CN104445724A - Device for recycling high chlorine wastewater generated during production of polyvinyl chloride by calcium carbide method and application method thereof - Google Patents
Device for recycling high chlorine wastewater generated during production of polyvinyl chloride by calcium carbide method and application method thereof Download PDFInfo
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- CN104445724A CN104445724A CN201410667049.2A CN201410667049A CN104445724A CN 104445724 A CN104445724 A CN 104445724A CN 201410667049 A CN201410667049 A CN 201410667049A CN 104445724 A CN104445724 A CN 104445724A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/38—Polymers
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Abstract
The invention relates to the technical field of high chlorine wastewater recovery and provides a device for recycling high chlorine wastewater generated during production of polyvinyl chloride by a calcium carbide method and an application method thereof. The device comprises an oxidation tank, a reaction tank, a sloping plate sedimentation basin, a plate-and-frame filter press and a water storage tank. The device is mainly applied to the technology for recycling the high chlorine wastewater generated during production of polyvinyl chloride by the calcium carbide method to be used as primary brine. The device has the beneficial effects that environmental pollution caused by direct discharge of chlorine wastewater is reduced by dechlorinating the high chlorine wastewater by adopting the device; waste of water resources can be avoided by recycling clear liquid; after being recovered, filter cakes are used for producing cement, so that waste can be turned into wealth and the application value of the high chlorine wastewater can be increased; the content of sulfur impurities in the clear liquid obtained after the high chlorine wastewater is treated is reduced below 0.1mg/1 and the content of phosphorus impurities in the clear liquid is reduced below 1mg/1, so that the salt dissolving standards of primary brine salt dissolving units are satisfied.
Description
Technical field
the present invention relates to high chlorine root technical field of wastewater recovery, is high chlorine root wastewater recycling device and using method thereof during a kind of generated by polyvinyl chloride by calcium carbide is produced.
Background technology
in the Technology of calcium carbide method acetylene production, in order to remove the impurity such as S, P in thick acetylene gas, the chlorine bleach liquor added in process removes the impurity component such as sulphur, phosphorus in acetylene gas, and this process is called peace and quiet process, and reaction equation is:
PH
3
+4NaClO→H
3
PO
4
+4NaCl
H
2
S+4NaClO→H
2
SO
4
+4NaCl
the useless sodium hypochlorite solution produced in peace and quiet process is back to clorox configuration-system again after reclaiming the acetylene gas dissolved, the accumulative rising of salt concn will be caused after reuse is of long duration, the useless chlorine bleach liquor of high salt concentration is referred to as high chlorine root waste water, high chlorine root waste water has a strong impact on the activity of chlorine bleach liquor, considerable influence is had to except desulfuration, phosphorus impurities, this just must arrange displacement outward high chlorine root waste water, the direct discharge of high chlorine root waste water will certainly cause serious pollution to environment, causes the waste of water resources simultaneously.
Summary of the invention
the invention provides high chlorine root wastewater recycling device and using method thereof in the production of a kind of generated by polyvinyl chloride by calcium carbide, overcome the deficiency of above-mentioned prior art, it provides a kind of removal in high chlorine root waste water to recycle the high device of chlorine root waste water and the using method of this device thereof after sulphur, phosphorus impurities, and it effectively can remove sulphur in high chlorine root waste water, phosphorus impurities the high chlorine root waste water after removing sulphur, phosphorus impurities is carried out recovery be used for being used for of primary brine technique salt.
one of technical scheme of the present invention is realized by following measures: high chlorine root wastewater recycling device in a kind of generated by polyvinyl chloride by calcium carbide production, and it comprises oxidation tank, retort, inclined-plate clarifying basin, plate-and-frame filter press and water tank, at oxidation tank and retort internal fixtion, whipping appts is installed, oxidation tank feed liquor pipeline and oxygenant pipeline is installed with respectively in the upper end of oxidation tank, the lower end of oxidation tank to retort upper end between be installed with retort feed liquor pipeline, retort feed liquor pipeline is installed with oxidation discharging pump, S-WAT pipeline is also installed with in the upper end of retort, calcium hydroxide pipeline and sodium hydroxide pipeline, the lower end of retort to inclined-plate clarifying basin upper end between be installed with settling tank feeding line, settling tank feeding line is installed with reaction discharging pump, flocculant line is installed with in the upper end of inclined-plate clarifying basin, the lower end of inclined-plate clarifying basin to plate-and-frame filter press import between be installed with slag slurry feed-stock pipeline, slag slurry feed-stock pipeline is installed with Pulp pump, the top of inclined-plate clarifying basin to water tank upper end between be installed with clear liquid line of pipes, the filtrate outlet of plate-and-frame filter press to water tank upper end between be installed with filtrate line, the lower end of water tank is installed with tapping line, tapping line is installed with clear liquid pump, oxidation tank feed liquor pipeline is installed with oxidation tank liquid inlet control valve, oxygenant pipeline is installed with oxidizer control valve, S-WAT pipeline is installed with S-WAT control valve, calcium hydroxide pipeline is installed with calcium hydroxide control valve, sodium hydroxide pipeline is installed with sodium hydroxide control valve, flocculant line is installed with flocculation agent control valve, oxidation discharging pump before and after retort feed liquor pipeline on be installed with respectively oxidation discharging pump before control valve and oxidation discharging pump after control valve, reaction discharging pump before and after settling tank feeding line on be installed with respectively reaction discharging pump before control valve and reaction discharging pump after control valve, slag slurry feed-stock pipeline before and after Pulp pump to be installed with respectively before Pulp pump control valve after control valve and Pulp pump, tapping line before and after clear liquid pump to be installed with respectively before clear liquid pump control valve after control valve and clear liquid pump, at retort feed liquor pipeline, settling tank feeding line, slag slurry feed-stock pipeline and tapping line are installed with sampling valve respectively, the first reflux pipeline is installed with between retort feed liquor pipeline after oxidation discharging pump and the upper end of oxidation tank, the second reflux pipeline is installed with between retort feed liquor pipeline after reaction discharging pump and retort, tapping line after clear liquid pump and be installed with the 3rd reflux pipeline between water tank.
