CN105233515A - Treatment device and treatment method for organic solvent cleaning waste liquid - Google Patents
Treatment device and treatment method for organic solvent cleaning waste liquid Download PDFInfo
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- CN105233515A CN105233515A CN201510603906.7A CN201510603906A CN105233515A CN 105233515 A CN105233515 A CN 105233515A CN 201510603906 A CN201510603906 A CN 201510603906A CN 105233515 A CN105233515 A CN 105233515A
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Abstract
The invention provides a treatment device and treatment method for an organic solvent cleaning waste liquid. The device is characterized in that the device comprises a raw material tank, wherein the liquid-phase outlet of the raw material tank and a feed pump are in sealing connection; the material inlet of a distillation kettle and the outlet of the feed pump are in sealing connection; the gas-phase inlet of a rectifying tower and the gas-phase outlet of the distillation kettle are in sealing connection, and the gas-phase outlet of the rectifying tower is hermetically connected with a condenser; the gas-phase inlet of the condenser and the gas-phase outlet of the rectifying tower are in sealing connection, and the liquid-phase outlet of the condenser is hermetically connected with the inlet of a separator; and the finished-product inlet of a finished-product tank and the outlet of the separator are in sealing connection, and the finished-product outlet of the finished-product tank and a packaging system are hermetically connected via a finished-product pump. The treatment method comprises the following steps: raw material treatment, feeding, heating, concentration with the distillation kettle, distillation with the distillation kettle, rectification with the rectifying tower, condensation, separation, cooling, and residual material discharging.
Description
Technical field
The present invention relates to organic solvent waste liquid disposal, is a kind of organic solvent waste liquid disposal device and processing method thereof.
Background technology
According to the regulation in " National Hazard refuse register ", in automobile production, the organic solvent cleaning waste liquid that painting process produces contains toluene, dimethylbenzene, butanols etc., thus belongs to HW42 dyestuff, coating class danger wastes (HW42900-451-42 class), does not allow direct discharge.
Summary of the invention
Technical problem to be solved by this invention is: the shortcoming overcoming prior art, a kind of organic solvent waste liquid disposal device and processing method thereof are provided, fully can reclaim the organic solvent cleaning waste liquid in automotive lacquer production process, realize liquid debris recycling, added value can be improved again simultaneously, obtain considerable economic benefit, thus have huge economic and social benefit.
The scheme of technical solution problem of the present invention is: a kind of organic solvent waste liquid disposal device, it is characterized in that: it comprises head tank, distillation still, rectifying column, condenser and finished pot, described head tank top inlet porting, bottom arrange liquid-phase outlet, sediment outlet is set below liquid-phase outlet, the entrance of head tank is tightly connected with Raw material pail with filter by discharging pump, sediment outlet is connected with sediment storage tank seal by sludge pump, and the liquid-phase outlet of head tank is connected with the inlet seal of feed pump, described distillation still top arranges material inlet and gaseous phase outlet, bottom arranges residue outlet, the top of distillation still arranges temperature raising medium entrance and cooling medium outlet, bottom arranges temperature raising medium outlet and cooling medium entrance, the material inlet of distillation still is connected with the exit seal of feed pump, residue outlet is connected with the residual pump seal of still, the temperature raising medium entrance of distillation still is connected with heat-conducting oil system or vapour system exit seal by sub-cylinder, temperature raising medium outlet is connected with heat-conducting oil system or vapour system inlet seal, the cooling medium entrance of distillation still and cooling medium outlet are connected with the outlet of recirculating cooling water system and inlet seal respectively, described rectifier bottoms arranges gas phase entrance, top arranges gaseous phase outlet, the gas phase entrance of rectifier bottoms and the gaseous phase outlet of distillation still is tightly connected, the gaseous phase outlet at top and condenser are tightly connected, described condenser top arranges gas phase entrance, bottom arranges liquid-phase outlet, the top of condenser arranges circulating water outlet, bottom arranges recirculated water entrance, the gaseous phase outlet of condenser gas phase entrance and rectifying column is tightly connected, liquid-phase outlet and separator inlet are tightly connected, and the circulating water outlet of condenser is communicated with circulating water pool, recirculated water entrance is communicated with upper water with circulating water pool by water circulating pump, it is described that finished pot top arranges finished-product entrance, bottom arranges product outlet, the finished-product entrance of finished pot is connected with the exit seal of separator and is tightly connected by separator and condenser, and the product outlet of finished pot is tightly connected by discharge pump and packaging system.
