WO2016058437A1 - 一种污泥深度脱水的处理方法 - Google Patents

一种污泥深度脱水的处理方法 Download PDF

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WO2016058437A1
WO2016058437A1 PCT/CN2015/085666 CN2015085666W WO2016058437A1 WO 2016058437 A1 WO2016058437 A1 WO 2016058437A1 CN 2015085666 W CN2015085666 W CN 2015085666W WO 2016058437 A1 WO2016058437 A1 WO 2016058437A1
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sludge
water
minutes
added
waste
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English (en)
French (fr)
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谭忠冠
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谭忠冠
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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
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/06—Treatment of sludge; Devices therefor by oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
    • C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
    • C02F11/148—Combined use of inorganic and organic substances, being added in the same treatment step
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/06—Sludge reduction, e.g. by lysis

Definitions

  • the invention relates to a treatment method for deep dewatering of sludge generated by urban sewage treatment plants and sewage treatment, and belongs to the technical field of sludge dewatering technology.
  • the excess sludge of water content is also the secondary pollutant in the sewage treatment process.
  • the sludge contains a large number of pathogenic bacteria, parasites, pathogenic microorganisms, and heavy metals such as arsenic, copper, chromium, and mercury, and toxic and harmful substances such as dioxins and radionuclides that are difficult to degrade, due to high moisture content of the sludge. It is bulky and poses difficulties for stacking and transportation. If the urban sludge is improperly disposed or treated irregularly, such as the abandonment of farmland abuse, it will pose a serious potential threat to the ecological environment. On the other hand, the excess sludge contains high organic nutrient and combustion value.
  • lime quenching and tempering process lime dosage rate is 20% to 30%, lime dosage is increased by large sludge, sludge volume is large, and production cycle is long.
  • the mud cake and the filtrate are alkaline, and the filtrate needs to be adjusted to pH value.
  • the anti-corrosion requirements of the equipment are also high, and the operation cost is high.
  • Sludge dosing modification generally uses chemicals to condition the sludge. There is no substantial change in the sludge. Reducing the moisture content of the sludge depends on the improvement of mechanical equipment.
  • Sludge dosing and modification technology is divided into sludge mold micelle sedimentation performance modification and sludge bacteria micelle bacteria modification.
  • sludge sedimentation performance modification sludge dewatering rate can only be reduced to about 65%, and conditioning
  • the total addition amount of the agent accounts for more than 20% of the dry basis of the sludge, and the problem of sludge capacity increase is serious. In fact, the sludge reduction is not realized. Due to the high moisture content of the sludge, the hot value of the sludge can not maintain the dry sludge operation of the sludge.
  • the external energy source needs to be increased, the energy consumption is large, and the operating cost is high.
  • the electro-osmosis dry method has disadvantages such as high investment in equipment, high operating cost, and high maintenance requirements of equipment. These methods are not required to meet the requirements of the fact that the water content cannot meet the requirements or the operating cost is too high or the sludge capacity is increased.
  • the current problem of deep dewatering of sludge is that the existing conditioning agent has high cost, large dosage, complicated conditioning process, high equipment investment and running cost, and no sludge reduction, which easily affects the sludge. Disadvantages such as regeneration or subsequent use, poor environmental benefits.
  • the object of the present invention is to provide an environmentally-friendly and deep dehydration treatment method for sludge generated by urban sewage treatment plants and sewage treatment.
  • the invention provides a method for treating deep dewatering of sludge, which is characterized in that: under normal temperature and normal pressure, the waste water is pretreated by adding waste sulfuric acid, O 3 and FeCl 3 in the sludge to be treated; Then, by adding Fe 2 (SO 4 ) 3 and PAM (polyacrylamide) to strengthen the solidification, the coagulation and sedimentation treatment is carried out; finally, the water is dehydrated by a filter press to finally reduce the moisture content of the sludge to less than 50%.
  • the method for treating deep dewatering of sludge comprises the following specific steps:
  • Sludge quenching and tempering In the oxidative membrane-breaking reaction tank composed of two small pools, the sludge to be treated is first extracted into the first small tank, and waste sulfuric acid and O 3 are added to have a water content of 90-99.9.
  • % sludge meter, waste sulfuric acid and O 3 are added in the amount of 10 ⁇ 100g / t wet mud, 1 ⁇ 10g / t wet mud, after stirring reaction, the sludge mixture is extracted into the second small pool, adding FeCl 3 , based on the sludge with a water content of 90 to 99.9%, the amount of FeCl 3 added is 10 ⁇ 100g / t wet mud, and then stirred to achieve the oxidative cracking of the sludge micelle structure and the bacterial cell membrane, so that A large amount of structural water, water-in-water and unit cell water in the sludge become interstitial water; the sludge mixture treated by the oxidation and membrane-breaking reaction tank enters the flocculation reaction tank, and Fe 2 (SO 4 ) 3 and PAM are added to contain water.
  • the addition amount of Fe 2 (SO 4 ) 3 and PAM is 10 to 100 g/t wet mud and 1 to 4 g/t wet mud, respectively, and then stirred to react.
  • the hydration product of the condensed nature forms a network structure between the sludge particles, which constitutes the skeleton of the sludge, and the hydrated product of the crystals fills the pores of the network structure to make the sludge Portion becomes dense, greatly improving water stability and strength stability sludge;
  • Step (2) the sludge adjusted in step (1) is sent to a sedimentation tank for standing;
  • the mass concentration of the waste sulfuric acid in the step (1) is 98%
  • the pH is controlled at 6 to 6.5
  • the O 3 , FeCl 3 and Fe 2 (SO 4 ) 3 are compressed air and waste iron scraps.
  • the waste sulfuric acid and the waste hydrochloric acid are prepared by a reaction, and the stirring reaction time is 10 to 20 minutes; the standing time in the step (2) is 20 to 30 minutes; and the filter press in the step (3) is Plate and frame filter press.
