CN101628722A - Process for refining crude salt - Google Patents
Process for refining crude salt Download PDFInfo
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- CN101628722A CN101628722A CN200910070162A CN200910070162A CN101628722A CN 101628722 A CN101628722 A CN 101628722A CN 200910070162 A CN200910070162 A CN 200910070162A CN 200910070162 A CN200910070162 A CN 200910070162A CN 101628722 A CN101628722 A CN 101628722A
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Abstract
The invention discloses a process for refining crude salt. A salt-leaching step comprises the following steps: sending crude salt to a salt leaching device, a ball mill, a primary salt slurry barrel, a thickener and a primary centrifuge in sequence; then sending salt slurry separated from the primary centrifuge to a secondary salt slurry barrel, a classificator and an immediate washing barrel for washing and thickening; then using condensate water to wash the salt slurry after entering the secondary centrifuge so as to remove bittern, thereby obtaining qualified leached salt; a crude bittern treatment step comprises the following steps: mixing leaching crude bittern in the salt leaching step in a crude bittern pool, and subsequently sending to a calcium-magnesium reactor so as to remove Ca<2+> and Mg<2+>; then entering a clarifying tank for clarifying; after increasing the temperature of the clarified clear liquor by a bittern heater, sending portion of clarified clear liquor to a refining bittern barrel for vacuum salt manufacturing with portion of clarified clear liquor for salt leaching use; and a vacuum salt manufacturing step comprises the following steps: sending refined salt water in the refining bittern barrel to a multi-effect evaporator for evaporating; finally discharging separated solid salt to the salt slurry barrel, the salt slurry thickener and the vacuum centrifuge, thereby obtaining leached salt. The method reduces the crude salt loss and lowers the content of SO4<2-> in the leached salt.
Description
Technical field
The present invention relates to a kind of technology of refining crude salt.
Background technology
The manufacture method of soda ash mainly contains two kinds: solvay soda process and connection alkaline process.Wherein joining alkaline process employing solid salt is raw material, the closed cycle of mother liquor system utilizes, and in this process, the insoluble and soluble impurity in the solid salt enters system, will inevitably have influence on the quality of the finished product, therefore need be to being that the crude salt of raw material is made with extra care with the solid salt.
The quality of the desalinization of soil by flooding or leaching serves as the examination target with foreign matter content in the desalinization of soil by flooding or leaching and desalinization of soil by flooding or leaching granularity, and foreign matter content in the desalinization of soil by flooding or leaching serves as the examination composition with Ca2+, Mg2+, SO42-; The granularity of the desalinization of soil by flooding or leaching also is an important quality index.Traditional desalinization of soil by flooding or leaching technology is main purpose with Ca2+, Mg2+ and micro-SO42-impurity and desalinization of soil by flooding or leaching granularity in the washing crude salt only, can reduce the AII turbidity, but can not remove SO42-; In fact SO42-'s is very harmful, and it can be accumulated in the mother liquor system, influences the quality of soda ash, industrial ammonium chloride at last.
Existing desalinization of soil by flooding or leaching technological process is generally washing process twice, after adopting twice clarifying lime-soda method art breading of the method for fractional steps, washing bittern recycles, the desalinization of soil by flooding or leaching that finally obtains is second-rate, can not satisfy the needs that high quality soda ash and industrial ammonium chloride are produced; Wherein height is invested and clarifying effect is bad comparatively speaking in the bittern treating part; This technology is if will reach the high-quality desalinization of soil by flooding or leaching, and its outer discharge capacity is bigger, and the salt loss is bigger.
Summary of the invention
The object of the present invention is to provide a kind of solid material salt can being made with extra care, make the SO in the desalinization of soil by flooding or leaching product
4 2The technology of a kind of refining crude salt of the high-quality desalinization of soil by flooding or leaching that mass content≤0.1% is following.
The present invention is achieved by the following technical programs.
