CN1003506B - Mfr. of sodium carbonate by solvent extraction - Google Patents
Mfr. of sodium carbonate by solvent extraction Download PDFInfo
- Publication number
- CN1003506B CN1003506B CN86104760.5A CN86104760A CN1003506B CN 1003506 B CN1003506 B CN 1003506B CN 86104760 A CN86104760 A CN 86104760A CN 1003506 B CN1003506 B CN 1003506B
- Authority
- CN
- China
- Prior art keywords
- slurry
- sodium carbonate
- solution
- crystallizer
- soda ash
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
The present invention relates to a method for preparing sodium carbonate from natural sodium bicarbonate minerals by a solution extraction method, which comprises the steps: (a) water solution of sodium hydrate, which is used as solvent contacts the underground deposition layer which comprising sodium bicarbonate to prepare water solution; (b) a part of the prepared water solution is at least pumped from a deposition layer of minerals; (c) the pumped water solution is thickened selectively by a sodium carbonate source; (d) the water solution is selectively filtered to remove entrainment solids and insoluble matter; (e) sodium carbonate-oxide hydrate is continuously crystallized by evaporating water to generate crystallizing slurry; (f) a part of crystallizing slurry is taken from the process step by a crystallizer, crystallized sodium carbonate-oxide hydrate is extracted from the water solution by a centrifugal device, and the sodium carbonate-oxide hydrate is dried.
Description
It generally is to adopt Suhl dimension ammonia-alkaline process that whole world technical scale is made soda ash, if containing NaHCO
3The crude sedimentation layer in ore deposit exists down, generally can reclaim from these ore deposits just than coming cheaply from the solvay process preparation.For example U.S.'s overwhelming majority soda ash is the yellow soda ash stone ore from underground settled layer, promptly naturally occurring trona (Na
2CO
3NaHCO
32H
2O) form provides.The yellow soda ash stone ore is general to be adopted and traditional driedly adopts that extraction method reclaims from its underground settled layer.The dried then thick urao trona of adopting can adopt the crystallization of trona method by trona, or preferably adopts the monohydrate method to become soda ash by the crystal refining of yellow soda ash monohydrate.
With produce soda ash cost related benefit from the natural crystal resource and make the soda ash of it and solvay process production compete mutually more and more to demonstrate superiority.Contain NaHCO
3The underground settled layer of natural crystal adopt the solution extraction method to reclaim with the soda ash form, even more more effective than using traditional dried extraction method of adopting.
Solution extraction method advantage of the present invention is to be particularly suitable for containing NaHCO
3Underground natural ore deposit such as trona are processed into high-grade soda ash product effectively and do not have the impurity of following ore to exist usually.
According to the present invention, from containing NaHCO
3The natural crystal resource in prepare the solution extraction method that soda ash adopts and comprise the steps:
(a) with 0.5～15%(weight) NaOH aqueous solution solvent contact and contain NaHCO
3The underground settled layer in ore deposit makes at least a portion ore, is dissolved into the yellow soda ash form, contains Na thereby generate
2CO
3The aqueous solution;
(b) extract a part at least from [underground settling zone and contain Na
2CO
3The resultant aqueous solution;
(c) selectively add Na
2CO
3-source comes this solution of enrichment so that obtain containing Na
2CO
3Be at least a kind of denseer aqueous sodium carbonate of 25% weight;
(d) selectively filter this aqueous sodium carbonate and remove entrained solids and insoluble substance;
(e) this aqueous sodium carbonate is added the crystallizer operation and come continuous crystallisation yellow soda ash monohydrate, water is evaporated under 35 ℃ to 109 ℃ temperature and produces a kind of slurry in the crystallizer operation;
(f) from the crystallizer operation, shift out a part of slurry, and adopt the yellow soda ash monohydrate of following a few step fractional crystallizations and the aqueous solution of slurry;
(ⅰ) in first step hydrocyclone, concentrate the slurry that is shifted out;
(ⅱ) use aqueous sodium carbonate to dilute above-mentioned spissated slurry as the crystallizer charging;
(ⅲ) slurry that concentration and dilution is crossed in the hydrocyclone of the second stage; Then
(ⅳ) in whizzer, spissated slurry dewatered and come fractional crystallization solid and water-bearing mother liquor; Then
(g) generation of the yellow soda ash monohydrate of dry above-mentioned centrifugal mistake contains Na under 100 ° to 175 ℃ temperature
2CO
3Be at least 95%(weight) a kind of soda ash of exsiccant basically.
