CN1327949A - Cool-hot fusion method for preparing anhydrous sodium sulfate and its hot-fusion tower - Google Patents
Cool-hot fusion method for preparing anhydrous sodium sulfate and its hot-fusion tower Download PDFInfo
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- CN1327949A CN1327949A CN 00112995 CN00112995A CN1327949A CN 1327949 A CN1327949 A CN 1327949A CN 00112995 CN00112995 CN 00112995 CN 00112995 A CN00112995 A CN 00112995A CN 1327949 A CN1327949 A CN 1327949A
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Abstract
A process for preparing anhydrous sodium sulfate by cool-hot fusion method includes such steps as preparing salt water from mirabilite, cooling to about 0 deg.C, separating to obtain decahydrated sodium sulfate, loading in hot-fusion tower, heating from 0 deg.c to 100 deg.c for removing crystal water, discharging from hot-fusion tower in 10-15% of solid/liquid ratio, separation and drying. Said hot-fusion tower has feed part on top, discharge port at bottom, overflow port at upper part, material returning port at lower part and jacket-type heat exchanger at upper part. Its advantages are short process, high quality of product and low cost.
Description
The present invention relates to the Chemicals production technique, particularly the anhydrous slufuric acid production method of sodium relates to the customizations construction equipment that is used for this production method simultaneously.
In the chemical industry, existing anhydrous sodium sulphate production technology mainly is a vacuum-evaporation system nitre: its principle is with the extremely boiling of the smart glass gall indirect heating of purified, wherein most moisture content vaporization to be removed with saturated vapor; Sodium sulfate concentration goes out anhydrous sodium sulphate until saturated crystallization in the smart glass gall to improve.Its technical process is referring to Fig. 1.Its technology mainly comprises: 1, glass gall is refining: the water miscible compound of calcium, magnesium etc. obtains smart glass gall through precipitation, filtration to the initial glass gall (solution of water-soluble cpdss such as contains sodium sulfate and small amount of N ACL, calcium, magnesium) that is transported by the mine through removing wherein with soda ash, the processing of burning caustic soda.2, evaporation: heat adverse current pump circulation vacuum-evaporation flow process outward as the quadruple effect that generally adopts now.The heating chamber that outer heating pump circulation is an evaporating pot is what to separate with evaporator room, feed liquid is by the recycle pump pump circulation and be heated to boiling point, enter the evaporator room flash distillation, the secondary steam that vapor-liquid separation produces is by the thermal source of evaporator room discharge as next effect, and the crystallization that solution produces in concentration process (sodium sulfate) is sunk to the bottom and discharged on time.So-called adverse current is meant that feed liquid (glass gall) adds from end effect evaporating pot, be heated evaporation concentration after to a certain degree, change the higher last effect evaporating pot of pressure over to pump and imitate (or II is imitated) evaporation discharge from I at last, heating steam is then imitated from I and is entered, and it flows to and flows to opposite with feed liquid.3, separate with dry: glass gall is separated out anhydrous sodium sulphate and is discharged evaporating pot by solid-to-liquid ratio 10-15% (volume) through the evaporation moisture content post crystallization that reaches capacity, and carries out centrifugation and obtain containing the anhydrous sodium sulphate of free-water about 4% after the spinning liquid separation is thickened to 70% (volume).Drying generally adopts dry air-flow process again, makes anhydrous sodium sulphate, i.e. Sodium sulfate anhydrous.min(99).As being that the enterprise in the Sichuan of raw material adopts above-mentioned processing method with the glauberite.In addition, vacuum-evaporation system nitre comprises that also with natural sal glauberi be raw material, and the glass gall through water dissolution system makes finished product through vacuum-evaporation again, as the manufacturing enterprise of Yuncheng, Shanxi.With the saltcake ore be that the vacuum-evaporation system nitre technology of raw material exists that Production Flow Chart is long, equipment is many, complex process, project construction investment greatly, higher weak point and the shortcoming of production cost.
The objective of the invention is to provide at the weak point of existing production technique and shortcoming a kind of cooling, hot fusion method of production anhydrous sodium sulphate, this novel process has the advantages that Production Flow Chart is short, equipment is less and production cost is lower; For this reason, the present invention also will provide a kind of hot-fusion tower that is used for this novel process.