here is the further optimization and/or improvements to one of foregoing invention technical scheme:
retort feed liquor pipeline for subsequent use is installed with between retort feed liquor pipeline before above-mentioned oxidation discharging pump before control valve and after oxidation discharging pump after control valve, retort feed liquor pipeline for subsequent use is installed with oxidation discharging pump for subsequent use, the retort feed liquor pipeline for subsequent use before and after oxidation discharging pump for subsequent use is installed with the first control valve and the second control valve respectively; Or/and, settling tank feeding line for subsequent use is installed with between settling tank feeding line before reaction discharging pump before control valve and after reaction discharging pump after control valve, settling tank feeding line for subsequent use is installed with reaction discharging pump for subsequent use, the settling tank feeding line for subsequent use before and after reaction discharging pump for subsequent use is installed with respectively the 3rd control valve and the 4th control valve.
slag for subsequent use slurry feed-stock pipeline is installed with between slag slurry feed-stock pipeline before above-mentioned Pulp pump before control valve and after Pulp pump after control valve, slag slurry feed-stock pipeline for subsequent use is installed with Pulp pump for subsequent use, the slag slurry feed-stock pipeline for subsequent use before and after Pulp pump for subsequent use is installed with the 5th control valve and the 6th control valve respectively; Or/and, tapping line for subsequent use is installed with between tapping line before clear liquid pump before control valve and after clear liquid pump after control valve, tapping line for subsequent use is installed with clear liquid pump for subsequent use, the tapping line for subsequent use before and after clear liquid pump for subsequent use is installed with respectively the 7th control valve and the 8th control valve.
above-mentionedly be that the top of oxidation tank is installed with oxidation tank upflow tube, be installed with oxidation tank pipe connecting between the bottom of oxidation tank and oxidation tank upflow tube, oxidation tank pipe connecting is installed with control valve.
the top of above-mentioned water tank is installed with water tank upflow tube, is installed with water tank pipe connecting, water tank pipe connecting is installed with control valve between the bottom of water tank and water tank upflow tube.
two of technical scheme of the present invention is realized by following measures: the using method of high chlorine root wastewater recycling device in a kind of generated by polyvinyl chloride by calcium carbide production, and it carries out in the steps below: the first step, closes oxidizer control valve, S-WAT control valve, calcium hydroxide control valve, sodium hydroxide control valve, flocculation agent control valve, control valve before oxidation discharging pump, control valve after oxidation discharging pump, control valve before reaction discharging pump, control valve after reaction discharging pump, control valve before Pulp pump, control valve after Pulp pump, control valve before clear liquid pump, control valve and sampling valve after clear liquid pump, open oxidation tank liquid inlet control valve, high chlorine root waste water is injected oxidation tank, start the whipping appts in oxidation tank, when the liquid level of high chlorine root waste water reaches 80%, close oxidation tank liquid inlet control valve, open oxidizer control valve, in oxidation tank, add clorox, after clorox adds, close oxidizer control valve, then stir 30 minutes to 60 minutes, the available chlorine content of material in oxidation tank is detected by the sampling valve on retort feed liquor pipeline, when mass content>=0.02% of available chlorine, the sampling valve on off-response tank feed liquor pipeline, second step, open oxidation discharging pump before control valve and oxidation discharging pump after control valve, by oxidation discharging pump, the material in oxidation tank is delivered in retort, after mass transport completes, close oxidation discharging pump before control valve and oxidation discharging pump after control valve, start the whipping appts in retort, open sodium hydroxide control valve, sodium hydroxide solution is added in retort, when in question response tank, the pH value of material is 9-10, close sodium hydroxide control valve, open S-WAT control valve and calcium hydroxide control valve, add carbide slag slurry and S-WAT, carbide slag slurry and S-WAT add rear closedown S-WAT control valve and calcium hydroxide control valve, then stirring 30 minutes to 60 minutes is continued, open phosphate radical in the sampling valve detection reaction tank on settling tank feeding line, the content of sulfate radical and calcium ion, as the mass content≤0.1mg/L of sulfate radical, mass content≤the 1mg/L of phosphate radical, during mass content≤the 5mg/L of calcium ion, close the sampling valve on settling tank feeding line, 3rd step, open reaction discharging pump before control valve and reaction discharging pump after control valve, by reaction discharging pump, the material in retort is delivered in inclined-plate clarifying basin, after band mass transport completes, before off-response discharging pump control valve and reaction discharging pump after control valve, open flocculation agent control valve, iron(ic) chloride is added in inclined-plate clarifying basin, after the material in inclined-plate clarifying basin completes precipitation, to open before Pulp pump control valve after control valve and Pulp pump, the clear liquid overflow at inclined-plate clarifying basin top is in water tank, slag slurry bottom inclined-plate clarifying basin is delivered in plate-and-frame filter press through Pulp pump and carries out press filtration, obtain filter cake and filtrate respectively, filtrate is delivered in water tank through filtrate line, to open before clear liquid pump control valve after control valve and clear liquid pump, liquid in water tank is discharged through clear liquid pump.