A kind of technology of refining crude salt, it comprises, and the desalinization of soil by flooding or leaching, thick halogen are handled, three parts of vacuum salt production,
(1) desalinization of soil by flooding or leaching step, it comprises:
(a) crude salt is sent into desalinization of soil by flooding or leaching machine, and adopted SO
4 2-Content is sent into ball mill after being not more than the saturated brine washings countercurrent washing of 10g/l, and it is 0.3-0.42mm and the particle distribution in described particle size range＞70% that described ball mill is crushed to median size with crude salt;
(b) crude salt after the described pulverizing is sent in salt slurry bucket to be adjusted to and looked the salt slurry that the solid-liquid volume ratio is 25%-35%, then described salt slurry is delivered to stiff device stiff successively, adopts at whizzer and coagulate water washing salt and starch then with pump with secondary bittern;
(C) will send in the secondary salt slurry bucket from the isolated salt of described whizzer slurry and use SO
4 2-Three grades of bittern that content is not more than 3.76g/l are adjusted to and look solid-to-liquid ratio is 25%-35%, adopt three grades of bittern to carry out the flotation classification with pump delivery to classifier then, qualified salt slurry after classified flows into upright cask washing washing and stiff, entering the secondary centrifuging machine then adopt to coagulate and to obtain the qualified desalinization of soil by flooding or leaching after water washing removes bittern, the underflow of described classifier enters sand separator by the macrogranule salt jar and adopts the described water dissolution of coagulating, and described three grades of bittern are the overflowing liquid of cask washing of supporting oneself, saturated brine after the dissolving of described sand separator and send into the mixed mixed solution of storage bucket jointly from the filtrate of described secondary centrifuging machine;
(2) thick halogen treatment step, it comprises:
(a) filtrate that will remove from the overflowing liquid of the bittern after the desalinization of soil by flooding or leaching the described step (1) machine washing is washed, stiff device and whizzer is mixed the back by thick halogen pond and is added and coagulate water with the dissolving fine salt, then it is sent into calcium reactive magnesium device, in described calcium reactive magnesium device, add simultaneously by sodium carbonate solution and aqua calcis reaction back and mix the causticization liquid formed to remove the Ca in the described bittern mixed solution
2+, Mg
2+
(b) remove Ca
2+, Mg
2+After described bittern mixed solution enter settling tank clarification through the labyrinth groove, clear liquor after the described clarification is a part of refining bittern bucket of delivering to the vacuum salt production step after bittern well heater raising temperature is to 35-40 ℃, a part is returned described desalinization of soil by flooding or leaching step and is continued to use, and described settling tank underflow is transported after the pressure filter press filtration;
(3) vacuum salt production step, it comprises:
(a) will handle the refined brine deliver in the refining bittern bucket through described step (2) and send into the solid salt that the multiple-effect evaporator evaporation separates out and drain into salt slurry bucket, the water that coagulates of described multiple-effect evaporator is sent into water pot with fixed attention;
(b) the salt slurry of described salt being starched the bucket bottom is sent into salt slurry stiff device stiff to the salt slurry of solid-liquid apparent volume ratio for 50%-70%, then the salt after described stiff slurry being sent into desalinization of soil by flooding or leaching device adopts to send into after the overflowing liquid washing from the storage bucket of described step (1) and obtains purified salt after the vacuum salt whizzer removes moisture content, the overflowing liquid of described salt slurry stiff device drains into old halogen bucket, the SO in the solution in the old halogen bucket
4 2-Concentration reaches 55g/l after old halogen pump discharges, and the filtrate of described vacuum salt whizzer is returned the multiple-effect evaporator evaporation through filtrate pump;
Saturated brine washings in the described step (1) is for coagulating the water composition from the part bittern of the bittern well heater in the described step (2) and from described part of coagulating in the water pot;
Secondary bittern in the described step (1) is the overflowing liquid from the upright cask washing in the part bittern of the bittern well heater in the described step (2) and the described step (2);
The described water that coagulates is from the water that coagulates that coagulates water pot in the described step (3).
Adopting inventive method to compare with existing technology has the following advantages:
(1) because the washing water of desalinization of soil by flooding or leaching step enter system again uses, thereby improves system temperature to 35 ~ 40 ℃ after the bittern heater heats, thereby increased the solubleness of calcium sulfate, reduce the washings internal circulating load.
(2) the part fine salt of taking away in the water-soluble solution recovery washing overflowing liquid is coagulated in employing, has reduced the crude salt loss.
(3) adopt the method for three washings, two times centrifugal to wash crude salt in this technology, reduced the impurity in the desalinization of soil by flooding or leaching to greatest extent, guarantee the quality of soda ash, industrial ammonium chloride.
(4) employing is removed Ca earlier with washings
2+, Mg
2+, keep high-content SO
4 2-(10g/l) method of washings washing crude salt on the basis that guarantees desalinization of soil by flooding or leaching quality, reduces the scale of vacuum salt production to greatest extent, cuts down the consumption of energy, and removes SO simultaneously
4 2-
(5) lime--the soda ash refined by one-step method recycles the employing of washing back bittern, has reduced fresh water consumption;
(6) brine refining is made causticization liquid earlier, has improved the settling velocity of bittern, has reduced the quantity of settling tank.
(7) adopt the large-size ball mill that the unit grindability is big, crush efficiency is high, guarantee that the granularity of the desalinization of soil by flooding or leaching is qualified, thereby guaranteed desalinization of soil by flooding or leaching quality.