For achieving the above object, the present invention adopts following technical scheme: a kind of cooling of production anhydrous sodium sulphate, hot fusion method, comprise the steps: that with the saltcake ore deposit be raw material, and get coarse sulfide water through water extraction, coarse sulfide water gets glass gall after filtration; The gained glass gall is cooled off in cooling room (3), be cooled to about 0 ℃, the sal glauberi crystallization is separated out; The solidliquid mixture that is come out by cooling room separates through first separator, and the solid phase after the separation deposits sal glauberi material storehouse in, and the temperature in this material storehouse is controlled at about 0 ℃; To expect that sal glauberi is under 0 ℃ of left and right sides situation in initial temperature in the storehouse, add from hot-fusion tower (8) its top feed mouth, in hot-fusion tower from the process of top to bottom, progressively be heated to 100-110 ℃, under normal pressure, remove crystal water, in solid-to-liquid ratio is under 10-15% situation, discharges through hot-fusion tower bottom discharge mouth; The nitre liquid that overflows is discharged a little less than the overflow port of opening for feed position through hot-fusion tower top; In the whole process, cold medium flow is through being arranged on the jacketed pipe heat exchanger on hot-fusion tower top, to remove the unnecessary heat in the material of top; The material that the hot-fusion tower discharge port is discharged makes the finished product anhydrous sodium sulphate after solid-liquid separation, drying.The present invention also adopts following technical scheme: a kind of hot-fusion tower that is used for aforementioned production method, its tower body are vertically installed cylindrical, and this tower body shell upper is provided with jacketed pipe heat exchanger, and its topped height is a tower body height about 1/3; This tower body top is provided with opening for feed, and top is lower than the opening for feed position and is provided with overflow port; The bottom is provided with discharge port, and this discharge port is provided with valve, and the tower body bottom is provided with a little more than the discharge port position and is used to import thermal material to keep the pressure returning charge mouth of temperature rating in the tower.
According to technique scheme, the present invention adopts the crystallisation by cooling sal glauberi, reheat is sloughed crystal water and is produced the anhydrous sodium sulphate novel process, because crystallisation by cooling removes impurity such as small amount of N ACL in the coarse sulfide water and calcium, magnesium ion naturally, thereby, the present invention has saved glass gall FF complicated in the existing vacuum-evaporation system nitre technology, simultaneously, adopt a hot-fusion tower to replace existing numerous and jumbled quadruple effect evaporation equipment (referring to Fig. 1), therefore, technical process is simplified, and the equipment configuration reduces, and production cost reduces (II sees Appendix) by a relatively large margin.
Below in conjunction with accompanying drawing the present invention is elaborated.
Fig. 1 is that existing quadruple effect heats adverse current pump circulation vacuum evaporation technology schema outward;
Fig. 2 is a process flow sheet of the present invention;
Fig. 3 is the sectional view of the hot-fusion tower of special use of the present invention;
Shown in Fig. 3, the tower body 24 of hot-fusion tower is the garden tubular, pressing vertical direction installs, this tower body top is provided with the opening for feed 21 of sal glauberi, corresponding feed control mechanism can be set, the position that tower body top is lower than opening for feed 21 is provided with overflow port 23, and the tower body bottom is provided with discharge port 22, and discharge port 22 is provided with valve and corresponding controlling organization; The tower body bottom is provided with a little more than discharge port 22 positions and forces returning charge mouth 25, is used to import thermal material to keep temperature rating in the tower.The tower body shell upper is provided with jacketed pipe heat exchanger 9, and to remove the unnecessary heat of tower body internal upper part material, its topped height is about 1/3 of a tower body height.Temperature of charge is controlled at from top to bottom from about 0 ℃ of opening for feed (2 ℃-10 ℃, be preferably 0 ℃-2 ℃, be preferably 0 ℃) and progressively is elevated to 100-110 ℃ at discharge port place in the whole tower, is preferably 100 ℃-106 ℃, is preferably 100 ℃.
