CN210595271U - Waste sulfuric acid recycling device for drying chlorine - Google Patents
Waste sulfuric acid recycling device for drying chlorine Download PDFInfo
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- CN210595271U CN210595271U CN201921250330.0U CN201921250330U CN210595271U CN 210595271 U CN210595271 U CN 210595271U CN 201921250330 U CN201921250330 U CN 201921250330U CN 210595271 U CN210595271 U CN 210595271U
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Abstract
The utility model discloses a waste sulfuric acid cyclic utilization device of dry chlorine belongs to waste acid recycle technical field. The system comprises a buffer tank, an acid-acid heat exchanger, an acid cooler, a dilute sulfuric acid concentration kettle and a sulfuric acid separation tower, wherein the buffer tank is used for storing a raw material liquid containing chlorine gas waste sulfuric acid, an outlet of the buffer tank is connected with a raw material liquid feeding port of the acid-acid heat exchanger, a concentrated acid discharging port of the acid-acid heat exchanger is connected with a feeding port of the acid cooler, and a discharging port of the acid cooler is connected with a finished product intermediate tank; the raw material liquid discharge port of the acid-acid heat exchanger is connected with the feed port of the sulfuric acid separation tower, the discharge port of the sulfuric acid separation tower is connected with the feed port of the dilute sulfuric acid concentration kettle, the concentrated acid discharge port of the dilute sulfuric acid concentration kettle is connected with the concentrated acid feed port of the acid-acid heat exchanger, and the steam outlet of the dilute sulfuric acid concentration kettle is connected with the steam inlet of the sulfuric acid separation tower. The utility model discloses realize the recycle of dilute sulfuric acid and follow-up concentrated sulfuric acid, save manufacturing cost and alleviate the protection pressure.
Description
Technical Field
The utility model belongs to the technical field of waste acid recovery utilizes, more specifically say, relate to a waste sulfuric acid cyclic utilization device of dry chlorine.
Background
At present, most domestic chlorine drying devices adopt a sulfuric acid drying method, and each ton of caustic soda needs to consume about 12-16Kg of concentrated sulfuric acid with the concentration of 98%. By 2016, 12 months, the total annual production of caustic soda in China is about 3300 ten thousand tons; about 49.5-66 million tons of waste sulfuric acid with about 75% -80% of waste sulfuric acid is produced as a byproduct every year according to the actual production of the caustic soda in 2016. At present, chlorine gas drying waste sulfuric acid is treated by chlor-alkali enterprises mainly by selling the waste sulfuric acid to enterprises producing chemical fertilizers for producing the chemical fertilizers or using carbide mud for neutralizing and preparing gypsum for sale. As about 0.2 percent of chlorine is dissolved in the chlorine drying waste acid, the chlorine drying waste acid has stronger corrosivity than finished sulfuric acid, and the chlorine volatilized in the transportation and use processes seriously pollutes the environment.
In recent years, with the increasing national requirements for environmental protection, the concentration and recycling of waste sulfuric acid is becoming more and more popular. In developed economic bodies in europe and north america, chlorine drying waste sulfuric acid of chlor-alkali enterprises is recycled after almost 100% concentration. With the development of environmental protection policies and law enforcement environments in future, nearly 70 million tons/year of waste sulfuric acid generated by chlor-alkali and PVC enterprises in China can not be treated according to the current extensive method in the foreseeable future, and the recycling is a mainstream development direction.
SUMMERY OF THE UTILITY MODEL
1. Problems to be solved
Problem to prior art existence, the utility model provides a waste sulfuric acid cyclic utilization device of dry chlorine, it solves the problem of handling problem of dilute sulfuric acid and the problem of the cyclic utilization of follow-up concentrated sulfuric acid, saves manufacturing cost and alleviates the protective pressure.
2. Technical scheme
In order to solve the above problems, the utility model adopts the following technical proposal.
A waste sulfuric acid recycling device for drying chlorine comprises a buffer tank, an acid heat exchanger, an acid cooler, a dilute sulfuric acid concentration kettle and a sulfuric acid separation tower,
the buffer tank is used for storing the raw material liquid containing the chlorine gas waste sulfuric acid, the outlet of the buffer tank is connected with the raw material liquid feeding port of the acid-acid heat exchanger,
a concentrated acid discharge port of the acid-acid heat exchanger is connected with a feed port of the acid cooler,
the discharge port of the acid cooler is connected with the finished product intermediate tank;
a raw material liquid discharge port of the acid-acid heat exchanger is connected with a feed port of the sulfuric acid separation tower, a discharge port of the sulfuric acid separation tower is connected with a feed port of the dilute sulfuric acid concentration kettle, a concentrated acid discharge port of the dilute sulfuric acid concentration kettle is connected with a concentrated acid feed port of the acid-acid heat exchanger,
and a steam outlet of the dilute sulfuric acid concentration kettle is connected with a steam inlet of the sulfuric acid separation tower.
