CN215828658U - Thermal method PVDF milipore filter aftertreatment high salt waste liquid resource utilization device - Google Patents
Thermal method PVDF milipore filter aftertreatment high salt waste liquid resource utilization device Download PDFInfo
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Abstract
The utility model relates to a resource utilization device for post-treatment of high-salt waste liquid by a thermal PVDF ultrafiltration membrane, which is characterized in that the high-salt waste liquid after post-treatment of the thermal PVDF ultrafiltration membrane contains a large amount of ethanol, grease and calcium chloride, and the ethanol is recovered by an ethanol rectification system and returned to an ultrafiltration production process; then, recovering the grease by using an oil-water separation system; finally, evaporating flaky calcium chloride dihydrate by using an evaporation crystallization system, wherein the calcium chloride dihydrate can be sold as a snow-melting agent, and distilled water is recycled in a circulating water system; the purpose of resource utilization of the high-salt waste liquid after the hot-method PVDF ultrafiltration membrane is achieved.
Description
Technical Field
The utility model relates to a resource utilization device for post-treatment of high-salinity waste liquid by a thermal PVDF ultrafiltration membrane, belonging to the technical field of industrial wastewater treatment.
Background
The hot PVDF (polyvinylidene fluoride) ultrafiltration membrane has the characteristics of high strength, high toughness, corrosion resistance, long service life and the like, and is widely applied to various projects of industrial water treatment and wastewater treatment and recycling. The production of the hot PVDF ultrafiltration membrane mostly adopts PVDF resin, inorganic materials and organic acid ester to carry out mixing granulation, hollow fiber ultrafiltration fiber is prepared by high-temperature and high-pressure extrusion, stretching and annealing, then organic acid ester is removed by extraction, and inorganic materials are removed by reaction. The utility model provides a preparation method of a beta-crystal form polyvinylidene fluoride hollow fiber membrane by an improved TIPS (thermally induced phase separation) method, and the preparation method comprises the steps of mixing and granulating 40-60 wt% of PVDF resin, 20-40 wt% of calcium carbonate and 10-20 wt% of phthalate or benzoate respectively; then the hollow fiber ultrafiltration membrane filaments are prepared by the membrane preparation procedures of high-temperature and high-pressure extrusion, stretching, annealing and the like; and finally, carrying out post-treatment, extracting phthalic acid ester or benzoate by using ethanol, reacting calcium carbonate by using hydrochloric acid, and washing to produce a thermal PVDF ultrafiltration membrane product. In the post-treatment process of the hot PVDF ultrafiltration membrane, part of high-concentration high-salt waste liquid rich in ethanol, grease and calcium chloride is generated through continuous circulating concentration, although the amount of the waste liquid is small, the concentration is high, the chloride ions are high, and the waste liquid cannot be collected into a production wastewater treatment system for treatment. Currently, only partial waste water treatment patents for hollow fiber membrane wet process using dimethylacetamide as solvent, such as 201710957710.7 a recovery system of dimethylacetamide in ultrafiltration membrane production waste water, utilize a refining tower to recover DMAC (dimethylacetamide) and condensed water. The high-salt waste liquid generated by the post-treatment of the thermal PVDF ultrafiltration membrane is required to be separately collected and treated, a novel device is required to be designed and developed, ethanol, grease, calcium chloride and distilled water in the high-salt waste liquid are effectively recovered, and the purpose of resource utilization of the high-salt waste liquid after the post-treatment of the thermal PVDF ultrafiltration membrane is realized.
Disclosure of Invention
The utility model provides a resource utilization device for post-treatment of high-salt waste liquid by a hot-method PVDF ultrafiltration membrane, aiming at the characteristic that the post-treatment of the high-salt waste liquid by the hot-method PVDF ultrafiltration membrane contains a large amount of ethanol, grease and calcium chloride, and the typical weight percentage of the components of the high-salt waste liquid is as follows: 65-80% of ethanol, 3-5% of lipid and CaCl23-8% of (calcium chloride), 0.2-1% of HCl (hydrochloric acid), and H210-28% of O (water) and is acidic. Firstly, neutralizing by using an ethanol rectification system, adjusting the pH to 6.5-8.5 by adding calcium hydroxide, and recovering ethanol by using ethanol rectification, wherein the ethanol content is more than or equal to 90 percent, and the water content is less than or equal to 10 percent, so that the recycling requirement of the hot PVDF ultrafiltration membrane production process is met; the weight percentage of the effluent components of the ethanol rectification system becomes: 2.9-4.8% of lipid and CaCl2 3.6～9.2%、H2And O86-93.5%. The oil-water separation system is used for recovering oil from the effluent of the ethanol rectification system, the oil content is more than or equal to 90 percent, the water content is less than or equal to 10 percent, and the oil-water separation system can be used for an oil-fired boiler; the salt content of the brine of the oil-water separation system becomes: CaCl23.7～9.7%、H290.3 to 96.3 percent of O. Finally evaporating and crystallizing CaCl from the brine of the oil-water separation system by using an evaporative crystallization system2Flake calcium chloride dihydrate with the content of more than or equal to 74 percent is sold for a snow-melting agent, and condensed water is recovered.
