CN211111047U - Calcium carbide method PVC mercury-containing waste acid treatment system - Google Patents
Calcium carbide method PVC mercury-containing waste acid treatment system Download PDFInfo
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- CN211111047U CN211111047U CN201921160101.XU CN201921160101U CN211111047U CN 211111047 U CN211111047 U CN 211111047U CN 201921160101 U CN201921160101 U CN 201921160101U CN 211111047 U CN211111047 U CN 211111047U
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- 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 mercury waste acid processing system is contained to carbide method PVC, 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 an acid treatment system still relates to a calcium carbide method PVC mercury-containing waste acid treatment system 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 mercury-containing 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 system that the power consumption is few, waste acid recovery conversion efficiency is high.
In order to solve the technical problem, the utility model discloses a calcium carbide method PVC mercury waste acid processing system for with the cooperation of combination absorption tower carry out the analytic recovery of spent acid, combination absorption tower top has an acid waste water import, combination absorption tower middle part has a 20 ~ 23% hydrochloric acid import, combination absorption tower bottom has a tail gas import and a 31% hydrochloric acid export, its innovation point lies in that processing system includes analytic tower, analytic tower reboiler, HC L primary condenser, HC L secondary condenser, condensation acid jar, concentrated hydrochloric acid storage tank, concentrated hydrochloric acid preheater, negative pressure concentration tower, concentration tower reboiler, concentration tower top condenser, vacuum buffer tank, evacuation unit, vacuum condensate water pump, concentration tower discharge pump, concentration tower cooler and 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 HC L primary condenser and the HC L secondary condenser are respectively provided with a condensation channel, a cooling water channel and a condensate outlet positioned at the bottom, the condensation channel inlet of the HC L primary condenser is communicated with the top of the desorption tower, the condensation channel outlet of the HC L primary condenser is communicated with the condensation channel inlet of the HC L secondary condenser, the condensation channel outlet of the HC L secondary condenser is a hydrogen chloride gas outlet, the condensate outlets of the hydrochloric acid primary condenser and the hydrochloric acid secondary condenser are respectively communicated with the inlet of a condensed acid tank, and the outlet of the condensed acid tank is connected to the inlet of a concentrated hydrochloric acid storage tank;
the concentrated hydrochloric acid preheater is provided with a refrigerant channel and a heat medium channel, an inlet of the refrigerant channel is communicated with a 31% hydrochloric acid outlet at the bottom of the combined absorption tower and an outlet of the concentrated hydrochloric acid storage tank, an outlet of the refrigerant channel is connected to the top of the desorption tower, a heat medium channel inlet of the concentrated hydrochloric acid preheater is communicated with a 19% dilute hydrochloric acid outlet at the bottom of the desorption tower, and an 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 the continuous circulating temperature rise 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 an acidic wastewater inlet of the combined absorption tower;
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 sequentially communicated with a discharge pump of the concentration tower and a cooler of the concentration tower and is finally connected to a 20-23% hydrochloric acid inlet of the combined absorption 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.
Preferably, the outlet of the vacuum condensate pump is also communicated with the top of the negative pressure concentration tower to realize reflux.
Preferably, the treatment system further comprises a dilute hydrochloric acid cooler, a dilute hydrochloric acid tank and a dilute hydrochloric acid pump, wherein a heat medium inlet of the dilute hydrochloric acid cooler is communicated with a heat medium channel outlet of the concentrated hydrochloric acid preheater, a heat medium outlet of the dilute hydrochloric acid cooler is connected to the dilute hydrochloric acid tank, and the dilute hydrochloric acid tank is communicated with the combined absorption tower through the dilute hydrochloric acid pump.
The utility model has the advantages that:
directly feeding 18-20% of dilute hydrochloric acid in a concentrated hydrochloric acid preheater below the desorption tower into a negative pressure concentration tower without cooling, and connecting a dilute hydrochloric acid flash tank between the concentrated hydrochloric acid preheater and the negative pressure concentration tower in series; carrying out gas-liquid separation on 18-20% of liquid phase diluted hydrochloric acid by using a diluted hydrochloric acid flash tank to form water vapor containing hydrogen chloride, and then feeding the hydrogen chloride and the water vapor into a negative pressure concentration tower by using and controlling a pressure difference between an analytic tower and the negative pressure concentration tower; 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. More importantly: through reasonable control, make it when utilizing the heat, can effectual reduction dilute hydrochloric acid directly advance the enrichment tower and to the vibration that the enrichment tower caused, played the cushioning effect, avoid causing the destruction to the stability of system to improve the life of system.