The device for recycling the waste sulfuric acid of the dry chlorine gas further comprises a raw material pump, and the raw material pump is used for conveying the feed liquid in the cache tank to the acid-acid heat exchanger.
The device for recycling the waste sulfuric acid of the dry chlorine gas further comprises a discharge pump, and the discharge pump is used for conveying the feed liquid in the acid cooler to the finished product intermediate tank.
In the above-mentioned waste sulfuric acid recycling device for drying chlorine, the condensed water outlet of the dilute sulfuric acid concentration kettle is connected with the steam condensed water tank.
In the above apparatus for recycling waste sulfuric acid from drying chlorine, the dilute sulfuric acid concentration kettle is further provided with an air inlet for raw steam to enter.
In the above-mentioned waste sulfuric acid cyclic utilization device of dry chlorine, the steam outlet of sulphuric acid knockout tower links to each other with the air inlet of tail gas cooler, the condensate outlet of tail gas cooler links to each other with the feed inlet of chlorine tail gas scrubbing tower.
In the above apparatus for recycling waste sulfuric acid from drying chlorine, the tail gas cooler is connected to the chlorine tail gas washing tower through the chlorine water storage tank.
In the above apparatus for recycling waste sulfuric acid from drying chlorine, the gas outlet of the tail gas cooler is connected to the gas inlet of the chlorine tail gas washing tower through a three-stage steam jet vacuum system and a vacuum cooler.
The process for recycling the waste sulfuric acid of the dried chlorine comprises the following steps:
(1) conveying the raw materials from outside the battery limits to a buffer tank for later use;
(2) conveying the raw material liquid in the buffer tank into an acid heat exchanger by using a raw material pump, and then conveying the raw material liquid into a sulfuric acid separation tower;
(3) separating the raw material liquid by a sulfuric acid separation tower to prepare a separation liquid and generate steam, and then conveying the separation liquid into a dilute sulfuric acid concentration kettle;
(4) concentrating the separated liquid by a dilute sulfuric acid concentration kettle to prepare concentrated liquid and generate steam, then conveying the concentrated liquid into an acid heat exchanger and transferring the concentrated liquid into an acid cooler, and conveying the steam into a sulfuric acid separation tower;
(5) the acid cooler cools the concentrated solution and conveys the concentrated solution to a finished product intermediate tank;
(6) conveying the concentrated solution of the finished product intermediate tank to a dechlorination drying section;
wherein, the raw material liquid in the step (2) and the concentrated solution in the step (4) are subjected to dividing wall type heat exchange in an acid-acid heat exchanger;
wherein, the steam generated by the sulfuric acid separation tower in the step (3) is conveyed to a tail gas cooler for condensation, and the condensate generated by condensation is conveyed to a chlorine tail gas washing tower through a chlorine water storage tank; conveying the uncondensable gas to a three-stage steam jet vacuum system for suction and discharge, cooling the sucked and discharged gas by a vacuum cooler, and conveying the cooling liquid generated by cooling to a chlorine tail gas washing tower;
wherein the waste liquid generated by the chlorine tail gas washing tower is conveyed to a sewage treatment system outside the battery limits.
In the above process for recycling waste sulfuric acid containing dry chlorine, the raw material from outside the battery limits in step (1) comprises a raw material solution containing waste sulfuric acid containing chlorine.
3. Advantageous effects
Compared with the prior art, the beneficial effects of the utility model are that:
the utility model discloses a device and technology, use the raw materials liquid that contains chlorine gas waste sulfuric acid as the raw materials, the upper reaches set up the buffer tank, the low reaches set up the finished product pans, through the sour heat exchanger, devices such as sulphuric acid separator and the concentrated cauldron of dilute sulfuric acid separate the concentration, it recycles to send back chlorine drying device respectively to the mass concentration about 98%, a small amount of waste gas that produces among the separation concentration technological process is sent back chlorine tail gas scrubbing tower in and is made sodium hypochlorite with the alkali absorption and retrieve, the waste water of production is sent to sewage treatment system and is handled the back and use as the process water. Compared with the traditional waste sulfuric acid circulating device and process, the device and the process completely avoid the pollution of acid smoke during high-concentration evaporation, have good operating environment and small discharge amount of three wastes, comprehensively utilize various anticorrosive materials with excellent performance, avoid frequent replacement after equipment corrosion, ensure the continuous and stable operation of the system, ensure the maximum average temperature difference between acid liquor and a service measuring medium, fully utilize energy, have low energy consumption and low labor intensity, and have few operators.