  • the invention aims to solve the problem that the water of the bacterial floc organic floc and the internal water of the microbial mass are used to study the high-energy electrons at the interface of sg and sl and the residual sludge micelle under normal temperature and pressure.
  • the structural bond bond orbital symmetry transfer realizes the oxidative cracking of the sludge micelle structure and the bacterial cell membrane, so that a large amount of structural water, water-in-water and unit cell water in the sludge become interstitial water, and then the solidified coagulating agent is added.
  • Waste sulfuric acid and O 3 as oxidation oxidizer can hydrolyze extracellular polymer in activated sludge and disintegrate microbial cells, which can effectively realize the oxidative cracking of sludge micelle structure and bacterial cell membrane, and make a large amount of structural water in sludge.
  • the water inhalation and the unit cell water are released to become interstitial water, thereby improving the degree of dehydration and achieving a good dehydration effect in a short period of time.
  • Deodorization and sterilization are achieved by destroying cell-based cell walls and cellular tissues of enzymes, acidic RNA, and carbohydrates.
  • FeCl 3 and Fe 2 (SO 4 ) 3 act as flocculants, and the iron ions are hydrolyzed to form a colloidal hydroxyl polymer or hydroxide precipitate.
  • the floc particles with bearing capacity, PAM as a coagulant can make the sludge form a porous network skeleton, improve the compressibility of the sludge and enhance the strength of the flocs.
  • the medicaments O 3 , FeCl 3 and Fe 2 (SO 4 ) 3 used in the invention can be prepared by a series of chemical reactions using compressed air, waste iron scraps, waste sulfuric acid and waste hydrochloric acid as raw materials, thereby greatly reducing the processing operation. cost.
  • the medicament provided by the invention can release the bound water inside the sludge floc, can change the surface charge of the sludge, promote the hydrolysis of the extracellular polymer (EPS), and reduce the affinity for water. In addition, it can also induce the conversion of sludge capillary water to free water in the sludge gap, reduce the viscosity of the sludge, and realize the deep dewatering of the sludge by the conventional plate and frame filter press.
  • EPS extracellular polymer
  • the present invention has the following features and advantages:
  • the excess sludge in the sewage plant is deeply dewatered under normal conditions to achieve the sludge deep treatment reduction: the method of the present invention realizes the in-situ treatment of the sludge of the sewage treatment plant, and the remaining water content is 90-99.5% under normal conditions.
  • the sludge is dewatered in one step to a moisture content of less than 50%, which meets the national environmental protection standards for direct sanitary landfill, and is in compliance with the “Notice on Strengthening the Prevention and Control of Sludge Pollution in Urban Sewage Treatment Plants” issued by the General Office of the Ministry of Environmental Protection in 2010 (Environmental Office [ 2010] No. 157).
  • the sludge is stable in nature and convenient for resource utilization: the chemical properties of the sludge change after oxidative dehydration, the particle agglomeration increases, the stability is improved, the solution is not dissolved, and the water does not swell. All the indicators are in line with GB/T23485 ⁇ 2009, which can be used as landfill for soil shale; the moisture content of sludge after deep treatment by the method of the invention is less than 50%, and no additives such as CaO affecting the calorific value of sludge are added.
  • the organic matter in the domestic dry sludge base is 35-65%, and the corresponding combustion value is 1800-3600 kcal. Therefore, the dry sludge is widely used as a fuel substitute for thermal power plants or cement plants and brick factories.
  • the raw materials used in the method of the present invention are compressed air and waste iron scrap, waste sulfuric acid, and waste hydrochloric acid, the operating cost is low, and the current moisture content is 80% according to Yangjiang City, Guangdong province (where the applicant's test base is located).
  • the treatment cost per ton of absolute dry sludge is about 2,300 yuan / ton; the treatment cost of the method of the invention is about 550 yuan / ton, and the water content of 80% wet sludge is 110 yuan per ton.
  • the method of the invention is used to complete the deep dewatering of the excess sludge, and the investment in the original sewage treatment plant (based on 50,000 tons/day sewage treatment capacity) is increased by about 4 million yuan (mid-range configuration, including spare ), wherein the pressure filtration operation is simple, the filter cloth has a long service life and low cost, and each set is 2,000 yuan (200 m 2 filtration system), which is convenient for cleaning.
  • the sludge advanced treatment system is completed in just three months from the start of construction to the commissioning, and the effect is quick.
  • FIG. 1 is a flow chart showing a process for deep dewatering of sludge according to an embodiment of the present invention.
  • O 3 , FeCl 3 and Fe 2 (SO 4 ) 3 are prepared by a reaction using compressed air, waste iron scrap, waste sulfuric acid, and waste hydrochloric acid.
  • oxidative membrane-breaking reaction tank composed of two small pools, 1t of excess sludge with a water content of 99.7% was extracted into the first small tank, and 30% of 98% of waste sulfuric acid (pH controlled at 6.5) and 2g of O 3 were respectively added and stirred. Reaction for 10 minutes.
  • the sludge mixture was introduced into another small tank, and 50 g of FeCl 3 solution was added thereto, and the reaction was stirred for 10 minutes.
  • the sludge mixture enters the flocculation reaction tank, 50 g of Fe 2 (SO 4 ) 3 solution is added, and 2 g of PAM is added, and the reaction is stirred for 20 minutes. Then, it was allowed to stand in the sedimentation tank for 30 minutes, and the precipitate was concentrated.
  • the concentrated sludge is extracted from the bottom of the sedimentation tank, introduced into the plate and frame filter press for pressure filtration and dehydration, and maintained at a pressure of 1.2 MPa for 40 minutes. After the pressure is completed, the pressure relief material is discharged, and a dry mud cake having a water content of 49.8% is obtained. .