The employed NaHCO that contains in technical process of the present invention
3The subterranean resource in ore deposit can be trona, wegscheiderite (Na
2CO
33NaHCO
3), nahcolite (NaHCO
3) or the mixture of these mineral, these mineral can exist with natural form.
Contain Na
2CO
3The subterranean resource in ore deposit is to use the aqueous sodium hydroxide solution solvent treatment on the spot.
Use solution extraction method commonly used that the aqueous sodium hydroxide solution solvent is imported [underground settling zone as requested by a bite well or many mouthfuls of wells.A kind of single solution extracts well generally to have injection tube and extracts pipe out.
Also can use independent injection and out well, their spacing distances are approximately from 50 to 500 meters.These wells are interconnected by the underground fracture seam that layer mineral forms, and can flow through by these faulted joint aqueous sodium hydroxide solution solvents.
It is from 0.5 to 15%(weight that the sodium hydroxide solution of making solvent contains NaOH), for the NaHCO as the nahcolite ore deposit
38-15%(weight is preferably adopted in the ore deposit that content is high) the higher sodium hydroxide solution of NaOH content.To mainly being the mineral wealth of trona, naoh concentration preferably approximately from 2 to 8%NaOH.
For the NaHCO that contains that also contains yellow soda ash
3Ore resource such as trona, the aqueous sodium hydroxide solution of making solvent should have enough concentration, so as in mineral promptly to NaHCO
3Again to Na
2CO
3Identical dissolving is provided, avoids dissolving inequality.Because yellow soda ash is solvent when taking the lead in dissolving, the further dissolving that not dissolved sodium bicarbonate stays solubilized mineral part may play direct barrier function.For the yellow soda ash stone ore, preferably use 2 to 8%(weight) NaOH concentration, generally can obtain identical dissolving.
The temperature of aqueous sodium hydroxide solution is not strict, the boiling point that its temperature range can be from the envrionment temperature to the solvent.Solvent temperature the best is from 30 ° to 60 ℃.
Make the aqueous sodium hydroxide solution of solvent and contain NaHCO
3[underground keep in touch and need time enough, thereby become the yellow soda ash form to generate sodium carbonate solution so that make to the small part mineral dissolution.
When containing NaHCO
3When the ore deposit is the yellow soda ash stone ore, can think that the aqueous sodium hydroxide solution of making solvent is to make soluble part dissolved in the mineral (for example trona) according to following reaction:
Na
2CO
3·NaHCO
3·2H
2O（s）+NaOH（aq）→2Na
2CO
3（aq）+3H
2O
In the solution that extracts mineral, the extraction solution that generates to small part is that aqueous sodium carbonate is extracted out by extracting well.Obviously, the amount of the extraction solution of recovery and speed equal to inject the amount of solvent and speed need to keep operate continuously are impossible.The pocket that stays at the dissolved ore that can estimate the solvent that injects nearly 1/10 stays, because these solution will be replaced by the extraction solution institute dissolved mineral of extraction.
The concentration of sodium carbonate of the extracting solution of extracting out depends on many factors.Residence time is that the cycle on the solvent impregnated surface to dissolution of minerals of aqueous sodium hydroxide solution is a particularly important.When the hole size in ore settling zone increased, the residence time of solvent also can increase (if the speed that solvent injects remains unchanged).The concentration sodium hydroxide in the solvent and the temperature of solvent are influential to dissolution rate, thereby to the Na of the extraction solution extracted out
2CO
3Concentration is influential.