Drawings
FIG. 1 is a process flow diagram of the waste sulfuric acid recycling device for drying chlorine gas.
Detailed Description
The present invention will be described in detail below with reference to the accompanying drawings and specific embodiments.
Furthermore, the utility model discloses based on solve dilute sulphuric acid's processing problem and follow-up concentrated sulfuric acid how recycle, how save manufacturing cost and how alleviate the problem of protective pressure and propose, the spent acid that is used for chlorine drying to produce at present can only go waste disposal because concentration is less than 85%, contains the unable reuse of chlorine about 0.2% in the acid, and environmental protection pressure is huge, still constantly drops into fresh concentrated sulfuric acid every year, has increased the cost of enterprise's production.
Feasibility analysis of chlorine drying with concentrated regenerated sulfuric acid:
when the water content in chlorine gas is reduced to very low value (such as about 0.01%), the partial pressure of water vapour is very small, so the mass transfer driving force in drying process is reduced to very low valueThe process is very difficult to carry out, so that the domestic chlorine drying device ensures that the water content in the chlorine is less than 0.01 percent (V/V percent), the concentration of supplemented sulfuric acid of the added chlorine drying device is more than or equal to 98 percent, while the dilute sulfuric acid vacuum concentration process is limited by the cost factor of concentration from the aspect of economy, and the concentration of the sulfuric acid of the device is controlled to be about 96 percent. The mass transfer driving force of the drying process in the sulfuric acid drying tower is equal to the pressure difference between the water vapor partial pressure in the gas phase and the equilibrium water vapor partial pressure of the sulfuric acid. When the water content in the chlorine is dried to be below 0.01 percent (V/V percent), calculating the partial pressure of water vapor in the chlorine at the moment according to 92KPa (absolute pressure) in a combined drying tower, and checking the partial pressure of the water vapor on sulfuric acid, wherein the equilibrium partial pressure of the water vapor on the sulfuric acid with the concentration of about 93 percent is 0.1Pa at the normal pressure and the temperature of 25 ℃; the partial pressure of water vapor over 98% sulfuric acid approaches zero at 25 ℃ under normal pressure. Thus, the mass transfer driving force of the drying process in the combined tower can be calculated: about 9.1Pa when using 93% strength sulphuric acid; approximately equal to 9.2Pa when using sulfuric acid of 98% concentration. Therefore, when the concentration of the added sulfuric acid is between 93 and 98 percent, the difference of mass transfer driving force in the drying process in the sulfuric acid drying tower is not large, so that about 96 percent concentrated sulfuric acid obtained by using the dilute sulfuric acid vacuum concentration process can meet the requirement of the chlorine gas drying process. There are many sulfuric acid concentration techniques, among which the earlier pot-type concentration technique has high energy consumption and environmental pollution, and the reaction of high-silicon cast iron pot with high-temperature sulfuric acid to produce Fe2(SO4)3The acid is yellow and Fe is easily generated in the drying tower2(SO4)3The crystalline plugging filler gradually fades out of the market. Foreign also include for example: the Bolin (Pauling) method; a step method of flowing down from an evaporation pan arranged in a stepwise manner; a method of feeding hot air to acid flowing down in the tower and an immersion combustion method represented by the diurnal method and the kemie method of spraying hot air in an acid liquid; a Mantius (Mantius) method in which the vertical tank is evacuated and the concentration is intermittently performed by a heating coil, and the like. These methods have problems such as unsuitability for large-scale treatment, high energy consumption, low yield, unstable operation, inability of high concentration, serious mechanical loss of the apparatus, gas generation and pollution.
