CN205061583U - System of washing is strained in soda ash crystallization - Google Patents
System of washing is strained in soda ash crystallization Download PDFInfo
- Publication number
- CN205061583U CN205061583U CN201520697984.3U CN201520697984U CN205061583U CN 205061583 U CN205061583 U CN 205061583U CN 201520697984 U CN201520697984 U CN 201520697984U CN 205061583 U CN205061583 U CN 205061583U
- Authority
- CN
- China
- Prior art keywords
- crystallization
- sode ash
- crystallizer
- diafiltration system
- sode
- 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 - Fee Related
Links
- 238000002425 crystallisation Methods 0.000 title claims abstract description 59
- 230000008025 crystallization Effects 0.000 title claims abstract description 56
- 238000005406 washing Methods 0.000 title claims abstract description 5
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 title abstract 15
- 229910000029 sodium carbonate Inorganic materials 0.000 title abstract 7
- 235000017550 sodium carbonate Nutrition 0.000 title abstract 7
- 238000011084 recovery Methods 0.000 claims abstract description 34
- 239000007788 liquid Substances 0.000 claims abstract description 24
- 239000007787 solid Substances 0.000 claims abstract description 21
- 239000002904 solvent Substances 0.000 claims abstract description 14
- 241000370738 Chlorion Species 0.000 claims abstract description 13
- NPYPAHLBTDXSSS-UHFFFAOYSA-N Potassium ion Chemical compound [K+] NPYPAHLBTDXSSS-UHFFFAOYSA-N 0.000 claims abstract description 13
- 229910001414 potassium ion Inorganic materials 0.000 claims abstract description 13
- 239000002002 slurry Substances 0.000 claims description 32
- 238000011026 diafiltration Methods 0.000 claims description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- 238000001914 filtration Methods 0.000 claims description 13
- 238000004140 cleaning Methods 0.000 claims description 10
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 238000003756 stirring Methods 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 4
- 230000007246 mechanism Effects 0.000 claims description 4
- 239000003595 mist Substances 0.000 claims description 4
- 230000000737 periodic effect Effects 0.000 claims description 3
- 239000003513 alkali Substances 0.000 abstract description 9
- 239000012535 impurity Substances 0.000 abstract description 9
- 230000015572 biosynthetic process Effects 0.000 abstract description 6
- 239000013078 crystal Substances 0.000 abstract description 4
- 230000006378 damage Effects 0.000 abstract description 4
- 230000008021 deposition Effects 0.000 abstract 1
- 239000011268 mixed slurry Substances 0.000 abstract 1
- 230000004087 circulation Effects 0.000 description 8
- 239000000428 dust Substances 0.000 description 7
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 6
- 210000005056 cell body Anatomy 0.000 description 6
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 5
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 5
- 229910052938 sodium sulfate Inorganic materials 0.000 description 5
- 235000011152 sodium sulphate Nutrition 0.000 description 5
- 238000013517 stratification Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000011780 sodium chloride Substances 0.000 description 3
- 241000282326 Felis catus Species 0.000 description 2
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 2
- SLSIUSREIHVOPK-UHFFFAOYSA-K S(=O)(=O)([O-])[O-].[Na+].[Na+].[Cl-].[K+] Chemical compound S(=O)(=O)([O-])[O-].[Na+].[Na+].[Cl-].[K+] SLSIUSREIHVOPK-UHFFFAOYSA-K 0.000 description 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 238000007689 inspection Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000011591 potassium Substances 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000001953 recrystallisation Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 229910000963 austenitic stainless steel Inorganic materials 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000006166 lysate Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000010587 phase diagram Methods 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Landscapes
- Processing Of Solid Wastes (AREA)
Abstract
The utility model relates to an alkali recovery equipment technical field, concretely relates to system of washing is strained in soda ash crystallization, including soda ash dissolving device, crystal filter device and the solid processing apparatus who connects gradually, soda ash dissolving device is including being used for soda ash and the mixed slurry transferring pump that forms the soda ash dissolving tank of thick liquids and be used for carrying thick liquids of solvent, the crystal filter device includes: crystallizer, circulating pump, heater and scrubber, crystallizer, circulating pump and heater be circulating connection in proper order, the scrubber with the crystallizer is connected. The utility model discloses relapse the heavy crystal in order to get rid of impurity after dissolving the formation thick liquids with the soda ash to avoid chlorion and the corruption and the destruction of potassium ion pair equipment in the impurity, reduce the deposition and the scale deposit phenomenon of soda recovery furnace.