A processing method for organic solvent cleaning waste liquid, is characterized in that: comprise the following steps:
1) after the raw material of barreled being put assigned address, open bung device of drawing a design and raw material is divided into four kinds: a expects clearly, b batch mixing, c paint and paint slag, d impurity; Described raw material is in automobile production, the spent organic solvent cleaning fluid that painting process cleaning paint spraying outfit produces, and composition comprises toluene, mixed xylenes, butanols, isobutanol, butyl acetate;
2) the barreled raw material of step 1) classification falls after larger granule foreign to use discharging pump by its storage tank corresponding according to classification input through metre filter, the static separation of raw material memory period in storage tank, solvent floats on top layer, contamination precipitation forms sediment to bottom, and moisture is between solvent and sediment; Described solvent is the mixing material comprising toluene, mixed xylenes, butanols, isobutanol, butyl acetate;
3) by step 2) liquid material that is separated is by feed pump input distillation still, liquid material charge weight reaches 3/4 of distillation still volume and closes feed pump, step 2) the sediment sludge pump that is separated extracts out, delivers in sediment storage tank; Described liquid material is for comprising step 2) mixing material of described solvent and portion of water;
4) distillation still to infusion fluid material passes into normal temperature conduction oil, after distillation still and conduction oil transmission system normally run 5 minutes, pass into the conduction oil slowly heated up again to heat, it is 15 minutes that the temperature of the conduction oil of slow intensification is warming up to 230 DEG C of used times by 35 DEG C, the temperature 35 DEG C of described normal temperature conduction oil, pressure 0.2MPa, the conduction oil pressure of described slow heating is 0.2MPa;
5) after the conduction oil that step 4) is used liquid material temperature distillation still be heated to wherein reaches boiling point, continue to distillation still liquid make-up material, all the time full state is in make alembic, the temperature simultaneously controlling distillation still top is 106-155 DEG C, and the pressure of distillation still is 0.25-0.35MPa; The liquid material that supplements be step 2) liquid material that is separated;
6) in the gaseous phase materials of step 5) distillation to be entered into connection rectifying column by distillation still top, carry out rectifying, the temperature in rectifying column is 135 DEG C, pressure is 0.01MPa, and the gaseous phase materials temperature after rectifying is 83 DEG C, pressure is 0.01MPa;
7) temperature obtained through step 6) is that the gaseous phase materials of 83 DEG C enters in condenser, and meanwhile, temperature is that the recirculated cooling water of 25 DEG C enters in condenser, the gaseous phase materials in condenser is cooled to the liquid phase material of temperature 35 DEG C;
8) temperature obtained through step 7) is that after the liquid phase material of 35 DEG C enters and isolates moisture in separator, finished product materials enters in finished pot, and enters finished product packing system by discharge pump, moisture drain separator;
9) get cauldron bottom residue sample analysis when temperature at the bottom of still 155 DEG C, in cauldron bottom residue, organic solvent content has operated production lower than 1000ppm i.e. this still;
10) can stop carrying conduction oil when after this still has operated production, the pressure in distillation still declines gradually, residue presents thick shape in distillation still, simultaneously to distillation still conveying cooling water, described cooling water temperature 25 DEG C, pressure 0.4MPa, flow 100m
3/ h;
11), when the pressure drop in distillation still is to 0.01MPa, conveying cooling water is stopped;
12) defective material is discharged when distilling temperature in the kettle and reaching 70 DEG C by the residual pump of still.
The present invention fully can reclaim the organic solvent cleaning waste liquid in automotive lacquer production process, realizes liquid debris recycling, can improve added value again simultaneously, obtain considerable economic benefit, thus have huge economic and social benefit.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention;
Fig. 2 is the I close-up schematic view of Fig. 1;
Fig. 3 is the II close-up schematic view of Fig. 1.
In figure: E103, E104 condenser, FT110 separator; P112, P113 discharging pump, the residual pump of P116, P117 still, P118, P119 discharge pump, P123, P124 water circulating pump, R101, R102 distillation still, SD111 sub-cylinder, T108, T109 rectifying column, V105, V106 head tank, V107 finished pot, V128 filter, V129 circulating water pool.
