CN100415338C - Method and equipment for purifying recirculated cooling water or town B-grade sewage - Google Patents

Method and equipment for purifying recirculated cooling water or town B-grade sewage Download PDF

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Publication number
CN100415338C
CN100415338C CNB2007100999699A CN200710099969A CN100415338C CN 100415338 C CN100415338 C CN 100415338C CN B2007100999699 A CNB2007100999699 A CN B2007100999699A CN 200710099969 A CN200710099969 A CN 200710099969A CN 100415338 C CN100415338 C CN 100415338C
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China
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zone
town
cooling water
recirculated cooling
purification
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CNB2007100999699A
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Chinese (zh)
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CN101117250A (en
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李永明
李尚志
惠兆华
罗德波
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华电水处理技术工程有限公司
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Publication of CN100415338C publication Critical patent/CN100415338C/en

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Abstract

The invention relates to a purification method and equipment for cool circulating water or town secondary sewage water, and is characterized in that the invention has the following steps: a quick mixing zone 1 for mixing a ready treated liquid and a mixing medicament, a flocculating reaction zone 2 for mixing and flocculating a mixed liquid with a backflow deposit substance to get a compact alum at an outlet of the zone, a depositing and concentrating zone 3 for separating a supernatant liquor and a suspension solid and for returning and draining a deposit substance, and a filtering facility zone 4 for purifying the supernatant liquor; the equipment of the invention mainly comprises the quick mixing zone, a high efficient clarification tank and a filtering zone; the invention designs the purification method and equipment for liquid and water; the water quality from the invention is stable, the cost is lower, which changes the prior purification method for liquid and water.

Description

The purification method of recirculated cooling water or town B-grade sewage and equipment

Technical field

The present invention relates to the purification method and the equipment of recirculated cooling water or town B-grade sewage, especially for the purification method and the equipment of thermal power plant's recirculated cooling water Treatment for Reuse or town sewage advanced treating.

Background technology

In the existing similar technology, separate and contact-type lime treatment depositing reservoir (Quan Chidi scrapes mud) with the body refuse after suspension body refuse type accelerator (Ban Chidi scrapes mud) or the improvement that is mostly that becomes fracture filtration device series connection use, the pond type is circle, medicament mixes, flocculation reaction, deposit refluxes, courses of reaction such as solid matter separation are all finished in a reactor, the service condition of can't independent optimization adjusting single course of reaction, the packing of the floccule body that generates is little, the efficient that solid separates is low, the suspension slime layer concentration instability that forms causes the floor space of reactor big, hardware is many, capacity of resisting impact load is poor.Said method has shortcomings such as floor space is big, cost of investment is higher, operational management is complicated, capacity of resisting impact load difference in use.

Summary of the invention

The purification method and the equipment that the purpose of this invention is to provide recirculated cooling water or town B-grade sewage, problems such as the prior art floor space is big, one-time investment is high, operational management is complicated to avoid, anti-load impact ability, it is optimization method and the equipment project organization that is fit to China's actual conditions.

The purification method of recirculated cooling water or town B-grade sewage is characterized in that, pass through following several steps:

A. pending liquid is introduced Mixed Zone 1, add plurality of reagents, and reagent and pending liquid are mixed, described plurality of reagents is lime medicament and one or more coagulant;

The pending liquid that b. will mix carries out high speed clarification in depositing reservoir, the supernatant upflow velocity is 10~30 meters/hour the supernatant that obtains drawn;

C. above-mentioned supernatant is introduced filtration zone 4, filling filtering material in the filtration zone 4.

After described pending liquid entered the mixed zone 12 in rapid mixing zone 1, pending liquid designs the time of staying in mixed zone 12 be 30~240 seconds, and the preferred time of staying is 45~180 seconds.

Described lime medicament is by the lime device it to be joined in the rapid mixing zone 1, and the lime device adopts dry powder metering, modular arrangements, whole process automation control and airtight operation.

Described dry powder metering is the amount of directly measuring dry powder, realizes that by the dosage that changes dry powder the ratio of lime dosage and depositing reservoir inlet water flow is regulated.

Described whole process automation control, be that make up a prescription unit, milk of lime of milk of lime added the unit and control automatically, comprise automatic operation and automatic control cleaning etc., the vibrations hopper of setting the lime silo blanking is simultaneously avoided system jams according to regularly anti-clogging concussion of grey matter.

Described coagulant can be a liquid polymerization ferric sulfate, and dosage is 10~15 mg/litre.

The pending liquid that described step b. will mix carries out the high speed clarification in depositing reservoir, wherein depositing reservoir comprises that flocculation reaction zone 2 and precipitation concentrate zone 3, clarification comprises that the pending liquid that mixes concentrates regional 3 rapid precipitation in the flocculation reaction in flocculation reaction zone 2 with in precipitation at a high speed.

Described flocculation reaction, be to adopt circulating granular to quicken flocculation to mixed uniform pending liquid, with multistage flocculation reaction, to reduce the best flocculation reaction time, its pending liquid is 10~20 minutes in this region design time of staying, the decision design time of staying is 10~15 minutes, is 1/3~1/2 of the conventional flocculation reaction time.

