CN102320575B - Method for evaporating sodium persulfate at low temperature - Google Patents
Method for evaporating sodium persulfate at low temperature Download PDFInfo
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- CN102320575B CN102320575B CN2011102480372A CN201110248037A CN102320575B CN 102320575 B CN102320575 B CN 102320575B CN 2011102480372 A CN2011102480372 A CN 2011102480372A CN 201110248037 A CN201110248037 A CN 201110248037A CN 102320575 B CN102320575 B CN 102320575B
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- LCPVQAHEFVXVKT-UHFFFAOYSA-N 2-(2,4-difluorophenoxy)pyridin-3-amine Chemical compound NC1=CC=CN=C1OC1=CC=C(F)C=C1F LCPVQAHEFVXVKT-UHFFFAOYSA-N 0.000 title claims abstract description 44
- CHQMHPLRPQMAMX-UHFFFAOYSA-L sodium persulfate Substances [Na+].[Na+].[O-]S(=O)(=O)OOS([O-])(=O)=O CHQMHPLRPQMAMX-UHFFFAOYSA-L 0.000 title claims abstract description 41
- 238000001704 evaporation Methods 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000013078 crystal Substances 0.000 claims abstract description 39
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000010438 heat treatment Methods 0.000 claims abstract description 16
- 239000010413 mother solution Substances 0.000 claims abstract description 12
- 238000002425 crystallisation Methods 0.000 claims description 21
- 238000007599 discharging Methods 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 12
- 239000012452 mother liquor Substances 0.000 claims description 12
- 230000008025 crystallization Effects 0.000 claims description 11
- 230000008020 evaporation Effects 0.000 claims description 11
- 239000012153 distilled water Substances 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 7
- 238000007701 flash-distillation Methods 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 238000009834 vaporization Methods 0.000 claims description 5
- 230000008016 vaporization Effects 0.000 claims description 5
- 239000000243 solution Substances 0.000 claims description 4
- 230000000740 bleeding effect Effects 0.000 claims description 3
- 230000003139 buffering effect Effects 0.000 claims description 3
- 238000005119 centrifugation Methods 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 230000005611 electricity Effects 0.000 abstract description 2
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 239000000463 material Substances 0.000 description 5
- 238000009835 boiling Methods 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 239000006200 vaporizer Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a method for evaporating sodium persulfate at a low temperature, and the technical problem needs to be solved, and the cost for evaporating the sodium persulfate needs to be lowered. The method disclosed by the invention comprises the following steps of: feeding and preheating, forcibly and circularly heating and evaporating, crystallizing and separating through a separator, extracting, and centrifuging to obtain sodium-persulfate crystal grains and a mother solution. Compared with the prior art, the sodium persulfate is evaporated by using a mechanical-type steam-recompression evaporator, so that the evaporating temperature of the sodium persulfate is decreased, energy is saved, and the environment is protected; the energy consumption for evaporating 1 ton of water is about 1/6 to 1/5 of that of a traditional evaporator, so that the method completely gets rid of the dependence on a steam boiler and can be used as along as electricity exists; and the method has a high automation degree and fully-automatic working flows and does not need to be manually monitored.
Description
Technical field
The present invention relates to a kind of production method of Sodium Persulfate, particularly a kind of method of evaporating Sodium Persulfate.
Background technology
Sodium Persulfate can decompose sex change when temperature is higher, generate other material, can not get the material of needs, and prior art adopts the method for low-temperature evaporation crystallization Sodium Persulfate, adopts steam boiler, and the thermo-efficiency of vaporizer is low, specific energy consumption is high.
Summary of the invention
The method that the purpose of this invention is to provide a kind of evaporating sodium persulfate at low temperature, the technical problem that solve are to reduce the cost of evaporation Sodium Persulfate.
