CN105461143A - Power plant desulfurization waste water membrane concentrating process and equipment - Google Patents
Power plant desulfurization waste water membrane concentrating process and equipment Download PDFInfo
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- CN105461143A CN105461143A CN201610039141.3A CN201610039141A CN105461143A CN 105461143 A CN105461143 A CN 105461143A CN 201610039141 A CN201610039141 A CN 201610039141A CN 105461143 A CN105461143 A CN 105461143A
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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
-
- 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
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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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
- C02F2301/00—General aspects of water treatment
- C02F2301/06—Pressure conditions
- C02F2301/066—Overpressure, high pressure
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Abstract
The invention discloses a power plant desulfurization waste water membrane concentrating process. The process comprises the step that water quantity and water quality of desulfurization waste water are adjusted in an adjusting tank, and the adjusted desulfurization waste water is reacted with lime in a first reaction tank, enters a second reaction tank in a coagulation fluid state to be reacted with sodium carbonate and then enters a concentrating water tank in a coagulation fluid state; waste water in the concentrating water tank is lifted to a UF membrane component, filtered contributing water enters a neutralizing tank, the pH value of the contributing water is adjusted through industrial hydrochloric acid, and concentrated water flows back to the concentrating water tank; ultra-filtered contributing water with the pH value adjusted in the neutralizing tank is pumped to a first-stage RO membrane component to be concentrated through a pump, obtained concentrated water is pumped into a second-stage RO membrane component through a pump, concentrated water enters an evaporator, the contributing water of the second-stage RO membrane component flows back to the first-stage RO membrane component to be treated, and the contributing water of the first-stage RO membrane component and evaporator condensate water are recycled for slurry mixing of production process agents. The invention discloses power plant desulfurization waste water membrane concentrating equipment. By means of the power plant desulfurization waste water membrane concentrating process and equipment, the concentrating effect of the desulfurization waste can be improved, the chemical agent and operating cost can be reduced, and the zero-release requirement can be met.
Description
Technical field
The present invention relates to power plant desulfurization technical field of waste water processing, refer in particular to a kind of power plant desulfurization wastewater membrane method concentration technology and equipment.
Background technology
In the desulfurization technology of thermal power generation, the Technical Introduction of Desulfurized technology maturation, is most widely used, but can discharge a part of absorption tower slurries when carrying out desulfurization by this method as desulfurization wastewater.Containing a large amount of suspended substance, Cl in desulfurization wastewater
-, F
-, SO
4 2-, Ca
2+, Mg
2+deng material, the heavy metal ion simultaneously containing trace, contaminative is strong.
In prior art, power plant desulfurization waste water conventional treatment method is chemical precipitation method, and operation is comparatively simple, but effect is unstable, and floor space is large, and can produce a large amount of inorganic mud, and sludge treatment costly.Along with environmental requirement is more and more stricter, conventional treatment method can not meet the demands, and membrane technique is a kind of high efficient separation technology without phase transformation, can realize the low cost purification of waste water, desalination.
Application number is 201220611598.4 disclose a kind of desulfurization wastewater embrane method process recovery system, carry out nanofiltration after dosing pretreatment desulfurizing waste water and divide salt, nanofiltration is produced the product water obtained after water enters reverse osmosis concentration and is entered reverse osmosis concentration again, the reverse osmosis concentrated water of twice all enters vaporizer process, but the dense water yield is on the high side, processing costs is high, and chemical feeding quantity is comparatively large, and cost is higher.It adds drug overdose coagulating sedimentation and obtains supernatant liquor after film, needs the link such as settling tank, multi-medium filtering, PAC/PAM(flocculation agent) comparatively large on the impact of film properties, and chemical feeding quantity is more, the inorganic mud of generation is more, and acid adding amount when neutralization tank alkali tune is spent is more.
Application number is the Wet desulphurization wastewater treatment device of 201310112212.4 open Wingdales and gypsum, comprise sedimenting system, ultrafiltration system, reverse osmosis system, washing unit and flushing arrangement, not high to hardness desulfurization wastewater carries out sofening treatment, follow-up reverse osmosis membrane is seriously polluted, and does not utilize reverse osmosis produced water.