generated by polyvinyl chloride by calcium carbide of the present invention produce in high chlorine root wastewater recycling device be mainly used in generated by polyvinyl chloride by calcium carbide produce in high chlorine root waste water recycling to the Technology of primary brine, in adopting generated by polyvinyl chloride by calcium carbide of the present invention to produce, high chlorine root wastewater recycling device carries out the high chlorine root waste water that dechlorinates, the environmental pollution that the direct discharge decreasing chlorine root waste water causes, the waste of water resources can be avoided to the recycling of clear liquid, for the production of cement after filter cake reclaims, can turn waste into wealth, improve the utility value of high chlorine root waste water, in the clear liquid that high chlorine root waste water obtains after treatment, sulphur impurity is reduced to below 0.1mg/l, phosphorus impurities content is down to below 1mg/l, meet primary brine salt blocking salt standard.
Accompanying drawing explanation
accompanying drawing 1 is the process structure schematic diagram of the embodiment of the present invention.
coding in accompanying drawing is respectively: 1 is oxidation tank, 2 is retort, 3 is oxidation tank feed liquor pipeline, 4 is oxygenant pipeline, 5 is retort feed liquor pipeline, 6 is oxidation discharging pump, 7 is S-WAT pipeline, 8 is calcium hydroxide pipeline, 9 is sodium hydroxide pipeline, 10 is inclined-plate clarifying basin, 11 is settling tank feeding line, 12 is reaction discharging pump, 13 is flocculant line, 14 is plate-and-frame filter press, 15 is slag slurry feed-stock pipeline, 16 is Pulp pump, 17 is water tank, 18 is clear liquid line of pipes, 19 is filtrate line, 20 is tapping line, 21 is clear liquid pump, 22 is oxidation tank liquid inlet control valve, 23 is oxidizer control valve, 24 is S-WAT control valve, 25 is calcium hydroxide control valve, 26 is sodium hydroxide control valve, 27 is flocculation agent control valve, 28 is control valve before oxidation discharging pump, 29 is control valve after oxidation discharging pump, 30 is control valve before reaction discharging pump, 31 is control valve after reaction discharging pump, 32 is control valve before Pulp pump, 33 is control valve after Pulp pump, 34 is control valve before clear liquid pump, 35 is control valve after clear liquid pump, 36 is sampling valve, 37 is the first reflux pipeline, 38 is the second reflux pipeline, 39 is the 3rd reflux pipeline, 40 is oxidation tank upflow tube, 41 is oxidation tank pipe connecting, 42 is control valve, 43 is water tank upflow tube, 44 is water tank pipe connecting, 45 is retort feed liquor pipeline for subsequent use, 46 is oxidation discharging pump for subsequent use, 47 is the first control valve, 48 is the second control valve, 49 is settling tank feeding line for subsequent use, 50 is reaction discharging pump for subsequent use, 51 is the 3rd control valve, 52 is the 4th control valve, 53 is slag for subsequent use slurry feeding tube, 54 is Pulp pump for subsequent use, 55 is the 5th control valve, 56 is the 6th control valve, 57 is tapping line for subsequent use, 58 is clear liquid pump for subsequent use, 59 is the 7th control valve, 60 is the 8th control valve.