The present invention is by the following technical solutions: a kind of method of evaporating sodium persulfate at low temperature, may further comprise the steps: one, charging, temperature is that 25 ℃ saturated Sodium Persulfate solution stoste A is stored in the original fluid container, squeezed in the plate-type heat exchanger by fresh feed pump, stoste A in plate-type heat exchanger and the secondary steam phlegma in the pump feed evaporator carry out heat exchange, stoste A through a preheating after, enter shell and tube heat exchanger, in shell and tube heat exchanger, stoste A with carry out heat exchange from the steam non-condensable gas C of pump feed evaporator and the secondary steam that is mixed in the steam non-condensable gas, stoste A rises to 38 ℃ through temperature behind the secondary preheating, be admitted to pump feed evaporator, stoste A after preheating enters in the pump feed evaporator, opens vacuum pump pump feed evaporator is vacuumized; Two, the stoste A after the preheating enters pump feed evaporator and carries out the pump circulation heating evaporation, reach 38 ℃ of vaporization temperatures, the supersaturation mother liquor begins to enter crystal separator from the discharge port of pump feed evaporator, close the opening for feed of pump feed evaporator, open vapour compressor, forced circulation pump and crystallisation cycle discharging pump; Three, the supersaturation mother liquor enters crystal separator, carries out flash distillation and vapor-liquid separation in crystal separator, and by elutriation, crystallization, slowly growth, the crystal grain after growing up is deposited in the crystal separator bottom to Sodium Persulfate crystal grain in crystal separator; Four, the crystallisation cycle discharging pump will contain crystalline mother solution B and extract out, reach discharging behind the criterion of acceptability, be discharged to the buffering reaction still by pump, from crystal separator secondary steam out, enter vapour compressor, after secondary steam is compressed, temperature is elevated to about 50 ℃, be admitted to the evaporator room heating stoste A in the pump feed evaporator, in the process of heating stoste A, steam is condensed into steam condensate and is discharged after plate-type heat exchanger and stoste A heat exchange by distilled water pump, its temperature is 30 ℃, after stoste A after the preheating enters pump feed evaporator, carry out heat exchange with the secondary steam that is elevated to 50 ℃ after the compression, pump feed evaporator reaches thermal equilibrium; Five, contain crystalline mother solution B through centrifugal, centrifugation goes out Sodium Persulfate crystal grain and mother liquor, be transported to the mother liquor reflux pump again, reenter plate-type heat exchanger, heating, pump circulation heating evaporation, crystallization, so do not stop circulation, stoste A all is disposed, the finished product are distilled water D and Sodium Persulfate crystallization.
The vacuum tightness that step 1 of the present invention is connected to the ratio adjusting valve setting device of vacuum pump bleeding point is below the 0.09mpa.
Evaporating pressure in the step 2 of the present invention is controlled in the 60mbar, in 60 minutes.
The steam output of vapour compressor of the present invention is 1.5t/h.
The flow of forced circulation pump of the present invention is 380m3/h, and lift is 20m.
The flow of crystallisation cycle discharging pump of the present invention is 20m
3/ h, lift are 20m.
The criterion of acceptability that contains crystalline mother solution B of the present invention for solid-to-liquid ratio after testing reach 1/5 and particle reach more than the 0.6mm.
The crystalline mother solution B that contains of the present invention does not reach criterion of acceptability, then reenters crystal separator and carries out flash distillation and vapor-liquid separation.
Thermal equilibrium of the present invention adopts vapour compressor to keep the thermal equilibrium of pump feed evaporator.
The present invention compared with prior art, use mechanical steam recompression evaporator evaporation Sodium Persulfate, reduce the Sodium Persulfate vaporization temperature, energy-conserving and environment-protective, the energy consumption of 1 ton of water of evaporation approximately is 1/6 to 1/5 of conventional evaporator, has been completely free of the dependence to steam boiler, as long as there is electricity just can use, and level of automation is high, and the fully automatic working flow process does not need manual monitoring.
Description of drawings
Fig. 1 is the structural representation that the present invention adopts equipment.