  • O 3 , FeCl 3 and Fe 2 (SO 4 ) 3 are prepared by a reaction using compressed air, waste iron scrap, waste sulfuric acid, and waste hydrochloric acid.
  • oxidative membrane-breaking reaction tank composed of two small pools, 1t of excess sludge with a moisture content of 99.7% was extracted into the first small tank, and 30% of 98% of waste sulfuric acid (pH controlled at 6.5) and 3g of O 3 were respectively added and stirred. Reaction for 10 minutes.
  • the sludge mixture was introduced into another small tank, and 50 g of FeCl 3 solution was added thereto, and the reaction was stirred for 10 minutes.
  • the sludge mixture enters the flocculation reaction tank, 50 g of Fe 2 (SO 4 ) 3 solution is added, and 2 g of PAM is added, and the reaction is stirred for 20 minutes. Then, it was allowed to stand in the sedimentation tank for 30 minutes, and the precipitate was concentrated.
  • the concentrated sludge is taken out from the bottom of the sedimentation tank, introduced into the plate and frame filter press for pressure filtration and dehydration, and maintained at a pressure of 1.2 MPa for 40 minutes. After the pressure is completed, the pressure relief material is discharged, and a dry mud cake having a water content of 48.3% is obtained. .
  • O 3 , FeCl 3 and Fe 2 (SO 4 ) 3 are prepared by a reaction using compressed air, waste iron scrap, waste sulfuric acid, and waste hydrochloric acid.
  • oxidative membrane-breaking reaction tank composed of two small pools, 1t of residual sludge with a moisture content of 99.7% was extracted into the first small tank, and 98% of 98% of waste sulfuric acid (pH controlled at 6.5) and 4g of O 3 were respectively added and stirred. Reaction for 10 minutes.
  • the sludge mixture was introduced into another small tank, 70 g of FeCl 3 solution was added, and the reaction was stirred for 10 minutes.
  • the sludge mixture enters the flocculation reaction tank, and 70 g of Fe 2 (SO 4 ) 3 solution is added thereto, and 2 g of PAM is added thereto, and the reaction is stirred for 20 minutes. Then, it was allowed to stand in the sedimentation tank for 25 minutes, and the precipitate was concentrated. The concentrated sludge was taken out from the bottom of the sedimentation tank, introduced into a plate and frame filter press for pressure filtration dehydration, and maintained at a pressure of 1.3 MPa for 30 minutes, and the pressure relief was discharged after the pressure was completed. A dry mud cake having a moisture content of 46.6% is obtained.
  • O 3 , FeCl 3 and Fe 2 (SO 4 ) 3 are prepared by a reaction using compressed air, waste iron scrap, waste sulfuric acid, and waste hydrochloric acid.
  • oxidative membrane-breaking reaction tank composed of two small pools, 1t of excess sludge with a moisture content of 99.7% was extracted into the first small tank, and 98% of 98% of waste sulfuric acid (pH controlled at 6.5) and 5g of O 3 were respectively added and stirred. Reaction for 10 minutes.
  • the sludge mixture was introduced into another small tank, 70 g of FeCl 3 solution was added, and the reaction was stirred for 10 minutes.
  • the sludge mixture enters the flocculation reaction tank, and 70 g of Fe 2 (SO 4 ) 3 solution is added thereto, and 2 g of PAM is added thereto, and the reaction is stirred for 20 minutes. Then, it was allowed to stand in the sedimentation tank for 25 minutes, and the precipitate was concentrated.
  • the concentrated sludge is taken out from the bottom of the sedimentation tank, introduced into the plate and frame filter press for pressure filtration and dehydration, and maintained at a pressure of 1.3 MPa for 30 minutes. After the pressure is maintained, the pressure relief material is discharged, and a dry mud cake having a water content of 45.4% is obtained. .
  • O 3 , FeCl 3 and Fe 2 (SO 4 ) 3 are prepared by a reaction using compressed air, waste iron scrap, waste sulfuric acid, and waste hydrochloric acid.
  • oxidative membrane-breaking reaction tank composed of two small pools, 1t of excess sludge with a moisture content of 99.7% was extracted into the first small tank, and 98% of 98% of waste sulfuric acid (pH controlled at 6.5) and 5g of O 3 were respectively added and stirred. Reaction for 10 minutes.
  • the sludge mixture was introduced into another small tank, 70 g of FeCl 3 solution was added, and the reaction was stirred for 10 minutes.
  • the sludge mixture enters the flocculation reaction tank, and 70 g of Fe 2 (SO 4 ) 3 solution is added thereto, and 2 g of PAM is added thereto, and the reaction is stirred for 20 minutes. Then, it was allowed to stand in the sedimentation tank for 25 minutes, and the precipitate was concentrated.
  • the concentrated sludge is extracted from the bottom of the sedimentation tank, introduced into the plate and frame filter press for pressure filtration and dehydration, and maintained at a pressure of 1.4 MPa for 40 minutes. After the pressure is completed, the pressure relief material is discharged, and a dry mud cake having a water content of 45.4% is obtained. .
  • FeCl 3 and Fe 2 (SO 4 ) 3 are prepared by a reaction using compressed air, waste iron scrap, waste sulfuric acid, and waste hydrochloric acid.
  • oxidative membrane-breaking reaction tank consisting of two small pools, 1t of excess sludge with a moisture content of 99.7% was extracted into the first small tank, and 98% of 98% waste sulfuric acid (pH controlled at 6.5) and 6gO 3 were added respectively. Reaction for 10 minutes.
  • the sludge mixture was introduced into another small tank, 80 g of FeCl 3 solution was added, and the reaction was stirred for 10 minutes.
  • the sludge mixture enters the flocculation reaction tank, 80 g of Fe 2 (SO 4 ) 3 solution is added, and 3 g of PAM is added, and the reaction is stirred for 20 minutes. Then, it was allowed to stand in the sedimentation tank for 25 minutes, and the precipitate was concentrated.