Description of drawings
Accompanying drawing is the process flow sheet of a kind of refining crude salt of the present invention.
Embodiment
The present invention is further illustrated below in conjunction with specific embodiment.
Following elder generation is illustrated the production principle of the desalinization of soil by flooding or leaching:
The desalinization of soil by flooding or leaching is adopted and is pulverized washing method, and this method is a kind of method of physical removal impurity.Mainly be the characteristic of utilizing sodium-chlor, sal epsom, calcium sulfate different solubility, carry out refining crude salt.With sodium chloride saturated solution or near saturated salt solution as washings, with dissolvings such as the soluble impurity magnesium chloride in the crude salt, calcium chloride, sal epsom, the calcium sulfate less to solubleness can be partly dissolved, the parts of fine crystalline suspension is floating removing in washings, and the impurity that is clipped in the crude salt granule interior can further be removed after crushed.
Bittern after the washing adopts lime-soda method to handle, and milk of lime and soda ash are joined in the causticizing tank simultaneously, makes causticization liquid (Na earlier
2CO
3And NaOH), and then join in the thick halogen, one step of deliming demagging carries out, and the add-on of described milk of lime and soda ash is according to the Ca in the thick halogen
2+, Mg
2+Content determine.In order to accelerate the sedimentation of precipitation particles, guarantee the effect of demagging, deliming process, need maintenance excessive milk of lime and soda ash liquid, and add an amount of settling agent, the add-on of settling agent is for guaranteeing that strength of solution is 2ppm in the settling tank.The reaction formula of above-mentioned reaction is expressed as follows:
Na
2CO
3+Ca(OH)
2＝2NaOH+CaCO
3↓
2NaOH+Mg
2+＝Mg(OH)
2↓+2Na
+
Ca
2++Na
2CO
3＝CaCO3↓+2Na
+
Thick halogen processing clear liquid after clarifying contains SO
4 2-About 10 grams per liters, a part is returned desalinization of soil by flooding or leaching system as slightly washing washings, another part method salt manufacturing of vacuum salt production, old halogen (contains SO
4 2-About 55 grams per liters) discharging is to remove SO
4 2-
Vacuum salt production adopts multiple-effect vacuum-evaporation, utilizes the different characteristic of solubility with temperature Changing Pattern of sodium sulfate and sodium-chlor, and the concentration of control sodium sulfate is separated out the sodium-chlor crystallization, and sodium sulfate discharges with old halogen.
Based on above-mentioned principle of work: the technology of a kind of refining crude salt of the present invention, it comprises, and the desalinization of soil by flooding or leaching, thick halogen are handled, three parts of vacuum salt production;
(1) desalinization of soil by flooding or leaching step, it comprises:
(a) crude salt is sent into desalinization of soil by flooding or leaching machine, and adopted SO
4 2-Content is sent into ball mill after being not more than the saturated brine washings countercurrent washing of 10g/l, and it is 0.3-0.42mm and the particle distribution in described particle size range＞70% that described ball mill is crushed to median size with crude salt;
(b) crude salt after the described pulverizing is sent in salt slurry bucket to be adjusted to and looked the salt slurry that the solid-liquid volume ratio is 25%-35%, then described salt slurry is delivered to stiff device stiff successively, adopts at whizzer and coagulate water washing salt and starch then with pump with secondary bittern;
(C) will send in the secondary salt slurry bucket from the isolated salt of described whizzer slurry and use SO
4 2-Three grades of bittern that content is not more than 3.76g/l are adjusted to and look solid-to-liquid ratio is 25%-35%, adopt three grades of bittern to carry out the flotation classification with pump delivery to classifier then, qualified salt slurry after classified flows into upright cask washing washing and stiff, enter then and obtain the qualified desalinization of soil by flooding or leaching after the secondary centrifuging machine adopts water washing with fixed attention and removes bittern, the underflow of described classifier enters sand separator by the macrogranule salt jar and adopts the described water washing dissolving of coagulating, and described three grades of bittern are the overflowing liquid of cask washing of supporting oneself, saturated brine after the dissolving of described sand separator and send into the mixed mixed solution of storage bucket jointly from the filtrate of described secondary centrifuging machine;
(2) thick halogen treatment step, it comprises:
(a) filtrate that will remove from the overflowing liquid of the bittern after the desalinization of soil by flooding or leaching the described step (1) machine washing is washed, stiff device and whizzer is mixed the back by thick halogen pond and is added and coagulate water with the dissolving fine salt, then it is sent into calcium reactive magnesium device, in described calcium reactive magnesium device, add simultaneously by sodium carbonate solution and aqua calcis reaction back and mix the causticization liquid formed to remove the Ca in the described bittern mixed solution
2+, Mg
2+Described causticization liquid preferably adopts the preparation of following method: with the overflowing liquid furnishing lime milk solution of white lime from described upright cask washing, sodium carbonate solution and described lime milk solution are joined the causticizing tank reaction make causticization liquid.Described sodium carbonate solution is the grey mother liquor of weight of soda ash production process discharging.