The technical solution of the utility model is as follows: the resource utilization device for the high-salt waste liquid after the thermal PVDF ultrafiltration membrane post-treatment structurally comprises an ethanol rectification system, an oil-water separation system and an evaporative crystallization system; wherein the high-salt waste liquid after the thermal PVDF ultrafiltration membrane is connected to a liquid inlet of an ethanol rectification system, the 1# steam is connected to a steam inlet of the ethanol rectification system, the 1# cooling water is connected to a cooling water inlet and a cooling water outlet of the ethanol rectification system, and the ethanol is sent out from an ethanol outlet of the ethanol rectification system; a liquid outlet of the ethanol rectification system is connected to a liquid inlet of the oil-water separation system, the 2# cooling water is connected to a cooling water inlet and a cooling water outlet of the oil-water separation system, and oil is sent out from an oil outlet of the oil-water separation system; the water outlet of the oil-water separation system is connected to the water inlet of the evaporative crystallization system, the No. 2 steam is connected to the steam inlet of the evaporative crystallization system, the No. 3 and No. 4 cooling water are connected to the cooling water inlet and outlet of the evaporative crystallization system, the condensed water outlet of the evaporative crystallization system sends out distilled water, and the salt outlet of the evaporative crystallization system sends out flaky calcium chloride dihydrate.
The resource utilization device for the high-salt waste liquid after the hot-process PVDF ultrafiltration membrane is characterized in that firstly, an ethanol rectification system is utilized to recover ethanol from the high-salt waste liquid after the hot-process PVDF ultrafiltration membrane, the ethanol content is more than or equal to 90%, and the ethanol is reused for the production of the hot-process PVDF ultrafiltration membrane; recycling the grease by using an oil-water separation system, wherein the water content of the grease is less than or equal to 10 percent and the grease is used for an oil-fired boiler; finally, the evaporation crystallization system is utilized to produce flaky calcium chloride dihydrate, the content of the calcium chloride is more than or equal to 74 percent, the quality requirement of class II products of GB/T26520-2011 industrial calcium chloride is met, the flaky calcium chloride dihydrate is sold as a snow-melting agent, and condensed water is recovered and reused for circulating water; the purpose of resource utilization of the high-salt waste liquid after the hot-method PVDF ultrafiltration membrane post-treatment is realized.
The device for recycling the high-salt waste liquid after the hot-process PVDF ultrafiltration membrane is characterized in that an ethanol rectification system is used for recovering ethanol and returning to an ultrafiltration production process; then, recovering the grease by using an oil-water separation system; finally, evaporating flaky calcium chloride dihydrate by using an evaporation crystallization system, wherein the calcium chloride dihydrate can be sold as a snow-melting agent, and distilled water is recycled in a circulating water system; the purpose of resource utilization of the high-salt waste liquid after the hot-method PVDF ultrafiltration membrane is achieved.
Drawings
FIG. 1 is a schematic structural diagram of a resource utilization device for post-treatment of high-salt waste liquid by a thermal PVDF ultrafiltration membrane.
In the drawing, WL represents high-Salt waste liquid, EL represents ethanol, OG represents oil and fat, Salt represents flaky calcium chloride dihydrate, DW represents distilled water, CW represents1Denotes No. 1 Cooling Water, CW2Denotes No. 2 Cooling Water, CW3/4Denotes No. 3 and No. 4 Cooling Water, SM1Denotes 1# steam, SM2Represents steam # 2; EDS represents an ethanol rectification system, OWSS represents an oil-water separation system, and VCS represents an evaporative crystallization system.
FIG. 2 is a schematic structural diagram of an ethanol rectification system of a hot-process PVDF ultrafiltration membrane post-treatment high-salt waste liquid resource utilization device.
EDS in the figure represents ethanol extractDistillation system, WL stands for high salt waste liquid, EDSoutRepresents the effluent of the ethanol rectification system, SM1Denotes No. 1 steam, CW1Denotes 1# cooling water, EL denotes ethanol; BT denotes feed tank, P11Denotes a feed pump, NRT denotes a neutralization tank, D11Calcium hydroxide adding device, NLT (NLT) neutralizing liquid tank and P12Denotes a rectification pump, EDT denotes an ethanol rectification column, CE1Denotes an ethanol condensation heat exchanger, ET denotes an ethanol tank, P13An ethanol recovery pump is shown.
