous sedimentation: be continuously added to flocculant in the one-level salt obtained, clarify, obtain one-level clear liquor；
D: continuously deliming: the one-level clear liquor of gained, carries out successive reaction, based on flow-rate ratio, flue gas with flue gas: one-level clear liquor=(2-5): 1, and controls pH >=10 of reactant liquor, as calcium content≤10PPM in reactant liquor, complete deliming step；
E: two grades of continuous sedimentation: after continuous deliming, are also continuously added to flocculant, then clarify, and obtain essence halogen, and described settling time is more than 1 hour；
F: during continuous demagging, continuous sedimentation and continuous deliming, collects discharge the most naturally by the precipitate timing of gained.The described process collecting discharge does not affect the continuation successive reaction of salt and purifies, and the successive reaction simultaneously carrying out salt during deslagging purifies.
Described salt-making mother liquor is that the salt before Salt Industry centrifuge is starched by the liquid substance of gained after centrifuge, and the solid matter obtained after being centrifuged is exactly purified salt, and the main component of salt-making mother liquor is sodium sulfate；The amount of the raw material added, according to the requirement being smoothed out of beneficially reaction, determines according to the amount of the material existed between its chemical substance；Utilize free flow and the liquid level discrepancy in elevation, flow at high speed mixing in pipe, flow into successive reaction generator bottom through pipeline, when arriving flow reactor, three kinds of material elementary mixing are complete, the carrying out of simultaneous reaction during flowing mixing.Three kinds of raw materials achieve the purpose of mixing under conditions of need not any mechanical agitation, decrease the consumption of the energy.Three kinds of raw materials are continuous feeds simultaneously, each charging is relatively stable uniformly, whole system is in the stable reaction environment of relative equilibrium (pH value is the most stable), it is to avoid the deficiency that instantaneous load is bigger, provides preferable early stage basis to stablizing of final salt quality simultaneously；
Described flue gas is the waste gas that power station generating produces, and goes out from flue, and certain carbon dioxide is contained in the inside, substantially for the waste gas containing certain carbon dioxide；
The present invention is in order to ensure the seriality produced, and the interpolation of all materials all uses " flow-rate ratio " to calculate, i.e. " m3/ h " as unit, no matter the material added is liquid or gas, all use " flow-rate ratio ".
The sedimentation of the present invention does not use machine power to stir, the structural behaviour feature using liquid natural flow power and reactor produces and rotates flocculation, improve reactant mixture initial velocity in flocculation generator, increase the rotation flow velocity containing precipitation mixture at flocculant generator, long great achievement larger particles, follow-up precipitation sedimentation operation are wrapped up in the flocculation strengthening precipitation；
As preferably: at least continuous fourth-order reaction during described continuous demagging.
As preferably: be additionally added soda ash solution at deliming last stage reaction, remove the calcium ion failing to remove.
As preferably: the flocculant added in one-level continuous sedimentation and two grades of continuous infall processes is organic flocculant.
Further: described organic flocculant is polyacrylamide.
As preferably: the addition of described flocculant is calculated as salt flow by flow-rate ratio: flocculant flow=(50-200): 1.
The present invention is to utilize the sodium sulfate in salt-making mother liquor to react with the lime cream (i.e. calcium hydroxide) of addition, generate calcium sulfate precipitation and sodium hydroxide, its main effect is, increase clearance and the growing amount of sodium hydroxide of sulfate radical, the growing amount of sodium hydroxide be affect bittern purifying secondary response mainly generate one of material, it affects the clearance of major impurity calcium ion in secondary response, use continuous feed the addition lime cream that gradually successively decreases, purpose is to improve conversion ratio (being i.e. converted into calcium sulfate precipitation) and the growing amount of sodium hydroxide of the sulfate radical in salt continuous purification first order reaction；
Described continuous feed mode is raw material and is respectively adopted dosing pump and measures continuous feed simultaneously；It is intermittent that this continuous feed mode is different between step raw material charging, after i.e. needing first certain raw material to be metered into reaction container, again another kind raw material pump is fed, also need it is metered in reaction container, again the third raw material is loaded in reaction container by same method, start reaction, and the continuous feed that the present invention uses is: raw material measures continuous feed according to corresponding proportion simultaneously, continuous feed, in order to reach a tandem reaction sequence of successive reaction, continuous discharge；
The reactant liquor flow velocity at reaction generators at different levels is reduced step by step during continuous demagging, this control mode can increase the time of staying and the response time of material, the continuation being beneficial to sedimentary sedimentation and reactant occurs, response time also closes with change in flow at different levels in tying up to step by step and is fully reacted, the material time of staying step by step extends the most therewith, the stop of material and response time with reaction flow velocity variation relation inversely, increase step by step or extend；
Successive reaction liquid fluidised form in the reactor of every grade is upper and lower by the locality control realization of inlet and outlet or upper and lower convolution nature flow path or the flow direction, carries out successive reaction；
The feature of the precipitate clarification of the present invention can be divided into: the sedimentation in tandem reaction sequence and the clarification in clarification steps, just part sedimentation is just carried out while reaction, reaction of high order generator device afterbody outlet add flocculant (follow-up arrange to have be same as reaction of high order generator 1-3 level flocculation add, mixing, clarification), the method taking again after adding flocculant to share sedimentation step by step, alleviate clarification load and the deslagging load of defecator, the mixing flow path of flocculant with fluidised form as reactant liquor, with regard to mixed flocculation in natural fluidised form, the method using natural flow, successively decrease flow velocity one by one, increase the sedimentation time step by step.