(b) remove Ca
2+, Mg
2+After described bittern mixed solution enter settling tank clarification through the labyrinth groove, clear liquor after the described clarification is a part of refining bittern bucket of delivering to the vacuum salt production step after bittern well heater raising temperature is to 35-40 ℃, a part is returned described desalinization of soil by flooding or leaching step and is continued to use, and described settling tank underflow is transported after the pressure filter press filtration;
(3) vacuum salt production step, it comprises:
(a) will handle the refined brine deliver in the refining bittern bucket through described step (2) and send into the solid salt that the multiple-effect evaporator evaporation separates out and drain into salt slurry bucket, the water that coagulates of described multiple-effect evaporator is sent into water pot with fixed attention;
(b) the salt slurry of described salt being starched the bucket bottom is sent into salt slurry stiff device stiff to the salt slurry of solid-liquid apparent volume ratio for 50%-70%, then the salt after described stiff slurry being sent into desalinization of soil by flooding or leaching device adopts to send into after the overflowing liquid washing from the storage bucket of described step (1) and obtains purified salt after the vacuum salt whizzer removes moisture content, the overflowing liquid of described salt slurry stiff device drains into old halogen bucket, the SO in solution in the old halogen bucket
4 2-Concentration reaches 55g/l after old halogen pump discharges, and the filtrate of described vacuum salt whizzer is returned the multiple-effect evaporator evaporation through filtrate pump, and described multiple-effect evaporator can be 4 effect or 5 single-effect evaporators.
Saturated brine washings in the described step (1) is for coagulating the water composition from the part bittern of the bittern well heater in the described step (2) and from described part of coagulating in the water pot;
Secondary bittern in the described step (1) is the overflowing liquid from the upright cask washing in the part bittern of the bittern well heater in the described step (2) and the described step (2);
The described water that coagulates is from the water that coagulates that coagulates water pot in the described step (3).
Embodiment 1
(1) desalinization of soil by flooding or leaching step: (a) crude salt is sent into desalinization of soil by flooding or leaching machine, and adopted SO
4 2-Content is sent into ball mill after being not more than the saturated brine washings countercurrent washing of 10g/l, and it is 0.35mm and the particle distribution in described particle size range＞70% that described ball mill is crushed to median size with crude salt; (b) crude salt after the described pulverizing is sent in salt slurry bucket and to be adjusted to secondary bittern that to look the solid-liquid volume ratio be 30% salt slurry, then described salt slurry is delivered to stiff device stiff, whizzer successively with pump and adopts and coagulate water washing salt and starch; (C) will send in the secondary salt slurry bucket from the isolated salt of described whizzer slurry and use SO
4 2-Three grades of bittern that content is not more than 3.76g/l are adjusted to and look solid-to-liquid ratio is 30%, adopt three grades of bittern to carry out the flotation classification with pump delivery to classifier then, qualified salt slurry after classified flows into upright cask washing washing and stiff and enters the secondary centrifuging machine then and adopt to coagulate and obtain the qualified desalinization of soil by flooding or leaching after water washing removes bittern, the underflow of described classifier enters sand separator by the macrogranule salt jar and adopts the described water dissolution of coagulating, and described three grades of bittern are the overflowing liquid of cask washing of supporting oneself, saturated brine after the dissolving of described sand separator and send into the mixed mixed solution of storage bucket jointly from the filtrate of described secondary centrifuging machine;
(2) thick halogen treatment step: (a) filtrate that will remove from the overflowing liquid of the bittern after the machine washing of the desalinization of soil by flooding or leaching the described step (1) is washed, stiff device and whizzer is mixed the back by thick halogen pond and is added and coagulate water with the dissolving fine salt, then it is sent into calcium reactive magnesium device, in described calcium reactive magnesium device, add simultaneously by sodium carbonate solution and aqua calcis reaction back and mix the causticization liquid formed to remove the Ca in the described bittern mixed solution
2+, Mg
2+, (b) remove Ca
2+, Mg
2+After described bittern mixed solution enter settling tank clarification through the labyrinth groove, clear liquor after the described clarification is a part of refining bittern bucket of delivering to the vacuum salt production step after the bittern well heater improves temperature to 38 ℃, a part is returned described desalinization of soil by flooding or leaching step and is continued to use, and described settling tank underflow is transported after the pressure filter press filtration;
(3) vacuum salt production step: (a) will handle the refined brine deliver in the refining bittern bucket through described step (2) and send into the solid salt that the multiple-effect evaporator evaporation separates out and drain into salt slurry bucket, the water that coagulates of described multiple-effect evaporator is sent into water pot with fixed attention; (b) the salt slurry of described salt slurry bucket bottom being sent into salt slurry stiff device stiff to solid-liquid apparent volume starches than the salt that is 60%, then the salt after described stiff slurry being sent into desalinization of soil by flooding or leaching device adopts to send into after the overflowing liquid washing from the storage bucket of described step (1) and obtains purified salt after the vacuum salt whizzer removes moisture content, the overflowing liquid of described salt slurry stiff device drains into old halogen bucket, the SO of the solution in old halogen bucket
4 2-After old halogen pump discharges, the filtrate of described vacuum salt whizzer is returned the evaporation of 5 single-effect evaporators through filtrate pump to concentration to 55g/l.