Detailed description of the invention
Below in conjunction with drawings and Examples, the present invention is further described.
With reference to accompanying drawing 1-3, a kind of organic solvent waste liquid disposal of the present embodiment device, it comprises head tank V105, distillation still R101, distillation still R102, rectifying column T108, rectifying column T109, condenser E103, condenser E104, finished pot V107, described head tank V105 top inlet porting, bottom arranges liquid-phase outlet, sediment outlet is set below liquid-phase outlet, the entrance of head tank V105 is by discharging pump P112 or P113, filter V128 and Raw material pail are tightly connected, sediment outlet is connected with sediment storage tank seal by sludge pump, the liquid-phase outlet of head tank V105 is connected with the inlet seal of feed pump, the equal top of described distillation still R101 and distillation still R102 arranges material inlet and gaseous phase outlet, bottom arranges residue outlet, the equal top of distillation still R101 and distillation still R102 arranges temperature raising medium entrance and cooling medium outlet, bottom arranges temperature raising medium outlet and cooling medium entrance, distillation still R101 is connected with the exit seal of feed pump respectively with the material inlet of distillation still R102, residue outlet and residual pump P116 or P117 of still are tightly connected, distillation still R101 is connected with heat-conducting oil system or vapour system exit seal by sub-cylinder SD111 with the temperature raising medium entrance of distillation still R102, temperature raising medium outlet is connected with heat-conducting oil system or vapour system inlet seal, the cooling medium entrance of distillation still R101 and distillation still R102 and cooling medium outlet are connected with the outlet of recirculating cooling water system and inlet seal respectively, the equal bottom of described rectifying column T108 and T109 arranges gas phase entrance, top arranges gaseous phase outlet, gas phase entrance bottom rectifying column T108 and the gaseous phase outlet of distillation still R101 is tightly connected, the gaseous phase outlet at top and condenser E103 are tightly connected, the gas phase entrance bottom rectifying column T109 and the gaseous phase outlet of distillation still R102 is tightly connected, the gaseous phase outlet at top and condenser E104 are tightly connected, the described equal top of condenser E103 and E104 arranges gas phase entrance, bottom arranges liquid-phase outlet, the equal top of condenser E103 and E104 arranges circulating water outlet, bottom arranges recirculated water entrance, the gaseous phase outlet of condenser E103 gas phase entrance and rectifying column T108 is tightly connected, liquid-phase outlet is connected with separator FT110 inlet seal, the gaseous phase outlet of condenser E104 gas phase entrance and rectifying column T109 is tightly connected, liquid-phase outlet is connected with separator FT110 inlet seal, the circulating water outlet of condenser E103 with E104 is communicated with circulating water pool V129, recirculated water entrance is communicated with upper water with circulating water pool V129 by water circulating pump P123 or P124, it is described that finished pot V107 top arranges finished-product entrance, bottom arranges product outlet, the finished-product entrance of finished pot V107 is connected with the exit seal of separator FT110 and is tightly connected respectively by separator FT110 and condenser E103 and E104, and the product outlet of finished pot V107 is tightly connected by discharge pump P118 or 119 and packaging system.