In sum, owing to have employed technique scheme, the invention has the beneficial effects as follows: salt is by preparing essence halogen after the continuous processing technology such as successive reaction, continuous sedimentation, continuous clarification, realize the novel technique of a kind of salt continuous purification, comprise: the technology such as demagging reaction continuously, continuous deliming reaction, continuous sedimentation clarification and deslagging.Select to add the quantity relative ratio relationship of raw material according to the content of calcium and magnesium impurity in raw material halogen and the chemical reaction condition (solution ph) of reactant liquor.Ensure that under reactive state, the concentration of each composition is moved relative to stable equilibrium, object wave, is conducive to the carrying out of reaction, decreases the response time.Can preferably control the pH in course of reaction simultaneously, reaction is made to carry out (when pH value is more than 12 in demagging step to the direction being beneficial to reaction, be conducive to the removal of magnesium and causticizing reaction occurs), the setting of flow velocity, mainly regulation solves the time that course of reaction needs, and the locality imported and exported of the hybrid reaction of material, the time of staying, utilization control that liquid flows through flow through path and fluidised form, also it it is the time of staying increasing material as far as possible, increase the time of material reaction, the short circuit that when avoiding reacting, material causes simultaneously manifests, and is unfavorable for the carrying out of reaction.Under the control of this flow velocity and fluidised form, add the continuous control homeostasis to reactant doses ratio, ensure that material hybrid reaction has time enough and disclosure satisfy that the environment of reaction, just reach the basic content requirement controlling to be issued to salt removing calcium and magnesium impurity within certain response time at this conditional.By controlling the quantity relative ratio relationship of raw material halogen with raw material, being achieved that in course of reaction the control to reacting liquid pH value, i.e. have which kind of pH value how many quantity relative ratio relationship reactant liquors just can reach, this is corresponding, interactional.While successive reaction, also there occurs that sedimentary part settles, during flocculant mixed flocculation, also achieve and sedimentary part is settled, the mixed flocculation present invention of flocculation is not required to mechanical force, relies on flow velocity and fluidised form to realize the purpose of mixed flocculation, alleviate the clarification load of defecator, simultaneously precipitate by step by step share precipitation capacity, the beneficially smooth discharge of waste residue.
Detailed description of the invention
The present invention is described in detail below.
In order to make the purpose of the present invention, technical scheme and advantage clearer, below in conjunction with embodiment, the present invention is further elaborated.Should be appreciated that specific embodiment described herein, only in order to explain the present invention, is not intended to limit the present invention.
Embodiment 1:
A kind of method of continuous preparation essence halogen, it is characterised in that: it includes that the mixing of continuous raw material, continuous demagging, continuous deliming, continuous sedimentation and sedimentary naturally collection are discharged, wherein,
A: raw material mixing continuously: the raw brine based on flow-rate ratio by raw brine and salt-making mother liquor: salt-making mother liquor=4:1 is continuously added to, and lime cream is continuously added in the lump by the concentration of 75ml/L after adding, utilize fluid nature flow velocity in premixing device and mix in conveyance conduit, obtain successive reaction liquid, carry out continuous five order reactions subsequently into Pyatyi reaction generator；
B: demagging continuously: use lime cream regulation successive reaction liquid, making successive reaction liquid pH is 12, (inlet velocity) of every order reaction generator of Pyatyi reaction generator: (exit velocity) is 2.5:1, and the successive reaction flow velocity entering first order reaction generator is 0.8m/s, and reduce the successive reaction liquid flow velocity at reaction generators at different levels step by step, when magnesium ion content is 4.5PPM, i.e. complete demagging step, obtain one-level salt；
C, one-level continuous sedimentation: be continuously added to polyacrylamide in the one-level salt obtained as flocculant, settle, obtain one-level clear liquor,
D: deliming continuously: the one-level clear liquor after one-level continuous sedimentation, successive reaction is carried out with flue gas, based on flow-rate ratio, flue gas: one-level clear liquor=3:1, and the pH controlling reactant liquor is 10, it is additionally added soda ash solution at last stage reaction, removes the calcium ion failing to remove, when calcium content is 9.5PPM in reactant liquor, complete deliming step；
E: two grades of continuous sedimentation: completing the reactant liquor after deliming and add polyacrylamide as flocculant, polyacrylamide addition is reactant liquor: flocculant=100:1, then clarifies, obtain essence halogen, and described settling time is 1.5 hours.