The Na that contains from the extraction of subsurface mineral sedimentary province
2CO
3The aqueous solution requires to contain Na
2CO
3At least 20%(weight), and to contain 25%(weight at least) for best.The aqueous sodium carbonate of extracting out is selectively used Na
2CO
3Enrichment is come as required so that obtain a kind of denseer aqueous sodium carbonate up to the concentration that reaches capacity in-source.Na
2CO
3-source can be dense or saturated sodium carbonate solution, also can be to contain Na
2CO
3Mineral are as the incinerating trona.Demanding carbonate content is to reduce to minimum for the water yield that must evaporate in next Crystallization Procedure.
The aqueous sodium carbonate of extracting out filters selectively, removes any entrained solids and other insoluble substances before entering Crystallization Procedure as in essence filter operation.
In the crystallizer operation, carry out the crystallization of yellow soda ash-hydrate from the sodium carbonate solution of extracting out, evaporate moisture content down to about 109 ℃ at 35 ℃ in the operate continuously mode.Tc preferably remains between 50-109 ℃.
Solids concn during yellow soda ash-crystal of hydrate in the slurry preferably remains on 20-50%(weight) solid, in 30-40%(weight) then better between the solid.
The continuous crystallisation of yellow soda ash-hydrate is to wish in a kind of multiple-effect crystallizer, in the temperature range of above regulation, carry out, in addition, also can replace with the single-action crystallizer, for example use the mode of machinery or hot steam recompression, in about 85 ℃ to 109 ℃ operations down.
In slurry, come the yellow soda ash-hydrate of fractional crystallization and water-bearing mother liquor result just to obtain a kind of purer solid crystalline product by a certain operation; nothing should can concentrate in the aqueous solution of slurry from mineral sources impurity usually from the pollution of mineral resources.
With prior art U.S. Patent number 4,401,635 and 3,653,848 compare, and the advantage that crystal recovery process of the present invention is had is to make washing water reduce to minimum, and these washing water can dissolve to be wished to obtain solid product and reduce the crystalline product yield.This operation also makes the dilution washing water trend of adding system minimum, avoids evaporating these washing water, has also saved the supply of pure water, and when pure water lacked the source, this was very important especially.
In this process, remove a part of slurry from the crystallizer operation, this slurry generally contains 30-40%(weight) solid, and be incorporated into first step hydrocyclone and do further to concentrate.This swirler produces a kind of dense slurry stream and for example contains solid 50%(weight) and a kind of solid liquid stream that do not contain.
This liquid stream is the simple aqueous solution that comes from crystallizer, generally contain organic and inorganic impurity (as NaCl, Na
2SO
4), wherein impurity concentration is more much higher than the impurity concentration that exists in the aqueous sodium carbonate of input crystallizer operation.The liquid stream that first step hydrocyclone comes can turn back in the crystallizer operation so that reclaim its residual alkali number.
Accumulation for organic in the crystallization control slurry and inorganic impurity, it is lower than yellow soda ash-crystal of hydrate solid is played the level of disadvantageous effect, should from the slurry of crystallizer, remove a part of solution, adopt branch to draw an aqueous solution (mother liquor) method and realize this situation more easily, this aqueous solution obtains (and other the aqueous solution turns back in the crystallizer operation) and merely emits as a kind of removing liquid from first step hydrocyclone, or uses it as a kind of aqueous solution in the sodium hydroxide extraction solvent reclamation.This removing has kept containing NaHCO effectively
3The concentration of unborn acceptable organic and inorganic impurity in the ore resources, otherwise these impurity can accumulate in slurry.
The concentrated slurry that obtains from first step hydrocyclone dilutes with the identical aqueous sodium carbonate of a part, and this aqueous sodium carbonate is usually as in the crystallizer charging input crystallizer operation.This concentrated slurry solids generally divides the crystallizer feedstock solution of drawing to be diluted to about 25%(weight from about 50% solids concn (the slurry discharging current concentration of coming out from first step hydrocyclone) by adding) solid.Therefore, the ratio ranges feeding liquid of dilution: thickened pulp can be from about 0.5: 1 to 3: 1.