  • the concentrated sludge is taken out from the bottom of the sedimentation tank, introduced into the plate and frame filter press for pressure filtration dehydration, and maintained at a pressure of 1.4 MPa for 40 minutes. After the pressure is completed, the pressure relief material is discharged, and a dry mud cake having a water content of 43.5% is obtained. .
  • FeCl 3 and Fe 2 (SO 4 ) 3 are prepared by a reaction using compressed air, waste iron scrap, waste sulfuric acid, and waste hydrochloric acid.
  • oxidative membrane-breaking reaction tank composed of two small pools, 1t of excess sludge with a moisture content of 99.7% was extracted into the first small tank, and 98% of 98% of waste sulfuric acid (pH controlled at 6.5) and 7gO 3 were added respectively. Reaction for 10 minutes.
  • the sludge mixture was introduced into another small tank, 80 g of FeCl 3 solution was added, and the reaction was stirred for 10 minutes.
  • the sludge mixture enters the flocculation reaction tank, 80 g of Fe 2 (SO 4 ) 3 solution is added, and 3 g of PAM is added, and the reaction is stirred for 20 minutes. Then, it was allowed to stand in the sedimentation tank for 25 minutes, and the precipitate was concentrated.
  • the concentrated sludge is taken out from the bottom of the sedimentation tank, introduced into the plate and frame filter press for pressure filtration and dehydration, and maintained at a pressure of 1.5 MPa for 40 minutes. After the pressure is completed, the pressure relief material is discharged, and a dry mud cake having a water content of 41.2% is obtained. .
  • O 3 , FeCl 3 and Fe 2 (SO 4 ) 3 are prepared by a reaction using compressed air, waste iron scrap, waste sulfuric acid, and waste hydrochloric acid.
  • oxidative membrane-breaking reaction tank composed of two small pools, 1t of residual sludge with a moisture content of 99.7% was extracted into the first small tank, and 98% of 98% of waste sulfuric acid (pH controlled at 6.5) and 8g of O 3 were respectively added and stirred. Reaction for 10 minutes. The sludge mixture enters another small tank, and 90 g of FeCl 3 solution is added thereto, and the reaction is stirred for 10 minutes.
  • the sludge mixture enters the flocculation reaction tank, and 90 g of Fe 2 (SO 4 ) 3 solution is added thereto, and 3 g of PAM is added thereto, and the reaction is stirred for 20 minutes. Then, it was allowed to stand in the sedimentation tank for 30 minutes, and the precipitate was concentrated. The concentrated sludge was taken out from the bottom of the sedimentation tank, introduced into a filter press for pressure filtration dehydration, and maintained at a pressure of 1.5 MPa for 35 minutes. After the pressure retention was completed, the pressure relief material was discharged, and a dry mud cake having a water content of 39.6% was obtained.
  • FeCl 3 and Fe 2 (SO 4 ) 3 are prepared by a reaction using compressed air, waste iron scrap, waste sulfuric acid, and waste hydrochloric acid.
  • oxidative membrane-breaking reaction tank composed of two small pools, 1t of excess sludge with a moisture content of 99.7% was extracted into the first small tank, and 98% of 98% of waste sulfuric acid (pH controlled at 6.5) and 9gO 3 were respectively added and stirred. Reaction for 10 minutes. The sludge mixture enters another small tank, and 90 g of FeCl 3 solution is added thereto, and the reaction is stirred for 10 minutes.
  • the sludge mixture enters the flocculation reaction tank, and 90 g of Fe 2 (SO 4 ) 3 solution is added thereto, and 3 g of PAM is added thereto, and the reaction is stirred for 20 minutes. Then, it was allowed to stand in the sedimentation tank for 30 minutes, and the precipitate was concentrated.
  • the concentrated sludge is taken out from the bottom of the sedimentation tank, introduced into the plate and frame filter press for pressure filtration and dehydration, and maintained at a pressure of 1.6 MPa for 35 minutes. After the pressure is maintained, the pressure relief material is discharged, and a dry mud cake having a water content of 38.9% is obtained. .
  • O 3 , FeCl 3 and Fe 2 (SO 4 ) 3 are prepared by a reaction using compressed air, waste iron scrap, waste sulfuric acid, and waste hydrochloric acid.
  • oxidative membrane-breaking reaction tank composed of two small pools, 1t of excess sludge with a moisture content of 99.7% was extracted into the first small tank, and 98% of 98% of waste sulfuric acid (pH controlled at 6.5) and 10g of O 3 were added respectively. Reaction for 10 minutes.
  • the sludge mixture was introduced into another small tank, 100 g of FeCl 3 solution was added, and the reaction was stirred for 10 minutes.
  • the sludge mixture enters the flocculation reaction tank, 100 g of Fe 2 (SO 4 ) 3 solution is added, and 4 g of PAM is added, and the reaction is stirred for 20 minutes. Then, it was allowed to stand in the sedimentation tank for 30 minutes, and the precipitate was concentrated.
  • the concentrated sludge is extracted from the bottom of the sedimentation tank, introduced into the plate and frame filter press for pressure filtration and dehydration, and maintained at a pressure of 1.6 MPa for 35 minutes. After the pressure is maintained, the pressure relief material is discharged, and a dry mud cake having a water content of 36.8% is obtained. .