Absorbing the mixed gas from chloroethylene into 31% hydrochloric acid by a combined absorption tower, heating by a concentrated hydrochloric acid preheater, and then sending into an analytical tower; the hydrogen chloride gas desorbed by the desorption tower is cooled and discharged by the primary and secondary condensers, the generated condensate is sent to a concentrated hydrochloric acid storage tank (the concentrated hydrochloric acid storage tank simultaneously recovers the concentrated hydrochloric acid of the combined absorption tower), and then the condensate is preheated by a concentrated hydrochloric acid preheater and then flows back to the desorption tower; the heating medium of the concentrated hydrochloric acid preheater is 19% dilute hydrochloric acid which is generated by the desorption tower and is sent into the negative pressure concentration tower, no additional heat source is needed, the heat consumption of the desorption tower is reduced, and the heights of the primary condenser and the secondary condenser can be reduced;
the comprehensive heat energy recycling is realized, so that the heat generated in the analysis system and the concentration system is recycled, and the resource utilization rate is further improved.
In addition, a heating medium inlet of the dilute hydrochloric acid cooler is communicated with a heating medium channel outlet of the concentrated hydrochloric acid preheater, and 18-20% of dilute hydrochloric acid can be directly pumped into the combined absorption tower to be absorbed by hydrogen chloride gas after being cooled.
Drawings
FIG. 1 is a schematic diagram of the utility model discloses calcium carbide method PVC mercury-containing waste acid treatment system.
FIG. 2 is a schematic diagram of the treatment process of the treatment system for waste acid containing mercury in PVC by calcium carbide method.
Detailed Description
The utility model discloses a carbide method PVC mercury-containing spent acid processing system for carry out the analytic recovery of spent acid with the cooperation of combination absorption tower, the combination absorption tower top has an acid waste water import, and the combination absorption tower middle part has a 20 ~ 23% hydrochloric acid import, and the combination absorption tower bottom has a tail gas import and 31% hydrochloric acid export.
As shown in FIG. 1 and FIG. 2, the processing system comprises
The device comprises an analytical tower 1, an analytical tower reboiler 2, an HC L primary condenser 3, an HC L secondary condenser 4, a condensed acid tank 5, a concentrated hydrochloric acid storage tank 6 and a concentrated hydrochloric acid preheater 7;
the system 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, a concentration tower cooler 15 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 HC L primary condenser 3 and the HC L secondary condenser 4 are respectively provided with a condensation channel, a cooling water channel and a condensate outlet positioned at the bottom, the condensation channel inlet of the HC L primary condenser 3 is communicated with the top of the desorption tower 1, the condensation channel outlet of the HC L primary condenser 3 is communicated with the condensation channel inlet of the HC L secondary condenser 4, the condensation channel outlet of the HC L secondary condenser 4 is a hydrogen chloride gas outlet, the condensate outlets of the HC L primary condenser 3 and the HC L secondary condenser 4 are respectively communicated with the inlet of the condensed acid tank 5, and the outlet of the condensed acid tank 5 is connected to the inlet of the 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 a 31% hydrochloric acid outlet at the bottom of the combined absorption tower and 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 heat medium channel inlet 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 an acidic wastewater inlet of the combined absorption tower. The outlet of the vacuum condensate pump 13 is also communicated with the top of the negative pressure concentration tower 8 to realize reflux.
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 sequentially communicated with a discharge pump 14 of the concentration tower and a cooler 15 of the concentration tower and is finally connected to a 20-23% hydrochloric acid inlet of the combined absorption 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.
The utility model discloses a processing system still includes rare hydrochloric acid cooler 18, rare hydrochloric acid jar 19 and rare hydrochloric acid pump 20, and the heat medium import of rare hydrochloric acid cooler 18 and the heat medium channel export intercommunication of concentrated hydrochloric acid pre-heater 7, the heat medium export of rare hydrochloric acid cooler 18 insert rare hydrochloric acid jar 19, and rare hydrochloric acid jar 19 communicates through rare hydrochloric acid pump 20 and combination absorption tower.
Based on the utility model discloses a system carries out the processing method who contains mercury spent acid and does:
30 +/-2% of concentrated hydrochloric acid discharged from the bottom of the combined absorption tower is fed into a concentrated hydrochloric acid storage tank, and the concentrated hydrochloric acid in the concentrated hydrochloric acid storage tank and the dilute hydrochloric acid discharged from the bottom of the desorption tower respectively enter a refrigerant channel and a heating medium channel for heat exchange, so that the concentrated hydrochloric acid is preheated to 65-85 ℃ and then is fed into the desorption tower;
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 is sent 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 condenser at the top of the concentration tower to form acid wastewater, one part of the acid wastewater is sent into the combined absorption tower, and the other part of the acid wastewater is sent into the negative pressure concentration tower;
the diluted hydrochloric acid is concentrated into 22 plus or minus 1 percent hydrochloric acid, and the 22 plus or minus 1 percent hydrochloric acid is sent into a combined absorption tower after being cooled.