Application number is 201410240730.9 disclose a kind of desulfurization wastewater recycle and Zero discharging system and method, by nanofiltration device, a point salt is carried out to desulfurization wastewater, the dense water of nanofiltration directly returns thionizer recycle, nanofiltration produces that water softening enters reverse osmosis by dosing, electrodialysis, crystallization combination process are recycled, and processing costs is higher.
Summary of the invention
The object of the present invention is to provide a kind of power plant desulfurization wastewater membrane method concentration technology and equipment, to improve desulfurization wastewater concentrated effect, reduce chemical agent and working cost, and reach zero emission requirement.
For reaching above-mentioned purpose, solution of the present invention is:
A kind of power plant desulfurization wastewater membrane method concentration technology, comprises the following steps:
One, desulfurization wastewater is the lime reaction of 1.8-2.3% with mass concentration after regulating pondage and water quality in equalizing tank in No. 1 reaction tank, enters after the soda ash being 2.0-2.5% with mass concentration in No. 2 reaction tanks reacts enter concentrated water tank with coagulant liquid state with coagulant liquid state;
Two, the waste water in concentrated water tank rises to tubular type UF membrane module by pump, and the product water after tubular type UF membrane module filters enters neutralization tank, and regulates potential of hydrogen with technical-grade hydrochloric acid, and concentrate recirculation is to concentrated water tank; The chemical feeding quantity of lime and soda ash enters Ca in the water quality of UF membrane module according to waste water
2+control at 450-650mg/L, Mg
2+control to determine in 200-600mg/L adjustment;
Three, the ultrafiltration mixing up potential of hydrogen at neutralization tank is produced water and is squeezed into one-level RO membrane module by pump and concentrate, dense water after the dense water obtained squeezes into secondary RO membrane module reconcentration by pump enters vaporizer, secondary RO membrane module produces water and is back to the process of one-level RO membrane module, and one-level RO membrane module produces water and evaporator condensation Water circulation is sized mixing in production technique medicament.
Further, concentrated water tank is outer blowdown mud regularly, and the mud of discharge enters filter press process after sludge thickener carries out concentrating, and mud cake is regularly transported outward or utilized, and the supernatant liquor of sludge thickener and the pressing filtering liquid of filter press are back to equalizing tank process.
Further, the pond body of described equalizing tank, No. 1 reaction tank, No. 2 reaction tanks and neutralization tank is PE impregnating material.
Further, described waste water is the continuous stirring reaction 10-20min of lime of 1.8-2.3% with mass concentration in No. 1 reaction tank, entering No. 2 reaction tanks with coagulant liquid state, is the continuous stirring reaction 10-20min of soda ash of 2.0-2.5% with mass concentration, carries out ultrafiltration test except strong with coagulant liquid state.
Further, in described concentrated water tank, coagulant liquid mass concentration is 0.5-5%.
Further, described coagulant liquid enters UF membrane module first through blue formula strainer or the filtration of pocket type cartridge filter of 1mm.
Further, described UF membrane module is resistant to pollution tubular type UF membrane module, and molecular weight cut-off is 10-25 ten thousand Dalton, and operating pressure is 1-6bar, and tubular membrane flow diameter is 6-12mm.
Further, described technical-grade hydrochloric acid mass concentration is 30-37%, and basicity regulates HCO
3 -to 300-500mg/L.
Further, the described ultrafiltration mixing up basicity is produced and is squeezed into the core type strainer of 5 μm by fresh feed pump before water enters one-level RO membrane concentration or pocket type cartridge filter filters, feed liquid after topping-up pump supercharging enters the further supercharging of online topping-up pump, under the driving of high pressure, part concentrate recirculation is to online topping-up pump.
Further, described one-level RO membrane module is high pressure resistant, and the selectable DTRO membrane module of ratio of desalinization (disc tube reverse osmosis (dt-ro) membrane module), operating pressure is 30-75bar.
Further, saltiness can be concentrated to 100000-110000mg/L from 30000-40000mg/L by described one-level RO membrane module.
Further, it is front through topping-up pump supercharging that the dense water of described one-level RO film enters secondary RO membrane concentration, then enter the further supercharging of online topping-up pump, and under the driving of high pressure, part concentrate recirculation is to online topping-up pump.
Further, described secondary RO membrane module is high pressure resistant, and the selectable DTRO membrane module of ratio of desalinization, operating pressure is 50-85bar.