Described employing circulating granular quickens flocculation, be after mixing with mechanical stirring device uniform pending liquid, the partly precipitated material is recycling, with settling velocity gradients in the control water velocity control flocculation reaction zone 2 at 250~450 seconds -1Scope, and add high molecular polymer, to realize the further closely knit of flocculation reaction product, improve the sinking speed of flocculation reaction product.

Described mechanical stirring device adopts the axial flow agitator, and guiding device is set.

Described multistage flocculation reaction comprises secondary flocculation reaction at least, and first order flocculation reaction is mechanical flocculation reaction, and second level flocculation reaction is the waterpower flocculation reaction.

Described high speed clarification, the flow velocity that its supernatant rises is 10~30 meters/hour, preferred upflow velocity is 10~20 meters/hour.

Described rapid precipitation comprises and treats the control method that the deposit interface is controlled, the discrete particle sedimentation was clarified, was similar to usefulness holey separator that treatment fluid carries out the preformed precipitate processing, treats treatment fluid.

Described deposit interface is controlled, be the pending liquid after the flocculation to be introduced precipitation concentrate zone 3, the suspended solid of holding back enters enrichment region 33, and being provided with in precipitation concentrates zone 3 that deposit strikes off gathering-device, side device and deposit tapping equipment are visited in the deposit interface, its deposit strikes off gathering-device and visits the signal controlling deposit tapping equipment that the side device provides, the operation that deposit strikes off gathering-device according to the deposit interface.

Described with the clarification of holey separator, be that pending liquid is risen by holey separator 32, obtain supernatant, the hydraulic radius of holey separator, setting height(from bottom) can be determined according to the water quality index of treatment fluid.

The control method of described approximate discrete particle sedimentation is to concentrate the Reynolds number in zone 3 and surface of solids load and make solid particles sediment speed after the flocculation reaction near the discrete particle sinking speed by adjusting precipitation.

Described high speed depositing reservoir, the deposit concentration of its discharging can reach 20~100mg/L (mg/litre), can directly dewater, and need not concentration.

Described step c is introduced filtration zone 4 with above-mentioned supernatant, be filled with the filtering material of porosity in the filtration zone 4 along Cheng Bianhua, be the water distributing area 41 of earlier above-mentioned supernatant being introduced filtration zone 4, enter influent weir chamber 42, filtration zone 4 body region 43 and outlet system 44 more successively; Supernatant carries out deep-bed filtration in filtration zone 4 body region 43.

The design current velocity of the filtration zone 4 of described step c is 10~18 meters/hour, and the decision design flow velocity is 10~14.5 meters/hour.

Described water distributing area 41 can add sulfuric acid or/and coagulant, and fully mixes.

The body region 43 of described filtration zone 4, porosity of the filtering material of filling is along Cheng Bianhua in it.

The washing of described filtering material can be adopted the mode of combined water and air backwash.

Described filtration zone 4 body region 43 adopt permanent liquid level drag flow deep-bed filtration.

Described coagulant can be molysite or aluminium salt.

It mainly comprises Mixed Zone 1, depositing reservoir and filtration zone 4, between Mixed Zone 1 and the depositing reservoir, have water channel to connect between high speed depositing reservoir and the filtration zone 4.

Described depositing reservoir can be divided into flocculation zone 2 and precipitation concentrates zone 3.

Described flocculation zone 2 comprises current stabilization district 21, inlet channel 22, mechanical flocculation zone 23 and plug-flow flocculation zone 24 again successively, in the wherein mechanical flocculation zone 23 agitator 25 is arranged.

Described precipitation concentrates regional 3 tops and is provided with the holey separator, and concentrated regional 3 bottoms of precipitation are provided with deposit and strike off gathering-device.

The top that the deposit in the concentrated zone 3 of described precipitation strikes off gathering-device is connected with the deposit tapping equipment.

Described filtration zone 4 mainly comprises water distributing area 41, influent weir chamber 42, body region 43 and exhalant region 44.

Described body region 43 is a drag flow deep-bed filtration device, promptly is provided with filtering material and supporting layer in the body region 43, under the supporting layer water and air distributing device is housed.

Described body region 43 also comprises the washing and filtering device, discharges the constant fluid level control device of filtered fluid.

Be provided with the suspended sediment concentration meter in the described Mixed Zone 1.

Be provided with a plurality of reagent dispensers in the described Mixed Zone 1.

The present invention conceives purification method and the equipment that has designed a kind of sewage, the present invention designs ingenious, novel, changed the mode of the purification of sewage in the past, avoid problems such as the prior art floor space is big, one-time investment is high, operational management is complicated, anti-load impact ability.

The present invention also has following advantage:

1, the present invention 1 adds reagent in the Mixed Zone, and pending liquid is fully mixed with reagent, helps the generation of floccule;

2, the lime medicament is by the lime device it to be joined in the Mixed Zone 1, help the lime medicament quantitatively, on time, do not have to leak ground and throw in;

3, adopt circulating granular to quicken flocculation, pending liquid is flocculated better, with speed and the degree of accelerating to purify;

4, it is can pending clarifying speed very fast to clarify pending liquid with the holey separator;

5, use multistage flocculation reaction, can make pending more flocculates that are settled out;

6, adopt the drag flow deep-bed filtration, supernatant is better purified, more existing filtration, degree of purification is better;

7, the present invention is optimization method and the equipment project organization that is fit to China's actual conditions.