Saturated brine washings in the described step (1) is for coagulating the water composition from the part bittern of the bittern well heater in the described step (2) and from described part of coagulating in the water pot;
Secondary bittern in the described step (1) is the overflowing liquid from the upright cask washing in the part bittern of the bittern well heater in the described step (2) and the described step (2);
The described water that coagulates is from the water that coagulates that coagulates water pot in the described step (3).
After tested: the crude salt loss reduces by 2.5%, the SO in the desalinization of soil by flooding or leaching product
4 2Mass content is 0.095%.
Embodiment 2
(1) desalinization of soil by flooding or leaching step: (a) crude salt is sent into desalinization of soil by flooding or leaching machine, and adopted SO
4 2-Content is sent into ball mill after being not more than the saturated brine washings countercurrent washing of 10g/l, and it is 0.3mm and the particle distribution in described particle size range＞70% that described ball mill is crushed to median size with crude salt; (b) crude salt after the described pulverizing is sent in salt slurry bucket and to be adjusted to one-level bittern that to look the solid-liquid volume ratio be 25% salt slurry, then described salt slurry is delivered to stiff device stiff, whizzer successively with pump and adopts and coagulate water washing salt and starch; (C) will send in the secondary salt slurry bucket from the isolated salt of described whizzer slurry and use SO
4 2-Three grades of bittern that content is not more than 3.76g/l are adjusted to and look solid-to-liquid ratio is 25%, adopt three grades of bittern to carry out the flotation classification with pump delivery to classifier then, qualified salt slurry after classified flows into upright cask washing washing and stiff and enters the secondary centrifuging machine then and adopt to coagulate and obtain the qualified desalinization of soil by flooding or leaching after water washing removes bittern, the underflow of described classifier enters sand separator by the macrogranule salt jar and adopts the described water dissolution of coagulating, and described three grades of bittern are the overflowing liquid of cask washing of supporting oneself, saturated brine after the described sand separator washing dissolving and send into the mixed mixed solution of storage bucket jointly from the filtrate of described secondary centrifuging machine;
(2) thick halogen treatment step: (a) filtrate that will remove from the overflowing liquid of the bittern after the machine washing of the desalinization of soil by flooding or leaching the described step (1) is washed, stiff device and whizzer is mixed the back by thick halogen pond and is added and coagulate water with the dissolving fine salt, then it is sent into calcium reactive magnesium device, in described calcium reactive magnesium device, add simultaneously by sodium carbonate solution and aqua calcis reaction back and mix the causticization liquid formed to remove the Ca in the described bittern mixed solution
2+, Mg
2+Described causticization liquid adopts the preparation of following method: with the overflowing liquid furnishing lime milk solution of white lime from described upright cask washing, sodium carbonate solution and described lime milk solution are joined the causticizing tank reaction make causticization liquid.Described sodium carbonate solution is the grey mother liquor of weight of soda ash production process discharging.(b) remove Ca
2+, Mg
2+After described bittern mixed solution enter settling tank clarification through the labyrinth groove, clear liquor after the described clarification is a part of refining bittern bucket of delivering to the vacuum salt production step after the bittern well heater improves temperature to 35 ℃, a part is returned described desalinization of soil by flooding or leaching step and is continued to use, and described settling tank underflow is transported after the pressure filter press filtration;
(3) vacuum salt production step: (a) will handle the refined brine deliver in the refining bittern bucket through described step (2) and send into the solid salt that the multiple-effect evaporator evaporation separates out and drain into salt slurry bucket, the water that coagulates of described multiple-effect evaporator is sent into water pot with fixed attention; (b) the salt slurry of described salt slurry bucket bottom being sent into salt slurry stiff device stiff to solid-liquid apparent volume starches than the salt that is 70%, then the salt after described stiff slurry being sent into desalinization of soil by flooding or leaching device adopts to send into after the overflowing liquid washing from the storage bucket of described step (1) and obtains purified salt after the vacuum salt whizzer removes moisture content, the overflowing liquid of described salt slurry stiff device drains into old halogen bucket, the SO of the solution in old halogen bucket
4 2-Concentration reaches 55g/l after old halogen pump discharges, and the filtrate of described vacuum salt whizzer is returned the evaporation of 4 single-effect evaporators through filtrate pump.