The principle of the invention: the present invention utilizes method of cooling (being cooled to about 0 ℃) that the sodium sulfate in the glass gall is separated out with the sal glauberi crystallization, after separating, again sal glauberi is melted and sloughs crystal water being higher than 32.38 ℃ of heat, obtain anhydrous sodium sulphate after separate.
Fig. 2 technical process explanation: 1. main contains sodium sulfate and the small amount of sodium chloride that is transported by the mine, water-soluble cpds and suspended substances such as calcium magnesium after system 1 filters after filtration, inject glass gall and store 2.Delivering to cooling room 3 by the glass galls of glass gall storage 2 outputs cools off.Glass gall cools off under the state of about 0 ℃ of cooling room (2 ℃-10 ℃), the exhausted major part of sodium sulfate in the glass gall will be separated out with the sal glauberi crystallization, 4.5% sodium sulfate is still arranged in liquid phase, the concentration and water-soluble cpdss such as sodium-chlor, calcium, magnesium still far reach capacity, basically still being retained in liquid phase is in the mother liquor, will obtain very purified sal glauberi after separating.Cooling can be adopted directly and indirect mode: direct mode is existing vacuum pump decompression refrigeration; Indirect mode can adopt existing lithiumbromide unit refrigeration or Ammonia Compressor Unit refrigeration.Nitre liquid sal glauberi behind separator 4 that sal glauberi is separated out in cooling is sent to washer 5 washings, and the liquid phase of being come out by separator 4 is sent to jacketed pipe heat exchanger 9 as cold medium.Come to carry out the two-way flow washing with next spillage at washer 5 to hot-fusion tower 8 overflow ports to the sal glauberi of separator 4, sal glauberi after the washing is delivered to separator 6, isolated sal glauberi is sent into sal glauberi material storehouse 7, the liquid phase of being come out by separator 4 and separator 6 is delivered to jacketed pipe heat exchanger 9 on the hot-fusion tower as heat-eliminating medium in the lump with washer 5 effusive nitre liquid, carries out can returning the water source of mine as the dissolving ore after the heat exchange.See Fig. 3, hot-fusion tower 8 is closed systems of a vertical stratification, there is sal glauberi opening for feed 21 on the top and has controlling organization, valve and corresponding controlling organization are installed on the bottom discharge mouth 22, be lower than opening for feed 21 positions on top and be provided with overflow port 23, its tower body 24 is the garden tubular, is jacketed pipe heat exchanger 9 around the tower body top, and the topped height of jacketed pipe heat exchanger accounts for whole tower body height about 1/3.The tower body bottom is provided with and forces returning charge mouth 25 a little more than discharge port 22 positions.In the operating process, the temperature distribution of tower body in the vertical direction is from 0 ℃ to 100 ℃.The fusing point of sal glauberi is 32.38 ℃, approximately is positioned at 1/3 position, tower height top.Enter hot-fusion tower from opening for feed to the sal glauberi of expecting the storehouse, temperature is heated from 0 ℃ and is warming up to 32.38 ℃ of its fusing points gradually, reaches 100 ℃ more gradually, and sal glauberi heat is melted the nitre liquid of separating out sodium sulfate and contains sodium sulfate, when bottom feed liquid solid-to-liquid ratio reaches 10-15%, discharge by discharge port.Through separator 10, moisture eliminator 11 (air stream drying), make finished product again, after packing, enter stockyard 12.The liquid phase feed liquid of being come out by separator 10 reaches 100 ℃ through heating chamber 13 steam heating, imports in the towers, to keep temperature rating in the tower through the pressure returning charge mouth 25 of hot-fusion tower with forcing pump again.Nitre liquid in the hot-fusion tower from the bottom to the overflow process on top temperature be reduced to 32.38 ℃ gradually from 100 ℃, be reduced to 0 ℃ gradually from 32.38 ℃ again, to be 4.5% nitre liquid overflow and be sent to washer 5 from overflow port the concentration through being cooled to 0 ℃.The sodium sulfate of separating out in hot-fusion tower lower heating district sinks to the bottom because of proportion greater than the proportion of heating zone nitre liquid, and the proportion of sal glauberi can not sink to being discharged from less than the proportion of heating zone nitre liquid, and separate out with sal glauberi because of the sodium sulfate major part in the nitre liquid on tower body top, at this moment the proportion of sal glauberi sinks greater than cooled nitre liquid, can not be suspended in its liquid level and is taken away by the nitre liquid that overflowed.