Above-mentioned then diluted slurry imports second stage hydrocyclone, concentrate the slurry of this dilution and produce a kind of this grade of solid solution stream hydrocyclone that do not contain the solids content of slurry is doubled, 25%(weight) the solid feed slurry is concentrated to about 50%(weight) solid flows out slurry.
The aqueous fluid stream that comes out from second stage hydrocyclone turns back to crystallizer.The clean effect of second stage hydrocyclone operation is to wash with the crystallizer feedstock solution, the slurry of the generation of first step hydrocyclone.This then wash feed solution enters into the crystallizer operation.Cause the remarkable decline of organic impurity and inorganic impurity with this " washing " diluting effect that process reached, separate these impurity then and can be present in the product crystallization if just merely carried out eddy flow.
The concentrated slurry that second stage hydrocyclone is come adds whizzer, makes the solid crystal dehydration and obtains a kind of wet cake, generally contains about 10%(weight) residual solution.Be similar to other solid-liquid separating equipments of whizzer and also can be used for replacing whizzer.
The solution that comes out from centrifugal separation processes can import the crystallizer operation with other solution stream of coming out from the hydrocyclone process.
Because with lower attached to the amount of the relevant organic and inorganic impurity of liquid residual in the crystallization, so before the crystallization filter cake of dry centrifugation, there is no need to wash the crystallization filter cake of this centrifugation, however, during centrifugation or later on, can wash selectively.
In another embodiment of the present invention, above-mentioned hydrocyclone " washing " process can be simplified by saving first step hydrocyclone.The slurry that is shifted out from the crystallizer operation directly dilutes the slurry that produces a kind of dilution with a part of crystallization feedstock solution.This grout imports hydrocyclone subsequently and concentrates.As previously described, above-mentioned spissated slurry dewaters in whizzer.
This another kind of process that only has with the one-level hydrocyclone can reach satisfied result according to the product foreign matter content, but when round-robin solution is controlled foreign matter content in will removing a part of swirler, can cause relatively large valuable alkali loss to fall.No solid solution is taken out in employing from the crystallizer quiescent centre and the such solution of discharging can be avoided this shortcoming as removing liquid.Therefore the aqueous material of a part of having avoided discharging to come out from swirler.
No matter use which kind of hydrocyclone process, the carbonic acid forging-crystal of hydrate that centrifugation is come out is dry under 100 ° of-175 ℃ of temperature.Drying process can carry out drying in thermopnore moisture eliminator, rotary dryer or traditional in addition drying plant.The dried soda ash that generates is a kind of product of high workability exclusion, and this product contains 95%(weight at least) Na
2CO
3, generally contain 99%(weight) and Na
2CO
3Or greater than 99%(weight) Na
2CO
3By the soda ash of the inventive method preparation, although there is not water to wash the centrifugation filter cake, organic and inorganic impurity is lower.The another one feature, it has mean particle size is that 20 orders are between 200 orders.
In most preferred embodiment of the present invention, carry out the solution leaching process with round-robin successive operating method.Cyclical operation needs the aqueous sodium hydroxide solution solvent source, preferably adopts to carry out the regenerated way from a part extract out to be extracted solution this provenance is provided, rather than all these solution all are processed into crystalline soda ash.
By the way that causticization is extracted the yellow soda ash composition that extracts solution out, can carry out the regeneration of solvent so that generate sodium hydroxide.Handle extraction solution with (ripe) milk of lime and can generate sodium hydroxide:
Na
2CO
3(liquid)+Ca(OH)
2(liquid or solid) → 2NaOH(liquid)+CaCO
3(Gu)
Replace dividing and draw under the situation of extracting solution, just also can carry out causticization so that needed aqueous sodium hydroxide solution solvent is provided with left a part of solution (mother liquor) after yellow soda ash-crystal of hydrate and the recovery.