Embodiment
Below in conjunction with drawings and Examples the present invention is described in further detail.As shown in Figure 1, the method for evaporating sodium persulfate at low temperature of the present invention may further comprise the steps:
One, charging, temperature are that 25 ℃ saturated Sodium Persulfate solution stoste A is stored in the original fluid container, are squeezed in the plate-type heat exchanger 1 by fresh feed pump, and the secondary steam phlegma in the stoste A in plate-type heat exchanger 1 and the pump feed evaporator 9 carries out heat exchange.Stoste A through a preheating after, enter shell and tube heat exchanger 8, in shell and tube heat exchanger 8, stoste A with carry out heat exchange from the steam non-condensable gas C of pump feed evaporator 9 and the secondary steam that is mixed in the steam non-condensable gas.Stoste A rises to 38 ℃ through temperature behind the secondary preheating, be admitted to pump feed evaporator 9, stoste A after preheating enters in the pump feed evaporator 9, open 5 pairs of pump feed evaporators 9 of vacuum pump and vacuumize, the vacuum tightness that is connected to the ratio adjusting valve setting device of vacuum pump 5 bleeding points is below the 0.09mpa.
Two, the stoste A after the preheating enters pump feed evaporator 9 and carries out pump circulation heating evaporation evaporating pressure and be controlled in the 60mbar, in 60 minutes, reach 38 ℃ of vaporization temperatures, the supersaturation mother liquor begins to enter crystal separator 11 from the discharge port of pump feed evaporator 9, close the opening for feed of pump feed evaporator 9, open vapour compressor 10, forced circulation pump 6 and crystallisation cycle discharging pump 7, vapour compressor 10 steam output 1.5t/h, forced circulation pump 6 flow 380m3/h, lift 20m, crystallisation cycle discharging pump 7 flow 20m
3/ h, lift 20m.
Three, the supersaturation mother liquor enters crystal separator 11, in crystal separator 11, carry out flash distillation and vapor-liquid separation, by pump feed evaporator 9, material is heated to 40 ℃ from 38 ℃ since with 3 meters liquid level difference of crystal separator 11 interior existence, this moment, boiling point was higher than temperature of charge, not evaporation, after material enters the lower crystal separator of pressure 11, boiling point lowering to 38 ℃, so material rapidly boiling vaporization and carry out two-phase and separate in separator.The principle of gas-liquid separation is to utilize gas-liquid two-phase density different in this device, and this moment, density of gas phase was 0.046kg/m3 and density of liquid phase is 1000kg/m3,, carry out gravity settling, upflow velocity is controlled in the 2m/s, and separating effect is more satisfactory.Sodium Persulfate crystal grain is interior by elutriation, crystallization, slowly growth at crystal separator 11, and the crystal grain after growing up is deposited in crystal separator 11 bottoms.
Four, crystallisation cycle discharging pump 7 will contain crystalline mother solution B and extract out, the criterion of acceptability that contains crystalline mother solution B for solid-to-liquid ratio after testing reach 1/5 and particle reach more than the 0.6mm, reach discharging behind the criterion of acceptability, be discharged to the buffering reaction still by pump.If do not reach design requirements, then reenter crystal separator 11 and carry out flash distillation and vapor-liquid separation.From crystal separator 11 secondary steam out, enter vapour compressor 10, after secondary steam is compressed, temperature is elevated to about 50 ℃, be admitted to the evaporator room heating stoste A in the pump feed evaporator 9, in the process of heating stoste A, this part steam is condensed into steam condensate and is discharged after plate-type heat exchanger 1 and stoste A heat exchange by distilled water pump 2, and its temperature is 30 ℃.After stoste A after the preheating enters pump feed evaporator 9, carry out heat exchange with the secondary steam that is elevated to 50 ℃ after the compression, pump feed evaporator 9 reaches thermal equilibrium, and only need vapour compressor 10 to keep the thermal equilibrium of pump feed evaporator 9 this moment.
Five, contain crystalline mother solution B through tripod pendulum type batch centrifugal, (power 7.5kw, capacity 200kg/ time), centrifugation goes out Sodium Persulfate crystal grain and mother liquor, is transported to the mother liquor reflux pump again, reenters plate-type heat exchanger 1, heating, pump circulation heating evaporation, crystallization, so do not stop circulation, stoste A all is disposed, the finished product are distilled water D and Sodium Persulfate crystallization.
