CN210683206U - Waste acid treatment system - Google Patents
Waste acid treatment system Download PDFInfo
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- CN210683206U CN210683206U CN201921160576.9U CN201921160576U CN210683206U CN 210683206 U CN210683206 U CN 210683206U CN 201921160576 U CN201921160576 U CN 201921160576U CN 210683206 U CN210683206 U CN 210683206U
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
- C01B7/0712—Purification ; Separation of hydrogen chloride by distillation
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Abstract
The utility model relates to a spent acid processing system, its characterized in that: the treatment system mainly comprises an analytical tower, a concentrated hydrochloric acid storage tank and a concentrated hydrochloric acid preheater; a negative pressure concentration tower; the liquid phase inlet of the dilute hydrochloric acid flash tank is communicated with the heat medium channel outlet of the concentrated hydrochloric acid preheater, the bottom liquid phase outlet and the top gas phase outlet are communicated with the middle part of the negative pressure concentration tower, and a flash evaporation pressure regulating valve is arranged between the dilute hydrochloric acid flash tank and the heat medium channel outlet of the concentrated hydrochloric acid preheater. The utility model has the advantages that: forming water vapor containing hydrogen chloride by 19% of dilute hydrochloric acid in a concentrated hydrochloric acid preheater through a dilute hydrochloric acid flash tank, and then sending the hydrogen chloride into a negative pressure concentration tower by utilizing pressure difference; compared with the prior art, the 19% dilute hydrochloric acid is cooled by the cooler and then stored by the dilute hydrochloric acid storage tank, and then pumped into the negative pressure concentration tower by the acid-resistant material pump, so that the heat in the 19% dilute hydrochloric acid is fully utilized, the power consumption of the acid-resistant material pump is avoided, and the concentration efficiency can be improved.
Description
Technical Field
The utility model relates to a waste acid processing system still relates to a waste acid processing method that the power consumption is few, waste acid recovery efficiency is high.
Background
The gas-liquid phase mercury-containing waste of the polyvinyl chloride prepared by the calcium carbide method mainly comprises waste acid and waste gas, the hydrochloric acid analysis technology is adopted, and the hydrogen chloride is recycled, and the principle is as follows:
the redundant hydrogen chloride gas from the chloroethylene reactor enters a combined absorption tower and absorbs the hydrogen chloride gas with < 1% of acid water from a waste water pump into about 31% hydrochloric acid, and the hydrochloric acid is heated by a concentrated hydrochloric acid preheater and then is sent into an analytical tower; the hydrogen chloride gas generated is resolved by matching the resolving tower with a resolving tower reboiler, a hydrogen chloride product is obtained by passing the hydrogen chloride gas through a hydrogen chloride condenser, and condensed acid condensed by the hydrogen chloride condenser directly flows back into the resolving tower. 19% dilute hydrochloric acid desorbed from the lower part of the desorption tower is sequentially cooled by a concentrated hydrochloric acid preheater and a cooler, stored by a dilute hydrochloric acid storage tank and pumped into a negative pressure concentration tower by an acid-resistant material pump. 23% hydrochloric acid is concentrated by the negative pressure concentration tower and the concentration reboiler and then is sent into the combined absorption tower from the bottom of the negative pressure concentration tower, meanwhile, evaporation steam evaporated from the top of the negative pressure concentration tower enters a condenser of the concentration tower, and condensed < 1% acid water is also pumped into the combined absorption tower, so that hydrogen chloride gas is circularly absorbed to form 31% hydrochloric acid, and the water balance in the system is basically met. However, this system has high heat energy consumption and low recovery efficiency.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to provide a calcium carbide method PVC mercury-containing waste acid processing method that the power consumption is few, waste acid recovery conversion efficiency is high.