Description of drawings

Fig. 1, device structure schematic diagram of the present invention;

The vertical view in the rapid mixing zone 1 of Fig. 2, present device;

The front view in the rapid mixing zone 1 of Fig. 3, present device;

The lime apparatus structure schematic diagram of Fig. 4, present device;

The vertical view in the flocculation reaction zone of the high speed depositing reservoir of Fig. 5, present device;

The front view in the flocculation reaction zone of the high speed depositing reservoir of Fig. 6, present device;

The vertical view in the precipitation reaction zone of the high speed depositing reservoir of Fig. 7, present device;

The front view in the precipitation reaction zone of the high speed depositing reservoir of Fig. 8, present device;

Filtration zone 4 vertical views of Fig. 9, present device;

Figure 10, Fig. 9 D-D cutaway view;

Figure 11, Figure 11 E-E cutaway view;

The process chart of Figure 12, method of the present invention.

Number in the figure wherein, 1 is the Mixed Zone, 2 are the flocculation reaction zone, 3 for precipitation concentrates the zone, and 4 is filtration zone, and 11 is irrigation channel, 12 is the mixed zone, and 13 for going out water channel, and 14 is agitator, 15 is lime, and 16 is overflow area, and 21 is the current stabilization district, 22 is inlet channel, and 23 is mechanical flocculation zone, and 24 is the plug-flow flocculation zone, 25 is agitator, and 31 is the preliminary sedimentation district, and 32 is the holey separator, 33 is enrichment region, and 34 is mud scraper, and 35 is the deposit return duct, 36 is the deposit delivery pipe, and 37 is the V-type Sludge Bed, and 38 is deposit interface analyzer, 41 is water distributing area, 42 is the influent weir chamber, and 43 is body region, and 44 is exhalant region.

The specific embodiment

The purification method of recirculated cooling water or town B-grade sewage is characterized in that, pass through following several steps:

A. pending liquid is introduced Mixed Zone 1, add one or more reagent, and reagent and pending liquid are mixed, this plurality of reagents is lime medicament and one or more coagulant;

The pending liquid that b. will mix carries out the high speed clarification in the high speed depositing reservoir, the supernatant upflow velocity is 10~30 meters/hour, and the supernatant that obtains is drawn;

C. above-mentioned supernatant is introduced filtration zone 4, filling filtering material in the filtration zone 4.

After described pending liquid entered the mixed zone 12 of Mixed Zone 1, pending liquid designs the time of staying in mixed zone 12 be 30~240 seconds, and the preferred time of staying is 45~180 seconds.

Described lime medicament is by the lime device it to be joined in the rapid mixing zone (1), and the lime device adopts dry powder metering, modular arrangements, whole process automation control and airtight operation.

The powdery calcium hydroxide is transported by closed tank truck, and strength is unloaded ash.Gas drains into atmosphere after being separated by the head space gas powder.The ash hole place is provided with the stifled facility of anti-canopy, and slaked lime powder enters batcher, and the rotary feeder motor adopts VFC, slaked lime powder dosage and the proportional adjusting of depositing reservoir inlet flow rate.Wherein the pulverized limestone batcher is selected import equipment for use, accurate measurement, and maintenance is little.

Dry powder metering, the concentration that changes lime slurry is to realize metering, and is accurately simple, and control easily is one of characteristics of native system.Like this, can keep pipeline sodalime breast under nominal flow rate, to move, with the wearing and tearing of avoiding changes in flow rate to cause.

Slaked lime powder is after metering delivered to the vapour powder separator on the top of lime agitator tank via conveying worm, dry powder meets and separated at vapour powder separator with the steam of discharging when entering agitator tank, and powder falls into case, and steam then drains into outside the case.Powder mixes, stirs, is dissolved into milk of lime with the clear water that enters from auxiliary water tank in agitator tank, is sent to depositing reservoir by Lime Milk Transfer Pump.

Calcium hydroxide is stored, metering, system breast, add and be the unit configuration, and each overlaps every depositing reservoir with one, and Lime Milk Transfer Pump 100% is standby.

Whole process automation control is another characteristics of native system.The vibrations hopper of lime silo blanking can block up to avoid down grey manteau according to regularly anti-clogging concussion of grey matter.But the start and stop of milk of lime dosing unit, Lime Milk Transfer Pump all program are operated, and each step all cleans up the inactive part of this system automatically.

All system and equipment are in the air-tight state operation, and the axle head of rotary machine etc. locates all to take lubricated and flushing measure, to alleviate wearing and tearing and to leak.

Described coagulant can be a liquid polymerization ferric sulfate, and dosage is 10~15 mg/litre.

The pending liquid that described step b. will mix carries out the high speed clarification in depositing reservoir, wherein depositing reservoir comprises that flocculation reaction zone 2 and precipitation concentrate zone 3, clarification comprises that the pending liquid that mixes concentrates regional 3 rapid precipitation in the flocculation reaction in flocculation reaction zone 2 with in precipitation at a high speed.

Described flocculation reaction is to adopt circulating granular to quicken flocculation and multistage flocculation reaction to mixed uniform pending liquid.