Saturated brine washings in the described step (1) is for coagulating the water composition from the part bittern of the bittern well heater in the described step (2) and from described part of coagulating in the water pot;
Secondary bittern in the described step (1) is the overflowing liquid from the upright cask washing in the part bittern of the bittern well heater in the described step (2) and the described step (2);
The described water that coagulates is from the water that coagulates that coagulates water pot in the described step (3).
After tested: the crude salt loss reduces by 2%, the SO in the desalinization of soil by flooding or leaching product
4 2Mass content is 0.09%.
Embodiment 3
(1) desalinization of soil by flooding or leaching step: (a) crude salt is sent into desalinization of soil by flooding or leaching machine, and adopted SO
4 2-Content is sent into ball mill after being not more than the saturated brine washings countercurrent washing of 10g/l, and it is 0.42mm and the particle distribution in described particle size range＞70% that described ball mill is crushed to median size with crude salt; (b) crude salt after the described pulverizing is sent in salt slurry bucket and to be adjusted to one-level bittern that to look the solid-liquid volume ratio be 35% salt slurry, then described salt slurry is delivered to stiff device stiff, whizzer successively with pump and adopts and coagulate water washing salt and starch; (C) will send in the secondary salt slurry bucket from the isolated salt of described whizzer slurry and use SO
4 2-Three grades of bittern that content is not more than 3.76g/l are adjusted to and look solid-to-liquid ratio is 35%, adopt three grades of bittern to carry out the flotation classification with pump delivery to classifier then, qualified salt slurry after classified flows into upright cask washing washing and stiff and enters the secondary centrifuging machine then and adopt to coagulate and obtain the qualified desalinization of soil by flooding or leaching after water washing removes bittern, the underflow of described classifier enters sand separator by the macrogranule salt jar and adopts the described water dissolution of coagulating, and described three grades of bittern are the overflowing liquid of cask washing of supporting oneself, saturated brine after the dissolving of described sand separator and send into the mixed mixed solution of storage bucket jointly from the filtrate of described secondary centrifuging machine;
(2) thick halogen treatment step: (a) will mix by thick halogen pond from the filtrate that the overflowing liquid of the bittern after the machine washing of the desalinization of soil by flooding or leaching the described step (1) is washed, stiff device and whizzer remove after describedly coagulate water washing and form the bittern mixed solution and send into calcium reactive magnesium device, and in described calcium reactive magnesium device, add simultaneously by sodium carbonate solution and aqua calcis and mix the causticization liquid formed to remove the Ca in the described bittern mixed solution
2+, Mg
2+Described causticization liquid adopts the preparation of following method: with the overflowing liquid furnishing lime milk solution of white lime from described upright cask washing, sodium carbonate solution and described lime milk solution are joined the causticizing tank reaction make causticization liquid.Described sodium carbonate solution is the grey mother liquor of weight of soda ash production process discharging.(b) remove Ca
2+, Mg
2+After described bittern mixed solution enter settling tank clarification through the labyrinth groove, clear liquor after the described clarification is a part of refining bittern bucket of delivering to the vacuum salt production step after the bittern well heater improves temperature to 40 ℃, a part is returned described desalinization of soil by flooding or leaching step and is continued to use, and described settling tank underflow is transported after the pressure filter press filtration;
(3) vacuum salt production step: (a) will handle the refined brine deliver in the refining bittern bucket through described step (2) and send into the solid salt that the multiple-effect evaporator evaporation separates out and drain into salt slurry bucket, the water that coagulates of described multiple-effect evaporator is sent into water pot with fixed attention; (b) the salt slurry of described salt slurry bucket bottom being sent into salt slurry stiff device stiff to solid-liquid apparent volume starches than the salt that is 50%, then the salt after described stiff slurry being sent into desalinization of soil by flooding or leaching device adopts to send into after the overflowing liquid washing from the storage bucket of described step (1) and obtains purified salt after the vacuum salt whizzer removes moisture content, the overflowing liquid of described salt slurry stiff device drains into old halogen bucket, the SO of the solution in old halogen bucket
4 2-After old halogen pump discharges, the filtrate of described vacuum salt whizzer is returned the evaporation of 5 single-effect evaporators through filtrate pump to concentration to 55g/l.