The present invention is based on the saltcake ore deposit, especially the glauberite in Sichuan is a raw material, it is a kind of brand-new technology, compare with the refining vacuum evaporation technology of existing glass gall, have the advantage that technical process is short, the equipment consumption is few, quality product is higher and production cost is low, shown in annex III, sample sodium sulfate without washing has reached 99.8%, than the high grade of existing GB top grade product (99.3%), if after washer 5 operations of the present invention are handled, its sodium sulphate content can reach more than 99.9%; As annex II, the initial estimate result, with Sichuan factory (glass gall is made with extra care vacuum-evaporation system nitre technology), production cost all is contrast above 300 yuan/T (to comprise 99 years) in recent years, production cost of the present invention be 213.64 yuan/T (original cost in 300 yuan/T), production cost reduces by 28.8%, under the same case, mean that promptly (what should propose is in profit rising 28.8%, also consider in the measuring and calculating because facility investment reduces, thereby the depreciation of fixed assets expense reduces and causes cost this factor that descends), Sodium sulfate anhydrous.min(99) itself is low profit product, the production cost fall is near 30%, and this has suitable competitive power in the Sodium sulfate anhydrous.min(99) production industry.
Annex I: about the heat Calculation of hot-fusion tower jacketed pipe heat exchanger is set: contain the water of 0.56 unit and the sodium sulfate of 0.44 unit in the sal glauberi of each unit, it is saturated nitre liquid (33.2%) that heat is melted back nitre liquid, therefore be dissolved with the sodium sulfate of 0.2782 unit in the water of 0.56 unit, thereby will have the sodium sulfate of (0.44-0.2782)=0.1618 unit to separate out.Heat is melted the wet sodium sulfate of discharge after separating and is contained 4% nitre liquid and be pulled away, be 0.1618 * 4%=0.005 unit, so go out from the saturated nitre hydrorrhea that will have 0.56-0.005=0.555 unit after the sal glauberi heat of the unit in heating zone is melted, nitre liquid is reduced to the sal glauberi absorption that 32.38 ℃ of institute's liberated heats are come from original area and have been warming up to 32.38 ℃ from 100 ℃ in overflow process, and be cooled to 0 ℃ the process from 32.38 ℃, the saturated nitre liquid of 0.555 unit with liberated heat is: 1, nitre liquid is cooled to 0 ℃ of institute's liberated heat from 32.38 ℃: (0.555 unit water * specific heat of water+0.2782 unit sodium sulfate * sodium sulfate specific heat) * temperature difference=(0.555 * 1+0.2782 * 0.23) is units of heat (32.38-0)=20.04.2, sodium sulfate is separated out institute's liberated heat with the sal glauberi crystallization from nitre liquid: nitre liquid saturation concentration near 0 ℃ the time is 4.5%, separates out with sal glauberi from nitre liquid at the actual 0.2782-0.025=0.2532 of having only unit sodium sulfate when 32.38 ℃ are cooled to 0 ℃ so the nitre liquid that therefore overflows will be taken away 0.555 * 4.5%=0.025 unit sodium sulfate.The sal glauberi of whenever separating out a unit needs the sodium sulfate of 0.44 unit, so the sodium sulfate of 0.2532 unit can be separated out 0.575 unit sal glauberi, whenever separates out the heat that a sal glauberi will be emitted 55 units.Therefore so the crystallization liberated heat is 55 * 0.575=31.63, is cooled to from 32.38 ℃ and overflows nitre liquid liberated heat near 0 ℃ and be: 20.04+31.63=51.67 units of heat.The sal glauberi of each unit enters original area from the material storehouse and is warming up to 32.38 ℃ of heat requirements from 0 ℃ and is: (0.56 * 1+0.44 * 0.23) is units of heat (32.38-0)=21.4.Comprehensive above-mentioned being derived as makes production operation continuously, the sodium sulfate that spillage is taken away is reduced to bottom line, therefore must be by carrying out heat exchange to take away unnecessary (51.67-21.4) individual unit unfavorable factor heat at original area (being the zone of hot-fusion tower upper temp 32.38 ℃ of-0 ℃ of scopes).