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Abstract

一种对城镇污水处理厂及污水处理产生的污泥环保高效的深度脱水的方法。该方法在常温常压下，在待处理的污泥中先通过投加废弃硫酸、O 3和FeCl 3进行氧化破膜预处理，实现污泥菌胶团结构和菌胞膜的氧化破解，使污泥中大量结构水、吸包水和晶胞水变成间隙水；再通过投加Fe 2(SO 4) 3和PAM强化固化，进行混凝沉淀处理，此时具有胶凝性质的水化产物在污泥颗粒间形成网状结构，结晶类的水化产物则填充网状结构的孔隙，使污泥内部变得致密；最后通过压滤机脱水，最终使污泥含水率降低至50％以下，实现污泥处理的减量化、稳定化、无害化。

Description

一种污泥深度脱水的处理方法 技术领域
本发明涉及一种对城镇污水处理厂及污水处理产生的污泥深度脱水的处理方法，属于污泥脱水工艺技术领域。
背景技术
污水处理厂所产生的剩余污泥处理处置是当今世界环保课题的一大难题，有效减低污泥含水率是课题中的一个技术瓶颈。目前，我国的污水处理厂普遍采用的机械脱水方式可将污泥含水率将至75％～80％之间，而环保部办公厅2010年发布的《关于加强城镇污水处理厂污泥污染防治工作的通知》(环办【2010】157号)中规定：污水处理厂以贮存(即不处理处置)为目的将污泥运出厂界的，必须将污泥脱水至50％以下。含水率剩余污泥也是污水处理过程中的二次污染物。一方面，污泥中含有大量的病原菌、寄生虫、致病微生物，以及砷、铜、铬、汞等重金属和二噁英、放射性核素等难以降解的有毒有害物质，由于污泥含水率高、体积大，给堆放和运输带来困难，城市污泥如果处理不当或不规范处理，如随意弃置农地滥用等，将对生态环境会造成严重的潜在威胁。另一方面，剩余污泥含有很高的有机营养质和燃烧值，污泥的土地利用与能量循环利用是一种具有广阔前景的污泥处置方法，而污泥含水率高低直接影响污泥再利用的再生成本。无论是响应国家政策还是资源再生利用，追求低污泥含水率都将势在必行。因此污泥深度脱水一直深受各国重视，污泥作为再生资源的有效利用是世界各国共同重视的问题，代表了人类环境生态效益、社会效益和经济效益均衡发展的方向。
机械脱水仅能使自由水和存在于污泥颗粒间的间隙水去除；毛细水和污泥颗粒之间的结合力较强，需借助较高的机械作用力和能量；胞内水的含量与污泥中微生物细胞所占的比例有关，使用机械方法去除这部分水是行不通的，而需采用高温加热和冷冻等措施。从破坏污泥水分结合形态的角度来看，可利用堆肥、石灰调质、污泥化学改性、热干化技术及电渗透等工艺。厌氧或含氧堆肥大多采用调理剂调理降低污泥含水率之后再堆肥生产，存在占地面积大，臭味较大，运行周期长，运行费用较高，处理能力较小等不足之处。石灰调质脱水工艺石灰投加率为20％～30％，石灰投加量大污泥增重较大，污泥容积较大，生产周期较长， 泥饼和滤液是碱性，滤液还需调节pH值处理，设备的防腐要求也较高，运行费用较高。污泥加药改性一般采用药剂对污泥进行调理，没有对污泥进行本质上的改变，降低污泥的含水率依赖的是机械设备的改进。污泥加药改性技术分污泥菌胶团沉降性能改性和污泥菌胶团细菌改性，针对污泥沉降性能改性，污泥的脱水率只能降到65％左右，且调理剂的总添加量占污泥干基比达到20％以上，污泥增容问题较严重，实际上并未实现污泥的减量化。热干技术由于污泥含水率较高，污泥热值不能维持自身污泥干化运行需要增加外源能源，能耗较大，运行成本很高。电渗透干法存在设备投资、运行成本费用较高，设备的维护要求很高等不足之处。这些方法不是存在含水率不能达到要求就是存在运行成本过高或增加污泥容量等缺点而不能满足现实所需。
因此，目前污泥深度脱水面临的难题在于，现有的调理剂存在成本高、用量大、调理工艺复杂，设备投资、运行成本过高，并未实现污泥减量化，容易影响污泥的再生或后续利用，环境效益差等缺点。
发明内容
本发明的目的在于提供一种对城镇污水处理厂及污水处理产生的污泥环保高效的深度脱水处理方法。
本发明提供的一种污泥深度脱水的处理方法，其特征在于：在常温常压下，在待处理的污泥中先通过投加废弃硫酸、O3和FeCl3进行氧化破膜预处理；再通过投加Fe2(SO4)3和PAM(聚丙烯酰胺)强化固化，进行混凝沉淀处理；最后通过压滤机脱水，最终使污泥含水率降低至50％以下。
进一步的，本发明提供的污泥深度脱水的处理方法，包括以下具体步骤：
(1)污泥调质：在由两个小池组成的氧化破膜反应池中，先将待处理的污泥抽取至第一小池中，加入废弃硫酸和O3，以含水率为90～99.9％的污泥计，废弃硫酸和O3的加入量分别为10～100g/t湿泥、1～10g/t湿泥，经搅拌反应后将污泥混合液抽取至第二小池中，加入FeCl3，以含水率为90～99.9％的污泥计，FeCl3的加入量为10～100g/t湿泥，再经搅拌反应，实现污泥菌胶团结构和菌胞膜的氧化破解，使污泥中大量结构水、吸包水和晶胞水变成间隙水；氧化破膜反应池处理后的污泥混合液再进入絮凝反应池，加入Fe2(SO4)3和PAM，以含水率为90～99.9％的污泥计，Fe2(SO4)3和PAM的加入量分别为10～100g/t湿泥、1～4g/t 湿泥，再经搅拌反应，此时具有胶凝性质的水化产物在污泥颗粒间形成网状结构，即构成了污泥的骨架，结晶类的水化产物则填充网状结构的孔隙，使污泥内部变得致密，大大提高污泥的水稳定性和强度稳定性；