In order to solve the technical problem, the utility model adopts the technical scheme that: the innovation point of the waste acid treatment system is as follows: the treatment system comprises an analytic tower, an analytic tower reboiler, an HCL primary condenser, an HCL secondary condenser, a condensed acid tank, a concentrated hydrochloric acid storage tank, a concentrated hydrochloric acid preheater, a negative pressure concentration tower, a concentration tower reboiler, a concentration tower top condenser, a vacuum buffer tank, a vacuumizing unit, a vacuum condensed water pump, a concentration tower discharge pump and a dilute hydrochloric acid flash tank;
the analysis tower reboiler is arranged at the bottom of the analysis tower in a matched manner and is communicated with the bottom of the analysis tower through a first reboiler circulating pipeline, so that continuous circulating temperature rise of a gas-liquid phase at the bottom of the analysis tower is realized;
the HCL primary condenser and the HCL secondary condenser are respectively provided with a condensing channel, a cooling water channel and a condensate discharging port positioned at the bottom, the condensing channel inlet of the HCL primary condenser is communicated with the top of the desorption tower, the condensing channel outlet of the HCL primary condenser is communicated with the condensing channel inlet of the HCL secondary condenser, and the condensing channel outlet of the HCL secondary condenser is a hydrogen chloride gas discharging port; condensate outlets of the HCL primary condenser and the HCL secondary condenser are communicated with an inlet of a condensed acid tank, and an outlet of the condensed acid tank is connected to an inlet of a concentrated hydrochloric acid storage tank;
the concentrated hydrochloric acid preheater is provided with a refrigerant channel and a heat medium channel, the inlet of the refrigerant channel is communicated with the outlet of the concentrated hydrochloric acid storage tank, the outlet of the refrigerant channel is connected to the top of the desorption tower 1, the inlet of the heat medium channel of the concentrated hydrochloric acid preheater is communicated with a 19% dilute hydrochloric acid outlet at the bottom of the desorption tower, and the outlet of the heat medium channel is connected to the dilute hydrochloric acid flash tank;
the negative pressure concentration tower reboiler is arranged at the bottom of the negative pressure concentration tower in a matched manner and is communicated with the bottom of the negative pressure concentration tower through a second reboiler circulating pipeline, so that continuous circulating heating of a gas-liquid phase at the bottom of the negative pressure concentration tower is realized;
the condensation tower top condenser is also provided with a condensation channel, a cooling water channel and a condensate outlet positioned at the bottom, the condensation channel inlet of the condensation tower top condenser is communicated with the top of the negative pressure condensation tower, and the condensation channel outlet of the condensation tower top condenser is simultaneously communicated with the top of the vacuum buffer tank and the vacuumizing unit;
the top of the vacuum buffer tank is also communicated with a vacuumizing unit, the bottom of the vacuum buffer tank is connected with an inlet of a vacuum condensate pump, and an outlet of the vacuum condensate pump is communicated with the top of the negative pressure concentration tower to realize the backflow of the acidic wastewater in the vacuum buffer tank;
the bottom of the negative pressure concentration tower is provided with a 20-23% hydrochloric acid outlet, and the 20-23% hydrochloric acid outlet is connected to the top of the desorption tower through a discharge pump of the concentration tower;
the dilute hydrochloric acid flash tank is provided with a liquid phase inlet, a top gas phase outlet and a bottom liquid phase outlet, the liquid phase inlet is communicated with a heat medium channel outlet of the concentrated hydrochloric acid preheater, the bottom liquid phase outlet and the top gas phase outlet are communicated with the middle part of the negative pressure concentration tower, and a flash evaporation pressure regulating valve is arranged between the dilute hydrochloric acid flash tank and the heat medium channel outlet of the concentrated hydrochloric acid preheater.
Drawings
FIG. 1 is a schematic diagram of the waste acid treatment system of the present invention.
Detailed Description
The utility model discloses a waste acid treatment system, as shown in fig. 1, the treatment system comprises an analytic tower 1, an analytic tower reboiler 2, a HCL primary condenser 3, a HCL secondary condenser 4, a condensed acid tank 5, a concentrated hydrochloric acid storage tank 6 and a concentrated hydrochloric acid preheater 7;
the system also comprises a negative pressure concentration tower 8, a concentration tower reboiler 9, a concentration tower top condenser 10, a vacuum buffer tank 11, a vacuumizing unit 12, a vacuum condensate pump 13, a concentration tower discharge pump 14 and a dilute hydrochloric acid flash tank 16;
the desorption tower reboiler 2 is arranged at the bottom of the desorption tower 1 in a sleeved mode, and the desorption tower reboiler 2 is communicated with the bottom of the desorption tower 1 through a first reboiler circulating pipeline to realize continuous circulating temperature rise of a gas-liquid phase at the bottom of the desorption tower;
the HCL primary condenser 3 and the HCL secondary condenser 4 are respectively provided with a condensing channel, a cooling water channel and a condensate discharging port positioned at the bottom, the condensing channel inlet of the HCL primary condenser 3 is communicated with the top of the desorption tower 1, the condensing channel outlet of the HCL primary condenser 3 is communicated with the condensing channel inlet of the HCL secondary condenser 4, and the condensing channel outlet of the HCL secondary condenser 4 is a hydrogen chloride gas discharging port; condensate outlets of the HCL primary condenser 3 and the HCL secondary condenser 4 are communicated with an inlet of a condensed acid tank 5, and an outlet of the condensed acid tank 5 is connected to an inlet of a concentrated hydrochloric acid storage tank 6.