Annex II: production cost measuring and calculating
Now just calculate with nickel lithium unit refrigeration.With the XZ-580 unit is example.7 ℃ of refrigerating duty 5800kw/h refrigeration temperature are gone into 12 ℃ of water temps, need the steam of gauge pressure 0.1Mpa, and 13630kg/h needs electric power 7.5kw+5.5kw+5.5kw=18.5kw, and water coolant 1421T/h sets lift 10m and needs electric power 70kw.Refrigeration water yield 1000T/h (rolling over effective refrigerating duty 5,000,000 kilocalories)
1, xz---580 unit operations (refrigeration expense) pricing is as follows: coal consumption: 540 kilocalories/kg (the vaporization calorific value of water), 1 kilocalorie/kg.Degree (water specific heat), temperature rise 25 ℃ (normal temperature) rises to 105 ℃.5500 kilocalories/kg (mark coal calorific value), 0.6 (boiler thermal output).Heavy (steam heat-transmission+water specific heat * temperature rise)/calorific value * boiler thermal output=13630[450+1 of its coal consumption=steam * (105-25)]/5500 * 0.6=2561kg/h, 130 yuan in every T coal (local coal price) is so coal consumption per hour is 332.93 yuan.Power consumption: unit operation power consumption 18.5kw, water coolant power consumption 70kw closes 88.5kw.Power consumption 88.5 * 0.35 (self power generation electricity price)=30.97 yuan.Xz---the effective refrigerating capacity of 580 units is 5,000,000 kilocalories, liberated heat is 5.5 ten thousand kilocalories/T during the sal glauberi crystallization, sodium sulfate specific heat is 0.23 kilocalorie/kg. degree, specific heat of water is 1 kilocalorie/kg. degree, lower the temperature 32.38 ℃, sodium sulfate molecular weight 142,10 molecular weight waters 180, sal glauberi molecular weight 322.Per hour can produce sal glauberi is: heavy (y) * 55 kilocalories of 5,000,000 kilocalories=sal glauberi/kg+ (sodium sulfate weight * sodium sulfate specific heat+water weight * water specific heat) * 32.38 (coolings), i.e. 5,000,000 kilocalories=y * 55 kilocalories/kg+ (142/322 * y * sodium sulfate specific heat+180/322 * y * water specific heat) * 32.38, calculate: sal glauberi is 68.33T.Heat is melted the sodium sulfate that the 68.33T sal glauberi can arrive: 68.33 * 142/322-68.33 * 0.55 * 4.5% (I sees Appendix)=28.37T.Therefore the refrigeration expense of every T sodium sulfate product is: 363.90 yuan/28.37T=12.83 unit/T.
2, heat is melted expense: every heat is melted one ton of sal glauberi needs 5.5 ten thousand kilocalorie heats (sal glauberi Heat of fusion), institute's heat requirement has been supplied with by the spillage liberated heat and from 0 ℃ to 100 ℃, and can obtain 0.1618 ton of sodium sulfate (annex I), therefore one ton of sodium sulfate heat requirement of every production is: 0.1618 * 5.5=34.06, ten thousand kilocalories.Need the consumption coal: heavy * 550 ten thousand kilocalories of 34.06 ten thousand kilocalories=coal/T (calorific value) * 0.6 (boiler thermal output), can get, it is 0.1031 ton * 130 yuan/T=13.40 unit that heat is melted coal consumption.
3, other fees project settings and certain factory maintain an equal level the moon: 36.46 yuan/T of electric power, 17.73 yuan/T of wage welfare, 21.50 yuan/T of packing, 46.67 yuan/T of manufacturing expense (depreciation, management etc.), 75.05 yuan/T of glass gall (4.61M
3Glass gall, 16.28 yuan/M of every side
3).Adding up to production cost according to 1,2,3 is 12.83+:13.40+36.46+17.73+21.50+46.67+75.05=213.64 unit/T.