FIG. 3 is a schematic structural diagram of an oil-water separation system of a hot-process PVDF ultrafiltration membrane post-treatment high-salt waste liquid resource utilization device.
In the drawing, OWSS represents an oil-water separation system, EDSoutDenotes the effluent of the ethanol rectification system, CW2Denotes No. 2 Cooling Water, OWSSoutBrine representing an oil-water separation system, OG representing grease; MT denotes an intermediate liquid tank, P21Indicating booster pump, CE2Denotes a waste liquid cooling heat exchanger, OWST denotes an oil-water separation tank, SWT denotes a brine tank, P denotes a brine tank22Denotes a saline transfer pump, OGT denotes a grease tank, P23A grease recovery pump is shown.
FIG. 4 is a schematic structural diagram of an evaporative crystallization system of a hot-process PVDF ultrafiltration membrane post-treatment high-salt waste liquid resource utilization device.
In the drawing, VCS denotes an evaporative crystallization system, OWSSoutRepresenting the effluent of the oil-water separation system, DW representing distilled water, Salt representing flaky calcium chloride dihydrate, CW3Denotes No. 3 Cooling Water, CW4Denotes No. 4 Cooling Water, SM2Represents steam # 2; VHE denotes evaporative heat exchanger, P32Showing a forced circulation pump, VE an evaporator, CE3Denotes a vapor condensing heat exchanger, DWT denotes a condensate tank, P33Indicating condensate-conveying pumps, P32The liquid calcium chloride delivery pump is shown, TT the heat preservation tank is shown, and RTM the drum-type tablet making machine is shown.
FIG. 5 is a process flow diagram of a resource utilization embodiment of hot PVDF ultrafiltration membrane post-treatment high-salt waste liquid.
Detailed Description
Referring to FIG. 1, the thermal methodThe PVDF ultrafiltration membrane post-treatment high-salinity waste liquid resource utilization device structurally comprises an ethanol rectification system EDS, an oil-water separation system OWSS and an evaporative crystallization system VCS; wherein the hot PVDF ultrafiltration membrane post-treatment high-salt waste liquid WL is connected to a liquid inlet of an EDS (ethanol distillation system), 1# steam SM1Connected to the steam inlet of the EDS of the ethanol rectification system, and cooling water CW 1#1Connecting the cooling water inlet and outlet of the ethanol rectification system EDS, and sending the ethanol EL out of an ethanol outlet of the ethanol rectification system EDS; the liquid outlet of the EDS of the ethanol rectification system is connected to the liquid inlet of the OWSS, and 2# cooling water CW2The oil outlet is connected to a cooling water inlet and a cooling water outlet of the oil-water separation system OWSS, and oil OG is sent out from an oil outlet of the oil-water separation system OWSS; the water outlet of the oil-water separation system OWSS is connected to the water inlet of the evaporative crystallization system VCS, 2# steam SM2Steam inlet connected to VCS of evaporative crystallization system, cooling water CW of 3# and 4#3/4The cooling water inlet and outlet are connected to a cooling water outlet of the evaporative crystallization system VCS, a condensed water outlet of the evaporative crystallization system VCS sends out distilled water DW, and a Salt outlet of the evaporative crystallization system VCS sends out flaky calcium chloride dihydrate Salt; the resource utilization device for the high-salt waste liquid after the hot-process PVDF ultrafiltration membrane is characterized in that firstly, an ethanol rectification system is utilized to recover ethanol from the high-salt waste liquid after the hot-process PVDF ultrafiltration membrane, the ethanol content is more than or equal to 90%, and the ethanol is reused for the production of the hot-process PVDF ultrafiltration membrane; recycling the grease by using an oil-water separation system, wherein the water content of the grease is less than or equal to 10 percent and the grease is used for an oil-fired boiler; finally, the evaporation crystallization system is utilized to produce flaky calcium chloride dihydrate, the content of the calcium chloride is more than or equal to 74 percent, the quality requirement of class II products of GB/T26520-2011 industrial calcium chloride is met, the flaky calcium chloride dihydrate is sold as a snow-melting agent, and condensed water is recovered and reused for circulating water; the purpose of resource utilization of the high-salt waste liquid after the hot-method PVDF ultrafiltration membrane post-treatment is realized.