The concentrated hydrochloric acid preheater 7 is provided with a refrigerant channel and a heat medium channel, the inlet of the refrigerant channel is communicated with the outlet of the concentrated hydrochloric acid storage tank 6, the outlet of the refrigerant channel is connected to the top of the desorption tower 1, the inlet of the heat medium channel of the concentrated hydrochloric acid preheater 7 is communicated with a 19% dilute hydrochloric acid outlet at the bottom of the desorption tower 1, and the outlet of the heat medium channel is connected to the dilute hydrochloric acid flash tank 16;
the negative pressure concentration tower reboiler 9 is arranged at the bottom of the negative pressure concentration tower 8 in a sleeved mode, and the negative pressure concentration tower reboiler 9 is communicated with the bottom of the negative pressure concentration tower 8 through a second reboiler circulating pipeline to achieve continuous circulating temperature rise of a gas-liquid phase at the bottom of the negative pressure concentration tower;
the concentrating tower top condenser 10 is also provided with a condensing channel, a cooling water channel and a condensate discharging port positioned at the bottom, the condensing channel inlet of the concentrating tower top condenser 10 is communicated with the top of the negative pressure concentrating tower 8, and the condensing channel outlet of the concentrating tower top condenser 10 is simultaneously communicated with the top of the vacuum buffer tank 11 and the vacuumizing unit 12;
the top of the vacuum buffer tank 11 is also communicated with a vacuumizing unit 12, the bottom of the vacuum buffer tank 11 is connected with an inlet of a vacuum condensate pump 13, and an outlet of the vacuum condensate pump 13 is communicated with the top of the negative pressure concentration tower 8 to realize the backflow of the acidic wastewater in the vacuum buffer tank 11.
The bottom of the negative pressure concentration tower 8 is provided with a 20-23% hydrochloric acid outlet, and the 20-23% hydrochloric acid outlet is connected to the top of the desorption tower 1 through a discharge pump 14 of the concentration tower.
The dilute hydrochloric acid flash tank 16 is provided with a liquid phase inlet, a top gas phase outlet and a bottom liquid phase outlet, the liquid phase inlet is communicated with a heat medium channel outlet of the concentrated hydrochloric acid preheater 7, the bottom liquid phase outlet and the top gas phase outlet are communicated with the middle part of the negative pressure concentration tower 8, and a flash evaporation pressure regulating valve 17 is arranged between the dilute hydrochloric acid flash tank 16 and the heat medium channel outlet of the concentrated hydrochloric acid preheater 7.