Description
Technical field
The utility model relates to alkali recovery equipment technical field, is specifically related to a kind of sode ash crystallization diafiltration system.
Background technology
Alkali recovery boiler is in operational process, and black liquor constantly enters hearth combustion, and the sode ash dust of formation, through recycling, owing to containing the impurity such as chlorion and potassium ion in dust, makes the chlorion in burner hearth and potassium content constantly raise.Chlorion and potassium content too high time can reduce the stick(ing)temperature of sode ash, increase the tackyness of sode ash, cause alkali stove dust stratification and scale formation frequently to occur.On tube wall, fouling can cause heat transfer coefficient to reduce, and generated energy is reduced, and the higher corrosion also accelerating tube wall of the chloride ion content in dust stratification, causes boiler pressure parts damages.
Given this, overcome above defect of the prior art, provide a kind of sode ash crystallization diafiltration system to remove chlorion and potassium ion becomes this area technical problem urgently to be resolved hurrily.
Summary of the invention
The purpose of this utility model is the above-mentioned defect for prior art, provides a kind of sode ash crystallization diafiltration system.
The purpose of this utility model realizes by following technical measures:
A kind of sode ash crystallization diafiltration system, compared with prior art, its difference is, this sode ash crystallization diafiltration system comprises the sode ash dissolver, crystallization filtration unit and the solids treatment device that connect successively;
Described sode ash dissolver comprises for sode ash and solvent being formed the sode ash dissolving tank of slurry and being used for carrying the slurry transferring pump of slurry;
Described crystallization filtration unit comprises: crystallizer, recycle pump, well heater and washer, described crystallizer, recycle pump and well heater circulate successively and are connected, described washer is connected with described crystallizer, slurry circulates through crystallizer successively, recycle pump, well heater carry out periodic crystallisation and heating to remove chlorion in slurry and potassium ion, the crystallization formed in crystallizer enters in washer carries out recoil washing by cleaning solvent;
Described solids treatment device comprises: a water trap be connected with described washer, the solids recovery tank be connected with water trap, the liquid recovery be connected respectively with water trap and crystallizer.
Preferably, described liquid recovery is connected with described crystallizer by the first transferpump.
Preferably, described crystallization filtration unit also comprises the flasher and condensation water collection tank that are connected with well heater, and described flash tank provides steam for well heater.
Preferably, described water trap is whizzer.
Preferably, the top of described crystallizer is provided with mist eliminator.
Preferably, described sode ash dissolving tank, solids recovery tank and liquid recovery inside are equipped with stirring rake.
Preferably, described sode ash dissolving tank, solids recovery tank and liquid recovery inside are equipped with Fang Xuan mechanism.
Preferably, described sode ash crystallization diafiltration system is also provided with the second transferpump be connected with described solids recovery tank.
Preferably, the porous plate for filtering is provided with in described sode ash dissolving tank.
Sode ash crystallization diafiltration system of the present utility model utilizes the difference of the ctystallizing point of sode ash main component sodium sulfate and impurity sodium-chlor, potassium sulfate and Repone K, sode ash is dissolved after forming slurry and carry out repeatedly recrystallization to remove impurity, thus avoid chlorion in impurity and potassium ion to the corrosion of equipment and destruction, reduce dust stratification and the scale formation of alkali recovery furnace; Sode ash crystallization diafiltration system of the present utility model is provided with the granularity of washer for crystallization control, for subsequent separation process creates favorable conditions below crystallizer.
Accompanying drawing explanation
Fig. 1 is the structural representation of the sode ash crystallization diafiltration system of the utility model embodiment.
Fig. 2 is the structural representation of sode ash dissolver in the sode ash crystallization diafiltration system of the utility model embodiment.