Further, low compared with one-level RO membrane module of the rejection of described secondary RO membrane module, time concentrated, comparatively one-level RO membrane module is low for required osmotic pressure, and dense for one-level RO film water is concentrated to saltiness 120000-130000mg/L.In high-voltage operation situation, the secondary RO membrane module that rejection is lower can improve the cycles of concentration of desulfurization wastewater further, reduces dense volume of water further.
A kind of power plant desulfurization wastewater membrane method thickening equipment, comprises equalizing tank, No. 1 reaction tank, No. 2 reaction tanks, concentrated water tank, UF membrane module, neutralization tank, one-level RO membrane module, secondary RO membrane module and vaporizer, equalizing tank entrance connects desulfurization wastewater, equalizing tank outlet connects No. 1 reaction tank entrance, No. 1 reaction tank entrance connects lime, No. 1 reaction tank outlet connects No. 2 reaction tank entrances, No. 2 reaction tank entrances connect soda ash, No. 2 reaction tank outlets connect condensed water tank inlet, concentrated tank outlet connects the entrance of UF membrane module, the dense water out of UF membrane module connects condensed water tank inlet, the product water out of UF membrane module connects neutralization tank entrance, neutralization tank entrance connects technical-grade hydrochloric acid, neutralization tank outlet connects one-level RO membrane module entrance, the dense water out of one-level RO membrane module connects secondary RO membrane module entrance, the dense water out of secondary RO membrane module connects evaporator inlet, the product water out of secondary RO membrane module connects one-level RO membrane module entrance.
Further, also comprise sludge thickener and plate-and-frame filter press, sludge thickener entrance connects the sludge outlet of concentrated water tank, and the sludge outlet of sludge thickener connects plate-and-frame filter press, and the outlet of sludge thickener supernatant liquor and the outlet of plate-and-frame filter press pressing filtering liquid connect equalizing tank entrance.
Further, set gradually fresh feed pump and accurate filter between concentrated water tank and UF membrane module, fresh feed pump entrance connects concentrated water tank, and fresh feed pump outlet connects accurate filter entrance, and accurate filter outlet connects UF membrane module.
Further, fresh feed pump, accurate filter, topping-up pump and online topping-up pump is set gradually between UF membrane module and one-level RO membrane module, fresh feed pump entrance connects UF membrane module, fresh feed pump outlet connects accurate filter, accurate filter connects topping-up pump, topping-up pump is connected on line topping-up pump, and online topping-up pump connects one-level RO membrane module.
Further, between one-level RO membrane module and secondary RO membrane module, set gradually topping-up pump and online topping-up pump, topping-up pump entrance connects one-level RO membrane module, and booster pump outlet is connected on line topping-up pump, and online topping-up pump connects secondary RO membrane module.
After adopting such scheme, inventive desulfurization waste water is the lime reaction of 1.8-2.3% with mass concentration after regulating pondage and water quality in equalizing tank in No. 1 reaction tank, enter after the soda ash being 2.0-2.5% with mass concentration in No. 2 reaction tanks reacts with coagulant liquid state and enter concentrated water tank with coagulant liquid state, there is following beneficial effect:
Enter tubular ultra-filtration membrane using coagulant liquid state after the present invention adopts desulfurization wastewater dosing softening to filter as pretreatment unit, the chemical feeding quantity of lime and soda ash is according to Ca in upgrading unit influent quality
2+and Mg
2+control overflow adjust and to determine, with routine add drug overdose coagulating sedimentation obtain supernatant liquor after film technique compared with, eliminate the link such as settling tank, multi-medium filtering, reduce PAC/PAM to the impact of film properties, and chemical feeding quantity is less, the inorganic mud produced is less, and acid adding amount when neutralization tank alkali tune is spent is less; Compared with tube type filter membrance, tubular ultra-filtration membrane filtering accuracy is higher, and hardness removal efficiency is higher, and need not backwash.
In concentrated water tank, coagulant liquid mass concentration controls at 0.5-5%, tubular type UF membrane module is risen to by pump, the turbulent motion of particulate matter in cross-flow working cycle of coagulant liquid prevents pollutent to build up on ultrafiltration face, the pollutent of cross-flow shearing force to film surface produced plays shearing, scrubbing action, slow down fouling membrane, higher membrane flux can be maintained.