Referring to FIG. 2, the EDS of the ethanol rectification system comprises a feed tank BT and a feed pump P11NRT and calcium hydroxide adding device D of neutralization reaction tank11Neutralization liquid tank NLT and rectification pump P12EDT of ethanol rectifying tower and CE of ethanol condensing heat exchanger1Ethanol tank ET and ethanol recovery pump P13(ii) a Wherein the high-salt waste liquid WL is connected to the liquid inlet of the liquid inlet tank BT, and the liquid outlet of the liquid inlet tank BT passes through the liquid supply pump P11With feed of NRT in neutralization reactorMouth-connected calcium hydroxide adding device D11The medicine outlet of the neutralization reaction tank NRT is connected to the medicine inlet of the neutralization reaction tank NRT, and the liquid outlet of the neutralization reaction tank NRT is connected to the liquid inlet of the neutralization liquid tank NLT; the liquid outlet of the neutralization liquid tank NLT passes through a rectification pump P12Connected with the liquid inlet of an ethanol rectifying tower EDT and 1# steam SM1Connected to the steam inlet of the ethanol rectification tower EDT, and the liquid outlet of the ethanol rectification tower EDT is sent out of the liquid outlet EDS of the ethanol rectification systemoutThe ethanol rectification outlet of the ethanol rectification tower EDT is connected to the ethanol condensation heat exchanger CE1Inlet of No. 1 Cooling Water CW1Is connected to an ethanol condensation heat exchanger CE1Cooling water inlet and outlet, and an ethanol condensation heat exchanger CE1The outlet of the ethanol tank is connected to the inlet of an ethanol tank ET, and the outlet of the ethanol tank ET passes through an ethanol recovery pump P13And sending out the ethanol EL. Neutralizing hydrochloric acid in the high-salt waste liquid by an ethanol rectification system, specifically adding calcium hydroxide, and adjusting the pH to 6.5-8.5; then, introducing steam and carrying out low-temperature rectification on the ethanol by using an ethanol rectification tower, wherein the temperature at the top of the tower is less than or equal to 80 ℃, and grease is not ensured to be evaporated; and finally, condensing and recovering the ethanol by using an ethanol condensation heat exchanger, wherein the content of the ethanol is more than or equal to 90 percent, and the ethanol is reused for the production of the PVDF ultrafiltration membrane by the thermal method.
Referring to FIG. 3, the oil-water separation system OWSS comprises a middle liquid tank MT and a booster pump P21Waste liquid cooling heat exchanger CE2An oil-water separation tank OWST, a brine tank SWT and a brine transfer pump P22Oil tank OGT and oil recovery pump P23(ii) a Wherein the ethanol rectification system goes out of the EDSoutConnected to the liquid inlet of the intermediate liquid tank MT, and the liquid outlet of the intermediate liquid tank MT passes through a booster pump P21CE heat exchanger for cooling waste liquid2The liquid inlet of the cooling water pump is connected with 2# cooling water CW2Is connected to a waste liquid cooling heat exchanger CE2Cooling water inlet and outlet, waste liquid cooling heat exchanger CE2The liquid outlet of the oil-water separation tank OWST is connected to the liquid inlet of the oil-water separation tank OWST, the oil outlet of the oil-water separation tank OWST is connected to the oil inlet of the grease tank OGT, and the oil outlet of the grease tank OGT passes through the grease recovery pump P23Sending out grease OG; the brine outlet of the oil-water separation tank OWST is connected to the brine inlet of the brine tank SWT, and the brine outlet of the brine tank SWT is connected with the brine delivery pump P through the brine delivery pump22Oil and water deliveryBrine OWSS of separation systemout. Cooling the effluent of an ethanol rectification system by an oil-water separation system, specifically by using a waste liquid cooling heat exchanger; then an oil-water separation tank is used for oil-water separation, the water content of the recovered grease is less than or equal to 10 percent, and the oil-water separation tank is used for an oil-fired boiler.