Fig. 3 is the structural representation of crystallization filtration unit in the sode ash crystallization diafiltration system of the utility model embodiment.
Fig. 4 is the structural representation of solids treatment device in the sode ash crystallization diafiltration system of the utility model embodiment.
Fig. 5 is the sode ash crystallization diafiltration system intermediate ion phase diagram of the utility model embodiment.
Embodiment
In order to make the purpose of this utility model, technical scheme and advantage clearly understand, below in conjunction with the drawings and specific embodiments, the utility model is described in further detail.Should be appreciated that specific embodiment described herein only in order to explain the utility model, and be not used in restriction the utility model.
Sode ash be concentrated after black liquid to burn in alkali recovery furnace the dust formed.The main component of sode ash is Na
2sO
4, also containing a small amount of NaCl, K in sode ash
2sO
4, KCl.Sode ash is dissolved in after in water, forms mixing solutions (being slurry).Along with the rising Na of temperature
2sO
4, NaCl, K
2sO
4, KCl solubleness also constantly raise, but NaCl, K
2sO
4, KCl ctystallizing point lower, therefore can utilize the difference of ctystallizing point, by mixing solutions (slurry) is heated to certain temperature, then cooling concentration formed crystallization, thus reach remove Cl-and K
+object.
Refer to shown in Fig. 1 to Fig. 4, illustrate the structural representation of the sode ash crystallization diafiltration system 100 of a preferred implementation of the present utility model.The sode ash crystallization diafiltration system 100 that this specification sheets institute accompanying drawings is painted and dependency structure thereof, ratio, size etc., content all only in order to coordinate specification sheets to disclose, understand for person skilled in the art scholar and read, and be not used to limit the enforceable qualifications of the utility model, therefore the not technical essential meaning of tool, the modification of any structure, the change of proportionlity or size, the adjustment of quantity, do not affecting under effect that sode ash crystallization diafiltration system 100 of the present utility model can produce and the object that can reach, all should still drop in scope that technology contents that the utility model discloses covers.Simultaneously, quote in this specification sheets as " on ", D score, "left", "right", " centre " and " one " etc. term, only clear for the ease of describing, and be not used to limit the enforceable scope of the utility model, the change of its relativeness or adjustment, under changing technology contents without essence, when being also considered as the enforceable category of the utility model.
Present embodiments provide a kind of sode ash crystallization diafiltration system 100, it comprises the sode ash dissolver 10, crystallization filtration unit 20 and the solids treatment device 30 that connect successively.
Wherein, refer to shown in Fig. 2, sode ash dissolver 10 comprises sode ash dissolving tank 101 and slurry transferring pump 102, sode ash dissolving tank 101 is for forming slurry by sode ash and solvent, slurry transferring pump 102 is for carrying slurry in crystallization filtration unit 20, and sode ash dissolving tank 101 inside is equipped with agitator 101a and Fang Xuan mechanism (not shown).The agitator 101a at sode ash dissolving tank 101 top stirs by motor straight tape splicing is dynamic, and power of motor is 4KW, and rotating speed is 1500rpm.The anti-whirlpool device of cell body inside, can make slurry agitation even.Further, porous plate can be set in cell body inside and sode ash dissolving tank be divided into two portions (dissolving stirring area and finished product district), slurry outlet is arranged on finished product district, ensures the slurries quality in finished product district after porous plate filters, thus ensures that equipment below and pipeline do not block.Be provided with inspection door at the top of cell body and bottom, and in cell body inside, cat ladder be housed, serviceman can by inspection and maintenance inside cat ladder to cell body.Sode ash dissolving tank 101 is Verticle atmospheric pressure container, and during normal running, cell body internal temperature is 70 DEG C, and housing and main raw can select 304L.