In operate continuously embodiment of the present invention, when in underground pocket because soluble mineral dissolution and when needing alternate solution to stay when removing is necessary supply solution or solvent.Should be noted that this solution of staying in the hole just plays a part a kind of liquid of removing, thereby this also can stop dissolved impurity accumulation in circulate soln.
Accompanying drawing has been represented a kind of optimum cycle embodiment of the present invention, and wherein the underground settled layer of trona ore is to reclaim by the successive soln extraction effect with aqueous sodium hydroxide solution solvent, and further is processed into pure yellow soda ash product.
Contain about 6%(weight) aqueous sodium hydroxide solution solvent [1] be pressed into the underground underground settled layer of yellow soda ash stone ore that enters into continuously by injecting well [A].Contain about 23%(weight) Na
2CO
3Contain aqueous extract [2] and extract out by extracting well [B] continuously, well [B] is away from injecting approximately 100-150 rice of well [A].The aqueous extract of extracting out [2] that contains removes by filter any insoluble substance at strainer [C].
The overwhelming majority is crossed the further processing of filterable extracting solution [3] and is reclaimed soda ash.The first part [4] of crossing filtered solution in this successive round-robin flow process carries out causticization conversion with lime or calcium oxide (as described below) and comes regeneration sodium hydroxide aqueous solution solvent.This second section [5] conversion of crossing filtered solution is used to dilute the spissated slurry of swirler (as described below).
The extracting solution that heating and filtering is crossed in heat exchanger [D] is added to vaporizer [E] to the filtrate of heat [6] as feedstock solution then to about 85 ℃ temperature.
In vaporizer [E], yellow soda ash-hydrate is carried out crystallization by removing moisture content [7], the moisture content that ejects [7] is used for the filterable extracting solution that preheating enters then in heat exchanger [D], vaporizer [E] or carry out operate continuously as single-action crystallizer (at the about 85-109 of temperature ℃) or as triple effect crystallizer (in the about 50-109 of temperature ℃ scope).The slurry density that keeps it is in about 35%(weight).From crystallizer [E] slurry [8] is discharged to the first step hydrocyclone [F], slurry in [F] [8] is carried this slurry of a kind of spissated slurry of dense generation [9] and is approximately contained solid 50%(weight).
Shunted from the come out part [10] of solution of first step hydrocyclone [F], and do not turned back to crystallizer.Shunting solution stream [10] merges so that carry out causticization regeneration aqueous sodium hydroxide solution with filterable extracting solution [4].The sub-fraction [11] of the solution stream [10] of shunting is removed and is discharged.
As shown in FIG., the balanced solution that comes out from first step hydrocyclone [F] turns back to crystallizer [E].
The liquid stream [10] of shunting and removing liquid [11] play the impurity concentration that remains in the crystalline mother solution will be lower than the concentration that certain a pair of crystalline product and crystalline form thereof play disadvantageous effect.All hydrocyclone solution circulated can cause in the circulate soln impurities accumulation out of hand to crystallizer, and this not only influences crystalline form but also can cause that the two salt of the undesirable NaSO of containing take place is the eutectic effect of burkeite in crystallizer.
Containing about 50%(weight) the spissated slurry of solid [9] dilutes with crystallization feedstock solution [5], and this crystallization feedstock solution [5] is by major ingredient stream [3] shunting that is added to crystallizer [E] and come.Shunt enough solution [5] and mix the slurry [12] that produces a kind of dilution with spissated slurry [9], this slurry contains about 25%(weight) solid.
The slurry of above-mentioned dilution [12] be added to second stage hydrocyclone [G] concentrate therein obtain containing about 50%(weight) solid slurry [13].The clear liquid [14] that comes out from second stage hydrocyclone [G] is recycled and turns back to crystallizer [E].
The concentrated slurry [13] that comes out from swirler [G] is transported to whizzer [H] crystal separation that produces is become a kind of wet cake [15] and clear solution [16].Spissated slurry [13] dewaters to produce to have in whizzer [H] and is lower than 10%(weight) crystallization [15] of the yellow soda ash-hydrate of raffinate.The clear liquid [16] that is come out by centrifugation is recycled to crystallizer [E].