The method of evaporating sodium persulfate at low temperature of the present invention, by programmable logic controller PLC control treating processes, all output and input signal, the operation of each equipment configuration is all finished by its supporting computer.
As shown in Figure 1, evaporating sodium persulfate at low temperature method of the present invention, employing realizes with lower device, described device is provided with heat exchanger assembly, heat exchanger assembly is composed in series by plate-type heat exchanger 1 and shell and tube heat exchanger 8, heat exchanger assembly connects the entrance of pump feed evaporator 9, the outlet of pump feed evaporator 9 connects crystal separator 11, the top vapour outlet of crystal separator 11 connects the steam input terminus of vapour compressor 10, the compressed vapour output terminal of vapour compressor 10 connects the steam-in of pump feed evaporator 9, the lower part outlet of crystal separator 11 is through the entrance of forced circulation pump 6 connection pump feed evaporators 9, and the outlet at bottom of crystal separator 11 is connected with crystallisation cycle discharging pump 7.Wherein, the tube side entrance of plate-type heat exchanger 1 connects Sodium Persulfate stoste A entrance, the tube side outlet of plate-type heat exchanger 1 connects the tube side entrance of shell and tube heat exchanger 8, and the tube side outlet of shell and tube heat exchanger 8 connects the entrance of pump feed evaporator 9 by forced circulation pump 6.Simultaneously, the distilled water outlet of pump feed evaporator 9 is connected with distillation water pot 3, and distillation water pot 3 is by the shell side distilled water entrance of distilled water pump 2 connecting plate type interchanger 1.The vapour outlet of pump feed evaporator 9 connects the shell side steam-in of shell and tube heat exchanger 8, and the shell side vapour outlet of shell and tube heat exchanger 8 connects water pot 4 by vacuum pump 5, and the distilled water outlet of shell and tube heat exchanger 8 connects distillation water pot 3.
Embodiment, the SUNE001 plate-type interchanger that plate-type heat exchanger 1 adopts the RuiShengHua Science Co., Ltd., Shenzhen City to produce; The SUNE002 type shell and tube heat exchanger that shell and tube heat exchanger 8 adopts the RuiShengHua Science Co., Ltd., Shenzhen City to produce; The SUNE003 type pump feed evaporator that pump feed evaporator 9 adopts the RuiShengHua Science Co., Ltd., Shenzhen City to produce; Horizontal heat exchanger adopts the horizontal heat exchanger of prior art; The SUNE004 type crystal separator that crystal separator 11 adopts RuiShengHua Science Co., Ltd., Shenzhen City company to produce; The SUNE005 type mechanical steam recompression vapour compressor that vapour compressor 10 adopts the RuiShengHua Science Co., Ltd., Shenzhen City to produce, PLC adopts the S7-300 of Siemens.
The running cost of the single-action steam evaporator of present embodiment and prior art compares:
The calculating of running cost is according to following data:
Inlet amount: present embodiment 2.5t/h, conventional evaporator 60t/h,
Steam output: present embodiment 1.5t/h, conventional evaporator 36t/h,
Load: present embodiment 1t/h, conventional evaporator 24t/h,
Input concentration: 40%,
Discharging is the Sodium Persulfate crystallization
Comparison of the operating energy consumption sees Table 1:
Table 11.5 ton/hour Sodium Persulfate MVR steam output Comparison of the operating energy consumption
MVR is the mechanical steam recompression vapour compressor.
The energy consumption of present embodiment be prior art the single-action steam evaporator 1/9.9.
The conversion of electric power and heat: 1kw=3600/4.2=861kcal/h,
The conversion of steam and heat: 1kg/h=540kcal/h,
The heat of 1kg steam and electric power converts: 1kg/h=540/861=0.63kw,
Working cost compares:
Commercial power: 0.7RMB/kwh,
The steam price: the 200RMB/ ton,
Process water: the 2.5RMB/ ton,
Table 21.5 ton/hour Sodium Persulfate MVR steam output running cost relatively
Present embodiment running cost is 1/4.8 of traditional single-action steam vaporizer.