Described employing circulating granular quickens flocculation, be after mixing with mechanical stirring device uniform pending liquid, the partly precipitated material is recycling, with settling velocity gradients in the control water velocity control flocculation reaction zone 2 at 250~450 seconds -1Scope, and add high molecular polymer.

The main effect that circulating granular quickens flocculation technique has: one, increase system anti-water quality impact load ability; Two, the flocculation particle constantly is squeezed, discharges wherein moisture, increase grain density; Three, form the stable suspersion slime layer,, improve the heavy speed of particle with slow particle (such as the magnesium hydroxide particle) collision of heavy speed.Four, by mechanism, hydraulic action, change the shape of floccule body, make it subglobular.

Described multistage flocculation reaction comprises secondary flocculation reaction at least, and first order flocculation reaction is mechanical flocculation reaction, and second level flocculation reaction is the waterpower flocculation reaction.

Described flocculation reaction, its pending liquid is 10~20 minutes in this region design time of staying, the decision design time of staying is 10~15 minutes.

Described rapid precipitation comprises that the deposit interface for the treatment of treatment fluid is controlled, usefulness holey separator is clarified, the control method of approximate discrete particle sedimentation.

Described deposit interface is controlled, be the pending liquid after the flocculation to be introduced precipitation concentrate zone 3, the suspended solid of holding back enters enrichment region 33, and in precipitation concentrates zone 3 deposit is set and strikes off gathering-device and deposit interface sniffer.

Described with the clarification of holey separator, be that pending liquid is risen by holey separator 32, obtain supernatant, the flow velocity of its rising is 10~30 meters/hour, preferred upflow velocity is 10~20 meters/hour.

The control method of described approximate discrete particle sedimentation is to make the solid particles sediment of flocculating near the discrete particle sinking speed by adjusting the Reynolds number and the surface of solids load that precipitate concentrated zone 33.

The reason that the depositing separation area upflow velocity increases mainly contains: one, quicken the density that flocculation technique has increased the flocculation particle by circulating granular; Two, adjust Reynolds number and reduce particle penetration resistance coefficient; Three, particle is spherical in shape, and average grain diameter reduces, and sinking speed is near the heavy speed of discrete particle; Four, control surface of solids load prevents the generation of crowded precipitation; Five, adopt the holey separator.

Described step c is introduced filtration zone 4 with above-mentioned supernatant, be filled with the filtering material of porosity in the filtration zone 4 along Cheng Bianhua, be the water distributing area 41 of earlier above-mentioned supernatant being introduced filtration zone 4, enter influent weir chamber 42, filtration zone 4 body region 43 and outlet system 44 more successively; Supernatant carries out deep-bed filtration in filtration zone 4 body region 43.

The design current velocity of the filtration zone 4 of described step c is 10~18 meters/hour, and the decision design flow velocity is 10~14.5 meters/hour.

Described water distributing area 41 can add sulfuric acid or/and coagulant, and fully mixes.

In handling water, add flocculant.Utilize that suspended particulate in the filtering layer hole orthokinetic flocculation takes place in the filter process, thereby increased small granular suspended matters and become bulky grain and, improved filter effect, improved filtering water by the possibility that filtrate stops.

The body region 43 of described filtration zone 4, porosity of the filtering material of filling is along Cheng Bianhua in it.

The main coarse media that uses, the surface filtration that has occurred when having avoided adopting the fine filtering material avoids suspension to penetrate filter material layer too early simultaneously, thereby reduces the filtering layer resistance, improves retaining power, helps improving filtering velocity.

In filtering layer, added a small amount of fine filtering material, and be dispersed in the whole filtering layer, mix with compressed air after each backwash, thereby reduced the local porosity of coarse media, make that the average pore passage of filtrate is very little, so just under the prerequisite that does not reduce retaining power, improved flocculation efficiency.

The washing of described filtering material can be adopted the mode of combined water and air backwash.

Described filtration zone 4 body region 43 adopt permanent liquid level drag flow deep-bed filtration.

Described coagulant can be molysite or aluminium salt.

The cleaning equipment of recirculated cooling water or town B-grade sewage is characterized in that, it mainly comprises Mixed Zone 1, depositing reservoir and filtration zone 4, between Mixed Zone 1 and the clarification, have water channel to connect between depositing reservoir and the filtration zone 4.

Described depositing reservoir can be divided into flocculation zone 2 and precipitation concentrates zone 3.

Described flocculation zone 2 comprises current stabilization district 21, inlet channel 22, mechanical flocculation zone 23 and plug-flow flocculation zone 24 again successively, in the wherein mechanical flocculation zone 23 agitator 25 is arranged.

Described precipitation concentrates regional 3 tops and is provided with the holey separator, and concentrated regional 3 bottoms of precipitation are provided with deposit and strike off gathering-device.

The top that the deposit in the concentrated zone 3 of described precipitation strikes off gathering-device is connected with the deposit tapping equipment.

Described filtration zone 4 mainly comprises water distributing area 41, influent weir chamber 42, body region 43 and exhalant region 44.

Described body region 43 is a drag flow deep-bed filtration device, promptly is provided with filtering material and supporting layer in the body region 43, under the supporting layer water and air distributing device is housed.

Described body region 43 also comprises the washing and filtering device, discharges the constant fluid level control device of filtered fluid.