The RO membrane module that the present invention adopts is high voltage bearing DTRO membrane module, compared with traditional rolling RO membrane module, adopt open runner, efficiently avoid film blocking and concentration polarization phenomenon, extend the membrane module life-span, and be easy to cleaning, and require lower to influent quality, ultrafiltration can be produced water and is concentrated to 120000-130000mg/L from saltiness 30000-40000mg/L by two-stage DTRO membrane module, the vaporizer process water yield can be reduced further, greatly reduce capital construction and working cost, economical effectiveness is obvious.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention;
Fig. 2 is UF membrane module filtering process figure of the present invention;
Fig. 3 is one-level RO membrane module concentration flow path figure of the present invention;
Fig. 4 is secondary RO membrane module concentration flow path figure of the present invention.
Label declaration
Equalizing tank No. 11 reaction tanks 21
No. 2 reaction tanks 22 concentrate water tank 3
UF membrane module 4 neutralization tank 5
One-level RO membrane module 61 secondary RO membrane module 62
Vaporizer 7 fresh feed pump 81
Accurate filter 82 topping-up pump 83
Online topping-up pump 84 sludge thickener 91
Plate-and-frame filter press 92.
Embodiment
Below in conjunction with drawings and the specific embodiments, the present invention is described in detail.
Consult shown in Fig. 1 to Fig. 3, a kind of power plant desulfurization wastewater membrane method concentration technology that the present invention discloses, comprise the following steps:
One, desulfurization wastewater 21 is the continuous stirring reaction 10-20min of lime of 1.8-2.3% with mass concentration after regulating pondage and water quality in equalizing tank 1 in No. 1 reaction tank, the continuous stirring reaction 10-20min of soda ash being 2.0-2.5% with mass concentration in No. 2 reaction tanks 21 is entered with coagulant liquid state, after enter concentrated water tank 3 with coagulant liquid state, and coagulant liquid is constantly stirred, control coagulant liquid mass concentration in concentrated water tank 3 and remain on 0.5-5%.
Two, the waste water of concentrated 3 li, water tank rises to tubular type UF membrane module 4 by pump, and the product water after tubular type UF membrane module 4 filters enters neutralization tank 5, and regulates potential of hydrogen with technical-grade hydrochloric acid, and concentrate recirculation is to concentrated water tank 3.The chemical feeding quantity of lime and soda ash enters Ca in the water quality of UF membrane module 4 according to waste water
2+control at 450-650mg/L, Mg
2+control to determine in 200-600mg/L adjustment.
Three, the ultrafiltration mixing up potential of hydrogen at neutralization tank 5 is produced water and is squeezed into one-level RO membrane module 61 by pump and concentrate, dense water after the dense water obtained squeezes into secondary RO membrane module 62 reconcentration by pump enters vaporizer 7, secondary RO membrane module 62 produces water and is back to one-level RO membrane module 61 and processes, and one-level RO membrane module 61 produces water and vaporizer 7 recycling condensing water is sized mixing in production technique medicament.
As shown in Figure 2, when the waste water of concentrated 3 li, water tank rises to tubular type UF membrane module 4 by pump, by fresh feed pump 81 coagulant liquid in concentrated water tank 3 squeezed into the blue formula strainer of accurate filter 82(or the pocket type cartridge filter of 1mm) filter after enter UF membrane module 4 and carry out pre-treatment, UF film (ultra-filtration membrane) used is the organic tubular ultra-filtration membrane of antipollution, molecular weight cut-off is 10-25 ten thousand Dalton, working pressure controls at 1-6bar, tubular membrane flow diameter is 6-12mm, be that the product water that the coagulant liquid of 0.5-5% is filtered into clarification enters neutralization tank 5 by mass concentration, produce Ca in water
2+for 450-650mg/L, Mg
2+for 200-600mg/L, functional quality concentration is that 30-37% technical-grade hydrochloric acid regulates basicity HCO
3 -to 300-500mg/L, ultrafiltration concentrate recirculation is to concentrated water tank 3.
As shown in Figure 3, during the 61 dense water treatment of one-level RO membrane module, accurate filter 82(core type strainer or the pocket type cartridge filter that water introduces 5 μm is produced in the ultrafiltration by fresh feed pump 81 neutralization tank 5 being mixed up basicity) filter after enter topping-up pump 83 and pressurize, ultrafiltration is produced the dense water mixing of part of water and backflow and is entered the process of one-level DTRO membrane concentration after supercharging further by online topping-up pump 84.