The organic solvent waste liquid disposal method of the present embodiment comprises the following steps:
1) after the raw material of barreled being put assigned address, open bung and raw material is divided into four kinds: a expects clearly, b batch mixing, c paint and paint slag, d impurity; Described raw material is in automobile production, the spent organic solvent cleaning fluid that painting process cleaning paint spraying outfit produces, and composition comprises toluene, mixed xylenes, butanols, isobutanol, butyl acetate;
2) the barreled raw material of step 1) classification filters out after larger granule foreign through filter V128 and inputs corresponding head tank V105 in by it according to classification with discharging pump P112 or P113, raw material is the static separation of memory period in head tank V105, solvent floats on top layer, contamination precipitation forms sediment to bottom, and moisture is between solvent and sediment; Described solvent is the mixing material comprising toluene, mixed xylenes, butanols, isobutanol, butyl acetate;
3) by step 2) liquid material that is separated is by feed pump input distillation still R101 or R102, liquid material charge weight reaches 3/4 of distillation still volume and closes feed pump, step 2) the sediment sludge pump that is separated extracts out, delivers in sediment storage tank; Described liquid material is for comprising step 2) mixing material of described solvent and portion of water;
4) in the distillation still R101 or R102 of infusion fluid material, normal temperature conduction oil is passed into, after distillation still R101 or R102 and conduction oil transmission system normally run 5 minutes, pass into the conduction oil slowly heated up again to heat, it is 15 minutes that the temperature of the conduction oil of slow intensification is warming up to 230 DEG C of used times by 35 DEG C, the temperature 35 DEG C of described normal temperature conduction oil, pressure 0.2MPa, the conduction oil pressure of described slow heating is 0.2MPa;
5) conduction oil that step 4) is used is after by distillation still R101 or R102, the liquid material temperature be heated to wherein reaches boiling point, continue to distillation still R101 or R102 liquid make-up material, all the time full state is in make alembic, the head temperature simultaneously controlling distillation still R101 or R102 is 106-155 DEG C, and the pressure of distillation still R101 or R102 is 0.25-0.35MPa; The liquid material that supplements be step 2) liquid material that is separated;
6) in the gaseous phase materials of step 5) distillation to be entered into connection rectifying column T108 or T109 by the top of distillation still R101 or R102, rectifying is carried out, temperature in rectifying column T108 or T109 is 135 DEG C, pressure is 0.01MPa, and the gaseous phase materials temperature after rectifying is 83 DEG C, pressure is 0.01MPa;
7) temperature obtained through step 6) is that the gaseous phase materials of 83 DEG C enters in condenser E103 or E104, simultaneously, temperature is that the recirculated cooling water of 25 DEG C enters in condenser E103 or E104, the gaseous phase materials in condenser E103 or E104 is cooled to the liquid phase material of temperature 35 DEG C;
8) temperature obtained through step 7) is that after the liquid phase material of 35 DEG C enters and isolates moisture in separator FT110, finished product materials enters in finished pot V107, and enters finished product packing system by discharge pump P118 or P119, in moisture drain separator FT110;
9) according to analysis result, the sample analysis when temperature at the bottom of still 155 DEG C, determines whether the operation of this still completes production; In cauldron bottom residue, organic solvent content is lower than 1000ppm;
10) can stop carrying conduction oil when after this still has operated production, the pressure in distillation still declines gradually, residue presents thick shape in distillation still, simultaneously to distillation still conveying cooling water, described cooling water temperature 25 DEG C, pressure 0.4MPa, flow 100m
3/ h;
11), when the pressure drop in distillation still R101 or R102 is to 0.01MPa, conveying cooling water is stopped;
12) defective material is discharged when temperature in distillation still R101 or R102 reaches 70 DEG C by the residual pump of still.
Claims (2)
1. an organic solvent waste liquid disposal device, it is characterized in that: it comprises head tank, distillation still, rectifying column, condenser and finished pot, described head tank top inlet porting, bottom arrange liquid-phase outlet, sediment outlet is set below liquid-phase outlet, the entrance of head tank is tightly connected with Raw material pail with filter by discharging pump, sediment outlet is connected with sediment storage tank seal by sludge pump, and the liquid-phase outlet of head tank is connected with the inlet seal of feed pump, described distillation still top arranges material inlet and gaseous phase outlet, bottom arranges residue outlet, the top of distillation still arranges temperature raising medium entrance and cooling medium outlet, bottom arranges temperature raising medium outlet and cooling medium entrance, the material inlet of distillation still is connected with the exit seal of feed pump, residue outlet is connected with the residual pump seal of still, the temperature raising medium entrance of distillation still is connected with heat-conducting oil system or vapour system exit seal by sub-cylinder, temperature raising medium outlet is connected with heat-conducting oil system or vapour system inlet seal, the cooling medium entrance of distillation still and cooling medium outlet are connected with the outlet of recirculating cooling water system and inlet seal respectively, described rectifier bottoms arranges gas phase entrance, top arranges gaseous phase outlet, the gas phase entrance of rectifier bottoms and the gaseous phase outlet of distillation still is tightly connected, the gaseous phase outlet at top and condenser are tightly connected, described condenser top arranges gas phase entrance, bottom arranges liquid-phase outlet, the top of condenser arranges circulating water outlet, bottom arranges recirculated water entrance, the gaseous phase outlet of condenser gas phase entrance and rectifying column is tightly connected, liquid-phase outlet and separator inlet are tightly connected, and the circulating water outlet of condenser is communicated with circulating water pool, recirculated water entrance is communicated with upper water with circulating water pool by water circulating pump, it is described that finished pot top arranges finished-product entrance, bottom arranges product outlet, the finished-product entrance of finished pot is connected with the exit seal of separator and is tightly connected by separator and condenser, and the product outlet of finished pot is tightly connected by discharge pump and packaging system.