As shown in figure 1, the waste sulfuric acid recycling device for drying chlorine comprises a buffer tank, an acid heat exchanger, an acid cooler, a dilute sulfuric acid concentration kettle and a sulfuric acid separation tower,
the buffer tank is used for storing raw material liquid containing chlorine gas waste sulfuric acid, an outlet of the buffer tank is connected with a raw material liquid feeding port of the acid-acid heat exchanger, and the raw material pump is used for conveying the raw material liquid in the buffer tank into the acid-acid heat exchanger; the volume of the cache tank is 10 cubic, and the cache tank is made of fiber reinforced composite material; the type specification of the preheater is YKB40-15, the material of the preheater is graphite/CS anticorrosion, and the shell side of the preheater is lined with rubber; the raw material pump is used for conveying the feed liquid in the raw material cache tank into the preheater, wherein the flow rate of the raw material pump is 2 cubic/h, the lift of the raw material pump is 30 meters, and the raw material pump is made of steel lining PTFE;
a concentrated acid discharge port of the acid-acid heat exchanger is connected with a feed port of the acid cooler; the type of the acid-acid heat exchanger is E1102, and the acid-acid heat exchanger is a bidirectional anticorrosive tubular heat exchanger; wherein the acid cooler is type E1101;
the discharge port of the acid cooler is connected with the finished product intermediate tank; the finished product intermediate tank can resist vacuum, the volume in the intermediate tank is 1 cube, and the intermediate tank is made of PTFE/CS; the discharging pump is used for conveying the feed liquid in the acid cooler to the finished product intermediate tank, wherein the flow rate of the discharging pump is 1 cubic meter per hour, the lift of the discharging pump is 20 meters, and the discharging pump is made of steel lined PTFE;
a raw material liquid discharge port of the acid-acid heat exchanger is connected with a feed port of the sulfuric acid separation tower, a discharge port of the sulfuric acid separation tower is connected with a feed port of the dilute sulfuric acid concentration kettle, and a concentrated acid discharge port of the dilute sulfuric acid concentration kettle is connected with a concentrated acid feed port of the acid-acid heat exchanger; the model of the sulfuric acid separation tower is T1101, wherein the model of a dilute sulfuric acid concentration kettle is also T1101, the dilute sulfuric acid concentration kettle is a kettle of the sulfuric acid separation tower, and the dilute sulfuric acid concentration kettle is a battle axe type reboiler made of tantalum materials. Under the high vacuum condition of more than 90 kilopascals, the dilute sulfuric acid concentration kettle adopts a horizontal vacuum concentration technology, the boiling point of waste acid is low, the energy consumption is low, and the quality of concentrated acid is excellent, so that the technology is advanced and comprehensive; the related process principle of dilute sulfuric acid vacuum concentration is as follows: after being heated, dilute sulfuric acid enters a dilute sulfuric acid concentration kettle according to the flow and flow rate controlled by the process, under the condition of high vacuum, acid liquor in a plurality of concentration chambers in the dilute sulfuric acid concentration kettle is boiled and evaporated at a lower temperature, glass lining is arranged in a shell of the dilute sulfuric acid concentration kettle, tantalum tubes are used for heating, the dilute sulfuric acid concentration kettle is divided into a plurality of concentration chambers, the dilute sulfuric acid flows along the concentration chambers of the concentration kettle, the concentration is gradually increased, the partition plates of the concentration chambers prevent the acid liquor from flowing back, the maximum average temperature difference between the acid liquor and heating steam is ensured, the heating area on the surface of the tantalum tubes is fully utilized, and therefore the sulfuric acid flowing out of the last stage of concentration chamber reaches the target concentration; compared with other concentration methods, the dilute sulfuric acid vacuum concentration wage has obvious advantages, firstly, the operation environment is good, the pollution of acid smoke is completely avoided, the discharge amount of three wastes is small, secondly, a plurality of anticorrosive materials with excellent performance are adopted, the frequent replacement of equipment after corrosion is avoided, the labor intensity is greatly reduced, a plurality of concentration chambers continuously operate, the number of operators is small, and the energy consumption is low;
and a steam outlet of the dilute sulfuric acid concentration kettle is connected with a steam inlet of the sulfuric acid separation tower.