As shown in Figure 4, the dense water of one-level DTRO film enters another topping-up pump 83 again and pressurizes, the dense water of part of dense for one-level DTRO film water and backflow mixes and enters the process of secondary DTRO membrane concentration after further supercharging by another online topping-up pump 84, after two-stage DTRO membrane sepn, ultrafiltration is produced water and is concentrated to 120000-130000mg/L from saltiness 30000-40000mg/L, and secondary DTRO film product water can be back to production technique medicament and size mixing.
During secondary RO membrane module 62 dense water treatment, after two-stage DTRO membrane concentration, desulfurization wastewater concentrates more than 4 times, and the wastewater flow rate entering vaporizer 7 process is little, and the water of condensation of acquisition can be back to production technique medicament and size mixing, and salt is recycled.
Under normal running status, a part of mud is arranged to sludge thickener 91 to reduce sludge concentration outside regular from concentrated water tank 4, mud after concentrated carries out plate-and-frame filter press 92 press filtration process further, mud cake is regularly transported outward or is utilized, and the supernatant liquor of sludge thickener and the pressing filtering liquid of filter press are back to equalizing tank process.
The pond body of described equalizing tank 1, No. 1 reaction tank 21, No. 2 reaction tanks 22 and neutralization tank 5 is PE impregnating material.
The present invention also discloses a kind of power plant desulfurization wastewater membrane method thickening equipment, comprises equalizing tank 1, No. 1 reaction tank 21, No. 2 reaction tanks 22, concentrated water tank 3, UF membrane module 4, neutralization tank 5, one-level RO membrane module 61, secondary RO membrane module 62 and vaporizer 7.
Equalizing tank 1 entrance connects desulfurization wastewater, equalizing tank 1 outlet connects No. 1 reaction tank entrance 21, No. 1 reaction tank 21 entrance connects lime, No. 1 reaction tank 21 outlet connects No. 2 reaction tank 22 entrances, No. 2 reaction tank 22 entrances connect soda ash, No. 2 reaction tank 22 outlets connect concentrated water tank 3 entrance, concentrated water tank 3 outlet connects the entrance of UF membrane module 4, the dense water out of UF membrane module 4 connects concentrated water tank 3 entrance, the product water out of UF membrane module 4 connects neutralization tank 5 entrance, neutralization tank 5 entrance connects technical-grade hydrochloric acid, neutralization tank 5 outlet connects one-level RO membrane module 61 entrance, the dense water out of one-level RO membrane module 61 connects secondary RO membrane module 62 entrance, the dense water out of secondary RO membrane module 62 connects vaporizer 7 entrance, the product water out of secondary RO membrane module 62 connects one-level RO membrane module 61 entrance.
As shown in Figure 2, set gradually fresh feed pump 81 and accurate filter 82 between concentrated water tank 3 and UF membrane module 4, fresh feed pump 81 entrance connects concentrated water tank 3, and fresh feed pump 81 outlet connects accurate filter 82 entrance, and accurate filter 82 outlet connects UF membrane module 4.
As shown in Figure 3, fresh feed pump 81, accurate filter 82, topping-up pump 83 and online topping-up pump 84 is set gradually between UF membrane module 4 and one-level RO membrane module 61, fresh feed pump 81 entrance connects UF membrane module 4, fresh feed pump 81 outlet connects accurate filter 82, accurate filter 82 connects topping-up pump 83, topping-up pump 83 is connected on line topping-up pump 84, and online topping-up pump 84 connects one-level RO membrane module 61.
As shown in Figure 4, topping-up pump 83 and online topping-up pump 84 is set gradually between one-level RO membrane module 61 and secondary RO membrane module 62, topping-up pump 83 entrance connects one-level RO membrane module 61, and topping-up pump 83 outlet is connected on line topping-up pump 84, and online topping-up pump 84 connects secondary RO membrane module 62.
As shown in Figure 1, the present invention also comprises sludge thickener 91 and plate-and-frame filter press 92, sludge thickener 91 entrance connects the sludge outlet of concentrated water tank 3, the sludge outlet of sludge thickener 91 connects plate-and-frame filter press 92, and the outlet of sludge thickener 91 supernatant liquor and the outlet of plate-and-frame filter press 92 pressing filtering liquid connect equalizing tank 1 entrance.