Referring to FIG. 4, the evaporative crystallization system VCS comprises an evaporative heat exchanger VHE and a forced circulation pump P32VE evaporator, CE steam condensing heat exchanger3DWT (dry weight transfer) of condensate tank and condensate delivery pump P33Liquid calcium chloride delivery pump P32A heat preservation tank TT and a drum-type pelleter RTM; water outlet OWSS of oil-water separation systemoutWater inlet to the vaporizing heat exchanger VHE, 2# steam SM2Connected to the steam inlet of the evaporating heat exchanger VHE, the steam outlet of the evaporating heat exchanger VHE is connected to the steam condensing heat exchanger CE3The water outlet of the evaporation heat exchanger VHE is connected to the water inlet of the evaporator VE; the vapor outlet of the evaporator VE is also connected to a vapor condensing heat exchanger CE3Inlet port of (3) # cooling water CW3To the steam condensing heat exchanger CE3Cooling water inlet and outlet, steam condensing heat exchanger CE3The water outlet of the condensed water pot DWT is connected to the water inlet of the condensed water pot DWT, and the water outlet of the condensed water pot DWT passes through a condensed water delivery pump P33Sending out distilled water DW; the outlet of the evaporator VE is passed through a forced circulation pump P32The water inlet of the evaporation heat exchanger VHE and the outlet of the evaporator VE are also connected with a liquid calcium chloride delivery pump P32Connected with the liquid calcium chloride inlet of the heat-preservation tank TT, the liquid calcium chloride outlet of the heat-preservation tank TT is connected with the liquid calcium chloride inlet of the drum-type tablet making machine RTM, and 4# cooling water CW4Connected to a cooling water inlet and a cooling water outlet of the cylinder pelleter RTM, and a Salt outlet of the cylinder pelleter RTM sends out the flaky calcium chloride dihydrate Salt; evaporating and concentrating the brine from the oil-water separation system by an evaporation and crystallization system, specifically by using forced circulation evaporation; storing 70-74% of liquid calcium chloride evaporated by an evaporator into a heat-preserving tank, preserving heat by using waste steam, then flowing into a drum-type sheet making machine, spraying cooling water on the surface of the inner wall of a drum to solidify the liquid calcium chloride on the outer surface of the drum into solid calcium chloride with the thickness of 1-2 mm, and scraping off the solid calcium chloride by a scraperThe flaky calcium chloride dihydrate is produced, the content of the calcium chloride is more than or equal to 74 percent, the quality requirement of class II products of GB/T26520-2011 industrial calcium chloride is met, the flaky calcium chloride dihydrate is sold as a snow-melting agent, and condensed water is recovered and reused for circulating water; the purpose of resource utilization of the high-salt waste liquid after the hot-method PVDF ultrafiltration membrane post-treatment is realized.
The resource utilization method for post-treatment of the high-salt waste liquid by the thermal PVDF ultrafiltration membrane comprises the following steps:
1) recovering ethanol from the high-salt waste liquid after the hot PVDF ultrafiltration membrane post-treatment by an ethanol rectification system, wherein the ethanol content is more than or equal to 90 percent;
2) recovering oil from the effluent of the ethanol rectification system through an oil-water separation system, wherein the water content of the oil is less than or equal to 10%;
3) through the evaporative crystallization system, the saline water of the oil-water separation system is used for producing flaky calcium chloride dihydrate, and the content of calcium chloride is more than or equal to 74%.
Neutralizing hydrochloric acid in the high-salt waste liquid by an ethanol rectification system, specifically adding calcium hydroxide, and adjusting the pH to 6.5-8.5; then, introducing steam and carrying out low-temperature rectification on the ethanol by using an ethanol rectification tower, wherein the temperature at the top of the tower is less than or equal to 80 ℃, and grease is not ensured to be evaporated; and finally, condensing and recovering the ethanol by using an ethanol condensation heat exchanger, wherein the ethanol content is more than or equal to 90 percent, and reusing the ethanol for the production of the PVDF ultrafiltration membrane by a thermal method.
The step 2) is to cool the effluent of the ethanol rectification system through an oil-water separation system, specifically, a waste liquid cooling heat exchanger is firstly utilized; then an oil-water separation tank is used for oil-water separation, the water content of the recovered grease is less than or equal to 10 percent, and the oil-water separation tank is used for an oil-fired boiler.
In the step 3), salt water from an oil-water separation system is evaporated and concentrated through an evaporation crystallization system, specifically, forced circulation evaporation is firstly utilized; storing liquid calcium chloride containing 70-74% of calcium chloride evaporated by an evaporator into a heat-preserving tank, preserving heat by using waste steam, then flowing into a drum-type sheet making machine, spraying cooling water on the surface of the inner wall of a drum to solidify the liquid calcium chloride on the outer surface of the drum into solid calcium chloride with the thickness of 1-2 mm, scraping by using a scraper to produce flaky calcium chloride dihydrate, wherein the content of the calcium chloride is not less than 74%, the quality requirement of II-type products of GB/T26520-2011 industrial calcium chloride is met, the flaky calcium chloride is sold as a snow-melting agent, and condensed water is recovered and reused for circulating water; the purpose of resource utilization of the high-salt waste liquid after the hot-method PVDF ultrafiltration membrane post-treatment is realized.