Be provided with the suspended sediment concentration meter in the described Mixed Zone 1.

Be provided with a plurality of reagent dispensers in the described Mixed Zone 1.

The recirculated cooling water that the present invention relates to or the purification method of town B-grade sewage, it is characterized in that it comprises: a Mixed Zone 1, be used to mix pending liquid and coagulated agent, a depositing reservoir, be used for mixed pending liquid flocculation and rapid precipitation, and a filtration zone 4 that is used to purify supernatant.

Concrete technological process is described as follows in conjunction with Fig. 1:

Mixed Zone 1

Pending liquid is entered the irrigation channel 11 of Mixed Zone 1 by the bottom, enter mixed zone 12 in the lump with the lime medicament that adds in this district, coagulant dosage under the effect of agitator 14, enters water outlet canal 13 after pending liquid, lime, coagulant fully mix in mixed zone 12.When the pending flow quantity that enters was excessive, unnecessary flow was by overflow area 16 dischargings.

The design time of staying suggestion of pending liquid in mixed zone 12 is 30s (second)~240s, and the preferred time of staying is 45s~180s.

Lime 15 dosing systems as shown in Figure 4, system's operational process is: the powdery calcium hydroxide is transported by closed tank truck, strength is unloaded ash, and gas drains into atmosphere after being separated by the head space gas powder, and the ash hole place is provided with the stifled facility of anti-canopy, slaked lime powder enters batcher, slaked lime powder is after metering delivered to the vapour powder separator on the top of lime agitator tank via conveying worm, dry powder meets also separated with the steam of discharging when entering agitator tank at vapour powder separator, powder falls into case, and steam then drains into outside the case.Powder mixes, stirs, is dissolved into milk of lime with the clear water that enters from auxiliary water tank in agitator tank, is sent to by Lime Milk Transfer Pump to add a little.The system is characterized in that: dry powder metering, calcium hydroxide are stored, metering, system breast, add and be the unit configuration, whole process automation control, and all systems and equipment are in the air-tight state operation.

Its dosage determines that according to the hardness of pending liquid coagulant can be selected molysite or aluminium salt, and dosage is determined by medicament kind and pending liquid water quality.

The powdery calcium hydroxide is transported by closed tank truck, and strength is unloaded ash.Gas drains into atmosphere after being separated by the head space gas powder.The ash hole place is provided with the stifled facility of anti-canopy, and slaked lime powder enters batcher, and the rotary feeder motor adopts VFC, slaked lime powder dosage and the proportional adjusting of depositing reservoir inlet flow rate.Wherein the pulverized limestone batcher is selected import equipment for use, accurate measurement, and maintenance is little.

Dry powder metering, the concentration that changes lime slurry is to realize metering, and is accurately simple, and control easily is one of characteristics of native system.Like this, can keep pipeline sodalime breast under nominal flow rate, to move, with the wearing and tearing of avoiding changes in flow rate to cause.

Slaked lime powder is after metering delivered to the vapour powder separator on the top of lime agitator tank via conveying worm, dry powder meets and separated at vapour powder separator with the steam of discharging when entering agitator tank, and powder falls into case, and steam then drains into outside the case.Powder mixes, stirs, is dissolved into milk of lime with the clear water that enters from auxiliary water tank in agitator tank, is sent to depositing reservoir by Lime Milk Transfer Pump.

Calcium hydroxide is stored, metering, system breast, add and be the unit configuration, and each overlaps every depositing reservoir with one, and Lime Milk Transfer Pump 100% is standby.

Whole process automation control is another characteristics of native system.The vibrations hopper of lime silo blanking can block up to avoid down grey manteau according to regularly anti-clogging concussion of grey matter.But the start and stop of milk of lime dosing unit, Lime Milk Transfer Pump all program are operated, and each step all cleans up the inactive part of this system automatically.

All system and equipment are in the air-tight state operation, and the axle head of rotary machine etc. locates all to take lubricated and flushing measure, to alleviate wearing and tearing and to leak.

Establish 1 suspended sediment concentration meter in the Mixed Zone 1,1 cover floating-ball level switch.

Depositing reservoir

Depositing reservoir comprises that flocculation reaction zone 2 and precipitation concentrate zone 3.

Flocculation reaction zone 2

The abundant mixed pending liquid that comes from water channel 13 enters current stabilization district 21 by the bottom distributing hole, by the rectification of water distribution weir after inlet channel 22 enters mechanical flocculation zone 23, under the effect of agitator 25, evenly mix, flocculate with the high molecular polymer, the backflow deposit that add, produce alumen ustum uniformly densely.The alumen ustum that the machinery flocculation zone produces further increases in plug-flow flocculation zone 24 and is closely knit.

The design time of staying suggestion of the pending liquid that mixes in the flocculation reaction zone for 10min~20min (minute), the decision design time of staying be 10min~15min (minute).

The dosage of high molecular polymer should be determined according to pending liquid water quality.

Precipitation concentrates zone 3

Pending liquid after the flocculation at first enters preliminary sedimentation district 31, behind this zone precipitation part suspended solid, enter holey separator 32, carry out separating of supernatant and suspended solid, supernatant enters filtration zone 4, the suspended solid of holding back enters enrichment region 33, strikes off gathering-device 34 at this bottom, district installing deposit, and deposit is concentrated, deposit after concentrating is back to mechanical flocculation zone 23 via a conveying device part, and a part is disposed to outside the system.

