CN212425437U - Dilute hydrochloric acid recovery processing system - Google Patents
Dilute hydrochloric acid recovery processing system Download PDFInfo
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- CN212425437U CN212425437U CN202020979730.1U CN202020979730U CN212425437U CN 212425437 U CN212425437 U CN 212425437U CN 202020979730 U CN202020979730 U CN 202020979730U CN 212425437 U CN212425437 U CN 212425437U
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Abstract
The utility model discloses a dilute hydrochloric acid recovery processing system, which comprises a dilute hydrochloric acid evaporation tower, wherein the dilute hydrochloric acid evaporation tower is connected with a dilute hydrochloric acid liquid inlet pipe, the bottom of the dilute hydrochloric acid evaporation tower is respectively connected with an evaporation tower reboiler and a vacuum concentration tower, the top of the evaporation tower reboiler is connected with the bottom of the dilute hydrochloric acid evaporation tower, and an air inlet of the evaporation tower reboiler is connected with a high-temperature steam conduit; the leakage fluid dram of vacuum concentration tower bottom is connected respectively on concentrating column reboiler and concentrated hydrochloric acid discharge pipe, and the circulation entry at vacuum concentration tower bottom is connected to the leakage fluid dram on concentrating column reboiler top, and the air inlet and the dilute hydrochloric acid evaporating tower of concentrating column reboiler are connected, and the gas vent at vacuum concentration tower top is connected with steam condenser, and steam condenser's gas vent is connected with the vacuum pump, is connected with chlorine-containing noncondensable gas discharge pipe on the vacuum pump. The utility model has the characteristics of can realize simultaneously that dilute hydrochloric acid concentrates and dechlorination, in addition, still have the energy consumption low, the dechlorination is effectual, and operation and investment cost are low, the characteristics of operation environmental protection.
Description
Technical Field
The utility model relates to a dilute hydrochloric acid recovery processing system, especially a dilute hydrochloric acid dechlorination concentration recovery processing system.
Background
Hydrochloric acid is used as a common chemical product and a pickling agent and is widely applied to chemical production and pickling production of steel structural members, waste hydrochloric acid with large amount and low concentration is discharged in the processes, the concentration of the hydrochloric acid is low, and the hydrochloric acid is discharged after being neutralized to be neutral by common industrial alkali, so that the treatment mode is high in cost and can cause resource waste and secondary pollution.
The waste hydrochloric acid is recycled, which is an important means for solving the problems of high treatment cost, resource waste and environmental pollution of the waste hydrochloric acid, wherein the HCL in the dilute hydrochloric acid is returned to a PVC factory to produce the VCM, but the application of the waste hydrochloric acid needs to carry out certain concentration on the dilute hydrochloric acid when the application is really implemented, and most importantly, free chlorine needs to be completely removed, otherwise, the free chlorine and acetylene in the VCM conversion process are used for synthesizing an explosive byproduct, namely chloroethyne, so that serious potential safety hazards are brought to the VCM process. However, the concentration process of dilute hydrochloric acid is common at present, and the removal of free chlorine still lacks related technologies.
Therefore, the realization of dechlorination and concentration of the waste dilute hydrochloric acid is the key for solving the real recycling of the waste hydrochloric acid.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a dilute hydrochloric acid recovery processing system. The utility model discloses the system has the characteristics that can realize dilute hydrochloric acid concentration and dechlorination simultaneously, and in addition, it is low still to have the energy consumption, and the dechlorination is effectual, and operation and investment cost are low, the characteristics of operation environmental protection.
The technical scheme of the utility model: a dilute hydrochloric acid recovery treatment system comprises a dilute hydrochloric acid evaporation tower, wherein a liquid inlet at the top of the dilute hydrochloric acid evaporation tower is connected with a dilute hydrochloric acid liquid inlet pipe of 7% hydrochloric acid and 0.2% free chlorine, a liquid outlet at the bottom of the dilute hydrochloric acid evaporation tower is respectively connected with the bottom of an evaporation tower reboiler and the top of a vacuum concentration tower through a three-way pipe, the liquid outlet at the top of the evaporation tower reboiler is connected with a circulation inlet at the bottom of the dilute hydrochloric acid evaporation tower, and a gas inlet at the service side of the evaporation tower reboiler is connected with a 0.8MPa high-temperature steam conduit; the drain outlet of vacuum concentration tower bottom is connected respectively on the bottom of concentration tower reboiler and 21% concentrated hydrochloric acid discharge pipe through the three-way pipe, the circulation entry at vacuum concentration tower bottom is connected to the drain outlet on concentration tower reboiler top, the gas vent at dilute hydrochloric acid evaporation tower top is connected to the service side gas inlet of concentration tower reboiler, the gas vent at vacuum concentration tower top is connected with steam condenser, steam condenser's gas vent is connected with the vacuum pump, be connected with chlorine-containing noncondensable gas discharge pipe on the vacuum pump.