Saturated brine washings in the described step (1) is for coagulating the water composition from the part bittern of the bittern well heater in the described step (2) and from described part of coagulating in the water pot;
Secondary bittern in the described step (1) is the overflowing liquid from the upright cask washing in the part bittern of the bittern well heater in the described step (2) and the described step (2);
The described water that coagulates is from the water that coagulates that coagulates water pot in the described step (3).
After tested: the crude salt loss reduces by 2.5%, the SO in the desalinization of soil by flooding or leaching product
4 2Mass content is 0.1%.
Claims (4)
1. the technology of a refining crude salt, it comprises, and the desalinization of soil by flooding or leaching, thick halogen are handled, three parts of vacuum salt production, it is characterized in that:
(1) desalinization of soil by flooding or leaching step, it comprises:
(a) crude salt is sent into desalinization of soil by flooding or leaching machine, and adopted SO
4 2-Content is sent into ball mill after being not more than the saturated brine washings countercurrent washing of 10g/l, and it is 0.3-0.42mm and the particle distribution in described particle size range＞70% that described ball mill is crushed to median size with crude salt;
(b) crude salt after the described pulverizing is sent in salt slurry bucket to be adjusted to and looked the salt slurry that the solid-liquid volume ratio is 25%-35%, then described salt slurry is delivered to stiff device stiff successively, adopts at whizzer and coagulate water washing salt and starch then with pump with secondary bittern;
(C) will send in the secondary salt slurry bucket from the isolated salt of described whizzer slurry and use SO
4 2-Three grades of bittern that content is not more than 3.76g/l are adjusted to and look solid-to-liquid ratio is 25%-35%, adopt three grades of bittern to carry out the flotation classification with pump delivery to classifier then, qualified salt slurry after classified flows into upright cask washing washing and stiff, entering the secondary centrifuging machine then adopt to coagulate and to obtain the qualified desalinization of soil by flooding or leaching after water washing removes bittern, the underflow of described classifier enters sand separator by the macrogranule salt jar and adopts the described water dissolution of coagulating, and described three grades of bittern are the overflowing liquid of cask washing of supporting oneself, saturated brine after the dissolving of described sand separator and send into the mixed mixed solution of storage bucket jointly from the filtrate of described secondary centrifuging machine;
(2) thick halogen treatment step, it comprises:
(a) filtrate that will remove from the overflowing liquid of the bittern after the desalinization of soil by flooding or leaching the described step (1) machine washing is washed, stiff device and whizzer is mixed the back by thick halogen pond and is added and coagulate water with the dissolving fine salt, then it is sent into calcium reactive magnesium device, in described calcium reactive magnesium device, add simultaneously by sodium carbonate solution and aqua calcis reaction back and mix the causticization liquid formed to remove the Ca in the described bittern mixed solution
2+, Mg
2+.
(b) remove Ca
2+, Mg
2+After described bittern mixed solution enter settling tank clarification through the labyrinth groove, clear liquor after the described clarification is a part of refining bittern bucket of delivering to the vacuum salt production step after bittern well heater raising temperature is to 35-40 ℃, a part is returned described desalinization of soil by flooding or leaching step and is continued to use, and described settling tank underflow is transported after the pressure filter press filtration;
(3) vacuum salt production step, it comprises:
(a) will handle the refined brine deliver in the refining bittern bucket through described step (2) and send into the solid salt that the multiple-effect evaporator evaporation separates out and drain into salt slurry bucket, the water that coagulates of described multiple-effect evaporator is sent into water pot with fixed attention;
(b) the salt slurry of described salt being starched the bucket bottom is sent into salt slurry stiff device stiff to the salt slurry of solid-liquid apparent volume ratio for 50%-70%, then the salt after described stiff slurry being sent into desalinization of soil by flooding or leaching device adopts to send into after the overflowing liquid washing from the storage bucket of described step (1) and obtains purified salt after the vacuum salt whizzer removes moisture content, the overflowing liquid of described salt slurry stiff device drains into old halogen bucket, the SO in solution in the old halogen bucket
4 2-Concentration reaches 55g/l after old halogen pump discharges, and the filtrate of described vacuum salt whizzer is returned the multiple-effect evaporator evaporation through filtrate pump;
Saturated brine washings in the described step (1) is for coagulating the water composition from the part bittern of the bittern well heater in the described step (2) and from described part of coagulating in the water pot;
Secondary bittern in the described step (1) is the overflowing liquid from the upright cask washing in the part bittern of the bittern well heater in the described step (2) and the described step (2);
The described water that coagulates is from the water that coagulates that coagulates water pot in the described step (3).