The design upflow velocity suggestion of holey separator 32 is 10m/h~30m/h (meter/hour), and preferred upflow velocity is 10m/h~20m/h (meter/hour).

Precipitation concentrates zone 3 and comprises:

Be provided with a water leg device that is used to collect supernatant at an upper portion thereof, these devices are uniformly distributed in holey separator 32 tops;

Holey separator 32 belows are enrichment region 33, are provided with into the bucket-shaped V-type Sludge Bed 37 of awl in enrichment region 33 bottoms, are used for the concentrating and precipitating material, a deposit is set on it strikes off gathering-device 34.

Filtration zone 4

Supernatant behind the coagulation enters water distributing area 41, and can add sulfuric acid, coagulant, and coagulant can be selected molysite or aluminium salt.Mixed supernatant is introduced influent weir chamber 42, and current stabilization is laggard goes into body region 43, and mixed supernatant carries out deep-bed filtration in body region 43, is collected after exhalant region 44 enters next step handling process by collecting system of being located at this bottom, district.

Body region 43 is provided with the filter that is used for fluid purification, have unlimited pond, a inside to be provided with and be provided with water and air distributing device below supporting layer and filtering material, the supporting layer, filter also comprises and is used to introduce behind the coagulation supernatant and discharges the turnover mill weir chamber of cleaning solution, the device of washing and filtering material, a fluid level control device of discharging filtered fluid.This device is characterised in that: the porosity with the filtering material of this drag flow depth-type filtration device of " flocculation " in the same way theoretical design adopts constant fluid level control device at the fluid level control device that vertically changes, discharges filtered fluid on the height, introduces liquid to be filtered and discharges cleaning solution all by passing in and out the mill weir chamber.

The suggestion of filtering area flow rate of liquid is 10~18m/h (meter/hour), and the decision design flow velocity is 10-14.5m/h (meter/hour).

The mode of combined water and air backwash is adopted in the flushing of filtering material.

Equipment of the present invention as shown in Figure 1, concrete structure such as Fig. 2-shown in Figure 13, be one embodiment of the present of invention here: equipment of the present invention is by Mixed Zone 1, depositing reservoir and filtration zone 4.

Mixed Zone 1

Mixed Zone 1 specifically comprises overflow area 16, irrigation channel 11, mixed zone 12 and goes out water channel 13, is provided with agitator 14 in the mixed zone 12, and sewage, milk of lime, coagulant are fully mixed.Establish 1 suspended sediment concentration meter in the Mixed Zone 1,1 cover floating-ball level switch.

Depositing reservoir

Depositing reservoir comprises that flocculation reaction zone 2 and precipitation concentrate zone 3.

Flocculation reaction zone 2 mainly comprises current stabilization district 21, inlet channel 22, mechanical flocculation zone 23 and plug-flow flocculation zone 24; Be provided with agitator 25 in the wherein mechanical flocculation zone 23.

Precipitation concentrates zone 3 and mainly comprises preliminary sedimentation district 31, inclined tube Disengagement zone and enrichment region 33; Wherein enrichment region 33 bottoms are provided with mud scraper, are provided with V-type Sludge Bed 37 in the lower floor of mud scraper, and are provided with deposit return duct 35 and deposit delivery pipe 36.

In enrichment region 33, also be provided with mud level meter 38.

Deposit return duct 35 and deposit delivery pipe 36 must be connected with deposit backflow/tapping equipment respectively.

Filtration zone 4

Filtration zone 4 mainly comprises

Supernatant behind the coagulation enters water distributing area 41, influent weir chamber 42, body region 43 and exhalant region 44.Body region 43 has filtering material to carry out deep-bed filtration.

Backwash water inlet collector pipe and compressed air distributing pipe also are housed in the body region 43 of filtration zone 4.

Lime is joined the throwing system specialization

The powdery calcium hydroxide is transported by closed tank truck, and strength is unloaded ash.Gas drains into atmosphere after being separated by the head space gas powder.The ash hole place is provided with the stifled facility of anti-canopy.Wherein the pulverized limestone batcher is selected import equipment for use, accurate measurement, and maintenance is little.

Dry powder metering, the concentration that changes lime slurry is to realize metering, and is accurately simple, and control easily is one of characteristics of native system.Like this, can keep pipeline sodalime breast under nominal flow rate, to move, with the line clogging of avoiding changes in flow rate to cause.Slaked lime powder enters batcher, and with metering pulverized limestone amount, the batcher powder delivering amount adopts variable frequency adjustment, can be according to the proportional adjusting slaked lime powder of depositing reservoir inlet flow rate dosage.

Slaked lime powder after the metering is delivered to the lime agitator tank via conveying worm and vapour powder separator, and dry powder enters agitator tank, meets and separated at vapour powder separator with steam, and powder falls into case, and steam then drains into outside the case.Powder mixes, stirs, is dissolved into milk of lime with the clear water that enters from auxiliary water tank in agitator tank, is sent to by Lime Milk Transfer Pump to add a little.