Wherein, refer to as indicated at 3, crystallization filtration unit 20 comprises: crystallizer 201, recycle pump 202, well heater 203, washer 204, flasher (not shown), condensation water collection tank 205, mist eliminator (not shown), described crystallizer 201, recycle pump 202 circulates successively with well heater 203 and is connected, washer 204 is connected with the bottom of crystallizer 203, slurry circulates through crystallizer 201 successively, recycle pump 202, well heater 203 carries out periodic crystallisation and heating to remove chlorion in slurry and potassium ion, the crystallization formed in crystallizer 203 enters in washer 204 carries out recoil washing by cleaning solvent, flash tank provides the steam needed for heating for well heater 203, the water of condensation got rid of from well heater 203 collected by condensation water collection tank 205, the top of crystallizer is located at by mist eliminator.
Particularly, the selective freezing of sodium sulfate is carried out in one-level pump circulation crystallizer 201, and this crystallizer 201 is mixing suspension graded product tripping devices with one way outer pipe type well heater 203.In crystallization filtration unit 20, slurry keeps certain concentration, and the heat exchanger being pumped into well heater 203 from the evaporator room of crystallizer 201 is recycled to the evaporator room of crystallizer 201, is realized the pump circulation of slurry by an axial flow circulating pump 202.Steam needed for evaporating, concentrating and crystallizing or energy is provided by tubular heater 203.Vapor condensation provides the energy needed for moisture evaporation.Water of condensation is then sent to alkali recovery furnace.Along with the evaporation of moisture, sodium sulfate crystallizes out from size circulations liquid, and in size circulations liquid, the concentration of chlorion and potassium ion also can be more and more higher simultaneously.Crystallization (main component the is sodium sulfate) density formed in crystallizer 201 is greater than the size circulations liquid of surrounding, crystallization overcomes the frictional force of liquid under the effect of gravity and buoyancy, produce downward motion, enter in washer 204, in washer 204, recoil passes into cleaning solvent (such as, slurry is preferably adopted as recoil cleaning solvent) in the present embodiment, it is contrary with the direction that crystalline particle falls that cleaning solvent rinses direction, by designing the sectional dimension of crystallizer 201 and adjusting the amount of feeding of recoil cleaning solvent, the granularity of crystallization is controlled, namely large, first heavy ingot is removed from crystallizer 201, slurry as cleaning solvent can carry out crystallization in crystallizer 201, as supplementing size circulations liquid.In addition, the problem that the concentration for chlorion and potassium ion in size circulations liquid also can be more and more higher, is removed chlorine, potassium ion by the mode of discharge section size circulations liquid from whole system 100.The wave-shaped plate demister arranged in crystallizer 201 top gas exit, can effectively except carrying secretly in devaporation.Well heater 203 adopts low-pressure steam to heat slurry, makes slurry outlet temperature remain on 104 DEG C, and well heater 203 is preferably designed for single tube journey, monoshell journey counterflow configuration form, steam walks shell side, slurries walk tube side, and wherein, tube side and tube sheet material adopt super austenitic stainless steel S31254; Tube bank is by diameter 38.1mm, wall thickness 0.7mm, titanium (Gr2) the pipe composition of overall length 8000mm, diameter of the housing is 1650mm, and case material is Q345R, be 2050mm at steam-in place diameter of the housing, and steam-in adopts expander structure, can pass through dilatation step-down like this, reduce the impact of steam exchange heat pipe, in the work-ing life of increase equipment, spring supporting considered by interchanger.
Wherein, refer to shown in Fig. 4, solids treatment device 30 comprises: water trap 301, solids recovery tank 302, liquid recovery 303, first transferpump 304 and the second transferpump 305.Water trap 301 is connected with washer 204, and solids recovery tank 302 is connected with water trap 301, and liquid recovery 303 is connected respectively with water trap 301 and crystallizer 201.Liquid recovery 303 is connected with crystallizer 201 by the first transferpump 304.Second transferpump 305 is connected 302 and connects with solids recovery tank.
Particularly, the sulfate crystal that isolated granularity is larger from washer 204 contains micro-moisture owing to have passed through the recoil of cleaning solvent, because recoil cleaning solvent is slurry, causing may containing micro-chlorion and potassium ion in moisture, therefore, water trap 301 is adopted to carry out dehydration to remove chlorion and the potassium ion of these trace to it, water trap 301 is preferably whizzer, through water trap 301 process after crystallization enter in solids recovery tank 302 carry out dissolvings formation lysate mix with night, enter in alkali recovery furnace after concentrated and burn away.The liquid component removed in water trap 301 mainly slurry, again can be delivered in crystallizer 201 and carry out crystallization.Solids recovery tank and liquid recovery inside are equipped with stirring rake and Fang Xuan mechanism.