Embodiment
the present invention by the restriction of following embodiment, can not determine concrete embodiment according to technical scheme of the present invention and practical situation.Unless stated otherwise, the % in the present invention is mass percent; Unless stated otherwise, preparation process is carried out under normal temperature, atmospheric pressure state; Unless stated otherwise, the reagent adopted in the present invention, method and apparatus are the art conventional reagent, method and apparatus; Unless stated otherwise, in the present invention, agents useful for same is commercial; Unless stated otherwise, the water in the present invention is tap water; Unless stated otherwise, the solution in the present invention is the aqueous solution that solvent is water, and such as, if illustrate, hydrochloric acid soln is aqueous hydrochloric acid.
in the present invention, for convenience of description, the description of the relative position relation of each parts is all be described according to the Butut mode of Figure of description 1, as: the position relationship of upper and lower, left and right etc. determines according to the Butut direction of Figure of description.
below in conjunction with embodiment and accompanying drawing, the invention will be further described:
embodiment 1, as shown in Figure 1, in the production of this generated by polyvinyl chloride by calcium carbide, high chlorine root wastewater recycling device comprises oxidation tank 1, retort 2, inclined-plate clarifying basin 10, plate-and-frame filter press 14 and water tank 17, at oxidation tank 1 and retort 2 internal fixtion, whipping appts is installed, oxidation tank feed liquor pipeline 3 and oxygenant pipeline 4 is installed with respectively in the upper end of oxidation tank 1, the lower end of oxidation tank 1 to retort 2 upper end between be installed with retort feed liquor pipeline 5, retort feed liquor pipeline 5 is installed with oxidation discharging pump 6, S-WAT pipeline 7 is also installed with in the upper end of retort 2, calcium hydroxide pipeline 8 and sodium hydroxide pipeline 9, the lower end of retort 2 to inclined-plate clarifying basin 10 upper end between be installed with settling tank feeding line 11, settling tank feeding line 11 is installed with reaction discharging pump 12, flocculant line 13 is installed with in the upper end of inclined-plate clarifying basin 10, the lower end of inclined-plate clarifying basin 10 to plate-and-frame filter press 14 import between be installed with slag slurry feed-stock pipeline 15, slag slurry feed-stock pipeline 15 is installed with Pulp pump 16, the top of inclined-plate clarifying basin 10 to water tank 17 upper end between be installed with clear liquid line of pipes 18, the filtrate outlet of plate-and-frame filter press 14 to water tank 17 upper end between be installed with filtrate line 19, the lower end of water tank 17 is installed with tapping line 20, tapping line 20 is installed with clear liquid pump 21, oxidation tank feed liquor pipeline 3 is installed with oxidation tank liquid inlet control valve 22, oxygenant pipeline 4 is installed with oxidizer control valve 23, S-WAT pipeline 7 is installed with S-WAT control valve 24, calcium hydroxide pipeline 8 is installed with calcium hydroxide control valve 25, sodium hydroxide pipeline 9 is installed with sodium hydroxide control valve 26, flocculant line 13 is installed with flocculation agent control valve 27, retort feed liquor pipeline 5 before and after oxidation discharging pump 6 to be installed with respectively before oxidation discharging pump control valve 29 after control valve 28 and oxidation discharging pump, settling tank feeding line 11 before and after reaction discharging pump 12 to be installed with respectively before reaction discharging pump control valve 31 after control valve 30 and reaction discharging pump, slag slurry feed-stock pipeline 15 before and after Pulp pump 16 to be installed with respectively before Pulp pump control valve 33 after control valve 32 and Pulp pump, tapping line 20 before and after clear liquid pump 21 to be installed with respectively before clear liquid pump control valve 35 after control valve 34 and clear liquid pump, at retort feed liquor pipeline 5, settling tank feeding line 11, slag slurry feed-stock pipeline 15 and tapping line 20 are installed with sampling valve 36 respectively, the first reflux pipeline 37 is installed with between retort feed liquor pipeline 5 after oxidation discharging pump 6 and the upper end of oxidation tank 1, the second reflux pipeline 38 is installed with between retort feed liquor pipeline 11 after reaction discharging pump 12 and retort 2, tapping line 20 after clear liquid pump 21 and be installed with the 3rd reflux pipeline 39 between water tank 17.In oxidation tank 1, add clorox by oxygenant pipeline 4, one is can with sulphur, the phosphorus reaction in high chlorine root waste water, and two is that clorox is excessive, and the PH keeping solution in oxidation tank 1 is 5 to 6; In retort 2, add carbide slag slurry or unslaked lime by calcium hydroxide pipeline 8, carbide slag alkali lye or unslaked lime and sulfate radical, phosphate radical reaction generate calcium sulfate, calcium phosphate precipitation; Clorox excessive in S-WAT removing retort 2 is added in retort 2; In oxidation tank 1 and retort 2, install whipping appts can make material reaction even, and inclined-plate clarifying basin 10 needs the gravity leaving standstill dependence material itself to precipitate, and does not therefore need to install whipping appts; First reflux pipeline 37, second reflux pipeline 38 and the 3rd reflux pipeline 39 can ensure liquid level in oxidation tank 1 or retort 2 or water tank 17 and pressure steady; Can carry out recovery by filter cake out in plate-and-frame filter press 14 to deliver to cement mill and produce cement, the clear liquid in water tank 17 delivers to the primary brine salt unit of potroom for changing salt through clear liquid pump 21; Oxidation tank 1, retort 2 and water tank 17 all adopt the container of existing known technology, inclined-plate clarifying basin 10 adopts the inclined-plate clarifying basin of existing known technology, plate-and-frame filter press 14 adopts the plate-and-frame filter press of existing known technology, and oxidation discharging pump 6, reaction discharging pump 12, Pulp pump 16 and clear liquid pump 21 are the pump in existing known technology.