Based on the utility model discloses a system carries out the processing method who contains mercury spent acid and does:
30 +/-2% concentrated hydrochloric acid in the concentrated hydrochloric acid storage tank and dilute hydrochloric acid discharged from the bottom of the desorption tower respectively enter the refrigerant channel and the heating medium channel for heat exchange, so that the concentrated hydrochloric acid is preheated to
Feeding the mixture into an analytical tower at 65-85 ℃;
after the concentrated hydrochloric acid is circularly heated in an analytic tower through a reboiler of the analytic tower, hydrogen chloride and part of steam in the concentrated hydrochloric acid are separated out, part of hydrogen chloride and saturated steam in the concentrated hydrochloric acid are evaporated and sequentially enter a first-stage condenser and a second-stage condenser for cooling, most of steam is cooled into a liquid phase and then absorbs hydrogen chloride gas again to form concentrated hydrochloric acid with the concentration of more than 36%, and the concentrated hydrochloric acid with the concentration of more than 36% enters a condensed acid tank for storage and flows back to a concentrated hydrochloric acid storage tank; the hydrogen chloride gas with most of water vapor removed is discharged with a small amount of water vapor and recycled;
the method comprises the following steps that 18-20% of dilute hydrochloric acid in a hot medium channel of a concentrated hydrochloric acid preheater enters a dilute hydrochloric acid flash tank, the temperature of the dilute hydrochloric acid before the dilute hydrochloric acid enters a flash tank pressure regulating valve is 80-120 ℃, and the pressure of the dilute hydrochloric acid is controlled through the opening and closing and the opening of the flash tank pressure regulating valve before the dilute hydrochloric acid enters the dilute hydrochloric acid flash tank, so that the pressure of the dilute hydrochloric acid is not lower than 0.1-0.25 MPa; meanwhile, the vacuum degree of the negative pressure concentration tower is controlled to be-0.09 MPa; after the dilute hydrochloric acid with heat enters a dilute hydrochloric acid flash tank, under the action of the pressure difference between the positive pressure of the desorption tower and the negative pressure of the negative pressure concentration tower,
separating the dilute hydrochloric acid into water vapor and liquid by flash evaporation, and respectively entering a negative pressure concentration tower; water vapor containing a small amount of hydrogen chloride gas is pumped out of the negative pressure concentration tower under the action of negative pressure, meanwhile, the dilute hydrochloric acid with the increased concentration is heated by a reboiler of the concentration tower, water in the dilute hydrochloric acid is continuously evaporated and pumped out,
after being discharged from the negative pressure concentration tower, the water vapor containing a small amount of hydrogen chloride gas is condensed by a cooler at the top of the concentration tower to form acid wastewater, and the acid wastewater is sent into the negative pressure concentration tower in a reflux manner;
the diluted hydrochloric acid is concentrated into 22 +/-1% hydrochloric acid, and the 22 +/-1% hydrochloric acid is directly connected to the top of the analytical tower without being cooled.
Claims (1)
1. A spent acid treatment system, its characterized in that: the treatment system comprises an analytic tower, an analytic tower reboiler, an HCL primary condenser, an HCL secondary condenser, a condensed acid tank, a concentrated hydrochloric acid storage tank, a concentrated hydrochloric acid preheater, a negative pressure concentration tower, a concentration tower reboiler, a concentration tower top condenser, a vacuum buffer tank, a vacuumizing unit, a vacuum condensed water pump, a concentration tower discharge pump and a dilute hydrochloric acid flash tank;
the analysis tower reboiler is arranged at the bottom of the analysis tower in a matched manner and is communicated with the bottom of the analysis tower through a first reboiler circulating pipeline, so that continuous circulating temperature rise of a gas-liquid phase at the bottom of the analysis tower is realized;
the HCL primary condenser and the HCL secondary condenser are respectively provided with a condensing channel, a cooling water channel and a condensate discharging port positioned at the bottom, the condensing channel inlet of the HCL primary condenser is communicated with the top of the desorption tower, the condensing channel outlet of the HCL primary condenser is communicated with the condensing channel inlet of the HCL secondary condenser, and the condensing channel outlet of the HCL secondary condenser is a hydrogen chloride gas discharging port; condensate outlets of the HCL primary condenser and the HCL secondary condenser are communicated with an inlet of a condensed acid tank, and an outlet of the condensed acid tank is connected to an inlet of a concentrated hydrochloric acid storage tank;