The sode ash crystallization diafiltration system of the utility model embodiment utilizes the difference of the ctystallizing point of sode ash main component sodium sulfate and impurity sodium-chlor, potassium sulfate and Repone K, sode ash is dissolved after forming slurry and carry out repeatedly recrystallization to remove impurity, thus avoid chlorion in impurity and potassium ion to the corrosion of equipment and destruction, reduce dust stratification and the scale formation of alkali recovery furnace; The sode ash crystallization diafiltration system of the utility model embodiment is provided with the granularity of washer for crystallization control, for subsequent separation process creates favorable conditions below crystallizer.
The foregoing is only preferred embodiment of the present utility model; not in order to limit the utility model; all do within spirit of the present utility model and principle any amendment, equivalent to replace and improvement etc., all should be included within protection domain of the present utility model.
Claims (9)
1. a sode ash crystallization diafiltration system, is characterized in that, this sode ash crystallization diafiltration system comprises the sode ash dissolver, crystallization filtration unit and the solids treatment device that connect successively;
Described sode ash dissolver comprises for sode ash and solvent being formed the sode ash dissolving tank of slurry and being used for carrying the slurry transferring pump of slurry;
Described crystallization filtration unit comprises: crystallizer, recycle pump, well heater and washer, described crystallizer, recycle pump and well heater circulate successively and are connected, described washer is connected with described crystallizer, slurry circulates through crystallizer successively, recycle pump, well heater carry out periodic crystallisation and heating to remove chlorion in slurry and potassium ion, the crystallization formed in crystallizer enters in washer carries out recoil washing by cleaning solvent;
Described solids treatment device comprises: a water trap be connected with described washer, the solids recovery tank be connected with water trap, the liquid recovery be connected respectively with water trap and crystallizer.
2. sode ash crystallization diafiltration system according to claim 1, is characterized in that, described liquid recovery is connected with described crystallizer by the first transferpump.
3. sode ash crystallization diafiltration system according to claim 1, is characterized in that, described crystallization filtration unit also comprises the flasher and condensation water collection tank that are connected with well heater, and described flash tank provides steam for well heater.
4. sode ash crystallization diafiltration system according to claim 1, it is characterized in that, described water trap is whizzer.
5. sode ash crystallization diafiltration system according to claim 1, it is characterized in that, the top of described crystallizer is provided with mist eliminator.
6. sode ash crystallization diafiltration system according to claim 1, it is characterized in that, described sode ash dissolving tank, solids recovery tank and liquid recovery inside are equipped with stirring rake.
7. sode ash crystallization diafiltration system according to claim 6, it is characterized in that, described sode ash dissolving tank, solids recovery tank and liquid recovery inside are equipped with Fang Xuan mechanism.
8. sode ash crystallization diafiltration system according to claim 1, is characterized in that, described sode ash crystallization diafiltration system is also provided with the second transferpump be connected with described solids recovery tank.
9. sode ash crystallization diafiltration system according to claim 1, is characterized in that, being provided with the porous plate for filtering in described sode ash dissolving tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520697984.3U CN205061583U (en) | 2015-09-10 | 2015-09-10 | System of washing is strained in soda ash crystallization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520697984.3U CN205061583U (en) | 2015-09-10 | 2015-09-10 | System of washing is strained in soda ash crystallization |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205061583U true CN205061583U (en) | 2016-03-02 |
Family
ID=55388164
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520697984.3U Expired - Fee Related CN205061583U (en) | 2015-09-10 | 2015-09-10 | System of washing is strained in soda ash crystallization |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205061583U (en) |
-
2015
- 2015-09-10 CN CN201520697984.3U patent/CN205061583U/en not_active Expired - Fee Related
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|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
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| CF01 | Termination of patent right due to non-payment of annual fee |