embodiment 2, preferred as above-described embodiment, as shown in Figure 1, retort feed liquor pipeline 45 for subsequent use is installed with between retort feed liquor pipeline 5 before oxidation discharging pump before control valve 28 and after oxidation discharging pump after control valve 29, retort feed liquor pipeline 45 for subsequent use is installed with oxidation discharging pump 46 for subsequent use, the retort feed liquor pipeline 45 for subsequent use before and after oxidation discharging pump 46 for subsequent use is installed with respectively the first control valve 47 and the second control valve 48; Or/and, settling tank feeding line 49 for subsequent use is installed with between settling tank feeding line 11 before reaction discharging pump before control valve 30 and after reaction discharging pump after control valve 31, settling tank feeding line 49 for subsequent use is installed with reaction discharging pump 50 for subsequent use, the settling tank feeding line 49 for subsequent use before and after reaction discharging pump 50 for subsequent use is installed with respectively the 3rd control valve 51 and the 4th control valve 52; Or/and, slag for subsequent use slurry feed-stock pipeline 53 is installed with between slag slurry feed-stock pipeline 15 before Pulp pump before control valve 32 and after Pulp pump after control valve 33, slag slurry feed-stock pipeline 53 for subsequent use is installed with Pulp pump 54 for subsequent use, the slag slurry feed-stock pipeline 53 for subsequent use before and after Pulp pump 54 for subsequent use is installed with the 5th control valve 55 and the 6th control valve 56 respectively; Or/and, tapping line 57 for subsequent use is installed with between tapping line 20 before clear liquid pump before control valve 34 and after clear liquid pump after control valve 35, tapping line 57 for subsequent use is installed with clear liquid pump 58 for subsequent use, the tapping line for subsequent use 57 before and after clear liquid pump 58 for subsequent use is installed with respectively the 7th control valve 59 and the 8th control valve 60.When be oxidized discharging pump 6 or reaction discharging pump 12 or Pulp pump 16 or clear liquid pump 21 go wrong need to be serviced or overhaul time, oxidation discharging pump 46 for subsequent use or reaction discharging pump 50 for subsequent use or Pulp pump for subsequent use 54 or clear liquid pump for subsequent use 58 can be enabled; When needing to carry a large amount of material, also can enable oxidation discharging pump 6 and oxidation discharging pump 46 for subsequent use or reaction discharging pump for subsequent use 50 and reaction discharging pump 12 or Pulp pump for subsequent use 54 and Pulp pump 16 or clear liquid pump for subsequent use 58 and clear liquid pump 21 simultaneously.
embodiment 3, preferred as above-described embodiment, as shown in Figure 1, is that the top of oxidation tank 1 is installed with oxidation tank upflow tube 40, be installed with oxidation tank pipe connecting 41 between the bottom of oxidation tank 1 and oxidation tank upflow tube 40, oxidation tank pipe connecting 41 is installed with control valve 42; Or/and the top of water tank 17 is installed with water tank upflow tube 43, is installed with water tank pipe connecting 44 between the bottom of water tank 17 and water tank upflow tube 43, water tank pipe connecting 44 is installed with control valve 42.Oxidation tank upflow tube 40 and water tank upflow tube 43 can prevent oxidation tank 1 or water tank 17 canful, when oxidation tank 1 or water tank 17 canful, when having little time discharge opeing, open control valve 42, by oxidation tank pipe connecting 41 or water tank pipe connecting 44 and oxidation tank upflow tube 40 or water tank upflow tube 43 discharge opeing simultaneously, for safety in production provides safeguard.