The foregoing is only the preferred embodiments of the present invention, not to the restriction of this case design, all equivalent variations done according to the design key of this case, all fall into the protection domain of this case.
Claims (10)
1. a power plant desulfurization wastewater membrane method concentration technology, is characterized in that, comprises the following steps:
One, desulfurization wastewater is the lime reaction of 1.8-2.3% with mass concentration after regulating pondage and water quality in equalizing tank in No. 1 reaction tank, enters after the soda ash being 2.0-2.5% with mass concentration in No. 2 reaction tanks reacts enter concentrated water tank with coagulant liquid state with coagulant liquid state;
Two, the waste water in concentrated water tank rises to tubular type UF membrane module by pump, and the product water after tubular type UF membrane module filters enters neutralization tank, and regulates potential of hydrogen with technical-grade hydrochloric acid, and concentrate recirculation is to concentrated water tank; The chemical feeding quantity of lime and soda ash enters Ca in the water quality of UF membrane module according to waste water
2+control at 450-650mg/L, Mg
2+control to determine in 200-600mg/L adjustment;
Three, the ultrafiltration mixing up potential of hydrogen at neutralization tank is produced water and is squeezed into one-level RO membrane module by pump and concentrate, dense water after the dense water obtained squeezes into secondary RO membrane module reconcentration by pump enters vaporizer, secondary RO membrane module produces water and is back to the process of one-level RO membrane module, and one-level RO membrane module produces water and evaporator condensation Water circulation is sized mixing in production technique medicament.
2. a kind of power plant desulfurization wastewater membrane method concentration technology as claimed in claim 1, it is characterized in that, concentrated water tank regularly outer blowdown mud, discharge mud to sludge thickener carry out concentrate after enter filter press process, mud cake is regularly transported outward or is utilized, and the supernatant liquor of sludge thickener and the pressing filtering liquid of filter press are back to equalizing tank process.
3. a kind of power plant desulfurization wastewater membrane method concentration technology as claimed in claim 1, it is characterized in that, described waste water is the continuous stirring reaction 10-20min of lime of 1.8-2.3% with mass concentration in No. 1 reaction tank, No. 2 reaction tanks are entered with coagulant liquid state, with the continuous stirring reaction 10-20min of soda ash that mass concentration is 2.0-2.5%, carry out ultrafiltration with coagulant liquid state and test except strong.
4. a kind of power plant desulfurization wastewater membrane method concentration technology as claimed in claim 1, it is characterized in that, in described concentrated water tank, coagulant liquid mass concentration is 0.5-5%.
5. a kind of power plant desulfurization wastewater membrane method concentration technology as claimed in claim 1, it is characterized in that, described technical-grade hydrochloric acid mass concentration is 30-37%, and basicity regulates HCO
3 -to 300-500mg/L.
6. a kind of power plant desulfurization wastewater membrane method concentration technology as claimed in claim 1, is characterized in that, described coagulant liquid enters UF membrane module and first filters through the blue formula strainer of 1mm or pocket type cartridge filter; Described UF membrane module is resistant to pollution tubular type UF membrane module, and molecular weight cut-off is 10-25 ten thousand Dalton, and operating pressure is 1-6bar, and tubular membrane flow diameter is 6-12mm; The described ultrafiltration mixing up basicity is produced and is squeezed into the core type strainer of 5 μm by fresh feed pump before water enters one-level RO membrane concentration or pocket type cartridge filter filters, feed liquid after topping-up pump supercharging enters the further supercharging of online topping-up pump, under the driving of high pressure, part concentrate recirculation is to online topping-up pump; Described one-level RO membrane module is high pressure resistant, the selectable DTRO membrane module of ratio of desalinization, and operating pressure is 30-75bar; Saltiness can be concentrated to 100000-110000mg/L from 30000-40000mg/L by described one-level RO membrane module.