the concentrated hydrochloric acid preheater is provided with a refrigerant channel and a heat medium channel, the inlet of the refrigerant channel is communicated with the outlet of the concentrated hydrochloric acid storage tank, the outlet of the refrigerant channel is connected to the top of the desorption tower 1, the inlet of the heat medium channel of the concentrated hydrochloric acid preheater is communicated with a 19% dilute hydrochloric acid outlet at the bottom of the desorption tower, and the outlet of the heat medium channel is connected to the dilute hydrochloric acid flash tank;
the negative pressure concentration tower reboiler is arranged at the bottom of the negative pressure concentration tower in a matched manner and is communicated with the bottom of the negative pressure concentration tower through a second reboiler circulating pipeline, so that continuous circulating heating of a gas-liquid phase at the bottom of the negative pressure concentration tower is realized;
the condensation tower top condenser is also provided with a condensation channel, a cooling water channel and a condensate outlet positioned at the bottom, the condensation channel inlet of the condensation tower top condenser is communicated with the top of the negative pressure condensation tower, and the condensation channel outlet of the condensation tower top condenser is simultaneously communicated with the top of the vacuum buffer tank and the vacuumizing unit;
the top of the vacuum buffer tank is also communicated with a vacuumizing unit, the bottom of the vacuum buffer tank is connected with an inlet of a vacuum condensate pump, and an outlet of the vacuum condensate pump is communicated with the top of the negative pressure concentration tower to realize the backflow of the acidic wastewater in the vacuum buffer tank;
the bottom of the negative pressure concentration tower is provided with a 20-23% hydrochloric acid outlet, and the 20-23% hydrochloric acid outlet is connected to the top of the desorption tower through a discharge pump of the concentration tower;
the dilute hydrochloric acid flash tank is provided with a liquid phase inlet, a top gas phase outlet and a bottom liquid phase outlet, the liquid phase inlet is communicated with a heat medium channel outlet of the concentrated hydrochloric acid preheater, the bottom liquid phase outlet and the top gas phase outlet are communicated with the middle part of the negative pressure concentration tower, and a flash evaporation pressure regulating valve is arranged between the dilute hydrochloric acid flash tank and the heat medium channel outlet of the concentrated hydrochloric acid preheater.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
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| CN201910599268 | 2019-07-04 | ||
| CN2019105992684 | 2019-07-04 |
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| CN210683206U true CN210683206U (en) | 2020-06-05 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201910665960.2A Active CN110642228B (en) | 2019-07-04 | 2019-07-23 | Calcium carbide method PVC mercury-containing waste acid treatment system and method for treating waste acid by using same |
| CN201921160101.XU Withdrawn - After Issue CN211111047U (en) | 2019-07-04 | 2019-07-23 | Calcium carbide method PVC mercury-containing waste acid treatment system |
| CN201921160576.9U Active CN210683206U (en) | 2019-07-04 | 2019-07-23 | Waste acid treatment system |
| CN201910665608.9A Active CN110407173B (en) | 2019-07-04 | 2019-07-23 | Waste acid treatment system and method for treating waste acid by using same |
| CN201910724689.5A Active CN110498398B (en) | 2019-07-04 | 2019-08-07 | Waste hydrochloric acid differential pressure regeneration treatment system and regeneration treatment method |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201910665960.2A Active CN110642228B (en) | 2019-07-04 | 2019-07-23 | Calcium carbide method PVC mercury-containing waste acid treatment system and method for treating waste acid by using same |
| CN201921160101.XU Withdrawn - After Issue CN211111047U (en) | 2019-07-04 | 2019-07-23 | Calcium carbide method PVC mercury-containing waste acid treatment system |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201910665608.9A Active CN110407173B (en) | 2019-07-04 | 2019-07-23 | Waste acid treatment system and method for treating waste acid by using same |