2. a processing method for organic solvent cleaning waste liquid, is characterized in that: comprise the following steps:
1) after the raw material of barreled being put assigned address, open bung device of drawing a design and raw material is divided into four kinds: a expects clearly, b batch mixing, c paint and paint slag, d impurity; Described raw material is in automobile production, the spent organic solvent cleaning fluid that painting process cleaning paint spraying outfit produces, and composition comprises toluene, mixed xylenes, butanols, isobutanol, butyl acetate;
2) the barreled raw material of step 1) classification falls after larger granule foreign to use discharging pump by its storage tank corresponding according to classification input through metre filter, the static separation of raw material memory period in storage tank, solvent floats on top layer, contamination precipitation forms sediment to bottom, and moisture is between solvent and sediment; Described solvent is the mixing material comprising toluene, mixed xylenes, butanols, isobutanol, butyl acetate;
3) by step 2) liquid material that is separated is by feed pump input distillation still, liquid material charge weight reaches 3/4 of distillation still volume and closes feed pump, step 2) the sediment sludge pump that is separated extracts out, delivers in sediment storage tank; Described liquid material is for comprising step 2) mixing material of described solvent and portion of water;
4) distillation still to infusion fluid material passes into normal temperature conduction oil, after distillation still and conduction oil transmission system normally run 5 minutes, pass into the conduction oil slowly heated up again to heat, it is 15 minutes that the temperature of the conduction oil of slow intensification is warming up to 230 DEG C of used times by 35 DEG C, the temperature 35 DEG C of described normal temperature conduction oil, pressure 0.2MPa, the conduction oil pressure of described slow heating is 0.2MPa;
5) after the conduction oil that step 4) is used liquid material temperature distillation still be heated to wherein reaches boiling point, continue to distillation still liquid make-up material, all the time full state is in make alembic, the temperature simultaneously controlling distillation still top is 106-155 DEG C, and the pressure of distillation still is 0.25-0.35MPa; The liquid material that supplements be step 2) liquid material that is separated;
6) in the gaseous phase materials of step 5) distillation to be entered into connection rectifying column by distillation still top, carry out rectifying, the temperature in rectifying column is 135 DEG C, pressure is 0.01MPa, and the gaseous phase materials temperature after rectifying is 83 DEG C, pressure is 0.01MPa;
7) temperature obtained through step 6) is that the gaseous phase materials of 83 DEG C enters in condenser, and meanwhile, temperature is that the recirculated cooling water of 25 DEG C enters in condenser, the gaseous phase materials in condenser is cooled to the liquid phase material of temperature 35 DEG C;
8) temperature obtained through step 7) is that after the liquid phase material of 35 DEG C enters and isolates moisture in separator, finished product materials enters in finished pot, and enters finished product packing system by discharge pump, moisture drain separator;
9) get cauldron bottom residue sample analysis when temperature at the bottom of still 155 DEG C, in cauldron bottom residue, organic solvent content has operated production lower than 1000ppm i.e. this still;
10) can stop carrying conduction oil when after this still has operated production, the pressure in distillation still declines gradually, residue presents thick shape in distillation still, simultaneously to distillation still conveying cooling water, described cooling water temperature 25 DEG C, pressure 0.4MPa, flow 100m
3/ h;
11), when the pressure drop in distillation still is to 0.01MPa, conveying cooling water is stopped;
12) defective material is discharged when distilling temperature in the kettle and reaching 70 DEG C by the residual pump of still.
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| CN201510603906.7A CN105233515B (en) | 2015-09-22 | 2015-09-22 | A kind of organic solvent waste liquid disposal device and its processing method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106623215A (en) * | 2016-11-22 | 2017-05-10 | 广东新球清洗科技股份有限公司 | Energy-saving recycling method of hydrocarbon cleaning agent and hydrocarbon cleaning equipment |
| CN113045047A (en) * | 2021-03-29 | 2021-06-29 | 江西清绿环保有限公司 | Paint spraying wastewater purification and circulation system |
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| CN105233515B (en) | 2017-06-30 |
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