The basic principles and main features of the invention and the advantages of the invention have been shown and described above. It will be understood by those skilled in the art that the present invention is not limited to the above embodiments, and that the foregoing embodiments and descriptions are provided only to illustrate the principles of the present invention without departing from the spirit and scope of the present invention. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (3)
1. A treatment system for waste acid containing mercury in PVC (polyvinyl chloride) by a calcium carbide method is used for being matched with a combined absorption tower to analyze and recover the waste acid, the top of the combined absorption tower is provided with an acidic waste water inlet, the middle of the combined absorption tower is provided with a 20-23% hydrochloric acid inlet, and the bottom of the combined absorption tower is provided with a tail gas inlet and a 31% hydrochloric acid outlet, and is characterized in that the treatment system comprises the analysis tower, a reboiler of the analysis tower, a HC L primary condenser, a HC L secondary condenser, a condensed acid tank, a concentrated hydrochloric acid storage tank, a concentrated hydrochloric acid preheater, a negative pressure concentration tower, a reboiler of the concentration tower, a condenser at the top of the concentration tower, a vacuum buffer tank, a vacuumizing unit, a vacuum condensed water pump, a discharge pump;
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 HC L primary condenser and the HC L secondary condenser are respectively provided with a condensation channel, a cooling water channel and a condensate outlet positioned at the bottom, the condensation channel inlet of the HC L primary condenser is communicated with the top of the desorption tower, the condensation channel outlet of the HC L primary condenser is communicated with the condensation channel inlet of the HC L secondary condenser, the condensation channel outlet of the HC L secondary condenser is a hydrogen chloride gas outlet, the condensate outlets of the hydrochloric acid primary condenser and the hydrochloric acid secondary condenser are respectively communicated with the inlet of a condensed acid tank, and the outlet of the condensed acid tank is connected to the inlet of a concentrated hydrochloric acid storage tank;
the concentrated hydrochloric acid preheater is provided with a refrigerant channel and a heat medium channel, an inlet of the refrigerant channel is communicated with a 31% hydrochloric acid outlet at the bottom of the combined absorption tower and an outlet of the concentrated hydrochloric acid storage tank, an outlet of the refrigerant channel is connected to the top of the desorption tower, a heat medium channel inlet of the concentrated hydrochloric acid preheater is communicated with a 19% dilute hydrochloric acid outlet at the bottom of the desorption tower, and an 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 the continuous circulating temperature rise 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 an acidic wastewater inlet of the combined absorption tower;
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 sequentially communicated with a discharge pump of the concentration tower and a cooler of the concentration tower and is finally connected to a 20-23% hydrochloric acid inlet of the combined absorption 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.
2. The calcium carbide process PVC mercury-containing waste acid treatment system as claimed in claim 1, wherein: and the outlet of the vacuum condensate pump is also communicated with the top of the negative pressure concentration tower to realize reflux.
3. The calcium carbide process PVC mercury-containing waste acid treatment system as claimed in claim 1, wherein: the treatment system further comprises a dilute hydrochloric acid cooler, a dilute hydrochloric acid tank and a dilute hydrochloric acid pump, wherein a heat medium inlet of the dilute hydrochloric acid cooler is communicated with a heat medium channel outlet of the concentrated hydrochloric acid preheater, a heat medium outlet of the dilute hydrochloric acid cooler is connected to the dilute hydrochloric acid tank, and the dilute hydrochloric acid tank is communicated with the combined absorption tower through the dilute hydrochloric acid pump.
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| CN201910599268 | 2019-07-04 | ||
| CN2019105992684 | 2019-07-04 |
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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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| 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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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110642228A (en) * | 2019-07-04 | 2020-01-03 | 南通星球石墨设备有限公司 | Calcium carbide-process PVC mercury-containing waste acid treatment system and method for treating waste acid by using same |
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| 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 |
| 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 |
| 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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| 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 |
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| 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 |
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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
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110642228A (en) * | 2019-07-04 | 2020-01-03 | 南通星球石墨设备有限公司 | Calcium carbide-process PVC mercury-containing waste acid treatment system and method for treating waste acid by using same |
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| Publication number | Publication date |
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| CN110407173A (en) | 2019-11-05 |
| CN110642228B (en) | 2023-07-21 |
| CN110498398A (en) | 2019-11-26 |
| CN110407173B (en) | 2023-06-30 |
| CN110498398B (en) | 2022-07-19 |
| CN110642228A (en) | 2020-01-03 |
| CN210683206U (en) | 2020-06-05 |
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