embodiment 4, as shown in Figure 1, in the production of this generated by polyvinyl chloride by calcium carbide, the using method of high chlorine root wastewater recycling device is carried out in the steps below: the first step, closes oxidizer control valve 23, S-WAT control valve 24, calcium hydroxide control valve 25, sodium hydroxide control valve 26, flocculation agent control valve 27, control valve 28 before oxidation discharging pump, control valve 29 after oxidation discharging pump, control valve 30 before reaction discharging pump, control valve 31 after reaction discharging pump, control valve 32 before Pulp pump, control valve 33 after Pulp pump, control valve 34 before clear liquid pump, control valve 35 and sampling valve 36 after clear liquid pump, open oxidation tank liquid inlet control valve 22, high chlorine root waste water is injected oxidation tank 1, start the whipping appts in oxidation tank 1, when the liquid level of high chlorine root waste water reaches 80%, close oxidation tank liquid inlet control valve 22, open oxidizer control valve 23, in oxidation tank 1, add clorox, after clorox adds, close oxidizer control valve 23, then stir 30 minutes to 60 minutes, the available chlorine content of material in oxidation tank 1 is detected by the sampling valve 36 on retort feed liquor pipeline 5, when mass content>=0.02% of available chlorine, the sampling valve 36 on off-response tank feed liquor pipeline 5, second step, to open before oxidation discharging pump control valve 29 after control valve 28 and oxidation discharging pump, by oxidation discharging pump 6, the material in oxidation tank 1 is delivered in retort 2, after mass transport completes, to close before oxidation discharging pump control valve 29 after control valve 28 and oxidation discharging pump, start the whipping appts in retort 2, open sodium hydroxide control valve 26, sodium hydroxide solution is added in retort 2, when in question response tank 2, the pH value of material is 9-10, close sodium hydroxide control valve 26, open S-WAT control valve 24 and calcium hydroxide control valve 25, add carbide slag slurry and S-WAT, carbide slag slurry and S-WAT add rear closedown S-WAT control valve 24 and calcium hydroxide control valve 25, then stirring 30 minutes to 60 minutes is continued, open phosphate radical in the sampling valve 36 detection reaction tank 2 on settling tank feeding line 11, the content of sulfate radical and calcium ion, as the mass content≤0.1mg/L of sulfate radical, mass content≤the 1mg/L of phosphate radical, during mass content≤the 5mg/L of calcium ion, close the sampling valve 36 on settling tank feeding line 11, 3rd step, to open before reaction discharging pump control valve 31 after control valve 30 and reaction discharging pump, by reaction discharging pump 12, the material in retort 2 is delivered in inclined-plate clarifying basin 10, after band mass transport completes, control valve 31 after control valve 30 and reaction discharging pump before off-response discharging pump, open flocculation agent control valve 27, iron(ic) chloride is added in inclined-plate clarifying basin 10, after the material in inclined-plate clarifying basin 10 completes precipitation, to open before Pulp pump control valve 33 after control valve 32 and Pulp pump, the clear liquid overflow at inclined-plate clarifying basin 10 top is in water tank 17, slag slurry bottom inclined-plate clarifying basin 10 is delivered in plate-and-frame filter press 14 through Pulp pump 16 and carries out press filtration, obtain filter cake and filtrate respectively, filtrate is delivered in water tank 17 through filtrate line 19, to open before clear liquid pump control valve 35 after control valve 34 and clear liquid pump, liquid in water tank 17 is discharged through clear liquid pump 21.
in adopting generated by polyvinyl chloride by calcium carbide of the present invention to produce high chlorine root wastewater recycling device be mainly used in generated by polyvinyl chloride by calcium carbide produce in high chlorine root waste water recycling to the Technology of primary brine, high chlorine root waste water passes through to add excessive clorox by sulphur at a low price in weakly acidic condition, phosphorus plasma oxygen turns to sulfate radical, phosphate radical, then carbide slag slurry or unslaked lime is added after the high chlorine root waste water pH value after oxidation being adjusted to 9 to 10, carbide slag slurry is by phosphate radical, sulfate radical instead Fan Ying not generate calcium phosphate, calcium sulfate precipitation, add S-WAT and remove excessive clorox, it is settlement separate that flocculation agent adopts iron trichloride to make the material in inclined-plate clarifying basin 10 carry out further, carrying out of potroom primary brine salt unit salt delivered to by the clear liquid obtained, throw out is delivered to cement mill and is produced cement after forming filter cake by plate-and-frame filter press 14, in adopting generated by polyvinyl chloride by calcium carbide of the present invention to produce, high chlorine root wastewater recycling device carries out the high chlorine root waste water that dechlorinates, the environmental pollution that the direct discharge decreasing chlorine root waste water causes, the waste of water resources can be avoided to the recycling of clear liquid, for the production of cement after filter cake reclaims, can turn waste into wealth, improve the utility value of high chlorine root waste water.In the clear liquid obtained after high chlorine root wastewater recycling device process height chlorine root waste water during generated by polyvinyl chloride by calcium carbide of the present invention is produced, sulphur impurity is reduced to below 0.1mg/l, phosphorus impurities content is down to below 1mg/l, meets primary brine salt blocking salt standard.
above technical characteristic constitutes embodiments of the invention, and it has stronger adaptability and implementation result, can increase and decrease non-essential technical characteristic according to actual needs, meet the demand of different situations.