The dilute hydrochloric acid evaporation tower is a graphite packing tower; the vacuum concentration tower is a graphite packing tower; the reboiler of the evaporation tower is a graphite heat exchanger; the reboiler of the concentration tower is a graphite heat exchanger.
Aforementioned dilute hydrochloric acid recovery processing system, dilute hydrochloric acid feed liquor union coupling is on the dilute hydrochloric acid storage tank, and the liquid outlet of dilute hydrochloric acid storage tank is connected with the pre-heater, and the liquid outlet of pre-heater is connected at dilute hydrochloric acid evaporation tower top inlet, and the preheating water entry of pre-heater is connected with first steam condensation water pitcher, and first steam condensation water pitcher is connected the exhaust port department of evaporation tower reboiler, the preheating water entry of pre-heater is connected with steam condensation water discharge pipe.
The preheater is a graphite heat exchanger.
Aforementioned dilute hydrochloric acid recovery processing system, the gas outlet of concentrating tower reboiler is connected with second steam condensate water pitcher, and the leakage fluid dram of second steam condensate water pitcher is connected with the waste water cooler, and the leakage fluid dram of waste water cooler is connected with the waste water holding vessel, is connected with 0.3% HCl waste water discharge pipe on the waste water holding vessel.
The waste water cooler is a graphite heat exchanger.
In the dilute hydrochloric acid recovery processing system, the waste water collection tank is connected with the liquid outlet of the steam condenser.
The steam condenser is a graphite condenser.
In the dilute hydrochloric acid recovery processing system, the waste water collection tank is respectively connected with the air inlet and the liquid outlet of the vacuum pump.
The beneficial effects of the utility model
1. The utility model utilizes H in dilute hydrochloric acid solution at the same temperature2O gameThe water and the free chlorine in the dilute hydrochloric acid are evaporated out by different vapor pressures of the free chlorine and the hydrogen chloride, so that the concentration of the dilute hydrochloric acid is improved, and the synchronous completion of concentration and dechlorination is realized;
2. the system of the utility model is carried out under a certain vacuum condition, thereby greatly reducing the solubility of free chlorine in the hydrochloric acid solution and the boiling point of hydrochloric acid, reducing the energy consumption to the maximum extent and having the advantage of low energy consumption;
3. the utility model discloses two-effect rectification concentration (containing dechlorination) system compares the advantage obvious with other concentrated systems (like kettle-type multiple-effect concentration), at first the mass transfer separation ability of rectification concentration tower is far greater than the balanced distillation separation ability of kettle-type, nearly 100% of free chlorine in the dilute hydrochloric acid is got rid of, secondly the waste water that adopts the concentrated top of the tower of rectification contains little HCL volume, furthest has utilized the hydrogen chloride resource in the dilute hydrochloric acid, the flow of two-effect rectification has been adopted in addition, heat recovery and utilization has been realized, steam consumption has effectively been reduced, have the low advantage with dechlorination effect;
4. the system of the utility model adopts the following current two-effect rectification concentration, adopts low-pressure saturated steam as a heating source, has the advantages of energy conservation and environmental protection, and reduces the operation and investment cost.
5. The utility model discloses the dilute hydrochloric acid (containing 0.02% free chlorine) about a large amount of concentrations ~ 7% of by-product among the recoverable CPE apparatus for producing, realized chlorine resource recycle, cleaner production not only is favorable to environmental protection, can realize the cyclic utilization of resource moreover.
6. The utility model can normally and stably run in the range of 30-110% when in actual use, and has larger operation elasticity; the purity of the product concentrated hydrochloric acid is more than or equal to 99.5 wt%, and free chlorine is not contained; the utility model discloses a system can normal use more than 8 years under the condition that equipment material guaranteed.
Drawings
FIG. 1 is a schematic structural view of the present invention;
description of reference numerals: 1-dilute hydrochloric acid liquid inlet pipe, 2-dilute hydrochloric acid storage tank, 3-high temperature steam conduit, 4-steam condensate water discharge pipe, 5-preheater, 6-dilute hydrochloric acid evaporation tower, 7-vacuum concentration tower, 8-steam condenser, 9-vacuum pump, 10-chlorine-containing noncondensable gas discharge pipe, 11-first steam condensate water tank, 12-evaporation tower reboiler, 13-second steam condensate water tank, 14-concentration tower reboiler, 15-wastewater cooler, 16-wastewater collection tank, 17-concentrated hydrochloric acid discharge pipe, and 18-wastewater discharge pipe.
Detailed Description
The present invention will be further described with reference to the following examples, which are not intended as a limitation of the present invention.
Embodiments of the utility model
A dilute hydrochloric acid recovery processing system is shown in figure 1 and comprises a dilute hydrochloric acid evaporation tower 6, wherein a liquid inlet at the top of the dilute hydrochloric acid evaporation tower 6 is connected with a dilute hydrochloric acid liquid inlet pipe 1, a liquid outlet at the bottom of the dilute hydrochloric acid evaporation tower 6 is respectively connected with the bottom of an evaporation tower reboiler 12 and the top of a vacuum concentration tower 7 which are controlled by a graphite column through a three-way pipe, the liquid outlet at the top of the evaporation tower reboiler 12 is connected with a circulating inlet at the bottom of the dilute hydrochloric acid evaporation tower 6, and a gas inlet of the evaporation tower reboiler 12 is connected with a high-temperature steam conduit 3; a liquid discharge port at the bottom of the vacuum concentration tower 7 is respectively connected to the bottom of a concentration tower reboiler 14 and a concentrated hydrochloric acid discharge pipe 17 which are made of graphite columns through a three-way pipe, a liquid discharge port at the top end of the concentration tower reboiler 14 is connected to a circulating inlet at the bottom of the vacuum concentration tower 7, an air inlet of the concentration tower reboiler 14 is connected to an air outlet at the top of a dilute hydrochloric acid evaporation tower 6, an air outlet at the top of the vacuum concentration tower 7 is connected with a steam condenser 8, an air outlet of the steam condenser 8 is connected with a vacuum pump 9, and the vacuum pump 9 is connected with a chlorine; the dilute hydrochloric acid liquid inlet pipe 1 is connected to a dilute hydrochloric acid storage tank 2, a liquid outlet of the dilute hydrochloric acid storage tank 2 is connected with a preheater 5 which is made of graphite columns, a liquid outlet of the preheater 5 is connected with a liquid inlet at the top of a dilute hydrochloric acid evaporation tower 6, a preheated water inlet of the preheater 5 is connected with a first steam condensate water tank 11, the first steam condensate water tank 11 is connected with an exhaust port of an evaporation tower reboiler 12, and a preheated water inlet of the preheater 5 is connected with a steam condensate water discharge pipe 4; a gas outlet of the concentration tower reboiler 14 is connected with a second steam condensate water tank 13, a liquid outlet of the second steam condensate water tank 13 is connected with a graphite column-controlled wastewater cooler 15, a liquid outlet of the wastewater cooler 15 is connected with a wastewater collection tank 16, and a wastewater discharge pipe 18 is connected to the wastewater collection tank 16; the waste water collecting tank 16 is connected with a liquid outlet of a steam condenser 8 controlled by a graphite column; the waste water collecting tank 16 is respectively connected with an air inlet and a liquid outlet of the vacuum pump 9.
Working principle of the embodiment
Hydrochloric acid solution flow path: a dilute hydrochloric acid solution with concentration of 7% and containing 0.2% of free chlorine enters a dilute hydrochloric acid storage tank 2 from a dilute hydrochloric acid liquid inlet pipe 1, is pumped into a preheater 5 under the action of a pump feeder to perform heat exchange with a preheating medium, the preheated dilute hydrochloric acid enters the top of a dilute hydrochloric acid evaporation tower 6 and is sprayed from top to bottom to perform heat and mass transfer with steam from a tower kettle, part of water and most of free chlorine in the dilute hydrochloric acid are stripped out of the tower, the first evaporation and gas stripping are completed, and the dilute hydrochloric acid is preliminarily concentrated to about 11% and falls into the tower kettle; one part of the solution enters an evaporation tower reboiler 12 to continue thermosiphon circulating evaporation and circularly enters the bottom of a dilute hydrochloric acid evaporation tower 6, gas and liquid are separated in a tower kettle, and the steam is upwards transferred with the dilute hydrochloric acid solution sprayed from top to bottom;
controlling the liquid level of the tower kettle of the dilute salt evaporation tower 6 according to the concentration of about 11 percent of dilute hydrochloric acid, extracting a part of dilute hydrochloric acid through a pipeline tee joint, directly entering the top of the vacuum concentration tower 7 under the action of a pump feeder, spraying from top to bottom, carrying out heat and mass transfer with steam from the tower kettle of the vacuum concentration tower 7, carrying out reduced pressure steam stripping under a certain vacuum condition, stripping part of steam and residual free chlorine in the dilute hydrochloric acid out of the tower to complete second concentration evaporation and gas stripping, and further concentrating the hydrochloric acid solution until about 21 percent of the dilute hydrochloric acid falls into the tower kettle; part of the solution enters a reboiler 14 of the concentration tower to be continuously heated, thermally siphoned and circularly evaporated, and circularly enters the bottom of the vacuum concentration tower 7, part of the solution is directly discharged through a concentrated hydrochloric acid discharge pipe 17 under the action of a pump feeder to be applied, gas and liquid in a tower kettle are separated, and the steam is upwards transferred with the dilute hydrochloric acid solution which is sprayed from top to bottom for mass transfer; the tower still obtains a pure hydrochloric acid solution with the concentration of 21%. Controlling the diluted hydrochloric acid concentrated to about 21% according to the liquid level of a tower bottom of a vacuum concentration tower 7, and extracting a part of diluted hydrochloric acid to produce a finished product through a pipeline tee joint; the hydrochloric acid which is taken out of a tower kettle of a vacuum concentration tower 7 and 21% is subjected to vacuum stripping dechlorination, and the theoretical value of free chlorine in the acid is reduced to PPB magnitude; the hydrochloric acid can be further conveyed to a dilute hydrochloric acid desorption process for use through a 21% hydrochloric acid conveying pump, and the produced hydrogen chloride is recycled.
Raw steam flow path: high-temperature steam with 0.8MPa is used as a heating source and directly enters the evaporation tower reboiler 12 from the high-temperature steam guide pipe 3, and the dilute hydrochloric acid solution flowing through the evaporation tower reboiler 12 is heated and evaporated; after heat exchange, the resulting water vapor mixture enters the first steam condensate tank 11.
Under the action of an evaporation tower reboiler 12, carrying out thermosiphon cyclic evaporation on the dilute hydrochloric acid solution, circularly entering the bottom of the dilute hydrochloric acid evaporation tower 6, carrying out gas-liquid separation in a tower kettle, and enabling steam to flow upwards from the bottom of the dilute hydrochloric acid evaporation tower 6 and transfer heat and mass with the dilute hydrochloric acid solution sprayed from top to bottom; part of the water and most of the free chlorine in the dilute hydrochloric acid is stripped and discharged from the top, and the secondary water vapor discharged from the tower is sent to a concentration tower reboiler 14 to be used as heating steam.
Gas generated by evaporation in the vacuum concentration tower 7 is pumped into a steam condenser 8 under the action of a vacuum pump 9, water vapor is gradually condensed to form solution by the steam condenser 8 under the cooling action of circulating cold water, and the rest non-condensable gas is pumped into the vacuum pump 9 and is discharged from a chlorine-containing non-condensable gas discharge pipe 10 to the next process for treatment, so that dechlorination is completed; the free chlorine in the dilute hydrochloric acid is stripped in two towers, particularly under vacuum condition, almost 100 percent of the free chlorine is separated from the dilute hydrochloric acid, most of the free chlorine is sent out of a battery limit area by a vacuum pump in a gaseous state, and the free chlorine is removed from a tail chlorine absorption tower for centralized treatment.
Wastewater flow path: after high-temperature steam of 0.8MPa enters an evaporation tower reboiler 12 from a high-temperature steam guide pipe 3 for heat exchange, a generated water-steam mixture enters a first steam condensate water tank 11, a high-temperature steam part can flow back to the high-temperature steam guide pipe 3 through a pipeline, water still having higher temperature flows into a preheater 5, cold dilute hydrochloric acid serving as a preheating medium is preheated, the temperature is further reduced after preheating and the water is directly discharged from a steam condensate water discharge pipe 4, and the waste water of the part is pure condensate water and can be directly discharged or recycled;
secondary water vapor discharged from the dilute hydrochloric acid evaporation tower 6; after entering the concentration tower reboiler 14, heat exchange occurs, partial condensation forms a water-vapor mixture, the mixture enters the second steam condensate water tank 13, partial high-temperature steam still can enter the concentration tower reboiler 14 through a pipeline for heat exchange, condensed water enters the wastewater cooler 15, the temperature of the condensed circulating water is reduced to be lower than 50 ℃ by low temperature cooling, and the condensed circulating water enters the wastewater collection tank 16 for storage.
The steam generated by evaporation from the vacuum concentration tower 7 is condensed into water under the action of a steam condenser 8, and the part of the water is also fed into a waste water collecting tank 16, and the waste water in the waste water collecting tank 16 is waste water containing 0.3% hydrochloric acid and needs to be fed into the next working procedure for treatment; meanwhile, the volatile gas in the wastewater collection tank 16 is pumped to the vacuum pump 9 and then is discharged through the chlorine-containing non-condensable gas discharge pipe 10, and a small amount of condensed water generated in the vacuum pump 9 is collected in the wastewater collection tank 16 and finally conveyed to a water treatment station through a wastewater pump for centralized treatment.
The three wastes discharge index of this example
The vacuum pump exhausts the gas depending on the content of free chlorine in the raw acid and the amount of non-condensable gas in the system.
Acid condensate (wastewater) of evaporation tail gas: the water vapor mainly evaporated from the dilute hydrochloric acid evaporation tower is condensed in a reboiler of the concentration tower, and the water vapor evaporated from the vacuum concentration tower is condensed in a vapor condenser.
Pipe and connector of the present embodiment
According to different media, temperature and pressure conditions, the hydrochloric acid-containing media adopt pipelines made of FRP (fiber reinforced plastic), PVC/FRP (polyvinyl chloride/fiber reinforced plastic), fluorine lining and the like, and valves adopt stainless steel, PTFE lining and the like; the water and steam pipelines adopt equal No. 20 fluid conveying pipelines, and pipe valves are selected according to relevant specifications and conventions.
The system plumbing connections must be sufficiently flexible. The PTFE elastic connecting piece, the special elastic gasket, the special fastener and the special supporting structure are arranged at necessary positions. These special materials and special connecting elements are necessary for the stable and reliable operation of the entire device.
When the system is implemented, the system is also provided with overrun alarm and linkage cut-off of main parameters.
The control system of the dilute hydrochloric acid dechlorination and concentration device is used as a sub-function control station of the DCS system and is brought into a DCS center for control according to a unit system, and operators can directly complete monitoring on system parameters and equipment of the dilute hydrochloric acid dechlorination and concentration device through a DCS operator station of a unit in a central control room.
The above, only do the utility model discloses create the embodiment of preferred, nevertheless the utility model discloses the protection scope of creation is not limited to this, and any technical personnel who is familiar with this technical field are in the utility model discloses create the technical scope of disclosure, according to the utility model discloses technical scheme and the utility model design that creates of the utility model are equivalent replacement or change, all should be covered within the protection scope of creation of the utility model.
Claims (5)
1. A dilute hydrochloric acid recovery processing system is characterized in that: the device comprises a dilute hydrochloric acid evaporation tower (6), wherein a liquid inlet at the top of the dilute hydrochloric acid evaporation tower (6) is connected with a dilute hydrochloric acid liquid inlet pipe (1), a liquid outlet at the bottom of the dilute hydrochloric acid evaporation tower (6) is respectively connected with the bottom of an evaporation tower reboiler (12) and the top of a vacuum concentration tower (7) through a three-way pipe, a liquid outlet at the top of the evaporation tower reboiler (12) is connected with a circulating inlet at the bottom of the dilute hydrochloric acid evaporation tower (6), and a gas inlet of the evaporation tower reboiler (12) is connected with a high-temperature steam guide pipe (3); the leakage fluid dram of vacuum concentration tower (7) bottom is connected respectively on the bottom and concentrated hydrochloric acid discharge pipe (17) of concentration tower reboiler (14) through the three-way pipe, the circulation entry in vacuum concentration tower (7) bottom is connected to the leakage fluid dram on concentration tower reboiler (14) top, the air inlet of concentration tower reboiler (14) is connected on the gas vent at dilute hydrochloric acid evaporating tower (6) top, the gas vent at vacuum concentration tower (7) top is connected with steam condenser (8), the gas vent of steam condenser (8) is connected with vacuum pump (9), be connected with chlorine-containing noncondensable gas discharge pipe (10) on vacuum pump (9).
2. The dilute hydrochloric acid recovery treatment system according to claim 1, characterized in that: dilute hydrochloric acid feed liquor pipe (1) is connected on dilute hydrochloric acid storage tank (2), and the liquid outlet of dilute hydrochloric acid storage tank (2) is connected with pre-heater (5), and the liquid outlet of pre-heater (5) is connected at dilute hydrochloric acid evaporation tower (6) top inlet, and the preheating water entry of pre-heater (5) is connected with first steam condensate water pitcher (11), and first steam condensate water pitcher (11) are connected the exhaust port department of evaporation tower reboiler (12), and the preheating water entry of pre-heater (5) is connected with steam condensate water discharge pipe (4).
3. The dilute hydrochloric acid recovery treatment system according to claim 1, characterized in that: the gas outlet of the concentration tower reboiler (14) is connected with a second steam condensate water tank (13), the liquid outlet of the second steam condensate water tank (13) is connected with a wastewater cooler (15), the liquid outlet of the wastewater cooler (15) is connected with a wastewater collection tank (16), and a wastewater discharge pipe (18) is connected to the wastewater collection tank (16).
4. The dilute hydrochloric acid recovery treatment system according to claim 3, characterized in that: the waste water collecting tank (16) is connected with a liquid outlet of the steam condenser (8).
5. The dilute hydrochloric acid recovery treatment system according to claim 3, characterized in that: and the waste water collecting tank (16) is respectively connected with an air inlet and a liquid outlet of the vacuum pump (9).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020979730.1U CN212425437U (en) | 2020-06-02 | 2020-06-02 | Dilute hydrochloric acid recovery processing system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202020979730.1U CN212425437U (en) | 2020-06-02 | 2020-06-02 | Dilute hydrochloric acid recovery processing system |
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| CN212425437U true CN212425437U (en) | 2021-01-29 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN113041772A (en) * | 2021-03-30 | 2021-06-29 | 夏县运力化工有限公司 | Novel dilute hydrochloric acid rectifying tower |
-
2020
- 2020-06-02 CN CN202020979730.1U patent/CN212425437U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN111606304B (en) * | 2020-06-02 | 2024-08-16 | 贵州兰鑫石墨机电设备制造有限公司 | Dilute hydrochloric acid dechlorination concentration system |
| CN113041772A (en) * | 2021-03-30 | 2021-06-29 | 夏县运力化工有限公司 | Novel dilute hydrochloric acid rectifying tower |
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: A dilute hydrochloric acid recovery and treatment system Effective date of registration: 20220627 Granted publication date: 20210129 Pledgee: Qiannan Financing Guarantee Co.,Ltd. Pledgor: GUIZHOU LANXIN GRAPHITE ELECTROMECHANICAL EQUIPMENT MANUFACTURING CO.,LTD. Registration number: Y2022980009030 |
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| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20230706 Granted publication date: 20210129 Pledgee: Qiannan Financing Guarantee Co.,Ltd. Pledgor: GUIZHOU LANXIN GRAPHITE ELECTROMECHANICAL EQUIPMENT MANUFACTURING CO.,LTD. Registration number: Y2022980009030 |
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| PC01 | Cancellation of the registration of the contract for pledge of patent right |