Calcium hydroxide is stored, metering, system breast, add and be the unit configuration, and each overlaps every depositing reservoir with one, and Lime Milk Transfer Pump 100% is standby.

Whole process automation control is another characteristics of native system.The vibrations hopper of lime silo blanking can regularly shake according to grey matter, to avoid fluffy stifled.But the start and stop of milk of lime dosing unit, Lime Milk Transfer Pump all program are operated.

All system and equipment are in the air-tight state operation, and the axle head of rotary machine etc. is located all to take appropriate measures, to alleviate wearing and tearing and to leak.

Claims (35)

1. the purification method of recirculated cooling water or town B-grade sewage is characterized in that, pass through following several steps:
A. pending liquid is introduced Mixed Zone (1), add plurality of reagents, and reagent and pending liquid are mixed, described plurality of reagents is lime medicament and one or more coagulant;
The pending liquid that b. will mix carries out high speed in the flow velocity that supernatant rises is 10~30 meters/hour depositing reservoir clarifies, and the supernatant that obtains is drawn;
C. above-mentioned supernatant is introduced filtration zone (4), filling filtering material in the filtration zone (4).
2. the purification method of recirculated cooling water according to claim 1 or town B-grade sewage, it is characterized in that, after described pending liquid entered the mixed zone (12) of Mixed Zone (1), pending liquid designs the time of staying in mixed zone (12) be 30~240 seconds.
3. the purification method of recirculated cooling water according to claim 2 or town B-grade sewage is characterized in that, described pending liquid designs the time of staying in mixed zone (12) be 45~180 seconds.
4. the purification method of recirculated cooling water according to claim 1 or town B-grade sewage, it is characterized in that, described lime medicament is by the lime device it to be joined in the Mixed Zone (1), and the lime device adopts dry powder metering, modular arrangements, whole process automation control and airtight operation.
5. the purification method of recirculated cooling water according to claim 4 or town B-grade sewage, it is characterized in that, described dry powder metering is the amount of directly measuring dry powder, realizes that by the dosage that changes dry powder the ratio of lime dosage and depositing reservoir inlet water flow is regulated.
6. the purification method of recirculated cooling water according to claim 4 or town B-grade sewage, it is characterized in that, described whole process automation control, be that make up a prescription unit, milk of lime of milk of lime added the unit and control automatically, comprise automatic operation and automatic control cleaning, the vibrations hopper of setting the lime silo blanking is simultaneously avoided system jams according to regularly anti-clogging concussion of grey matter.
7. the purification method of recirculated cooling water according to claim 1 or town B-grade sewage is characterized in that, described coagulant is a liquid polymerization ferric sulfate, and dosage is 10~15 mg/litre.
8. the purification method of recirculated cooling water according to claim 1 or town B-grade sewage, it is characterized in that, described step b. depositing reservoir comprises that flocculation reaction zone (2) and precipitation concentrate zone (3), clarification comprises that the pending liquid that mixes is in the flocculation reaction of flocculation reaction zone (2) with in the rapid precipitation that precipitates concentrated zone (3).
9. the purification method of recirculated cooling water according to claim 8 or town B-grade sewage, it is characterized in that, described flocculation reaction, be to adopt circulating granular to quicken flocculation to mixed uniform pending liquid, with multistage flocculation reaction, to reduce the best flocculation reaction time, its pending liquid is 10~20 minutes in this region design time of staying.
10. the purification method of recirculated cooling water according to claim 9 or town B-grade sewage is characterized in that, pending liquid is 10~15 minutes in this region design time of staying, is 1/3~1/2 of the conventional flocculation reaction time.
11. purification method according to claim 9 or 10 described recirculated cooling waters or town B-grade sewage, it is characterized in that, described employing circulating granular quickens flocculation, is the uniform pending liquid, the partly precipitated material is recycling and control the interior settling velocity gradient in flocculation reaction zone (2) at 250~450 seconds with the control water velocity after mixing with mechanical stirring device -1Scope, and add high molecular polymer, to realize the further closely knit of flocculation reaction product, improve the sinking speed of flocculation reaction product.
12. purification method according to claim 9 or 10 described recirculated cooling waters or town B-grade sewage, it is characterized in that, described multistage flocculation reaction comprises secondary flocculation reaction at least, and first order flocculation reaction is mechanical flocculation reaction, and second level flocculation reaction is the waterpower flocculation reaction.
13. the purification method of recirculated cooling water according to claim 8 or town B-grade sewage is characterized in that, described clarification, and the flow velocity that its supernatant rises is 10~20 meters/hour.
14. the purification method of recirculated cooling water according to claim 8 or town B-grade sewage, it is characterized in that, described precipitation comprises that treating treatment fluid carries out preformed precipitate and handle, treat the control method that the deposit interface of treatment fluid is controlled, clarified and be similar to the discrete particle sedimentation with the holey separator.
15. the purification method of recirculated cooling water according to claim 14 or town B-grade sewage, it is characterized in that, described deposit interface is controlled, be the pending liquid after the flocculation to be introduced precipitation concentrate zone (3), the suspended solid of holding back enters enrichment region (33), and in precipitation concentrates zone (3), deposit is set and strikes off gathering-device, deposit interface sniffer and deposit tapping equipment, its deposit strike off the signal controlling deposit tapping equipment that gathering-device provides according to deposit interface sniffer, deposit strikes off the operation of gathering-device.