Claims (10)
1. a high chlorine root wastewater recycling device in generated by polyvinyl chloride by calcium carbide production, is characterized in that comprising oxidation tank, retort, inclined-plate clarifying basin, plate-and-frame filter press and water tank, at oxidation tank and retort internal fixtion, whipping appts is installed, oxidation tank feed liquor pipeline and oxygenant pipeline is installed with respectively in the upper end of oxidation tank, the lower end of oxidation tank to retort upper end between be installed with retort feed liquor pipeline, retort feed liquor pipeline is installed with oxidation discharging pump, S-WAT pipeline is also installed with in the upper end of retort, calcium hydroxide pipeline and sodium hydroxide pipeline, the lower end of retort to inclined-plate clarifying basin upper end between be installed with settling tank feeding line, settling tank feeding line is installed with reaction discharging pump, flocculant line is installed with in the upper end of inclined-plate clarifying basin, the lower end of inclined-plate clarifying basin to plate-and-frame filter press import between be installed with slag slurry feed-stock pipeline, slag slurry feed-stock pipeline is installed with Pulp pump, the top of inclined-plate clarifying basin to water tank upper end between be installed with clear liquid line of pipes, the filtrate outlet of plate-and-frame filter press to water tank upper end between be installed with filtrate line, the lower end of water tank is installed with tapping line, tapping line is installed with clear liquid pump, oxidation tank feed liquor pipeline is installed with oxidation tank liquid inlet control valve, oxygenant pipeline is installed with oxidizer control valve, S-WAT pipeline is installed with S-WAT control valve, calcium hydroxide pipeline is installed with calcium hydroxide control valve, sodium hydroxide pipeline is installed with sodium hydroxide control valve, flocculant line is installed with flocculation agent control valve, oxidation discharging pump before and after retort feed liquor pipeline on be installed with respectively oxidation discharging pump before control valve and oxidation discharging pump after control valve, reaction discharging pump before and after settling tank feeding line on be installed with respectively reaction discharging pump before control valve and reaction discharging pump after control valve, slag slurry feed-stock pipeline before and after Pulp pump to be installed with respectively before Pulp pump control valve after control valve and Pulp pump, tapping line before and after clear liquid pump to be installed with respectively before clear liquid pump control valve after control valve and clear liquid pump, at retort feed liquor pipeline, settling tank feeding line, slag slurry feed-stock pipeline and tapping line are installed with sampling valve respectively, the first reflux pipeline is installed with between retort feed liquor pipeline after oxidation discharging pump and the upper end of oxidation tank, the second reflux pipeline is installed with between retort feed liquor pipeline after reaction discharging pump and retort, tapping line after clear liquid pump and be installed with the 3rd reflux pipeline between water tank.
2. high chlorine root wastewater recycling device in generated by polyvinyl chloride by calcium carbide production according to claim 1, retort feed liquor pipeline for subsequent use is installed with between retort feed liquor pipeline before it is characterized in that being oxidized discharging pump before control valve and after oxidation discharging pump after control valve, retort feed liquor pipeline for subsequent use is installed with oxidation discharging pump for subsequent use, the retort feed liquor pipeline for subsequent use before and after oxidation discharging pump for subsequent use is installed with the first control valve and the second control valve respectively; Or/and, settling tank feeding line for subsequent use is installed with between settling tank feeding line before reaction discharging pump before control valve and after reaction discharging pump after control valve, settling tank feeding line for subsequent use is installed with reaction discharging pump for subsequent use, the settling tank feeding line for subsequent use before and after reaction discharging pump for subsequent use is installed with respectively the 3rd control valve and the 4th control valve.
3. high chlorine root wastewater recycling device in generated by polyvinyl chloride by calcium carbide production according to claim 1 and 2, slag for subsequent use slurry feed-stock pipeline is installed with between slag slurry feed-stock pipeline before it is characterized in that Pulp pump before control valve and after Pulp pump after control valve, slag slurry feed-stock pipeline for subsequent use is installed with Pulp pump for subsequent use, the slag slurry feed-stock pipeline for subsequent use before and after Pulp pump for subsequent use is installed with the 5th control valve and the 6th control valve respectively; Or/and, tapping line for subsequent use is installed with between tapping line before clear liquid pump before control valve and after clear liquid pump after control valve, tapping line for subsequent use is installed with clear liquid pump for subsequent use, the tapping line for subsequent use before and after clear liquid pump for subsequent use is installed with respectively the 7th control valve and the 8th control valve.
4. high chlorine root wastewater recycling device in generated by polyvinyl chloride by calcium carbide production according to claim 1 and 2, it is characterized in that the top of oxidation tank is installed with oxidation tank upflow tube, be installed with oxidation tank pipe connecting between the bottom of oxidation tank and oxidation tank upflow tube, oxidation tank pipe connecting is installed with control valve.
5. high chlorine root wastewater recycling device in generated by polyvinyl chloride by calcium carbide production according to claim 3, it is characterized in that the top of oxidation tank is installed with oxidation tank upflow tube, be installed with oxidation tank pipe connecting between the bottom of oxidation tank and oxidation tank upflow tube, oxidation tank pipe connecting is installed with control valve.