(2)沉淀：将步骤(1)中调质好的污泥送到沉淀池中静置；
(3)脱水：从沉淀池底部抽出浓缩污泥，引入压滤机进行压滤脱水，在1.2～1.6MPa的压力下保持20～40分钟，保压完成后卸压放料，污泥含水率降至50％以下。
上述处理方法中，步骤(1)中所述废弃硫酸的质量浓度为98％，pH控制在6～6.5，所述O3、FeCl3和Fe2(SO4)3利用压缩空气、废弃铁屑、废弃硫酸、废弃盐酸通过反应制备获得，所述搅拌反应的时间为10～20分钟；步骤(2)中所述静置时间为20～30分钟；步骤(3)中所述压滤机为板框式压滤机。
本发明是以破解菌胶团有机絮凝体的吸包水及菌胶团的内部水为研究方向，常温常压下，在氧化剂作用下完成高能态电子在s-g、s-l界面与剩余污泥胶束结构键合键轨道对称性转移，实现污泥菌胶团结构和菌胞膜的氧化破解，使污泥中大量结构水、吸包水和晶胞水变成间隙水，然后添加固化混凝药剂，改善污泥的絮凝性，增强絮凝体的比重及其水稳定性和强度稳定性，通过搅拌混合、静置养护，再通过板框压滤机高压压率提高污泥脱水率，达到降低污泥含水率的目的。
申请人在大量的实践探索中发现，在FeCl3、Fe2(SO4)3、PAM及少量的废弃硫酸的共同作用下，具有明显的增效性，可实现污泥的高效脱水，调理工艺简单、快捷，用量少，脱水后的污泥含水率可降至50％以下，pH值在6～6.5之间，无恶臭，不存在增容问题，可广泛应用于污泥脱水处理。
废弃硫酸、O3作为氧化破膜剂可使活性污泥中胞外聚合物水解、微生物细胞瓦解，可有效实现污泥菌胶团结构和菌胞膜的氧化破解，使污泥中大量结构水、吸包水和晶胞水释放出来变成间隙水，从而提高可脱水程度，能在较短时间内达到良好的脱水效果。通过破坏以蛋白质为基础的细胞壁和酶、酸性RNA、碳水化合物的细胞组织，从而达到除臭、杀菌的作用。
FeCl3、Fe2(SO4)3作为絮凝剂，其铁离子水解形成胶体羟基聚合物或氢氧化物沉淀，通过静电粘附、吸附、网捕等作用，卷扫小颗粒污泥形成有一定承载力的絮体颗粒，PAM作为助凝剂，可使污泥形成多孔网络状骨架，改善污泥的可压缩 性，增强絮体的强度。
本发明所用到的药剂O3、FeCl3、Fe2(SO4)3可利用压缩空气、废弃铁屑、废弃硫酸、废弃盐酸为原材料，通过一系列的化学反应制备得来，大大降低处理运行成本。
本发明提供的药剂能够使污泥絮体内部的结合水被释放出来，能够改变污泥的表面电荷，促进胞外聚合物(EPS)水解，降低了对水的亲和力。此外，还可诱导污泥毛细水向污泥间隙游离水转化，降低污泥的粘性，从而实现常规板框压滤机对污泥进行深度脱水。
与现有技术相比，本发明具有如下特点和优点：
(1)污水厂剩余污泥在常态下深度脱水，实现污泥深度处理减量化：本发明方法实现污水处理厂污泥就地深度处理，在常态条件下将含水率90～99.5％的剩余污泥一步深度脱水至含水率50％以下，达到直接卫生填埋的国家环保标准，符合环保部办公厅2010年发布的《关于加强城镇污水处理厂污泥污染防治工作的通知》(环办【2010】157号)中的规定。
(2)实现污泥处理处置无害化：应用本发明方法处理污水厂污泥，病毒体及菌落消亡，重金属离子固化；污泥臭度下降到1°以下；达到污泥安全处理处置环保标准。
(3)污泥性质稳定，便于资源利用：氧化脱水后污泥化学性质发生变化，颗粒聚结增大，稳定性提高，不返溶，不吸水膨胀。各项指标均合乎GB/T23485～2009，可作垃圾填埋场覆盖土泥质；应用本发明方法深度处理后的污泥含水率50％以下，不添加CaO等影响污泥热值的添加剂，国内污泥干基中有机质均在35～65％，对应的燃烧值在1800～3600大卡，因此干化污泥作为火电厂或水泥厂、砖厂燃料替代物，具有广泛的应用前景。
(4)经济效益明显：由于本发明方法所用原材料为压缩空气和废弃铁屑、废弃硫酸、废弃盐酸，故运行成本低，按广东省阳江市(申请人试验基地所在地)现行含水率80％的污泥处理处置费用计，每吨绝对干污泥处理处置费用约为2300元/吨；采用本发明方法处理费用约为550元/吨，折算含水80％湿污泥每吨110元。
(5)投资小，见效快：应用本发明方法完成剩余污泥深度脱水，在原有的污 水处理厂(按5万吨/日污水处理能力计)增加投资约400万元(中档配置，含备用)，其中压滤操作简单，滤布使用寿命长，成本低，每套2000元(200m2过滤系统)，便于清洗。污泥深度处理系统从开工建设到投产只需三个月完工，见效快。
(6)构建新型环保产业：以本发明为核心竞争力，建设废弃铁屑、废弃硫酸、废弃盐酸回收基地，建设相关的设备制造基地，提升我国的环保装备制造业水平，打造新型环保产业。
附图说明
图1为本发明实施例之污泥深度脱水的处理工艺流程图。
具体实施方式