7. a kind of power plant desulfurization wastewater membrane method concentration technology as claimed in claim 1, it is characterized in that, it is front through topping-up pump supercharging that the dense water of described one-level RO film enters secondary RO membrane concentration, then enter the further supercharging of online topping-up pump, under the driving of high pressure, part concentrate recirculation is to online topping-up pump; Described secondary RO membrane module is high pressure resistant, the selectable DTRO membrane module of ratio of desalinization, and operating pressure is 50-85bar; Low compared with one-level RO membrane module of the rejection of described secondary RO membrane module, time concentrated, comparatively one-level RO membrane module is low for required osmotic pressure, and dense for one-level RO film water is concentrated to saltiness 120000-130000mg/L; In high-voltage operation situation, the secondary RO membrane module that rejection is lower can improve the cycles of concentration of desulfurization wastewater further, reduces dense volume of water further.
8. a power plant desulfurization wastewater membrane method thickening equipment, is characterized in that: comprise equalizing tank, No. 1 reaction tank, No. 2 reaction tanks, concentrated water tank, UF membrane module, neutralization tank, one-level RO membrane module, secondary RO membrane module and vaporizer, equalizing tank entrance connects desulfurization wastewater, equalizing tank outlet connects No. 1 reaction tank entrance, No. 1 reaction tank entrance connects lime, No. 1 reaction tank outlet connects No. 2 reaction tank entrances, No. 2 reaction tank entrances connect soda ash, No. 2 reaction tank outlets connect condensed water tank inlet, concentrated tank outlet connects the entrance of UF membrane module, the dense water out of UF membrane module connects condensed water tank inlet, the product water out of UF membrane module connects neutralization tank entrance, neutralization tank entrance connects technical-grade hydrochloric acid, neutralization tank outlet connects one-level RO membrane module entrance, the dense water out of one-level RO membrane module connects secondary RO membrane module entrance, the dense water out of secondary RO membrane module connects evaporator inlet, the product water out of secondary RO membrane module connects one-level RO membrane module entrance.
9. a kind of power plant desulfurization wastewater membrane method thickening equipment as claimed in claim 8, it is characterized in that: also comprise sludge thickener and plate-and-frame filter press, sludge thickener entrance connects the sludge outlet of concentrated water tank, the sludge outlet of sludge thickener connects plate-and-frame filter press, and the outlet of sludge thickener supernatant liquor and the outlet of plate-and-frame filter press pressing filtering liquid connect equalizing tank entrance.
10. a kind of power plant desulfurization wastewater membrane method thickening equipment as claimed in claim 8, it is characterized in that: between concentrated water tank and UF membrane module, set gradually fresh feed pump and accurate filter, fresh feed pump entrance connects concentrated water tank, fresh feed pump outlet connects accurate filter entrance, and accurate filter outlet connects UF membrane module;
Fresh feed pump, accurate filter, topping-up pump and online topping-up pump is set gradually between UF membrane module and one-level RO membrane module, fresh feed pump entrance connects UF membrane module, fresh feed pump outlet connects accurate filter, accurate filter connects topping-up pump, topping-up pump is connected on line topping-up pump, and online topping-up pump connects one-level RO membrane module;
Between one-level RO membrane module and secondary RO membrane module, set gradually topping-up pump and online topping-up pump, topping-up pump entrance connects one-level RO membrane module, and booster pump outlet is connected on line topping-up pump, and online topping-up pump connects secondary RO membrane module.