6. high chlorine root wastewater recycling device in generated by polyvinyl chloride by calcium carbide production according to claim 1 and 2, it is characterized in that the top of water tank is installed with water tank upflow tube, be installed with water tank pipe connecting between the bottom of water tank and water tank upflow tube, water tank pipe connecting is installed with control valve.
7. high chlorine root wastewater recycling device in generated by polyvinyl chloride by calcium carbide production according to claim 3, it is characterized in that the top of water tank is installed with water tank upflow tube, be installed with water tank pipe connecting between the bottom of water tank and water tank upflow tube, water tank pipe connecting is installed with control valve.
8. high chlorine root wastewater recycling device in generated by polyvinyl chloride by calcium carbide production according to claim 4, it is characterized in that the top of water tank is installed with water tank upflow tube, be installed with water tank pipe connecting between the bottom of water tank and water tank upflow tube, water tank pipe connecting is installed with control valve.
9. high chlorine root wastewater recycling device in generated by polyvinyl chloride by calcium carbide production according to claim 5, it is characterized in that the top of water tank is installed with water tank upflow tube, be installed with water tank pipe connecting between the bottom of water tank and water tank upflow tube, water tank pipe connecting is installed with control valve.
10. in the generated by polyvinyl chloride by calcium carbide production according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, a using method for high chlorine root wastewater recycling device, is characterized in that carrying out in the steps below: the first step, closes oxidizer control valve, S-WAT control valve, calcium hydroxide control valve, sodium hydroxide control valve, flocculation agent control valve, control valve before oxidation discharging pump, control valve after oxidation discharging pump, control valve before reaction discharging pump, control valve after reaction discharging pump, control valve before Pulp pump, control valve after Pulp pump, control valve before clear liquid pump, control valve and sampling valve after clear liquid pump, open oxidation tank liquid inlet control valve, high chlorine root waste water is injected oxidation tank, start the whipping appts in oxidation tank, when the liquid level of high chlorine root waste water reaches 80%, close oxidation tank liquid inlet control valve, open oxidizer control valve, in oxidation tank, add clorox, after clorox adds, close oxidizer control valve, then stir 30 minutes to 60 minutes, the available chlorine content of material in oxidation tank is detected by the sampling valve on retort feed liquor pipeline, when mass content >=0.02% of available chlorine, the sampling valve on off-response tank feed liquor pipeline, second step, open oxidation discharging pump before control valve and oxidation discharging pump after control valve, by oxidation discharging pump, the material in oxidation tank is delivered in retort, after mass transport completes, close oxidation discharging pump before control valve and oxidation discharging pump after control valve, start the whipping appts in retort, open sodium hydroxide control valve, sodium hydroxide solution is added in retort, when in question response tank, the pH value of material is 9-10, close sodium hydroxide control valve, open S-WAT control valve and calcium hydroxide control valve, add carbide slag slurry and S-WAT, carbide slag slurry and S-WAT add rear closedown S-WAT control valve and calcium hydroxide control valve, then stirring 30 minutes to 60 minutes is continued, open phosphate radical in the sampling valve detection reaction tank on settling tank feeding line, the content of sulfate radical and calcium ion, as the mass content≤0.1mg/L of sulfate radical, mass content≤the 1mg/L of phosphate radical, during mass content≤the 5mg/L of calcium ion, close the sampling valve on settling tank feeding line, 3rd step, open reaction discharging pump before control valve and reaction discharging pump after control valve, by reaction discharging pump, the material in retort is delivered in inclined-plate clarifying basin, after band mass transport completes, before off-response discharging pump control valve and reaction discharging pump after control valve, open flocculation agent control valve, iron(ic) chloride is added in inclined-plate clarifying basin, after the material in inclined-plate clarifying basin completes precipitation, to open before Pulp pump control valve after control valve and Pulp pump, the clear liquid overflow at inclined-plate clarifying basin top is in water tank, slag slurry bottom inclined-plate clarifying basin is delivered in plate-and-frame filter press through Pulp pump and carries out press filtration, obtain filter cake and filtrate respectively, filtrate is delivered in water tank through filtrate line, to open before clear liquid pump control valve after control valve and clear liquid pump, liquid in water tank is discharged through clear liquid pump.
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| CN104445724B (en) | 2016-08-24 |
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Effective date of registration: 20181102 Address after: 830009 1868 Yimin West Street, MI Dong District, Urumqi, the Xinjiang Uygur Autonomous Region Co-patentee after: Xinjiang Zhongtai Chemical Co., Ltd. Patentee after: Xinjiang Huatai Heavy Chemical Co., Ltd. Address before: 830026 Yangcheng Lake Road, Urumqi economic and Technological Development Zone, the Xinjiang Uygur Autonomous Region 39 Patentee before: Xinjiang Zhongtai Chemical Co., Ltd. |