In addition, a condensed water outlet of the dilute sulfuric acid concentration kettle is connected with a steam condensed water tank, so that condensed water brought by steam can be effectively recovered;
the dilute sulfuric acid concentration kettle is also provided with an air inlet for raw steam to enter, and the raw steam from the outside of a boundary area is conveyed into the dilute sulfuric acid concentration kettle through a branch cylinder;
a steam outlet of the sulfuric acid separation tower is connected with an air inlet of a tail gas cooler, and a condensate outlet of the tail gas cooler is connected with a feed inlet of a chlorine tail gas washing tower; wherein the type of the tail gas cooler is E1103;
the tail gas cooler is connected with the chlorine tail gas washing tower through the chlorine water storage tank; the gas outlet of the tail gas cooler is connected with the gas inlet of the chlorine tail gas washing tower through a three-stage steam jet vacuum system and a vacuum cooler; the model of the three-stage steam jet vacuum system is J1101-1103, and the three-stage steam jet vacuum system is a hydraulic jet pump (Venturi) made of Hastelloy; wherein the model of the chlorine water storage tank is V1102;
the process for recycling the waste sulfuric acid of the dried chlorine comprises the following steps:
(1) conveying the raw materials from outside the battery limits to a buffer tank for later use; in the step (1), the raw material from outside the battery limits comprises raw material liquid containing chlorine gas waste sulfuric acid; concentrated sulfuric acid generated by chlorine drying is changed into waste sulfuric acid (namely raw material liquid) with the concentration of 75% after absorbing water in chlorine, but the chlorine containing about 0.2% in the waste sulfuric acid cannot be recycled, and the waste sulfuric acid can be conveyed into a buffer tank only by filtering;
(2) conveying the raw material liquid in the buffer tank into an acid heat exchanger by using a raw material pump, and then conveying the raw material liquid into a sulfuric acid separation tower; at the moment, after the raw material liquid absorbs the steam (disulfide trioxide) of the dilute sulfuric acid concentration kettle, the temperature and the concentration of the raw material liquid are both increased, the temperature of the raw material liquid is increased to 115 ℃, and the mass concentration of the raw material liquid is increased to 83%;
(3) separating the raw material liquid by a sulfuric acid separation tower to prepare a separation liquid and generate steam, and then conveying the separation liquid into a dilute sulfuric acid concentration kettle;
(4) concentrating the separated liquid by a dilute sulfuric acid concentration kettle to obtain a concentrated liquid (the mass concentration of the concentrated liquid is 96%) and generate steam, then conveying the concentrated liquid into an acid heat exchanger and transferring the concentrated liquid into an acid cooler, and conveying the steam into a sulfuric acid separation tower;
(5) the acid cooler cools the concentrated solution and conveys the concentrated solution to a finished product intermediate tank;
(6) concentrated solution of the finished product intermediate tank is conveyed to a dechlorination drying section (chlorine drying device) for recycling, so that the recycling of heat is improved;
wherein, the raw material liquid in the step (2) and the concentrated solution in the step (4) are subjected to dividing wall type heat exchange in an acid-acid heat exchanger;
wherein steam generated by the sulfuric acid separation tower in the step (3) is washed by dilute sulfuric acid with the mass concentration of 80% and then is conveyed to a tail gas cooler for condensation, and condensate generated by condensation is conveyed to a chlorine tail gas washing tower through a chlorine water storage tank (and by means of a wastewater conveying pump (model number P1102 AB)); conveying the uncondensable gas to a three-stage steam jet vacuum system for suction and discharge, cooling the sucked and discharged gas by a vacuum cooler, and conveying the cooling liquid generated by cooling to a chlorine tail gas washing tower;
wherein the waste liquid generated by the chlorine tail gas washing tower is conveyed to a sewage treatment system outside the battery limits.
In summary, with reference to fig. 1 and table 1, in the apparatus for recycling waste sulfuric acid from drying chlorine in this embodiment, a raw material solution containing waste sulfuric acid from chlorine is used as a raw material, a buffer tank is disposed at the upstream, a finished product intermediate tank is disposed at the downstream, and the raw material solution is separated and concentrated by an acid-acid heat exchanger, a sulfuric acid separator, and a dilute sulfuric acid concentration kettle to a mass concentration of about 98%, and the concentrated solution is respectively returned to a chlorine drying apparatus for recycling, a small amount of waste gas generated during the separation and concentration process is returned to a chlorine tail gas washing tower to be absorbed by alkali to produce sodium hypochlorite for recycling, and the generated waste water is sent to a sewage treatment system for treatment and then used as production water. Compared with the traditional waste sulfuric acid circulating device and process, the device and the process completely avoid the pollution of acid smoke during high-concentration evaporation, have good operating environment and small discharge amount of three wastes, comprehensively utilize various anticorrosive materials with excellent performance, avoid frequent replacement after equipment corrosion, ensure the continuous and stable operation of the system, ensure the maximum average temperature difference between acid liquor and a service measuring medium, fully utilize energy, have low energy consumption and low labor intensity, and have few operators.