Wet yellow soda ash-crystal of hydrate [15] is sent to thermopnore moisture eliminator [I], and therein, raffinate and crystal water [17] are removed under about 125 ℃ of temperature.Just be recovered to the dried soda ash product of a kind of high workability [18] by moisture eliminator [I].This soda ash [18] still has lower inorganic and organic impurity content although be characterised in that the washing water washing of no use of the filter cake [15] of its centrifugation.
In the causticization operation of preparation aqueous sodium hydroxide solution solvent [1], the filtrate of shunting [4] is done to mix for the first time with lime or calcium oxide [19] in limeslaker [J] lining.The shunting filtrate [4] that joins limeslaker comprises below the aqueous cleaning night [20] that lime carbonate rinse bath [M] comes and can mention, and also comprises the swirler clear liquid [10] of the shunting from first step hydrocyclone [F] as the aforementioned.
The last overflow [21] of limeslaker [J] by three grades of causticizer K ', K ", K " ', in causticizer, carry out causticizing reaction so that react completely just being lower than under the solution boiling temperature.
The last overflow [22] of causticizer [K] is directly to import settler [L], and therein, aqueous sodium hydroxide solution [23] separates with lime carbonate slag [24].Regulate aqueous sodium hydroxide solution [23] with supplementary feed [25] and be approximately 6%(weight to the concentration that requires) NaOH, and an aqueous sodium hydroxide solution [1] that generates turns back in the solution extraction cave.
For use in the causticization operation, these a series of operations are washed with filtrate [26] (from strainer [P]) rinse bath [M] so that reclaim from the lime carbonate slag [24] of settler [L] and are contained soda in the slag and begin by series of processes regenerating oxidation calcium.As previously mentioned, contain the wash water solution [20] of alkali (sodium) and filtrate [4] merging of shunting.Washed slag [27] is transported to groove [N], and further water [7] washs and removes residual soda therein, and water [7] is from the water vapor institute condensation of vaporizer [E].Filter from slag slurry [28] process of groove [N] then, water [7] carries out additional washing in strainer [p] lining.In the rinse bath [M] of lime carbonate slag, use filtrate [26] from strainer.
The part of filter residue [29] [30] is emitted to be controlled at the accumulation of insoluble impurity in the lime circulation.Add additional Wingdale [31] in the filter residue of non-discharging, the both is added to firing again [Q].
Around kiln [Q] the lime carbonate slag is changed into calcium oxide for reusing in the causticization operation again.Firing again [Q] is to burn coal, and the lime-ash of coal fuel is integrated in the kiln slag [19] and discharges.In addition, the kiln coal gas that also can burn must be removed the part [30] of filter residue and reduces to minimum with regard to having avoided the coal ash problem and having made in order to control the ash accumulation like this.
Material balance according to processing method recited above provides in the table.This processing method normally can be produced 100 ten thousand tonnes soda ash product every year.
In table, only be listed as the main liquid stream that illustrates in the technological process, and put on the liquid number of failing to be sold at auction in the drawings.The flow velocity of main liquid stream is given in the table (with kilogram/per hour represent), yellow soda ash, impurity (NaCl.Na
2SO
4), sodium hydroxide, water, CaCO
3, inert solid amount and total flux all be listed in the table.