16. the purification method of recirculated cooling water according to claim 14 or town B-grade sewage, it is characterized in that, described with the clarification of holey separator, be that pending liquid is risen by holey separator (32), obtain supernatant, the hydraulic radius of holey separator and setting height(from bottom) are determined according to the water quality index of pending liquid.
17. the purification method of recirculated cooling water according to claim 14 or town B-grade sewage, it is characterized in that, the control method of described approximate discrete particle sedimentation is to concentrate the Reynolds number in zone (3) and surface of solids load and make solid particles sediment speed after the flocculation reaction near the sinking speed of discrete particle by adjusting precipitation.
18. the purification method of recirculated cooling water according to claim 8 or town B-grade sewage is characterized in that, described depositing reservoir, and the deposit concentration of its discharging reaches 20~100mg/L, and directly dehydration need not concentration.
19. the purification method of recirculated cooling water according to claim 1 or town B-grade sewage, it is characterized in that, described step c is introduced filtration zone (4) with above-mentioned supernatant, be filled with the filtering material of porosity in the filtration zone (4) along Cheng Bianhua, be the water distributing area (41) of earlier above-mentioned supernatant being introduced filtration zone (4), enter influent weir chamber (42), filtration zone (4) body region (43) and outlet system (44) more successively; Supernatant carries out deep-bed filtration in filtration zone (4) body region (43).
20. the purification method of recirculated cooling water according to claim 1 or town B-grade sewage is characterized in that, the design current velocity of the filtration zone of described step c (4) is 10~18 meters/hour.
21. the purification method of recirculated cooling water according to claim 20 or town B-grade sewage is characterized in that, the design current velocity of filtration zone (4) is 10~14.5 meters/hour.
22. the purification method of recirculated cooling water according to claim 19 or town B-grade sewage is characterized in that, described water distributing area (41) adds sulfuric acid or/and coagulant, and fully mixes.
23. the purification method of recirculated cooling water according to claim 19 or town B-grade sewage is characterized in that, the body region (43) of described filtration zone (4), and porosity of the filtering material of filling is along Cheng Bianhua in it.
24. the purification method of recirculated cooling water according to claim 23 or town B-grade sewage is characterized in that, the mode of combined water and air backwash is adopted in the washing of described filtering material.
25. the purification method of recirculated cooling water according to claim 19 or town B-grade sewage is characterized in that, described filtration zone (4) body region (43) adopts permanent liquid level drag flow deep-bed filtration.
26. the purification method of recirculated cooling water according to claim 22 or town B-grade sewage is characterized in that, described coagulant is molysite or aluminium salt.
27. application rights requires the cleaning equipment of 1 described recirculated cooling water or town B-grade sewage purification method, it is characterized in that, it comprises that mainly Mixed Zone (1), supernatant upflow velocity are 10~30 meters/hour depositing reservoir and filtration zone (4), between Mixed Zone (1) and the depositing reservoir, the supernatant upflow velocity is to have water channel to connect between 10~30 meters/hour depositing reservoir and the filtration zone (4).
28. the cleaning equipment of recirculated cooling water according to claim 27 or town B-grade sewage is characterized in that, described supernatant upflow velocity is that 10~30 meters/hour depositing reservoir is divided into flocculation zone (2) and precipitation concentrates zone (3).
29. the cleaning equipment of recirculated cooling water according to claim 28 or town B-grade sewage, it is characterized in that, described flocculation zone (2) comprises current stabilization district (21), inlet channel (22), mechanical flocculation zone (23) and plug-flow flocculation zone (24) again successively, and agitator (25) is arranged in the wherein mechanical flocculation zone (23).
30. the cleaning equipment of recirculated cooling water according to claim 28 or town B-grade sewage, it is characterized in that, described precipitation concentrates (3) top, zone and is provided with the holey separator, and (3) bottom, the concentrated zone of precipitation is provided with deposit and strikes off gathering-device.
31. the cleaning equipment of recirculated cooling water according to claim 27 or town B-grade sewage is characterized in that, described filtration zone (4) comprises water distributing area (41), influent weir chamber (42), body region (43) and exhalant region (44).
32. the cleaning equipment of recirculated cooling water according to claim 31 or town B-grade sewage, it is characterized in that, described body region (43) is a drag flow deep-bed filtration device, promptly is provided with filtering material and supporting layer in the body region (43), under the supporting layer water and air distributing device is housed.
33. the cleaning equipment of recirculated cooling water according to claim 31 or town B-grade sewage is characterized in that, described body region (43) also comprises the washing and filtering device and discharges the constant fluid level control device of filtered fluid.
34. the cleaning equipment of recirculated cooling water according to claim 27 or town B-grade sewage is characterized in that, described Mixed Zone is provided with the suspended sediment concentration meter in (1).
35. the cleaning equipment of recirculated cooling water according to claim 27 or town B-grade sewage is characterized in that, is provided with a plurality of reagent dispensers in described Mixed Zone (1).
CNB2007100999699A 2007-06-01 2007-06-01 Method and equipment for purifying recirculated cooling water or town B-grade sewage CN100415338C (en)

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