Examples
A certain membrane technology enterprise produces a thermal method PVDF ultrafiltration membrane of 200 ten thousand square meters every year, and a small amount of acidic high-salt waste liquid containing ethanol, calcium chloride and grease is generated in the post-treatment process of the thermal method PVDF ultrafiltration membrane. Although the amount is small, the concentration is high, the pollution is serious, the material and the water quality of a production wastewater treatment system are greatly influenced, and the production wastewater cannot be collected into the production wastewater treatment system for treatment. The embodiment designs a set of resource utilization system for post-treatment of the high-salt waste liquid by the thermal PVDF ultrafiltration membrane, which is specially designed for the characteristics of the high-salt waste liquid, and effectively recovers ethanol, calcium chloride, grease and distilled water in the high-salt waste liquid.
Designing the composition and liquid amount of high-salt waste liquid
The hot method PVDF ultrafiltration membrane post-treatment high-salt waste liquid comprises the following components in percentage by weight:
| composition (I) | Ethanol | Lipids | CaCl2 | HCl | H2O |
| By weight% | 74.2 | 3.9 | 6.8 | 0.6 | 14.5 |
The liquid volume of the high-salt waste liquid after the thermal PVDF ultrafiltration membrane is 12T/D.
Process flow
2.1 Process flow
The process flow is shown in the attached figure 5, and the process flow chart of the resource utilization embodiment of the hot PVDF ultrafiltration membrane post-treatment high-salt waste liquid is shown in the figure.
2.2 flow sheet description
After the hot PVDF ultrafiltration membrane is subjected to post-treatment, the high-salt waste liquid enters a liquid inlet tank, is pumped into a neutralization reaction tank through a liquid supply pump, is adjusted to have a pH value of 7.5 by adding calcium hydroxide, is neutralized, enters the neutralization tank, is sent into an ethanol rectification tower through a rectification pump, is rectified at a low temperature by using No. 1 steam, has a tower top temperature of less than 80 ℃, is sent out to enter an ethanol condensation heat exchanger, condenses ethanol to a temperature of less than or equal to 25 ℃ through No. 1 cooling water, enters an ethanol tank, is sent out through an ethanol recovery pump, and is reused for an extraction process of the hot PVDF ultrafiltration membrane; sending the liquid discharged from the ethanol rectification system to an intermediate liquid tank at the tower bottom, pumping the liquid into a waste liquid cooling heat exchanger through a booster pump, cooling the waste liquid to be less than or equal to 30 ℃ by using 2# cooling water, then feeding the waste liquid into an oil-water separator, feeding the separated oil into an oil tank for storage, and sending the oil out through an oil recovery pump; the separated brine enters a brine tank, is pumped into an evaporation heat exchanger through a delivery pump, enters an evaporator after being heated through No. 2 steam, is forcibly circulated and evaporated by a forced circulation pump, waste steam between the top of the evaporator and the evaporation heat exchanger enters a steam condensation heat exchanger, is condensed by No. 3 cooling water, and condensed water is stored in a condensed water tank and is sent out through the delivery pump to be reused for circulating water; when the concentration of calcium chloride is evaporated and concentrated to 70-74%, the calcium chloride is conveyed into a heat-preserving tank by a calcium chloride conveying pump, heat preservation is carried out by waste steam before condensation, and then the waste steam flows into a drum-type tabletting machine to be prepared into a flaky calcium chloride dihydrate product under the cooling of No. 4 cooling water.
Effect of each unit processing
The treatment effect of each unit of the hot PVDF ultrafiltration membrane post-treatment high-salt waste liquid resource utilization system is as follows:
in the table, the water quality balance calculates that the steam consumption of the ethanol rectification system is 8.9T/D, and the added water is 0.657T/D and the added calcium hydroxide is 0.073T/D; the evaporative crystallization system consumes 7.3T/D of steam.