Na
2CO
3H
2The O inertia
Materials flow Na
2CO
3NaCl Na
2SO
4NaOH H
2The O crystallization
*CaCO
3Solid amount
1 11，077 14，907 7，453 83，598 1，357，747 - - - 1，474，782
2 404，470 17，568 8，784 - 1，327，744 - - - 1，758，566
3 369，714 16，079 8，040 - 1，213，481 - - - 1，607，314
4 34，811 1，514 757 - 114，270 - - - 151，352
5 193，826 8，427 4，214 - 636，253 - - - 842，720
7 - - - - 883，760 - - - 883，760
8 219，107 33，709 16，854 - 573，049 421，360 - - 1，264，079
9 109，553 16，854 8，427 - 286，525 421，360 - - 842，719
10 100，494 15，464 7，732 - 262，760 - - - 386，450
11 13，461 2，071 1，036 - 35，196 - - - 51，764
12 404，505 25，282 12，641 - 939，632 303，379 - - 1，685，439
13 88，486 5，478 2，739 - 206，466 303，379 - - 606，548
14 316，019 19，804 9，902 - 733，166 - - - 1，078，891
15 9，860 615 308 - 22，922 303，379 - - 337，084
16 78，626 4，863 2，431 - 183，544 - - - 269，464
17 - - - - 66，961 - - - 66，961
18 269，220 615 308 - - - - - 270，143
19 - - - - - - 58，519
＊＊15，666 74，185
23 11，077 14，907 7，453 83，598 1，126，675 - - - 1，243，710
Na
2CO
3H
2The O inertia
Materials flow Na
2CO
3NaCl Na
2SO
4NaOH H
2The O crystallization
*CaCO
3Solid amount
25 - - - - 231，072 - - - 231，072
29 - - - - 80，109 - 104，498 15，666 200，273
30 - - - - 6，553 - 8，550 1，277 16，380
31 - - - - - - 8，550 239 8，789
* do not comprise the Na in the solution
2CO
3
＊＊CaO
Claims (20)
1, a kind of extraction by solution contains NaHCO
3The nature mineral wealth prepare the processing method of soda ash, and this method comprises:
(a) with 0.5～15%(weight) the NaOH aqueous solution makes solvent and contains NaHCO
3Thereby the underground settled layer in ore deposit contacts and makes at least a portion ore be dissolved into yellow soda ash to generate and to contain Na
2CO
3The aqueous solution;
(b) extract a part at least from [underground settling zone and contain Na
2CO
3The aqueous solution;
(c) selectively add Na
2CO
3Come this aqueous solution of enrichment so that obtain containing Na
2CO
3Be 12 to 25%(weight) a kind of denseer aqueous sodium carbonate;
(d) selectively filter this aqueous sodium carbonate and remove entrained solid and insoluble substance;
(e) this aqueous sodium carbonate is added the crystallizer operation, evaporate moisture content under 35 ° to 109 ℃ temperature, the method that obtains a kind of slurry is come continuous crystallisation yellow soda ash-hydrate;
(g) yellow soda ash-hydrate of dry above-mentioned centrifugal gained under 100 ° to 175 ℃ temperature obtains containing Na
2CO
3Be at least 95%(weight) a kind of soda ash of substantially dry.
It is characterized in that: described
(c) obtain containing Na
2CO
3Be at least 25%(weight) a kind of denseer aqueous sodium carbonate, and
(f) from the crystallizer operation, shift out a part of slurry, and adopt following several steps from the aqueous solution of slurry, to isolate crystalline yellow soda ash-hydrate;
(ⅰ) in first step hydrocyclone, concentrate the slurry that is shifted out;
(ⅱ) use aqueous sodium carbonate to dilute above-mentioned spissated slurry as the crystallizer charging;
(ⅲ) slurry that concentration and dilution is crossed in the hydrocyclone of the second stage; Then
(ⅳ) in whizzer, spissated crystallization slurry dewatered crystalline solid is separated with water-bearing mother liquor.
2, method according to claim 1 is characterized in that wherein containing NaHCO
3The ore deposit is trona, wegscheiderite, nahcolite or their mixture.
3, method according to claim 1 is characterized in that this method also comprises and does not contain solid crystallizer liquid and control the accumulation of impurity and be lower than certain has disadvantageous effect for a moment to crystalline solid concentration clean a part from crystallizer.
4, method according to claim 1 is characterized in that this method comprises that also an aqueous fluid stream that is obtained from first step hydrocyclone turns back to the crystallizer operation.