Annex III: the industrial anhydrous sodium sulfate inspection report, the sodium sulfate sample is produced overview: 1. get glass gall and put in the container, get sal glauberi through the crystallisation by cooling after-filtration.2. sal glauberi heat is melted, treat that sodium sulfate separates out after-filtration and get sodium sulfate.3. the dried over sodium sulfate that will wet gets sample sodium sulfate.
Industrial anhydrous sodium sulfate
Survey report
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Claims (5)
1, a kind of cooling of production anhydrous sodium sulphate, hot fusion method are raw material with the saltcake ore deposit, get coarse sulfide water through water extraction, and coarse sulfide water makes glass gall after filtration, it is characterized in that, also comprises the steps:
(A) the gained glass gall is cooled off in cooling room (3), be cooled to about 0 ℃, the sal glauberi crystallization is separated out;
(B) solidliquid mixture that is come out by cooling room separates through separator (4), and the solid phase after the separation deposits sal glauberi material storehouse (7) in, and the temperature in this material storehouse is controlled at about 0 ℃;
(C) will expect that sal glauberi is under 0 ℃ of left and right sides situation in initial temperature in the storehouse, add from hot-fusion tower (8) its top feed mouth, in hot-fusion tower from the process of top to bottom, progressively be heated to 100-110 ℃, under normal pressure, remove crystal water, in solid-to-liquid ratio is under 10-15% situation, discharges through hot-fusion tower bottom discharge mouth; The nitre liquid that overflows is discharged a little less than the overflow port of opening for feed position through hot-fusion tower top; In the whole process, the jacketed pipe heat exchanger (9) of cold medium flow through being arranged on hot-fusion tower top is to remove the unnecessary heat in the material of top;
(D) material of hot-fusion tower discharge port discharge makes the finished product anhydrous sodium sulphate after solid-liquid separation, drying.
2, cooling according to claim 1, hot fusion method is characterized in that, also further may further comprise the steps:
(E) by the isolated solid phase of separator (4) after washer (5) washing, again through separator (6), isolated solid phase deposits sal glauberi material storehouse (7) in, and the jacketed pipe heat exchanger (9) on the isolated liquid phase introducing of separator (6) hot-fusion tower is as cold medium; The isolated liquid phase of separator (4) is introduced jacketed pipe heat exchanger (9) equally as cold medium; The nitre liquid that hot-fusion tower (8) overflow port overflows is introduced washer (5) as washings, and this washings is introduced jacketed pipe heat exchanger (9) equally again as cold medium after washer is discharged;
(F) material of discharging by the hot-fusion tower discharge port through solid-liquid separation and liquid phase again the pressure material hole through the hot-fusion tower bottom pump up and enter in the tower body.
3, cooling according to claim 1 and 2, hot fusion method is characterized in that, described glass gall cooling temperature in cooling room (3) is-2 ℃-10 ℃; The temperature in described sal glauberi material storehouse (7) is controlled at-2 ℃-4 ℃; Described sal glauberi is-2 ℃-10 ℃ in the initial temperature that enters hot-fusion tower, and described sal glauberi progressively is heated to 100 ℃-106 ℃ in hot-fusion tower.
4, cooling according to claim 3, hot fusion method is characterized in that, cooling temperature is 0 ℃ in the described cooling room (3), and the temperature in described sal glauberi material storehouse (7) is controlled at-2 ℃, and the initial temperature that described sal glauberi enters hot-fusion tower is 0 ℃; Described sal glauberi progressively is heated to 100 ℃ in hot-fusion tower.