Claims (9)
1. the method for an evaporating sodium persulfate at low temperature, may further comprise the steps: one, charging, temperature is that 25 ℃ saturated Sodium Persulfate solution stoste A is stored in the original fluid container, squeezed in the plate-type heat exchanger (1) by fresh feed pump, secondary steam phlegma in stoste A in plate-type heat exchanger (1) and the pump feed evaporator (9) carries out heat exchange, stoste A through a preheating after, enter shell and tube heat exchanger (8), in shell and tube heat exchanger (8), stoste A with carry out heat exchange from the steam non-condensable gas C of pump feed evaporator (9) and the secondary steam that is mixed in the steam non-condensable gas, stoste A rises to 38 ℃ through temperature behind the secondary preheating, be admitted to pump feed evaporator (9), stoste A after preheating enters in the pump feed evaporator (9), opens vacuum pump (5) pump feed evaporator (9) is vacuumized; Two, the stoste A after the preheating enters pump feed evaporator (9) and carries out the pump circulation heating evaporation, reach 38 ℃ of vaporization temperatures, the supersaturation mother liquor begins to enter crystal separator (11) from the discharge port of pump feed evaporator (9), close the opening for feed of pump feed evaporator (9), open vapour compressor (10), forced circulation pump (6) and crystallisation cycle discharging pump (7); Three, the supersaturation mother liquor enters crystal separator (11), in crystal separator (11), carry out flash distillation and vapor-liquid separation, by elutriation, crystallization, slowly growth, the crystal grain after growing up is deposited in crystal separator (11) bottom to Sodium Persulfate crystal grain in crystal separator (11); Four, crystallisation cycle discharging pump (7) will contain crystalline mother solution B and extract out, reach discharging behind the criterion of acceptability, be discharged to the buffering reaction still by pump, from crystal separator (11) secondary steam out, enter vapour compressor (10), after secondary steam is compressed, temperature is elevated to 50 ℃, be admitted to the evaporator room heating stoste A in the pump feed evaporator (9), in the process of heating stoste A, steam is condensed into steam condensate and is discharged after plate-type heat exchanger (1) and stoste A heat exchange by distilled water pump (2), its temperature is 30 ℃, after stoste A after the preheating enters pump feed evaporator (9), carry out heat exchange with the secondary steam that is elevated to 50 ℃ after the compression, pump feed evaporator (9) reaches thermal equilibrium; Five, contain crystalline mother solution B through centrifugal, centrifugation goes out Sodium Persulfate crystal grain and mother liquor, carry with the mother liquor reflux pump again, reenter plate-type heat exchanger (1), heating, pump circulation heating evaporation, crystallization, so do not stop circulation, stoste A all is disposed, the finished product are distilled water D and Sodium Persulfate crystallization.
2. the method for evaporating sodium persulfate at low temperature according to claim 1, it is characterized in that: the vacuum tightness that described step 1 is connected to the ratio adjusting valve setting device of vacuum pump (5) bleeding point is below the 0.09MPa.
3. the method for evaporating sodium persulfate at low temperature according to claim 2, it is characterized in that: the evaporating pressure in the described step 2 is controlled in the 60mbar, in 60 minutes.
4. the method for evaporating sodium persulfate at low temperature according to claim 3, it is characterized in that: the steam output of described vapour compressor (10) is 1.5t/h.
5. the method for evaporating sodium persulfate at low temperature according to claim 4, it is characterized in that: the flow of described forced circulation pump (6) is 380m
3/ h, lift are 20m.
6. the method for evaporating sodium persulfate at low temperature according to claim 5, it is characterized in that: the flow of described crystallisation cycle discharging pump (7) is 20m
3/ h, lift are 20m.