System major design parameters
4.1 civil engineering:
| serial number | Name (R) | Specification of | Unit of | Number of | |
|
| 1 | Evaporative crystallization workshop | 24.0 | Seat | 1 | Brick concrete |
4.2 Main equipment:
| serial number | Name (R) | Type and specification | Number of | Unit of |
| 1 | Ethanol rectification system | |||
| 1.1 | Liquid inlet tank | V=20m3Material of |
1 | Table (Ref. Table) |
| 1.2 | Liquid supply pump | Q=1.5m3H =20m, N =0.25KW, material fluoroplastic 1 is prepared from 1 | 2 | Table (Ref. Table) |
| 1.3 | Neutralization reactionPot for storing food | V=5m3Material of |
1 | Table (Ref. Table) |
| 1.4 | Calcium hydroxide adding device | Dosing chest V =2000m3PE material; a matched metering pump: q =250L/h, P =0.7MPa, N =0.55KW, material PE, 2 stands, 1 stands for 1 | 1 | Sleeve |
| 1.5 | Neutralizing liquid tank | V=5m3Material of |
1 | Table (Ref. Table) |
| 1.6 | Rectification pump | Q=1.5m3H =20m, N =0.25KW, |
2 | Table (Ref. Table) |
| 1.7 | Ethanol rectifying tower | DN =500mm, H =14m, and the material SS 304/ |
1 | Sleeve |
| 1.8 | Ethanol condensation heat exchanger | A=35m2Material SS304 | 1 | Table (Ref. Table) |
| 1.9 | Ethanol pot | V=20m3Material of |
1 | Table (Ref. Table) |
| 1.10 | Ethanol recovery pump | Q=5m3H =20m, N =1.1KW, material SS304, 1 is prepared with 1 | 2 | Table (Ref. Table) |
| 1.11 | Accident tank | V=20m3Material of |
1 | Table (Ref. Table) |
| 2 | Oil-water separation system | |||
| 2.1 | Intermediate liquid tank | V=5m3Material 2205 | 1 | Table (Ref. Table) |
| 2.2 | Booster pump | Q=1.5m3H =15m, N =0.25KW, |
2 | Table (Ref. Table) |
| 2.3 | Waste water cooling heat exchanger | A=40m2Material 2205 | 1 | Table (Ref. Table) |
| 2.4 | Oil-water separator | Q=1.5m3Material 2205,/ |
1 | Table (Ref. Table) |
| 2.5 | Grease tank | V=5m3Material of |
1 | Table (Ref. Table) |
| 2.6 | Grease recovery pump | Q=5m3H =20m, N =1.1KW, |
1 | Table (Ref. Table) |
| 2.7 | Brine tank | V=20m3Material of |
1 | Table (Ref. Table) |
| 2.8 | Delivery pump | Q=1.5m3H =20m, N =0.25KW, |
2 | Table (Ref. Table) |
| 3 | Evaporative crystallization system | |||
| 3.1 | Evaporation heat exchanger | A=40m2Material 2205 | 1 | Table (Ref. Table) |
| 3.2 | Evaporator with a heat exchanger | Q=12m3Titanium material of/ |
1 | Table (Ref. Table) |
| 3.3 | Condensing heat exchanger | A=40m2Material 2205 | 1 | Table (Ref. Table) |
| 3.4 | Condensed water pot | V=20m3Material SS304 | 1 | Table (Ref. Table) |
| 3.5 | Delivery pump | Q=5m3H =20m, N =1.1KW, |
1 | Table (Ref. Table) |
| 3.6 | Forced circulation pump | Q=35m3H =20m, N =4KW, |
2 | Table (Ref. Table) |
| 3.7 | Calcium chloride delivery pump | Q=5m3H =20m, N =1.1KW, |
2 | Table (Ref. Table) |
| 3.8 | Thermal insulation pot | V=20m3Material 2205 | 1 | Table (Ref. Table) |
| 3.9 | Drum-type pelleter | Q =200kg/h, material 2205 | 1 | Table (Ref. Table) |
| 4 | Valve gate | Matched manual and |
1 | Batch of |
| 5 | Instrument and meter | Matched with flow, pressure, liquid level, temperature, pH, density and the like | 1 | Batch of |
| 6 | Electric control system | Matched power cabinet, frequency conversion cabinet, local control box, PLC, industrial personal computer and the like | 1 | Batch of |
Claims (4)
1. The resource utilization device for the high-salt waste liquid after the thermal PVDF ultrafiltration membrane post-treatment is characterized by comprising an ethanol rectification system, an oil-water separation system and an evaporative crystallization system; wherein the high-salt waste liquid after the thermal PVDF ultrafiltration membrane is connected to a liquid inlet of an ethanol rectification system, the 1# steam is connected to a steam inlet of the ethanol rectification system, the 1# cooling water is connected to a cooling water inlet and a cooling water outlet of the ethanol rectification system, and the ethanol is sent out from an ethanol outlet of the ethanol rectification system; a liquid outlet of the ethanol rectification system is connected to a liquid inlet of the oil-water separation system, the 2# cooling water is connected to a cooling water inlet and a cooling water outlet of the oil-water separation system, and oil is sent out from an oil outlet of the oil-water separation system; the water outlet of the oil-water separation system is connected to the water inlet of the evaporative crystallization system, the No. 2 steam is connected to the steam inlet of the evaporative crystallization system, the No. 3 and No. 4 cooling water are connected to the cooling water inlet and outlet of the evaporative crystallization system, the condensed water outlet of the evaporative crystallization system sends out distilled water, and the salt outlet of the evaporative crystallization system sends out flaky calcium chloride dihydrate.