5, a kind of hot-fusion tower that is used for claim 1 method comprises that vertical installation is the tower body of garden tubular, it is characterized in that, described tower body (24) shell upper is provided with jacketed pipe heat exchanger (9), and its topped height is about 1/3 of a tower body height; This tower body top is provided with opening for feed (21); Top is lower than opening for feed (21) position and is provided with overflow port (23); The bottom is provided with discharge port (22), and this discharge port is provided with valve; This tower body bottom is provided with a little more than discharge port (22) position and is used to import thermal material to keep the pressure returning charge mouth (25) of temperature rating in the tower.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101112384B (en) * | 2006-07-24 | 2010-05-12 | 何元仲 | Preparation technics of Chinese traditional medicine mirabilite fine particles having better water absorptivity for external appliance |
| CN101844779A (en) * | 2010-05-20 | 2010-09-29 | 四川川眉特种芒硝有限公司 | Manufacturing process of coarse grained thenardite |
| CN101885514A (en) * | 2010-07-01 | 2010-11-17 | 吕文广 | Preparation for ultrafine anhydrous sulfate by a two-step method |
| CN101966997A (en) * | 2010-10-29 | 2011-02-09 | 江苏瑞普膜技术有限公司 | Process and device for producing pyrotechnite from sodium sulfate decahydrate |
| CN102320630A (en) * | 2011-09-05 | 2012-01-18 | 湖南衡阳新澧化工有限公司 | Production method of anhydrous sodium sulfate and production equipment thereof |
| CN104724873A (en) * | 2015-03-04 | 2015-06-24 | 四川理工学院 | Method for realizing zero discharge and resource utilization of production waste water of white carbon black |
| CN106007133A (en) * | 2016-05-27 | 2016-10-12 | 苏州乔发环保科技股份有限公司 | Desulfurization wastewater concentration, evaporation, crystallization and salt separation process |
| CN106219575A (en) * | 2016-07-11 | 2016-12-14 | 四川省洪雅青衣江元明粉有限公司 | Matrii Sulfas Exsiccatus produces industrial wastewater circulating disposal process |
| CN111533142A (en) * | 2020-06-04 | 2020-08-14 | 新疆中泰化学阜康能源有限公司 | Circular production method for heating precipitated anhydrous sodium sulphate, cooling, crystallizing and concentrating |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101112384B (en) * | 2006-07-24 | 2010-05-12 | 何元仲 | Preparation technics of Chinese traditional medicine mirabilite fine particles having better water absorptivity for external appliance |
| CN101844779A (en) * | 2010-05-20 | 2010-09-29 | 四川川眉特种芒硝有限公司 | Manufacturing process of coarse grained thenardite |
| CN101885514A (en) * | 2010-07-01 | 2010-11-17 | 吕文广 | Preparation for ultrafine anhydrous sulfate by a two-step method |
| CN101885514B (en) * | 2010-07-01 | 2012-08-29 | 吉林市弗兰达科技股份有限公司 | Preparation for ultrafine anhydrous sulfate by a two-step method |
| CN101966997A (en) * | 2010-10-29 | 2011-02-09 | 江苏瑞普膜技术有限公司 | Process and device for producing pyrotechnite from sodium sulfate decahydrate |
| CN101966997B (en) * | 2010-10-29 | 2012-07-25 | 江苏瑞能防腐设备有限公司 | Process and device for producing pyrotechnite from sodium sulfate decahydrate |
| CN102320630A (en) * | 2011-09-05 | 2012-01-18 | 湖南衡阳新澧化工有限公司 | Production method of anhydrous sodium sulfate and production equipment thereof |
| CN104724873A (en) * | 2015-03-04 | 2015-06-24 | 四川理工学院 | Method for realizing zero discharge and resource utilization of production waste water of white carbon black |
| CN106007133A (en) * | 2016-05-27 | 2016-10-12 | 苏州乔发环保科技股份有限公司 | Desulfurization wastewater concentration, evaporation, crystallization and salt separation process |
| CN106007133B (en) * | 2016-05-27 | 2019-11-05 | 苏州乔发环保科技股份有限公司 | A kind of desulfurization wastewater concentration and evaporation, crystallization, salt separating technology |
| CN106219575A (en) * | 2016-07-11 | 2016-12-14 | 四川省洪雅青衣江元明粉有限公司 | Matrii Sulfas Exsiccatus produces industrial wastewater circulating disposal process |
| CN111533142A (en) * | 2020-06-04 | 2020-08-14 | 新疆中泰化学阜康能源有限公司 | Circular production method for heating precipitated anhydrous sodium sulphate, cooling, crystallizing and concentrating |
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| CN1199861C (en) | 2005-05-04 |
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