下面通过对广东省阳江市阳东经济开发区污水处理剩余污泥为例，对本发明做进一步详细说明。以下实施例仅用于阐述本发明，而本发明的保护范围并非仅仅局限于以下实施例。所述技术领域的普通技术人员依据以上本发明公开的内容和各参数所取范围，均可实现本发明的目的。
实施例1
利用压缩空气、废弃铁屑、废弃硫酸、废弃盐酸通过反应制备O3、FeCl3和Fe2(SO4)3。在由两个小池组成的氧化破膜反应池中，抽取1t含水率为99.7％的剩余污泥至第一小池中，分别投加98％废弃硫酸30g(pH控制在6.5)和2gO3，搅拌反应10分钟。污泥混合液进入另外一个小池，投加50gFeCl3溶液，搅拌反应10分钟。污泥混合液进入絮凝反应池，投加50g Fe2(SO4)3溶液，及投加2gPAM，搅拌反应20分钟。然后进入沉淀池静置30分钟，让之沉淀浓缩。从沉淀池底部抽出浓缩污泥，引入板框压滤机进行压滤脱水，在1.2MPa的压力下保持40分钟，保压完成后卸压放料，可得含水率为49.8％的干泥饼。
实施例2
利用压缩空气、废弃铁屑、废弃硫酸、废弃盐酸通过反应制备O3、FeCl3和Fe2(SO4)3。在由两个小池组成的氧化破膜反应池中，抽取1t含水率为99.7％的剩余污泥至第一小池中，分别投加98％废弃硫酸30g(pH控制在6.5)和3gO3，搅拌反应10分钟。污泥混合液进入另外一个小池，投加50gFeCl3溶液，搅拌反应10分钟。污泥混合液进入絮凝反应池，投加50g Fe2(SO4)3溶液，及投加2gPAM， 搅拌反应20分钟。然后进入沉淀池静置30分钟，让之沉淀浓缩。从沉淀池底部抽出浓缩污泥，引入板框压滤机进行压滤脱水，在1.2MPa的压力下保持40分钟，保压完成后卸压放料，可得含水率为48.3％的干泥饼。
实施例3
利用压缩空气、废弃铁屑、废弃硫酸、废弃盐酸通过反应制备O3、FeCl3和Fe2(SO4)3。在由两个小池组成的氧化破膜反应池中，抽取1t含水率为99.7％的剩余污泥至第一小池中，分别投加98％废弃硫酸40g(pH控制在6.5)和4gO3，搅拌反应10分钟。污泥混合液进入另外一个小池，投加70gFeCl3溶液，搅拌反应10分钟。污泥混合液进入絮凝反应池，投加70g Fe2(SO4)3溶液，及投加2gPAM，搅拌反应20分钟。然后进入沉淀池静置25分钟，让之沉淀浓缩。从沉淀池底部抽出浓缩污泥，引入板框压滤机进行压滤脱水，在1.3MPa的压力下保持30分钟，保压完成后卸压放料。可得含水率为46.6％的干泥饼。
实施例4
利用压缩空气、废弃铁屑、废弃硫酸、废弃盐酸通过反应制备O3、FeCl3和Fe2(SO4)3。在由两个小池组成的氧化破膜反应池中，抽取1t含水率为99.7％的剩余污泥至第一小池中，分别投加98％废弃硫酸40g(pH控制在6.5)和5gO3，搅拌反应10分钟。污泥混合液进入另外一个小池，投加70gFeCl3溶液，搅拌反应10分钟。污泥混合液进入絮凝反应池，投加70g Fe2(SO4)3溶液，及投加2gPAM，搅拌反应20分钟。然后进入沉淀池静置25分钟，让之沉淀浓缩。从沉淀池底部抽出浓缩污泥，引入板框压滤机进行压滤脱水，在1.3MPa的压力下保持30分钟，保压完成后卸压放料，可得含水率为45.4％的干泥饼。
实施例5
利用压缩空气、废弃铁屑、废弃硫酸、废弃盐酸通过反应制备O3、FeCl3和Fe2(SO4)3。在由两个小池组成的氧化破膜反应池中，抽取1t含水率为99.7％的剩余污泥至第一小池中，分别投加98％废弃硫酸50g(pH控制在6.5)和5gO3，搅拌反应10分钟。污泥混合液进入另外一个小池，投加70gFeCl3溶液，搅拌反应10分钟。污泥混合液进入絮凝反应池，投加70g Fe2(SO4)3溶液，及投加2gPAM，搅拌反应20分钟。然后进入沉淀池静置25分钟，让之沉淀浓缩。从沉淀池底部抽出浓缩污泥，引入板框压滤机进行压滤脱水，在1.4MPa的压力下保持40分钟， 保压完成后卸压放料，可得含水率为45.4％的干泥饼。
实施例6
利用压缩空气、废弃铁屑、废弃硫酸、废弃盐酸通过反应制备O3、FeCl3和Fe2(SO4)3。在由两个小池组成的氧化破膜反应池中，抽取1t含水率为99.7％的剩余污泥至第一小池中，分别投加98％废弃硫酸50g(pH控制在6.5)和6gO3，搅拌反应10分钟。污泥混合液进入另外一个小池，投加80gFeCl3溶液，搅拌反应10分钟。污泥混合液进入絮凝反应池，投加80g Fe2(SO4)3溶液，及投加3gPAM，搅拌反应20分钟。然后进入沉淀池静置25分钟，让之沉淀浓缩。从沉淀池底部抽出浓缩污泥，引入板框压滤机进行压滤脱水，在1.4MPa的压力下保持40分钟，保压完成后卸压放料，可得含水率为43.5％的干泥饼。
实施例7
利用压缩空气、废弃铁屑、废弃硫酸、废弃盐酸通过反应制备O3、FeCl3和Fe2(SO4)3。在由两个小池组成的氧化破膜反应池中，抽取1t含水率为99.7％的剩余污泥至第一小池中，分别投加98％废弃硫酸60g(pH控制在6.5)和7gO3，搅拌反应10分钟。污泥混合液进入另外一个小池，投加80gFeCl3溶液，搅拌反应10分钟。污泥混合液进入絮凝反应池，投加80g Fe2(SO4)3溶液，及投加3gPAM，搅拌反应20分钟。然后进入沉淀池静置25分钟，让之沉淀浓缩。从沉淀池底部抽出浓缩污泥，引入板框压滤机进行压滤脱水，在1.5MPa的压力下保持40分钟，保压完成后卸压放料，可得含水率为41.2％的干泥饼。