5, method according to claim 1 is characterized in that this method comprises that also an aqueous fluid stream that comes out from second stage hydrocyclone turns back to the crystallizer operation.
6, method according to claim 1 is characterized in that this method comprises that also an aqueous solution that reclaims from centrifugation turns back to the crystallizer operation.
7, method according to claim 1, wherein adopt save in first step hydrocyclone, shift out slurry concentrate and use a part of aqueous sodium carbonate as the crystallizer charging directly to dilute the slurry way that is shifted out to improve step (f).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN86104760.5A CN1003506B (en) | 1986-07-17 | 1986-07-17 | Mfr. of sodium carbonate by solvent extraction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN86104760.5A CN1003506B (en) | 1986-07-17 | 1986-07-17 | Mfr. of sodium carbonate by solvent extraction |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN86104760A CN86104760A (en) | 1988-02-17 |
| CN1003506B true CN1003506B (en) | 1989-03-08 |
Family
ID=4802595
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN86104760.5A Expired CN1003506B (en) | 1986-07-17 | 1986-07-17 | Mfr. of sodium carbonate by solvent extraction |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1003506B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102198952B (en) * | 2011-03-27 | 2016-06-22 | 崔怀奇 | A kind of combined soda method systemic circulation technique |
| EP2871156A1 (en) * | 2013-11-12 | 2015-05-13 | Solvay SA | Process for treating a sodium carbonate purge |
-
1986
- 1986-07-17 CN CN86104760.5A patent/CN1003506B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| CN86104760A (en) | 1988-02-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US5766270A (en) | Solution mining of carbonate/bicarbonate deposits to produce soda ash | |
| US4344650A (en) | Recovery of alkali values from trona deposits | |
| US5283054A (en) | Process for producing sodium salts from brines of sodium ores | |
| US6589497B2 (en) | Process for preparing soda ash from solution mined bicarbonate brines | |
| US3655331A (en) | Production of sodium carbonate | |
| US7638109B2 (en) | Production of sodium sesquicarbonate and sodium carbonate monohydrate | |
| KR20210010576A (en) | Method for recovering lithium hydroxide | |
| US3933977A (en) | Process for producing sodium carbonate | |
| US6228335B1 (en) | Process for the production of sodium carbonate crystals | |
| CN112850753B (en) | Process for producing natural alkali | |
| CN104649286A (en) | Method for producing sodium metaborate and sodium perborate from boronic concentrate | |
| US3260567A (en) | Process for the recovery of soda ash from wyoming trona | |
| US4044097A (en) | Recovery of soda values from sodium carbonate crystallizer purge liquors | |
| CA1073185A (en) | Method for the large-scale industrial obtaining of magnesium oxide of high purity | |
| NO143492B (en) | PROCEDURE FOR PURIFICATION OF AN ALKALIC SODIUM CARBONATE-CONTAINING AND EVEN ALSO OCSALATE-CONTAINING SOLUTION OBTAINED BY BAYER DISSOLUTION OF BAUXITE | |
| HU180913B (en) | Process for preparing pure aluminium oxide by means of acid digestion | |
| US3656892A (en) | Method of producing soda ash | |
| US4781899A (en) | Purification of crystallized solids made via continuous crystallization | |
| CN212425464U (en) | Salt slurry elutriation and purification system for salt-nitrate co-production process by evaporation method and salt-nitrate co-production system | |
| CN1003506B (en) | Mfr. of sodium carbonate by solvent extraction | |
| US4093508A (en) | Process for recovering chemicals from the waste liquors of sulfate cellulose digestion and the waste waters of bleaching | |
| JPH11246217A (en) | Production of soda salt | |
| WO2001077021A1 (en) | Production of strontium carbonate from celestite | |
| JPS5673620A (en) | Separation of sodium sulfate and sodium chloride from mixed solution of sodium chloride and sodium sulfate | |
| US4158043A (en) | Process for producing soda ash from natural alkali metal carbonate-containing ores |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C13 | Decision | ||
| GR02 | Examined patent application | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |