CN211799426U - Production device for producing calcium formate by using yellow phosphorus tail gas through mixed serial-parallel method - Google Patents
Production device for producing calcium formate by using yellow phosphorus tail gas through mixed serial-parallel method Download PDFInfo
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- CN211799426U CN211799426U CN202020222674.7U CN202020222674U CN211799426U CN 211799426 U CN211799426 U CN 211799426U CN 202020222674 U CN202020222674 U CN 202020222674U CN 211799426 U CN211799426 U CN 211799426U
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Abstract
The utility model relates to a calcium formate apparatus for producing technical field, concretely relates to mix apparatus for producing that series-parallel method utilized yellow phosphorus tail gas to produce calcium formate. The production device for producing the calcium formate by using the yellow phosphorus tail gas by the mixed serial-parallel method comprises a coke filter, a dephosphorization tower, a desulfurization tower, a demister, a compressor, a first-stage pressure swing adsorption tower, a second-stage pressure swing adsorption tower and a reaction kettle which are sequentially connected; the air inlet of the coke filter is connected with a yellow phosphorus tail gas pipeline; the discharge hole of the reaction kettle is connected with a calcium formate product discharge pipeline. The production device of the utility model obtains high-purity carbon monoxide gas by dedusting, dephosphorizing, desulfurizing, removing carbon dioxide and purifying carbon monoxide from the yellow phosphorus tail gas, meets the requirement of calcium formate synthesis on the raw material gas, reduces the production cost and is environment-friendly; a plurality of reaction kettles are connected in series and in parallel to produce calcium formate, so that the highest-efficiency operation of the reaction kettles is realized, the comprehensive utilization of energy is improved, and the steam consumption is reduced.
Description
Technical Field
The utility model relates to a calcium formate apparatus for producing technical field, concretely relates to mix apparatus for producing that series-parallel method utilized yellow phosphorus tail gas to produce calcium formate.
Background
The production of yellow phosphorus usually adopts an electric furnace method, phosphorus-containing furnace gas enters a condensation tower, phosphorus steam in the condensation furnace gas is changed into liquid yellow phosphorus and enters a phosphorus collecting tank, finished yellow phosphorus is obtained through refining, and the uncondensed furnace gas is yellow phosphorus tail gas. The amount of the tail gas discharged by 1 ton of yellow phosphorus produced is 2700-3000 Nm3, the main component of the yellow phosphorus is 85-90 percent of CO, and the yellow phosphorus also contains H2S、COS、CH4SH、AsH3、PH3And harmful components such as HF and cyanide. The method effectively purifies the yellow phosphorus tail gas to prepare high-purity CO, provides clean raw material gas for the subsequent production process of high-added-value chemical products, and has extremely important significance for really realizing high coordination and unification of resources, energy sources and environmental protection and promoting the sustainable development of chemical industry.
Patent CN2019204292191 discloses a device for purifying yellow phosphorus tail gas, which comprises a washing tower, a desulfurizing tower, a fixed bed and an adsorption component, wherein the washing tower, the desulfurizing tower, the fixed bed and the adsorption component are sequentially connected, a yellow phosphorus tail gas inlet is formed in the washing tower, a dephosphorizing adsorbent is filled in the fixed bed, the adsorption component comprises a temperature swing adsorption bed, and a primary purified gas outlet is formed in the temperature swing adsorption bed. The device consists of a washing tower, a desulfurizing tower, a fixed bed and an adsorption component which are connected in sequence, wherein the yellow phosphorus tail gas is subjected to water washing, desulfurization, dephosphorization and temperature-variable adsorption to obtain a primary purified gas which can be used for steam production of a boiler, power generation and industrial devices with low requirements on CO impurities, and the defects of high operation cost, unstable operation, large wastewater discharge amount and the like of the prior art are overcome.
Patent CN2019106632667 discloses an utilize yellow phosphorus tail gas to prepare device and method of multiple synthetic gas, the device is including collection tank, scrubbing tower, thick desulfurizing tower, thick dephosphorization tower, compressor, converter, a purification tower group, secondary desulfurizing tower, decarbonization tower, fine desulfurization tower, secondary purification tower that communicate in proper order, and yellow phosphorus tail gas is followed the air inlet of collection tank gets into, and the synthetic gas is followed the purification gas outlet of secondary purification tower flows. The method realizes removal or partial removal of phosphorus, sulfur, arsenic, chlorine, fluorine and oxygen in the yellow phosphorus tail gas, meets the requirements of various synthesis gases, and is favorable for realizing industrialization of the utilization of the yellow phosphorus tail gas.
The above devices remove impurities in the yellow phosphorus tail gas, but the obtained purified gas still contains partial impurities, and the device is only suitable for industrial devices with low requirements on CO impurities. When calcium formate is synthesized by a one-step method, the requirement on the purity of CO is high, and the yellow phosphorus tail gas needs to be purified more thoroughly.
SUMMERY OF THE UTILITY MODEL
In order to solve the defects of the prior art, the utility model provides a mixed series-parallel method utilizes the production device of yellow phosphorus tail gas production calcium formate, removes dust, dephosphorizes, desulfurizes, removes carbon dioxide, purifies carbon monoxide with the yellow phosphorus tail gas, obtains high-purity carbon monoxide gas, satisfies the requirement of calcium formate synthesis to the feed gas, not only reduces the production cost but also reduces the environmental pollutants, and is environment-friendly; a plurality of reaction kettles are connected in series and in parallel to produce calcium formate, so that the highest-efficiency operation of the reaction kettles is realized, the comprehensive utilization of energy is improved, and the steam consumption is reduced.
The utility model discloses a mixed series-parallel method utilizes yellow phosphorus tail gas to produce the apparatus for producing calcium formate, including coke filter, dephosphorization tower, desulfurizing tower, demister, compressor, one-level pressure swing adsorption tower, second grade pressure swing adsorption tower and reation kettle that link to each other in proper order; the air inlet of the coke filter is connected with a yellow phosphorus tail gas pipeline; the discharge hole of the reaction kettle is connected with a calcium formate product discharge pipeline.
The coke filter is used for removing dust, free water and other impurities in the yellow phosphorus tail gas.
The dephosphorization tower is used for removing white phosphorus particles and PH3 in the yellow phosphorus tail gas, and the filler is activated carbon with high specific surface area.
The desulfurizing tower is used for removing sulfur-containing impurities in the yellow phosphorus tail gas.
The first-stage pressure swing adsorption tower is used for removing carbon dioxide in the yellow phosphorus tail gas, and the adsorbent is special silica gel for pressure swing adsorption.
The two-stage pressure swing adsorption tower is used for purifying carbon monoxide, and the adsorbent is a special adsorbent for CO.
The regeneration air inlet of dephosphorization tower passes through the heater and links to each other with PSA two-stage section unloading gas inlet line, and the regeneration gas outlet of dephosphorization tower links to each other with regeneration adsorption tower, and regeneration adsorption tower still links to each other with unloading pipeline.
The main component of the regeneration gas in the PSA two-stage emptying gas inlet pipeline is CO2And after being heated by the heater steam, the waste gas is used for regenerating the dephosphorization tower, and is discharged into a vent pipeline after being adsorbed by the regeneration adsorption tower for combustion or venting.
The liquid outlet of the desulfurizing tower is circularly communicated with the liquid inlets of the regeneration tank, the barren solution tank and the desulfurizing tower; the regeneration tank is also connected with the sulfur foam tank and the sulfur melting kettle in sequence; the discharge port of the sulfur melting kettle is connected with a sulfur pipeline.
Absorbing sulfur-containing impurities by absorption liquid of the desulfurizing tower, discharging into a regeneration tank for regeneration, allowing regenerated sulfur-containing barren solution to enter the desulfurizing tower through a barren solution tank for recycling, and enriching sulfur-containing pregnant solution again through a sulfur foam tank and a sulfur melting kettle to obtain a sulfur product, and collecting the sulfur product through a sulfur pipeline.
The number of the first-stage pressure swing adsorption towers is 3-5, the tops of the multiple first-stage pressure swing adsorption towers are respectively connected in parallel on the first-stage forward discharge pipeline and the first-stage exhaust pipeline, and the bottoms of the multiple first-stage pressure swing adsorption towers are respectively connected in parallel on the first-stage reverse discharge pipeline and the first-stage intake pipeline.
The number of the second-stage pressure swing adsorption towers is 4-6, the tops of the multiple second-stage pressure swing adsorption towers are respectively connected in parallel on a second-stage forward discharge pipeline and a second-stage exhaust pipeline, and the bottoms of the multiple second-stage pressure swing adsorption towers are respectively connected in parallel on a second-stage reverse discharge pipeline and a second-stage air inlet pipeline.
The first-stage forward-discharge pipeline, the first-stage exhaust pipeline, the first-stage reverse-discharge pipeline, the first-stage air inlet pipeline, the second-stage forward-discharge pipeline, the second-stage exhaust pipeline, the second-stage reverse-discharge pipeline and the second-stage air inlet pipeline are all provided with program control valves.
The first-stage air inlet pipeline is connected with the compressor; the primary forward discharge pipeline is connected with the secondary forward discharge pipeline through a No. 1 empty tower, and the secondary forward discharge pipeline is connected with a PSA secondary-stage discharged air exhaust pipeline through a No. 2 empty tower; the primary exhaust pipeline is connected with the secondary air inlet pipeline; the secondary reverse discharge pipeline is connected with a CO feeding pipeline.
The compressor leads the primarily purified yellow phosphorus tail gas into a primary pressure swing adsorption system through a primary air inlet pipeline, and carbon dioxide in the yellow phosphorus tail gas is removed after the yellow phosphorus tail gas is adsorbed by a plurality of primary pressure swing adsorption towers; then introducing the carbon monoxide into a first-stage pressure swing adsorption system, and purifying the carbon monoxide after adsorption by a plurality of second-stage pressure swing adsorption towers. The removed carbon dioxide is discharged through a PSA secondary-section vent gas exhaust pipeline and enters a PSA secondary-section vent gas inlet pipeline for regeneration of the dephosphorization tower; the purified carbon monoxide is discharged through a secondary reverse discharge pipeline and enters a CO feeding pipeline for synthesizing calcium formate.
The number of the reaction kettles is 3-6, the feed inlets of the reaction kettles are respectively connected in parallel on a CO feed pipeline and a raw material feed pipeline, and the discharge outlets of the reaction kettles are connected in parallel on a calcium formate product discharge pipeline; the heating channels of the reaction kettles are connected in parallel through a steam inlet pipeline and a steam condensate parallel pipeline, and are connected in series through a steam condensate series pipeline.
The synthesis of calcium formate adopts the series-parallel mixed combination of a plurality of reaction kettles, can realize the highest-efficiency operation of the reaction kettles, simultaneously improves the comprehensive utilization of energy sources and reduces the steam consumption.
The series-parallel combination of the reaction kettles comprises two parts: the CO feeding pipelines among the reaction kettles are communicated, so that CO gas higher than normal pressure can be discharged into the reaction kettle in a pressure boosting state through the communication pipeline after one reaction is finished so as to improve the utilization rate of CO, the reaction of each reaction kettle is independently carried out, and the normal operation of other reaction kettles cannot be influenced when each reaction kettle breaks down. The series-parallel connection is also embodied in the connection mode of heating steam, and the heat released in the cooling process after the reaction of each reaction kettle is finished can be transferred to another reaction kettle inner coil pipe in the temperature rising process to be used as a heat source. Therefore, the steam consumption can be reduced, and the heating rate of the reaction kettle is increased.
Compared with the prior art, the utility model discloses there is following beneficial effect:
(1) the utility model obtains the carbon monoxide gas with the concentration more than or equal to 98 percent by dedusting, dephosphorizing, desulfurizing, removing carbon dioxide and purifying the carbon monoxide tail gas, meets the requirement of calcium formate synthesis on the raw material gas, reduces the production cost and the environmental pollutants, and is environment-friendly;
(2) the utility model adopts the first-stage pressure swing adsorption system to remove carbon dioxide and the second-stage pressure swing adsorption system to purify carbon monoxide, thus improving the purity of carbon monoxide, and the removed carbon dioxide is used for the regeneration of the dephosphorization tower, and compared with the traditional device, the utility model reduces the power consumption and the energy consumption;
(3) the utility model recycles the sulfur-containing impurities removed from the yellow phosphorus tail gas, thereby having high economic benefit;
(4) the utility model discloses a many reation kettle series-parallel connection production calcium formate realize the operation of reation kettle maximum efficiency, improve energy comprehensive utilization simultaneously, reduce steam consumption.
Drawings
FIG. 1 is a schematic view of a production apparatus for producing calcium formate by using yellow phosphorus tail gas in a mixed series-parallel method according to the present invention;
in the figure: 1. a yellow phosphorus tail gas pipeline; 2. a PSA two-stage emptying gas inlet pipeline; 3. a coke filter; 4. a dephosphorization tower; 5. a heater; 6. regenerating the adsorption tower; 7. emptying the pipeline; 8. a desulfurizing tower; 9. a demister; 10. a regeneration tank; 11. a lean liquor tank; 12. A sulfur foam cell; 13. a sulfur melting kettle; 14. a sulfur pipeline; 15. a compressor; 16. a first-stage pressure swing adsorption tower; 17. a primary air inlet pipeline; 18. a first-stage forward discharge pipeline; 19. a first-stage reverse discharge pipeline; 20. 1# empty tower; 21. a primary exhaust line; 22. a second-stage pressure swing adsorption tower; 23. a secondary reverse discharge pipeline; 24. a secondary air inlet pipeline; 25. a secondary exhaust line; 26. a second-stage forward pipeline; 27. a PSA two-stage vent gas exhaust pipeline; 28. 2# empty tower; 29. a raw material feed line; 30. a steam inlet line; 31. a CO feed line; 32. a reaction kettle; 33. the steam condensate is connected with a pipeline in parallel; 34. the steam condensate is connected with a pipeline in series; 35. Calcium formate product discharge line.
Detailed Description
The following embodiments are combined to further explain the present invention, but the protection scope of the present invention is not limited thereto, and the professional in this field should be right the technical solution of the present invention should all belong to the protection scope of the present invention.
Example 1
As shown in fig. 1, the apparatus for producing calcium formate by using yellow phosphorus tail gas in a hybrid serial-parallel method according to the present invention comprises a coke filter 3, a dephosphorization tower 4, a desulfurization tower 8, a demister 9, a compressor 15, a first-stage pressure swing adsorption tower 16, a second-stage pressure swing adsorption tower 22, and a reaction kettle 32, which are connected in sequence; the air inlet of the coke filter 3 is connected with the yellow phosphorus tail gas pipeline 1; the discharge port of the reaction kettle 32 is connected with a calcium formate product discharge pipeline 35.
The coke filter 3 is used for removing dust, free water and other impurities in the yellow phosphorus tail gas.
The dephosphorization tower 4 is used for removing white phosphorus particles and PH3 in the yellow phosphorus tail gas, and the filler is activated carbon with high specific surface area.
The desulfurizing tower 8 is used for removing sulfur-containing impurities in the yellow phosphorus tail gas.
The first-stage pressure swing adsorption tower 16 is used for removing carbon dioxide in the yellow phosphorus tail gas, and the adsorbent is silica gel special for pressure swing adsorption.
The second-stage pressure swing adsorption tower 22 is used for purifying carbon monoxide, and the adsorbent is a special adsorbent for CO.
The regeneration air inlet of dephosphorization tower 4 passes through heater 5 and links to each other with PSA two-stage process unloading air inlet pipe way 2, and the 4 regeneration gas outlets of dephosphorization tower link to each other with regeneration adsorption tower 6, and regeneration adsorption tower 6 still links to each other with unloading pipeline 7.
Regenerated gas in PSA two-stage emptying gas inlet pipeline 2The main component is CO2And after being heated by steam of a heater 5, the waste gas is used for regenerating a dephosphorization tower 4, and is discharged into a vent pipeline 7 after being adsorbed by a regeneration adsorption tower 6 for combustion or venting.
A liquid outlet of the desulfurizing tower 8 is circularly communicated with a liquid inlet of the regeneration tank 10, the barren solution tank 11 and the desulfurizing tower 8; the regeneration tank 10 is also connected with a sulfur foam tank 12 and a sulfur melting kettle 13 in sequence; the discharge port of the sulfur melting kettle 13 is connected with a sulfur pipeline 14.
After absorbing sulfur-containing impurities by the absorption liquid of the desulfurizing tower 8, discharging into a regeneration tank 10 for regeneration, allowing the regenerated sulfur-containing barren solution to enter the desulfurizing tower 8 through a barren solution tank 11 for recycling, and allowing the sulfur-containing rich solution to be enriched again through a sulfur foam tank 12 and a sulfur melting kettle 13 to obtain a sulfur product, and collecting the sulfur product through a sulfur pipeline 14.
The number of the first-stage pressure swing adsorption towers 16 is 3, the tops of a plurality of the first-stage pressure swing adsorption towers 16 are respectively connected in parallel on a first-stage forward release pipeline 18 and a first-stage exhaust pipeline 21, and the bottoms of a plurality of the first-stage pressure swing adsorption towers 16 are respectively connected in parallel on a first-stage reverse release pipeline 19 and a first-stage air inlet pipeline 17.
The number of the second-stage pressure swing adsorption towers 22 is 5, the tops of the plurality of second-stage pressure swing adsorption towers 22 are respectively connected in parallel to a second-stage forward discharge pipeline 26 and a second-stage exhaust pipeline 25, and the bottoms of the plurality of second-stage pressure swing adsorption towers 22 are respectively connected in parallel to a second-stage reverse discharge pipeline 23 and a second-stage air inlet pipeline 24.
Program control valves are arranged on the primary forward pipeline 18, the primary exhaust pipeline 21, the primary reverse pipeline 19, the primary air inlet pipeline 17, the secondary forward pipeline 26, the secondary exhaust pipeline 25, the secondary reverse pipeline 23 and the secondary air inlet pipeline 24.
The primary air inlet pipeline 17 is connected with the compressor 15; the primary forward discharge pipeline 18 is connected with a secondary forward discharge pipeline 26 through a No. 1 empty tower 20, and the secondary forward discharge pipeline 26 is connected with a PSA secondary section discharge air exhaust pipeline 27 through a No. 2 empty tower 28; the primary exhaust pipeline 21 is connected with the secondary air inlet pipeline 24; the secondary reverse-flow line 23 is connected to the CO feed line 31.
The compressor 15 leads the primarily purified yellow phosphorus tail gas into a primary pressure swing adsorption system through a primary air inlet pipeline 17, and carbon dioxide in the yellow phosphorus tail gas is removed after the yellow phosphorus tail gas is adsorbed by a plurality of primary pressure swing adsorption towers 16; then the carbon monoxide is introduced into a first-stage pressure swing adsorption system and is adsorbed by a plurality of second-stage pressure swing adsorption towers 22, and then the carbon monoxide is purified. Wherein, the removed carbon dioxide is discharged through a PSA secondary-section vent gas exhaust pipeline 27 and enters a PSA secondary-section vent gas inlet pipeline 2 for the regeneration of a dephosphorization tower 4; the purified carbon monoxide is discharged through a secondary reverse discharge pipeline 23 and enters a CO feeding pipeline 31 for calcium formate synthesis.
The number of the reaction kettles 32 is 5, the feed inlets of the reaction kettles 32 are respectively connected in parallel to the CO feed pipeline 31 and the raw material feed pipeline 29, and the discharge outlets of the reaction kettles 32 are connected in parallel to the calcium formate product discharge pipeline 35; the heating channels of a plurality of reaction kettles 32 are connected in parallel through a steam inlet pipeline 30 and a steam condensate parallel pipeline 33, and are connected in series through a steam condensate series pipeline 34.
The synthesis of calcium formate adopts the series-parallel mixed combination of a plurality of reaction kettles 32, can realize the highest-efficiency operation of the reaction kettles 32, simultaneously improve the comprehensive utilization of energy and reduce the steam consumption.
The reactor 32 series-parallel combination comprises two parts: the CO feeding pipelines 31 among the reaction kettles 32 are communicated, so that CO gas higher than normal pressure can be discharged into the reaction kettle 32 in a pressure boosting state through a communication pipeline after one reaction is finished so as to improve the utilization rate of CO, the reaction of each reaction kettle 32 is independently carried out, and the normal operation of other reaction kettles 32 cannot be influenced when each reaction kettle 32 breaks down. The series-parallel connection is also embodied in the connection mode of heating steam, and the heat released in the cooling process after the reaction of each reaction kettle 32 is finished is transferred to the coil pipe in the other reaction kettle 32 in the temperature rising process to be used as a heat source. Therefore, the steam consumption can be reduced, and the heating rate of the reaction kettle is increased.
Claims (7)
1. The utility model provides a production device that mixed series-parallel method utilized yellow phosphorus tail gas production calcium formate which characterized in that: comprises a coke filter (3), a dephosphorization tower (4), a desulfurization tower (8), a demister (9), a compressor (15), a primary pressure swing adsorption tower (16), a secondary pressure swing adsorption tower (22) and a reaction kettle (32) which are connected in sequence; the air inlet of the coke filter (3) is connected with the yellow phosphorus tail gas pipeline (1); the discharge hole of the reaction kettle (32) is connected with a calcium formate product discharge pipeline (35).
2. The production device for producing calcium formate by using yellow phosphorus tail gas according to the mixed serial-parallel method of claim 1, which is characterized in that: the regeneration air inlet of the dephosphorization tower (4) is connected with the PSA two-section emptying air inlet pipeline (2) through the heater (5), the regeneration air outlet of the dephosphorization tower (4) is connected with the regeneration adsorption tower (6), and the regeneration adsorption tower (6) is also connected with the emptying pipeline (7).
3. The production device for producing calcium formate by using yellow phosphorus tail gas according to the mixed serial-parallel method of claim 1, which is characterized in that: a liquid outlet of the desulfurizing tower (8) is circularly communicated with liquid inlets of the regeneration tank (10), the barren solution tank (11) and the desulfurizing tower (8); the regeneration tank (10) is also sequentially connected with a sulfur foam tank (12) and a sulfur melting kettle (13); the discharge port of the sulfur melting kettle (13) is connected with a sulfur pipeline (14).
4. The production device for producing calcium formate by using yellow phosphorus tail gas according to the mixed serial-parallel method of claim 1, which is characterized in that: the number of the first-stage pressure swing adsorption towers (16) is 3-5, the tops of a plurality of the first-stage pressure swing adsorption towers (16) are respectively connected in parallel to a first-stage forward discharge pipeline (18) and a first-stage exhaust pipeline (21), and the bottoms of a plurality of the first-stage pressure swing adsorption towers (16) are respectively connected in parallel to a first-stage reverse discharge pipeline (19) and a first-stage air inlet pipeline (17);
the number of the two-stage pressure swing adsorption towers (22) is 4-6, the tops of a plurality of the two-stage pressure swing adsorption towers (22) are respectively connected in parallel on a two-stage forward discharge pipeline (26) and a two-stage exhaust pipeline (25), and the bottoms of a plurality of the two-stage pressure swing adsorption towers (22) are respectively connected in parallel on a two-stage reverse discharge pipeline (23) and a two-stage air inlet pipeline (24).
5. The production device for producing calcium formate by using yellow phosphorus tail gas according to the mixed serial-parallel method of claim 4, which is characterized in that: the primary air inlet pipeline (17) is connected with the compressor (15);
the primary forward discharge pipeline (18) is connected with the secondary forward discharge pipeline (26) through a No. 1 empty tower (20), and the secondary forward discharge pipeline (26) is connected with a PSA secondary-section vent gas exhaust pipeline (27) through a No. 2 empty tower (28);
the primary exhaust pipeline (21) is connected with the secondary air inlet pipeline (24);
the secondary reverse discharge pipeline (23) is connected with a CO feeding pipeline (31).
6. The production device for producing calcium formate by using yellow phosphorus tail gas according to the mixed serial-parallel method of claim 4, which is characterized in that: program control valves are arranged on the primary forward release pipeline (18), the primary exhaust pipeline (21), the primary reverse release pipeline (19), the primary air inlet pipeline (17), the secondary forward release pipeline (26), the secondary exhaust pipeline (25), the secondary reverse release pipeline (23) and the secondary air inlet pipeline (24).
7. The production device for producing calcium formate by using yellow phosphorus tail gas according to the mixed serial-parallel method of claim 1, which is characterized in that: the number of the reaction kettles (32) is 3-6, the feed inlets of a plurality of the reaction kettles (32) are respectively connected in parallel on a CO feed pipeline (31) and a raw material feed pipeline (29), and the discharge outlets of a plurality of the reaction kettles (32) are connected in parallel on a calcium formate product discharge pipeline (35);
the heating channels of a plurality of reaction kettles (32) are connected in parallel through a steam inlet pipeline (30) and a steam condensate parallel pipeline (33), and are connected in series through a steam condensate series pipeline (34).
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114560545A (en) * | 2022-03-08 | 2022-05-31 | 贵州开阳青利天盟化工有限公司 | A waste water cyclic utilization system for in yellow phosphorus storage |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114560545A (en) * | 2022-03-08 | 2022-05-31 | 贵州开阳青利天盟化工有限公司 | A waste water cyclic utilization system for in yellow phosphorus storage |
| CN114560545B (en) * | 2022-03-08 | 2023-10-03 | 贵州开阳青利天盟化工有限公司 | Wastewater recycling system for yellow phosphorus storage |
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