2. desalinization of soil by flooding or leaching technology according to claim 1, it is characterized in that causticization liquid in the described step (2) adopts following method preparation:, sodium carbonate solution and described lime milk solution are joined the causticizing tank reaction make causticization liquid with the overflowing liquid furnishing lime milk solution of white lime from described upright cask washing.
3. desalinization of soil by flooding or leaching technology according to claim 2 is characterized in that: described sodium carbonate solution is the grey mother liquor of weight of soda ash production process discharging.
4. desalinization of soil by flooding or leaching technology according to claim 1 is characterized in that: described multiple-effect evaporator is 4 effect or 5 single-effect evaporators.
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| CN102390845A (en) * | 2011-08-09 | 2012-03-28 | 中盐皓龙盐化有限责任公司 | Method for producing salt special for sodium metal by using elutriation method |
| CN103288104A (en) * | 2013-06-26 | 2013-09-11 | 河南城建学院 | Method for removing odor of refined salt through ferric salt |
| CN103979579A (en) * | 2014-05-26 | 2014-08-13 | 江苏井神盐化股份有限公司 | Method for preparing refined salt low in calcium and magnesium by utilizing underground denitration process |
| CN103991997A (en) * | 2014-05-30 | 2014-08-20 | 中国石油集团东北炼化工程有限公司吉林设计院 | Strong brine evaporating and crystallizing system |
| CN104891531A (en) * | 2015-05-13 | 2015-09-09 | 中盐舞阳盐化有限公司 | Preparation method of metal sodium salt |
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| CN102390845A (en) * | 2011-08-09 | 2012-03-28 | 中盐皓龙盐化有限责任公司 | Method for producing salt special for sodium metal by using elutriation method |
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| CN103979579A (en) * | 2014-05-26 | 2014-08-13 | 江苏井神盐化股份有限公司 | Method for preparing refined salt low in calcium and magnesium by utilizing underground denitration process |
| CN103991997B (en) * | 2014-05-30 | 2016-04-13 | 中国石油集团东北炼化工程有限公司吉林设计院 | Strong brine evaporation and crystallization system |
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| CN104891531B (en) * | 2015-05-13 | 2017-03-01 | 中盐舞阳盐化有限公司 | A kind of preparation method of metal sodium salt |
| CN104891531A (en) * | 2015-05-13 | 2015-09-09 | 中盐舞阳盐化有限公司 | Preparation method of metal sodium salt |
| CN105293530A (en) * | 2015-11-02 | 2016-02-03 | 中盐工程技术研究院有限公司 | Crushed and washed salt production method and device |
| CN109019634A (en) * | 2018-07-18 | 2018-12-18 | 南京简迪环境工程有限公司 | The purification of chemical industry abraum salt and resource utilization system and method |
| CN109019634B (en) * | 2018-07-18 | 2021-03-26 | 南京简迪环境工程有限公司 | Chemical waste salt refining and resource utilization system and method |
| CN110395781A (en) * | 2019-07-24 | 2019-11-01 | 博天环境集团股份有限公司 | Salt eluriates Processes and apparatus, salt making apparatus and high slat-containing wastewater processing system |
| CN112456517A (en) * | 2020-12-08 | 2021-03-09 | 天津渤化永利化工股份有限公司 | Method for treating sulfate radical in salt washing brine of combined-alkali system by using nanofiltration membrane technology |
| CN113666392A (en) * | 2021-08-31 | 2021-11-19 | 中盐工程技术研究院有限公司 | Salt discharge system of counter-current salt washer and counter-current salt discharge control method |
| CN113666392B (en) * | 2021-08-31 | 2023-06-06 | 中盐工程技术研究院有限公司 | Salt discharging system of countercurrent salt washer and control method for countercurrent salt discharging |
| CN114472474A (en) * | 2022-01-06 | 2022-05-13 | 山东绿满神州环境科技有限公司 | Industrial waste salt recycling treatment system and method |
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Address after: 300450 No. 87, Xinhua Road, Tanggu District, Tianjin Patentee after: Bo Huayongli chemical inc, Tianjin Address before: 300450 No. 87, Xinhua Road, Tanggu District, Tianjin Patentee before: Tianjin Alkali Plant, Bohai Chemical Co., Ltd, Tianjin |