实施例8
利用压缩空气、废弃铁屑、废弃硫酸、废弃盐酸通过反应制备O3、FeCl3和Fe2(SO4)3。在由两个小池组成的氧化破膜反应池中，抽取1t含水率为99.7％的剩余污泥至第一小池中，分别投加98％废弃硫酸60g(pH控制在6.5)和8gO3，搅拌反应10分钟。污泥混合液进入另外一个小池，投加90gFeCl3溶液，搅拌反应10分钟。污泥混合液进入絮凝反应池，投加90g Fe2(SO4)3溶液，及投加3gPAM，搅拌反应20分钟。然后进入沉淀池静置30分钟，让之沉淀浓缩。从沉淀池底部抽出浓缩污泥，引入压滤机进行压滤脱水，在1.5MPa的压力下保持35分钟，保压完成后卸压放料，可得含水率为39.6％的干泥饼。
实施例9
利用压缩空气、废弃铁屑、废弃硫酸、废弃盐酸通过反应制备O3、FeCl3和Fe2(SO4)3。在由两个小池组成的氧化破膜反应池中，抽取1t含水率为99.7％的剩余污泥至第一小池中，分别投加98％废弃硫酸70g(pH控制在6.5)和9gO3，搅拌反应10分钟。污泥混合液进入另外一个小池，投加90gFeCl3溶液，搅拌反应10分钟。污泥混合液进入絮凝反应池，投加90g Fe2(SO4)3溶液，及投加3gPAM，搅拌反应20分钟。然后进入沉淀池静置30分钟，让之沉淀浓缩。从沉淀池底部抽出浓缩污泥，引入板框压滤机进行压滤脱水，在1.6MPa的压力下保持35分钟，保压完成后卸压放料，可得含水率为38.9％的干泥饼。
实施例10
利用压缩空气、废弃铁屑、废弃硫酸、废弃盐酸通过反应制备O3、FeCl3和Fe2(SO4)3。在由两个小池组成的氧化破膜反应池中，抽取1t含水率为99.7％的剩余污泥至第一小池中，分别投加98％废弃硫酸70g(pH控制在6.5)和10gO3，搅拌反应10分钟。污泥混合液进入另外一个小池，投加100gFeCl3溶液，搅拌反应10分钟。污泥混合液进入絮凝反应池，投加100g Fe2(SO4)3溶液，及投加4gPAM，搅拌反应20分钟。然后进入沉淀池静置30分钟，让之沉淀浓缩。从沉淀池底部抽出浓缩污泥，引入板框压滤机进行压滤脱水，在1.6MPa的压力下保持35分钟，保压完成后卸压放料，可得含水率为36.8％的干泥饼。

Claims (7)

  1. 一种污泥深度脱水的处理方法，其特征在于：在常温常压下，在待处理的污泥中先通过投加废弃硫酸、O3和FeCl3进行氧化破膜预处理；再通过投加Fe2(SO4)3和PAM强化固化，进行混凝沉淀处理；最后通过压滤机脱水，最终使污泥含水率降低至50％以下。
  2. 根据权利要求1所述的污泥深度脱水的处理方法，其特征在于包括以下具体步骤：
    (1)污泥调质：在由两个小池组成的氧化破膜反应池中，先将待处理的污泥抽取至第一小池中，加入废弃硫酸和O3，以含水率为90～99.9％的污泥计，废弃硫酸和O3的加入量分别为10～100g/t湿泥、1～10g/t湿泥，经搅拌反应后将污泥混合液抽取至第二小池中，加入FeCl3，以含水率为90～99.9％的污泥计，FeCl3的加入量为10～100g/t湿泥，再经搅拌反应，实现污泥菌胶团结构和菌胞膜的氧化破解，使污泥中大量结构水、吸包水和晶胞水变成间隙水；氧化破膜反应池处理后的污泥混合液再进入絮凝反应池，加入Fe2(SO4)3和PAM，以含水率为90～99.9％的污泥计，Fe2(SO4)3和PAM的加入量分别为10～100g/t湿泥、1～4g/t湿泥，再经搅拌反应，此时具有胶凝性质的水化产物在污泥颗粒间形成网状结构，即构成了污泥的骨架，结晶类的水化产物则填充网状结构的孔隙，使污泥内部变得致密，大大提高污泥的水稳定性和强度稳定性；
    (2)沉淀：将步骤(1)中调质好的污泥送到沉淀池中静置；
    (3)脱水：从沉淀池底部抽出浓缩污泥，引入压滤机进行压滤脱水，在1.2～1.6MPa的压力下保持20～40分钟，保压完成后卸压放料，污泥含水率降至50％以下。
  3. 根据权利要求2所述的污泥深度脱水的处理方法，其特征在于：步骤(1)中所述废弃硫酸的质量浓度为98％，pH控制在6～6.5。
  4. 根据权利要求2所述的污泥深度脱水的处理方法，其特征在于：步骤(1)中所述O3、FeCl3和Fe2(SO4)3利用压缩空气、废弃铁屑、废弃硫酸、废弃盐酸通过反应制备获得。
  5. 根据权利要求2所述的污泥深度脱水的处理方法，其特征在于：步骤(1)中所述搅拌反应的时间为10～20分钟。
  6. 根据权利要求2所述的污泥深度脱水的处理方法，其特征在于：步骤(2)中所述静置时间为20～30分钟。
  7. 根据权利要求2所述的污泥深度脱水的处理方法，其特征在于：步骤(3)中所述压滤机为板框式压滤机。
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