| CN201910724689.5A Active CN110498398B (en) | 2019-07-04 | 2019-08-07 | Waste hydrochloric acid differential pressure regeneration treatment system and regeneration treatment method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115180594A (en) * | 2022-07-11 | 2022-10-14 | 新疆西部合盛硅业有限公司 | Recovery process for treating wastewater by using organic silicon pulp residues |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110642228B (en) * | 2019-07-04 | 2023-07-21 | 南通星球石墨股份有限公司 | Calcium carbide method PVC mercury-containing waste acid treatment system and method for treating waste acid by using same |
| CN111606304A (en) * | 2020-06-02 | 2020-09-01 | 贵州兰鑫石墨机电设备制造有限公司 | Dilute hydrochloric acid dechlorination concentration system |
| CN111825062A (en) * | 2020-07-28 | 2020-10-27 | 安徽东至广信农化有限公司 | Method for recovering waste sulfuric acid |
| CN111777041A (en) * | 2020-08-26 | 2020-10-16 | 伊犁南岗化工有限责任公司 | Deep analytical equipment of olefine acid concentration |
| CN111943141A (en) * | 2020-09-02 | 2020-11-17 | 南通山剑防腐科技有限公司 | Hydrochloric acid analysis device with negative pressure dehydration function and analysis process |
| CN115385303A (en) * | 2022-08-31 | 2022-11-25 | 鲁西化工集团股份有限公司硅化工分公司 | Dilute hydrochloric acid analysis system and process method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US3635664A (en) * | 1969-08-20 | 1972-01-18 | Daido Chem Eng Corp | REGENERATION OF HYDROCHLORIC ACID PICKLING WASTE BY H{11 SO{11 {0 ADDITION, DISTILLATION AND FeSO{11 {0 Precipitation |
| JPS56162050A (en) * | 1980-04-22 | 1981-12-12 | Dionex Corp | Liquid chromatography and method of using ion condensation |
| JP3975312B2 (en) * | 1999-03-30 | 2007-09-12 | 大阪瓦斯株式会社 | Waste hydrochloric acid treatment method |
| JP4169924B2 (en) * | 2000-09-12 | 2008-10-22 | 月島環境エンジニアリング株式会社 | Method and apparatus for concentrating dilute hydrochloric acid aqueous solution |
| US20070261437A1 (en) * | 2006-05-12 | 2007-11-15 | Boonstra Eric F | Enhanced process for the purification of anhydrous hydrogen chloride gas |
| CN102285641B (en) * | 2010-06-21 | 2013-07-10 | 南通星球石墨设备有限公司 | Recycling process of waste hydrochloric acid |
| DE102012219153B4 (en) * | 2012-10-19 | 2014-09-04 | Sgl Carbon Se | Process for concentrating aqueous hydrogen halide solutions |
| CN205381955U (en) * | 2016-03-08 | 2016-07-13 | 青岛绿苑环保技术有限公司 | Sour regenerating unit of abraum salt |
| CN208218404U (en) * | 2018-05-15 | 2018-12-11 | 杭州东日节能技术有限公司 | A kind of continuity method hydrochloric acid full stripping produces the device of hydrogen chloride gas |
| CN108483399A (en) * | 2018-05-29 | 2018-09-04 | 杭州东日节能技术有限公司 | A kind of VCM purification hydrochloric acid full stripping device and technique |
| CN108823419A (en) * | 2018-08-30 | 2018-11-16 | 云南临沧鑫圆锗业股份有限公司 | A kind of chlorination mentions the recovery and processing system and method for germanium and hydrochloric acid in germanium spent acid |
| CN208649420U (en) * | 2018-08-30 | 2019-03-26 | 云南临沧鑫圆锗业股份有限公司 | A kind of chlorination mentions the recovery and processing system of germanium and hydrochloric acid in germanium spent acid |
| CN110642228B (en) * | 2019-07-04 | 2023-07-21 | 南通星球石墨股份有限公司 | Calcium carbide method PVC mercury-containing waste acid treatment system and method for treating waste acid by using same |
-
2019
- 2019-07-23 CN CN201910665960.2A patent/CN110642228B/en active Active
- 2019-07-23 CN CN201921160101.XU patent/CN211111047U/en not_active Withdrawn - After Issue
- 2019-07-23 CN CN201921160576.9U patent/CN210683206U/en active Active
- 2019-07-23 CN CN201910665608.9A patent/CN110407173B/en active Active
- 2019-08-07 CN CN201910724689.5A patent/CN110498398B/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115180594A (en) * | 2022-07-11 | 2022-10-14 | 新疆西部合盛硅业有限公司 | Recovery process for treating wastewater by using organic silicon pulp residues |
| CN115180594B (en) * | 2022-07-11 | 2023-12-26 | 新疆西部合盛硅业有限公司 | Recovery process of wastewater from organosilicon slurry residue treatment |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110407173A (en) | 2019-11-05 |
| CN110642228B (en) | 2023-07-21 |
| CN110498398A (en) | 2019-11-26 |
| CN110407173B (en) | 2023-06-30 |
| CN211111047U (en) | 2020-07-28 |
| CN110498398B (en) | 2022-07-19 |
| CN110642228A (en) | 2020-01-03 |
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Address after: 226500 Jiangsu province Nantong City Jiuhua town Rugao City Huaxing Road No. 8 Patentee after: Nantong star graphite Co.,Ltd. Address before: 226500 Jiangsu province Nantong City Jiuhua town Rugao City Huaxing Road No. 8 Patentee before: NANTONG XINGQIU GRAPHITE EQUIPMENT Co.,Ltd. |
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