TABLE 1 economic efficiency analysis (8000 tons/year of equipment for example; direct economic efficiency 391.72 ten thousand yuan/year)
The present invention and its embodiments have been described above schematically, and the description is not limited thereto, and what is shown in the drawings is only one of the embodiments of the present invention, and the actual structure is not limited thereto. Therefore, if the person skilled in the art receives the teaching of the present invention, without departing from the inventive spirit of the present invention, the person skilled in the art should also design the similar structural modes and embodiments without creativity to the technical solution, and all shall fall within the protection scope of the present invention.
Claims (8)
1. The utility model provides a waste sulfuric acid cyclic utilization device of dry chlorine which characterized in that:
comprises a buffer tank, an acid-acid heat exchanger, an acid cooler, a dilute sulphuric acid concentration kettle and a sulphuric acid separation tower,
the buffer tank is used for storing the raw material liquid containing the chlorine gas waste sulfuric acid, the outlet of the buffer tank is connected with the raw material liquid feeding port of the acid-acid heat exchanger,
a concentrated acid discharge port of the acid-acid heat exchanger is connected with a feed port of the acid cooler,
the discharge port of the acid cooler is connected with a finished product intermediate tank;
a raw material liquid discharge port of the acid-acid heat exchanger is connected with a feed port of the sulfuric acid separation tower, a discharge port of the sulfuric acid separation tower is connected with a feed port of the dilute sulfuric acid concentration kettle, a concentrated acid discharge port of the dilute sulfuric acid concentration kettle is connected with a concentrated acid feed port of the acid-acid heat exchanger,
and a steam outlet of the dilute sulfuric acid concentration kettle is connected with a steam inlet of the sulfuric acid separation tower.
2. The apparatus of claim 1, wherein the apparatus comprises:
the acid-acid heat exchanger is characterized by also comprising a raw material pump, wherein the raw material pump is used for conveying the feed liquid in the cache tank into the acid-acid heat exchanger.
3. The apparatus of claim 1, wherein the apparatus comprises:
the feed liquid in the acid cooler is conveyed to the finished product intermediate tank by the discharge pump.
4. The apparatus of claim 1, wherein the apparatus comprises:
and a condensed water outlet of the dilute sulfuric acid concentration kettle is connected with a steam condensed water tank.
5. The apparatus of claim 1, wherein the apparatus comprises:
and the dilute sulfuric acid concentration kettle is also provided with an air inlet for raw steam to enter.
6. The apparatus of claim 1, wherein the apparatus comprises:
and a steam outlet of the sulfuric acid separation tower is connected with an air inlet of a tail gas cooler, and a condensate outlet of the tail gas cooler is connected with a feed inlet of a chlorine tail gas washing tower.
7. The apparatus of claim 6, wherein:
the tail gas cooler is connected with the chlorine tail gas washing tower through a chlorine water storage tank.
8. The apparatus of claim 7, wherein the apparatus comprises:
and the gas outlet of the tail gas cooler is connected with the gas inlet of the chlorine tail gas washing tower through a three-stage steam jet vacuum system and a vacuum cooler.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110422827A (en) * | 2019-08-05 | 2019-11-08 | 贵州兰鑫石墨机电设备制造有限公司 | A kind of the Waste Sulfuric Acid recycling device and technique of dry chlorine gas |
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2019
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110422827A (en) * | 2019-08-05 | 2019-11-08 | 贵州兰鑫石墨机电设备制造有限公司 | A kind of the Waste Sulfuric Acid recycling device and technique of dry chlorine gas |
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Denomination of utility model: A waste sulfuric acid recycling device for drying chlorine gas Effective date of registration: 20220627 Granted publication date: 20200522 Pledgee: Qiannan Financing Guarantee Co.,Ltd. Pledgor: GUIZHOU LANXIN GRAPHITE ELECTROMECHANICAL EQUIPMENT MANUFACTURING CO.,LTD. Registration number: Y2022980009030 |
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Date of cancellation: 20230706 Granted publication date: 20200522 Pledgee: Qiannan Financing Guarantee Co.,Ltd. Pledgor: GUIZHOU LANXIN GRAPHITE ELECTROMECHANICAL EQUIPMENT MANUFACTURING CO.,LTD. Registration number: Y2022980009030 |