2. The resource utilization device for the post-treatment high-salinity waste liquid of the thermal PVDF ultrafiltration membrane as claimed in claim 1, wherein the ethanol rectification system structurally comprises a liquid inlet tank, a liquid supply pump, a neutralization reaction tank, a calcium hydroxide adding device, a neutralization liquid tank, a rectification pump P, an ethanol rectification tower, an ethanol condensation heat exchanger, an ethanol tank and an ethanol recovery pump; wherein the high-salt waste liquid is connected to a liquid inlet of a liquid inlet tank, a liquid outlet of the liquid inlet tank is connected with a liquid inlet of a neutralization reaction tank through a liquid supply pump, a medicine outlet of a calcium hydroxide adding device is connected to a medicine inlet of the neutralization reaction tank, and a liquid outlet of the neutralization reaction tank is connected to a liquid inlet of the neutralization tank; the liquid outlet of the neutralization liquid tank is connected with the liquid inlet of the ethanol rectifying tower through a rectifying pump, 1# steam is connected to the steam inlet of the ethanol rectifying tower, the liquid outlet of the ethanol rectifying tower is sent out of the liquid outlet of the ethanol rectifying tower, the ethanol rectifying outlet of the ethanol rectifying tower is connected to the inlet of an ethanol condensing heat exchanger, 1# cooling water is connected to the cooling water inlet and outlet of the ethanol condensing heat exchanger, the outlet of the ethanol condensing heat exchanger is connected to the inlet of the ethanol tank, and the outlet of the ethanol tank is pumped out of ethanol through an ethanol recovery pump.
3. The resource utilization device for the post-treatment high-salinity waste liquid of the thermal PVDF ultrafiltration membrane as claimed in claim 1, wherein the oil-water separation system structurally comprises an intermediate liquid tank, a booster pump, a waste liquid cooling heat exchanger, an oil-water separation tank, a brine delivery pump, a grease tank and a grease recovery pump; the liquid outlet of the ethanol rectification system is connected to a liquid inlet of an intermediate liquid tank, a liquid outlet of the intermediate liquid tank is connected with a liquid inlet of a waste liquid cooling heat exchanger through a booster pump, 2# cooling water is connected to a cooling water inlet and a cooling water outlet of the waste liquid cooling heat exchanger, a liquid outlet of the waste liquid cooling heat exchanger is connected to a liquid inlet of an oil-water separation tank, an oil outlet of the oil-water separation tank is connected to an oil inlet of a grease tank, and grease is sent out from the oil outlet of the grease tank through a grease recovery pump; the brine outlet of the brine tank is connected to the brine inlet of the brine tank, and the brine outlet of the brine tank is pumped out of the brine of the oil-water separation system through a brine delivery pump.
4. The resource utilization device for the post-treatment high-salinity waste liquid of the thermal PVDF ultrafiltration membrane as claimed in claim 1, wherein the evaporative crystallization system structurally comprises an evaporative heat exchanger, a forced circulation pump, an evaporator, a steam condensation heat exchanger, a condensed water tank, a condensed water delivery pump, a liquid calcium chloride delivery pump, a heat preservation tank and a drum-type pelleter; the water outlet of the oil-water separation system is connected to the water inlet of the evaporation heat exchanger, the No. 2 steam is connected to the steam inlet of the evaporation heat exchanger, the steam outlet of the evaporation heat exchanger is connected to the air inlet of the steam condensation heat exchanger, and the water outlet of the evaporation heat exchanger is connected to the water inlet of the evaporator; the steam outlet of the evaporator is also connected to the air inlet of the steam condensation heat exchanger, the No. 3 cooling water is connected to the cooling water inlet and outlet of the steam condensation heat exchanger, the water outlet of the steam condensation heat exchanger is connected to the water inlet of the condensate water tank, and the water outlet of the condensate water tank pumps out distilled water through the condensate water conveying pump; the outlet of the evaporator is connected with the water inlet of the evaporating heat exchanger through a forced circulation pump, the outlet of the evaporator is also connected with the liquid calcium chloride inlet of the heat-insulating tank through a liquid calcium chloride delivery pump, the liquid calcium chloride outlet of the heat-insulating tank is connected to the liquid calcium chloride inlet of the drum-type sheet making machine, the No. 4 cooling water is connected to the cooling water inlet and outlet of the drum-type sheet making machine, and the salt outlet of the drum-type sheet making machine sends out the flaky calcium chloride dihydrate.
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| CN202120498229.8U CN215828658U (en) | 2021-03-09 | 2021-03-09 | Thermal method PVDF milipore filter aftertreatment high salt waste liquid resource utilization device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202120498229.8U CN215828658U (en) | 2021-03-09 | 2021-03-09 | Thermal method PVDF milipore filter aftertreatment high salt waste liquid resource utilization device |
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2021
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