7. the method for evaporating sodium persulfate at low temperature according to claim 6 is characterized in that: the described criterion of acceptability that contains crystalline mother solution B for solid-to-liquid ratio after testing reach 1/5 and particle reach more than the 0.6mm.
8. the method for evaporating sodium persulfate at low temperature according to claim 7, it is characterized in that: the described crystalline mother solution B that contains does not reach criterion of acceptability, then reenters crystal separator (11) and carries out flash distillation and vapor-liquid separation.
9. the method for evaporating sodium persulfate at low temperature according to claim 8 is characterized in that: described thermal equilibrium adopts vapour compressor (10) to keep the thermal equilibrium of pump feed evaporator (9).
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| CN2011102480372A CN102320575B (en) | 2011-08-26 | 2011-08-26 | Method for evaporating sodium persulfate at low temperature |
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| CN103318924A (en) * | 2013-06-25 | 2013-09-25 | 代元军 | Energy-saving equipment and energy-saving method for smelting mine by virtue of waste heat |
| CN106219573A (en) * | 2016-08-26 | 2016-12-14 | 海洲环保集团有限公司 | A kind of except scar salt production system |
| CN106362429A (en) * | 2016-08-31 | 2017-02-01 | 金川集团股份有限公司 | Nickel sulfate solution continuous evaporation system |
| CN106477796A (en) * | 2016-12-21 | 2017-03-08 | 北京燕山翔宇环保工程技术有限公司 | Desulfurization wastewater treatment system and method |
| CN109867399B (en) * | 2017-12-04 | 2023-12-19 | 北京沃特普特环境科技有限公司 | Gas field wastewater desulfurization and desalination treatment system and method containing surfactant |
| CN109550274A (en) * | 2018-12-13 | 2019-04-02 | 云南锡业股份有限公司化工材料分公司 | A kind of highly acidity thermal crystalline substance continuous crystallisation device |
| CN110793238A (en) * | 2019-10-18 | 2020-02-14 | 昆山三一环保科技有限公司 | ORC low temperature electricity generation coupling MVR heat pump evaporation structure |
| CN113881952A (en) * | 2021-10-28 | 2022-01-04 | 浙江工业大学 | A kind of electrolytic synthesis method of high sodium sulfate |
| CN114426260B (en) * | 2022-03-21 | 2023-04-28 | 铜陵华兴精细化工有限公司 | Improved process for producing sodium persulfate |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1315593A (en) * | 2000-02-23 | 2001-10-03 | 三菱瓦斯化学株式会社 | Process for producing sodium persulfate |
| CN101049913A (en) * | 2007-03-30 | 2007-10-10 | 广东西陇化工有限公司 | Deammonation Method in procedure for producing sodium persulfate |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1315593A (en) * | 2000-02-23 | 2001-10-03 | 三菱瓦斯化学株式会社 | Process for producing sodium persulfate |
| CN101049913A (en) * | 2007-03-30 | 2007-10-10 | 广东西陇化工有限公司 | Deammonation Method in procedure for producing sodium persulfate |
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Effective date of registration: 20141015 Address after: Two building 77, 518000, Sha Tau Road, Yantian District, Guangdong, Shenzhen Patentee after: Shenzhen Sunevap Technology Co., Ltd. Address before: 518057 SED science and technology building, No.1 science and technology road, Shenzhen, Guangdong, 1216-1220, Nanshan District Patentee before: Zhang Xiaojiang |
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| C56 | Change in the name or address of the patentee |
Owner name: SHENZHEN SUNEVAP TECH CO., LTD. Free format text: FORMER NAME: SHENZHEN SUNEVAP TECHNOLOGY CO., LTD. |
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| CP01 | Change in the name or title of a patent holder |
Address after: Two building 77, 518000, Sha Tau Road, Yantian District, Guangdong, Shenzhen Patentee after: SHENZHEN SUNEVAP TECH. CO., LTD. Address before: Two building 77, 518000, Sha Tau Road, Yantian District, Guangdong, Shenzhen Patentee before: Shenzhen Sunevap Technology Co., Ltd. |