F: during continuous demagging, continuous sedimentation and continuous deliming, the precipitate of gained is collected automatically at interval of 1h discharge.
The whole response time is 7.8 hours, i.e. achieves 1m3The continuous processing of/h disposal ability, in the smart halogen finally given, magnesium ion content is 4.5PPM, calcium ion content is 9.5 PPM, the removal rate of final sulfate radical can reach 30.9%, it is compared with the clearance 20.84% that intermittent reaction reaches, improve 10 percentage points, the clearance of sulfate radical is greatly improved.
Embodiment 2
A kind of method of continuous preparation essence halogen, it is characterised in that: it includes that the mixing of continuous raw material, continuous demagging, continuous deliming, continuous sedimentation and sedimentary naturally collection are discharged, wherein,
A: raw material mixing continuously: the raw brine based on flow-rate ratio by raw brine and salt-making mother liquor: salt-making mother liquor=3:1 is continuously added to, and lime cream is continuously added in the lump by the concentration of 50ml/L after adding, utilize fluid nature flow velocity in premixing device and mix in conveyance conduit, obtain successive reaction liquid, carry out continuous fourth-order reaction subsequently into fourth-order reaction generator；
B: demagging continuously: use lime cream regulation successive reaction liquid, making successive reaction liquid pH is 12.5, (inlet velocity) of every order reaction generator of Pyatyi reaction generator: (exit velocity) is 1.75:1, and the successive reaction flow velocity entering first order reaction generator is 1.6m/s, and reduce the successive reaction liquid flow velocity at reaction generators at different levels step by step, when magnesium ion content is 4.7PPM, i.e. complete demagging step, obtain one-level salt；
C, one-level continuous sedimentation: be continuously added to polyacrylamide in the one-level salt obtained as flocculant, settle, obtain one-level clear liquor,
D: deliming continuously: the one-level clear liquor after one-level continuous sedimentation, successive reaction is carried out with flue gas, based on flow-rate ratio, flue gas: one-level clear liquor=3.5:1, and the pH controlling reactant liquor is 10.2, it is additionally added soda ash solution at last stage reaction, removes the calcium ion failing to remove, when calcium content is 9.6PPM in reactant liquor, complete deliming step；
E: two grades of continuous sedimentation: completing the reactant liquor after deliming and add polyacrylamide as flocculant, polyacrylamide addition is reactant liquor: flocculant=50:1, then clarifies, obtain essence halogen, and described settling time is 1.2 hours.
F: during continuous demagging, continuous sedimentation and continuous deliming, the precipitate of gained is collected automatically at interval of 1h discharge.
The whole response time is 7.5 hours, i.e. achieves 1m3The continuous processing of/h disposal ability, i.e. achieves 1m3The continuous processing of/h disposal ability, in the smart halogen finally given, magnesium ion content is 4.7PPM, calcium ion content is 9.6 PPM, the removal rate of final sulfate radical can reach 31.0%, it is compared with the clearance 20.84% that intermittent reaction reaches, improve 10 percentage points, the clearance of sulfate radical is greatly improved.
Embodiment 3
A kind of method of continuous preparation essence halogen, it is characterised in that: it includes that the mixing of continuous raw material, continuous demagging, continuous deliming, continuous sedimentation and sedimentary naturally collection are discharged, wherein,
A: raw material mixing continuously: the raw brine based on flow-rate ratio by raw brine and salt-making mother liquor: salt-making mother liquor=5:1 is continuously added to, and lime cream is continuously added in the lump by the concentration of 100ml/L after adding, utilize fluid nature flow velocity in premixing device and mix in conveyance conduit, obtain successive reaction liquid, carry out continuous six order reactions subsequently into six order reaction generators；
B: demagging continuously: use lime cream regulation successive reaction liquid, making successive reaction liquid pH is 12.6, (inlet velocity) of every order reaction generator of Pyatyi reaction generator: (exit velocity) is 1.5:1, and the successive reaction flow velocity entering first order reaction generator is 2.8m/s, and reduce the successive reaction liquid flow velocity at reaction generators at different levels step by step, when magnesium ion content is 4.9PPM, i.e. complete demagging step, obtain one-level salt；
C, one-level continuous sedimentation: be continuously added to polyacrylamide in the one-level salt obtained as flocculant, settle, obtain one-level clear liquor,
D: deliming continuously: the one-level clear liquor after one-level continuous sedimentation, successive reaction is carried out with flue gas, based on flow-rate ratio, flue gas: one-level clear liquor=5:1, and the pH controlling reactant liquor is 10.5, it is additionally added soda ash solution at last stage reaction, removes the calcium ion failing to remove, when calcium content is 9.3PPM in reactant liquor, complete deliming step；
E: two grades of continuous sedimentation: completing the reactant liquor after deliming and add polyacrylamide as flocculant, polyacrylamide addition is reactant liquor: flocculant=75:1, then clarifies, obtain essence halogen, and described settling time is 2.5 hours.
