WO2012155466A1 - 一种机械搅拌内循环树脂离子交换与吸附反应器 - Google Patents

一种机械搅拌内循环树脂离子交换与吸附反应器 Download PDF

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Publication number
WO2012155466A1
WO2012155466A1 PCT/CN2011/082009 CN2011082009W WO2012155466A1 WO 2012155466 A1 WO2012155466 A1 WO 2012155466A1 CN 2011082009 W CN2011082009 W CN 2011082009W WO 2012155466 A1 WO2012155466 A1 WO 2012155466A1
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WIPO (PCT)
Prior art keywords
reactor
resin
diameter
bell
reaction tank
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PCT/CN2011/082009
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English (en)
French (fr)
Inventor
龙超
范俊
李爱民
双陈冬
Original Assignee
南京大学
南京大学盐城环保技术与工程研究院
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Application filed by 南京大学, 南京大学盐城环保技术与工程研究院 filed Critical 南京大学
Priority to US14/117,194 priority Critical patent/US8864987B2/en
Publication of WO2012155466A1 publication Critical patent/WO2012155466A1/zh

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Classifications

    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J47/00—Ion-exchange processes in general; Apparatus therefor
    • B01J47/02—Column or bed processes
    • B01J47/022—Column or bed processes characterised by the construction of the column or container
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J47/00—Ion-exchange processes in general; Apparatus therefor
    • B01J47/02—Column or bed processes
    • B01J47/06—Column or bed processes during which the ion-exchange material is subjected to a physical treatment, e.g. heat, electric current, irradiation or vibration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J47/00—Ion-exchange processes in general; Apparatus therefor
    • B01J47/10—Ion-exchange processes in general; Apparatus therefor with moving ion-exchange material; with ion-exchange material in suspension or in fluidised-bed form
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
    • B01J49/10—Regeneration or reactivation of ion-exchangers; Apparatus therefor of moving beds
    • 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
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • 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
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/285—Treatment of water, waste water, or sewage by sorption using synthetic organic sorbents
    • 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
    • C02F2001/007—Processes including a sedimentation 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
    • C02F2303/16—Regeneration of sorbents, filters