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106830441A (en) * | 2017-03-27 | 2017-06-13 | 福建欣宇卫浴科技股份有限公司 | Solid-liquid separation system |
| CN106830437A (en) * | 2017-03-13 | 2017-06-13 | 厦门嘉戎技术股份有限公司 | A kind of desulfurization wastewater reverse osmosis membrane concentration combination unit and technique |
| CN107032547A (en) * | 2017-06-07 | 2017-08-11 | 北京清新环境技术股份有限公司 | A kind of SO3Removing and the charging integrated apparatus and method of desulfurization wastewater zero-emission |
| CN107055863A (en) * | 2017-01-23 | 2017-08-18 | 烟台金正环保科技有限公司 | The technique that a kind of disc tube reverse osmosis (dt-ro) handles citric acid wastewater |
| CN108249646A (en) * | 2018-03-20 | 2018-07-06 | 厦门嘉戎技术股份有限公司 | Can resource recycling power plant desulfurization wastewater Zero-discharge treating process and device |
| WO2018218939A1 (en) * | 2017-05-31 | 2018-12-06 | 国家电投集团远达环保工程有限公司重庆科技分公司 | Zero-discharge wastewater treatment system for scr catalyst regeneration wastewater |
| CN109650636A (en) * | 2018-12-26 | 2019-04-19 | 国电新能源技术研究院有限公司 | A kind of brine waste processing system |
| CN109824183A (en) * | 2019-02-28 | 2019-05-31 | 苏州希图环保科技有限公司 | A kind of high concentrated organic waste liquid zero-emission efficient treatment process with high salt |
| CN113461109A (en) * | 2021-08-02 | 2021-10-01 | 广东工业大学 | Multistage reverse osmosis process and system capable of regulating and controlling desalination rate |
| CN114275929A (en) * | 2021-12-14 | 2022-04-05 | 四川德迈环保工程有限公司 | High-reuse-rate membrane treatment system and method for wastewater |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1085742A (en) * | 1996-09-12 | 1998-04-07 | Kawasaki Heavy Ind Ltd | Method and apparatus for treating desulfurization drainage |
| CN102503808A (en) * | 2011-10-20 | 2012-06-20 | 嘉戎科技(厦门)有限公司 | Production method and apparatus for high-power concentration of gulonic acid |
| CN202924865U (en) * | 2012-11-19 | 2013-05-08 | 苏州凯新分离科技有限公司 | Membrane-process treatment recycling system for desulfurization waste water |
| CN103214111A (en) * | 2013-04-02 | 2013-07-24 | 江苏一同环保工程技术有限公司 | Wet desulphurization wastewater treatment device for limestone and gypsum |
| CN103979729A (en) * | 2014-05-30 | 2014-08-13 | 西安西热水务环保有限公司 | Desulfurization waste water recycling and zero discharge system and method |
| CN205616697U (en) * | 2016-01-21 | 2016-10-05 | 厦门嘉戎技术股份有限公司 | Power plant's desulfurization waste water embrane method concentrator |
-
2016
- 2016-01-21 CN CN201610039141.3A patent/CN105461143B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1085742A (en) * | 1996-09-12 | 1998-04-07 | Kawasaki Heavy Ind Ltd | Method and apparatus for treating desulfurization drainage |
| CN102503808A (en) * | 2011-10-20 | 2012-06-20 | 嘉戎科技(厦门)有限公司 | Production method and apparatus for high-power concentration of gulonic acid |
| CN202924865U (en) * | 2012-11-19 | 2013-05-08 | 苏州凯新分离科技有限公司 | Membrane-process treatment recycling system for desulfurization waste water |
| CN103214111A (en) * | 2013-04-02 | 2013-07-24 | 江苏一同环保工程技术有限公司 | Wet desulphurization wastewater treatment device for limestone and gypsum |
| CN103979729A (en) * | 2014-05-30 | 2014-08-13 | 西安西热水务环保有限公司 | Desulfurization waste water recycling and zero discharge system and method |
| CN205616697U (en) * | 2016-01-21 | 2016-10-05 | 厦门嘉戎技术股份有限公司 | Power plant's desulfurization waste water embrane method concentrator |
Non-Patent Citations (1)
| Title |
|---|
| 董秉直: "混凝对膜污染的防止作用", 《环境科学》 * |
Cited By (14)
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|---|---|---|---|---|
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| CN106830441A (en) * | 2017-03-27 | 2017-06-13 | 福建欣宇卫浴科技股份有限公司 | Solid-liquid separation system |
| WO2018177289A1 (en) * | 2017-03-27 | 2018-10-04 | 福建欣宇卫浴科技股份有限公司 | Solid-liquid separation system |
| WO2018218939A1 (en) * | 2017-05-31 | 2018-12-06 | 国家电投集团远达环保工程有限公司重庆科技分公司 | Zero-discharge wastewater treatment system for scr catalyst regeneration wastewater |
| CN107032547A (en) * | 2017-06-07 | 2017-08-11 | 北京清新环境技术股份有限公司 | A kind of SO3Removing and the charging integrated apparatus and method of desulfurization wastewater zero-emission |
| CN108249646A (en) * | 2018-03-20 | 2018-07-06 | 厦门嘉戎技术股份有限公司 | Can resource recycling power plant desulfurization wastewater Zero-discharge treating process and device |
| CN108249646B (en) * | 2018-03-20 | 2023-07-11 | 厦门嘉戎技术股份有限公司 | Power plant desulfurization wastewater zero-emission treatment process and device capable of recycling resources |
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