F: during continuous demagging, continuous sedimentation and continuous deliming, the precipitate of gained is collected automatically at interval of 1h discharge.
The whole response time is 8.5 hours, i.e. achieves 1m3The continuous processing of/h disposal ability, in the smart halogen finally given, magnesium ion content is 4.9PPM, calcium ion content is 9.3 PPM, the removal rate of final sulfate radical can reach 32.62%, it is compared with the clearance 20.84% that intermittent reaction reaches, improve 11.78%, the clearance of sulfate radical is greatly improved.
Claims (5)
1. the method for a continuous preparation essence halogen, it is characterised in that: it includes that the mixing of continuous raw material, continuous demagging, continuous deliming, continuous sedimentation and sedimentary naturally collection are discharged, wherein,
A: raw material mixing continuously: by raw brine and salt-making mother liquor flow-rate ratio meter, raw brine: salt-making mother liquor=3-5:1 is continuously added to, and lime cream is continuously added in the lump by the concentration of 50-100ml/L after adding, utilize fluid nature flow velocity in premixing device and mix in conveyance conduit, obtain successive reaction liquid, carry out continuous multi-stage reaction subsequently into reaction of high order generator；
B: demagging continuously: use lime cream regulation successive reaction liquid, make successive reaction liquid pH >=12, the inlet velocity of every order reaction generator of reaction of high order generator: exit velocity is 2.5-1.5:1, and the successive reaction flow velocity entering first order reaction generator is 0.8-2.0m/s, and reduce the successive reaction liquid flow velocity at reaction generators at different levels step by step, control magnesium ion content≤5ppm, i.e. complete demagging step, obtain one-level salt；
C: one-level continuous sedimentation: be continuously added to flocculant in the one-level salt obtained, clarify, obtain one-level clear liquor；
D: continuously deliming: the one-level clear liquor of gained, carries out successive reaction, based on flow-rate ratio, flue gas with flue gas: one-level clear liquor=2-5:1, and controls pH >=10 of reactant liquor, as calcium content≤10ppm in reactant liquor, complete deliming step；
E: two grades of continuous sedimentation: after continuous deliming, are also continuously added to flocculant, then clarify, and obtain essence halogen, and described settling time is more than 1 hour；
F: in continuous demagging, continuous sedimentation and continuously during deliming, the precipitate timing of gained being collected discharge the most naturally, deliming last stage reaction is additionally added soda ash solution, removes and fails the calcium ion of removing.
The method of a kind of continuous preparation essence halogen the most according to claim 1, it is characterised in that: at least continuous fourth-order reaction during described continuous demagging.
The method of a kind of continuous preparation essence halogen the most according to claim 1, it is characterised in that: the flocculant added in one-level continuous sedimentation and two grades of continuous infall processes is organic flocculant.
The method of a kind of continuous preparation essence halogen the most according to claim 3, it is characterised in that: described organic flocculant is polyacrylamide.
The method of a kind of continuous preparation essence halogen the most according to claim 1, it is characterised in that: the addition of described flocculant is calculated as salt flow by flow-rate ratio: flocculant flow=50-200:1.
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| CN107244722A (en) * | 2017-04-13 | 2017-10-13 | 北京浦仁美华环保科技股份有限公司 | The technique for removing waste water hardness using boiler exhaust gas and quick lime |
| CN110182831A (en) * | 2019-05-28 | 2019-08-30 | 昌鑫生态科技(陕西)有限公司 | The technology of salt lake extraction lithium carbonate |
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| CN86107909A (en) * | 1986-11-21 | 1988-07-20 | 徐贵义 | Salt and pure soda combine production method |
| CN101289200A (en) * | 2007-04-16 | 2008-10-22 | 中国盐业总公司 | Technological process for purifying bittern |
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| CN86107909A (en) * | 1986-11-21 | 1988-07-20 | 徐贵义 | Salt and pure soda combine production method |
| CN101289200A (en) * | 2007-04-16 | 2008-10-22 | 中国盐业总公司 | Technological process for purifying bittern |
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