Definitions

  • the invention relates to a resin ion exchange and adsorption device, in particular to a mechanically stirred internal circulation resin ion exchange and adsorption reaction device, in particular to a mechanically stirred internal circulation ion using a solid powder resin or a magnetic powder resin having a diameter of 75-200 ⁇ m.
  • Exchange and adsorption reactors belong to the field of water treatment.
  • the powder resin is a solid acrylic polymer material with an average particle size of 75-200 ⁇ m. It is rich in pore structure and ionic groups and has dual functions of electrochemical adsorption and ion exchange.
  • New powder resin or magnetic powder The bulk resin has the characteristics of small particle size, large specific surface area and high reaction kinetic efficiency.
  • the powder resin can be mixed with the wastewater to be treated for a certain period of time, and then the resin is separated from the wastewater to be enriched.
  • the organic matter and inorganic substances in the water require a short time and a small amount of resin, and have the advantages of obvious anti-pollution, long service life and low production of desorption liquid.
  • the particle size of the powder resin or the magnetic powder resin is small and the relative density is small, when the conventional fixed bed or suspended bed is used, the resistance of the resin bed is large, the resin is easy to be compacted and broken, and the resin is easy to carry during backwashing.
  • MIEX® resin developed by Australia Orica and its application technology have been widely used in the advanced treatment of feed water; it uses strong alkali ion exchange acrylic resin and uses mechanical stirring and inclined tube separation to treat nitrate, sulfate and phosphoric acid in water.
  • Various anions such as roots and arsenate, and the removal of dissolved organic pollutants have good effects; domestically, Nanjing Zhongdianlian Environmental Engineering Co., Ltd. has also developed a perforated hydrojet magnetic resin reactor; however, the above reactors are fully mixed with resin.
  • the resin is distributed evenly in the reactor, the resin is used in a large amount when the reactor is used, and the resin is difficult to separate the reactor; at the same time, the amount of water treated by the above reactor monomer is small, and the reaction required in large-scale water treatment is required.
  • the amount of water treated by the above reactor monomer is small, and the reaction required in large-scale water treatment is required.
  • the present invention provides a small particle size, a low density, and excellent hydrodynamic performance of a solid powder resin or a magnetic powder resin.
  • the utility model relates to a mechanical stirring internal circulation resin ion exchange and adsorption reactor, which is suitable for the ion exchange and adsorption reaction device of the powder resin, can fully exert the advantages of the resin and realize the continuous operation of the resin reaction device.
  • the reactor can be applied to the deep treatment of wastewater, biochemical tail water and reclaimed water by solid powder resin or magnetic powder resin, and can also be used for advanced treatment of feed water.
  • a mechanically stirred internal circulation resin ion exchange and adsorption reactor of the present invention wherein the upper part of the reactor body is 2/3 to 4/5, which is an open cylinder, and the lower part is 1/5 to 1/3.
  • the turbine water diversion stirrer provided in the bell-shaped reaction tank is composed of a turbine, an upper agitating paddle of a turbine and a lower agitating paddle of a turbine, and the agitator rotates at a speed of 2 to 50 r/min;
  • the diameter of the turbine is a hollow cylinder of a bell-shaped reaction tank.
  • the cross-sectional diameter of the body is 1/4 ⁇ 1/3, the linear velocity of the outer edge of the turbine is 0.1 ⁇ 1.5m/s ;
  • the upper agitating paddle and the lower agitating paddle of the turbine are composed of 2 ⁇ 6 blades, and the outer edge of the paddle blade is agitated.
  • the line speed is 0.2 to 2.0 m/s.
  • the deflector is a hollow cylinder, the axis of which is identical to the reactor body, and the diameter of the reactor body is 1/2 ⁇ 3/4 of the diameter of the reactor body; the upper end of the deflector is flush with the upper end of the reactor body, and the lower end is spaced
  • the bottom end of the reactor body is 1.5 to 2.5 m.
  • the baffle is used to change the direction of the effluent flow of the bell-shaped reaction tank 4 and to precipitate the resin at the bottom of the reactor.
  • the inclined pipe separator is disposed between the outer casing of the reactor main body and the baffle plate at a distance of 1.5 to 3.5 m below the top end, and the inclined pipe separator is composed of a single pipe with a diameter of 50 mm to 80 mm, and the inclined pipe is made of PP and UPVC.
  • PE PE, FRP or FRP One type
  • the inclined pipe inclination angle is 45° ⁇ 60°
  • the inclined pipe length is 0.8m ⁇ 1.2m
  • the inclined pipe surface load is 3 ⁇ 6m 3 /(m 2 ⁇ h).
  • the annular resin collecting bucket bottom is 0.5 ⁇ 2.0m from the bottom of the reactor, the total height of the annular resin collecting bucket is 0.5 ⁇ 1.0m, and the upper ring diameter of the annular resin collecting bucket is 1/8 ⁇ 1/4 of the diameter of the reactor main body. .
  • the present invention is particularly suitable for ion exchange and adsorption reaction of a solid powder resin or a magnetic powder resin having a small particle diameter, and can fully exert the advantages of such a resin;
  • Solid powder resin or magnetic powder resin is mainly concentrated in the bell-shaped reaction tank, the resin is in full contact with water, the time required for ion exchange and adsorption is short, the amount of resin required is small, the floor space is small, and the amount of treated water is relatively small. Big;
  • the reactor is an open atmospheric vessel, which can be made of metal, organic composite or steel concrete, and has low manufacturing cost;
  • the reactor can be continuously operated, and the deactivated resin can be continuously removed and regenerated without stopping the water in the reactor, and the regenerated resin can be continuously returned to the main body of the apparatus, and the utilization rate of the equipment is high;
  • the reactor process is simple, and it is not necessary to set complicated water inlet and backwash pipelines, etc., and the operation is simple and convenient, and the automatic operation can be conveniently realized.
  • FIG. 1 is a schematic view showing the structure of a mechanically stirred internal circulation resin ion exchange and adsorption reactor of the present invention, in which: reactor main body 1, cone 2, cylinder 3, bell-shaped reaction tank 4, turbine water mixing and stirring 5, lower agitating paddle 6, turbine 7, upper agitating paddle 8, deflector 9, annular resin collecting bucket 10, inclined tube separator 11, water collecting weir 12, inlet pipe 13, outlet pipe 14, regenerated resin return pipe 15.
  • the resin removal tube 16 and the resin desorption tank 17 are provided.
  • the invention relates to a mechanically stirred internal circulation resin ion exchange and adsorption reactor.
  • the upper part of the reactor main body 1 is an open cylinder 3 and the lower part is a cone 2.
  • a bell-shaped reaction tank 4 is installed in the center of the reactor main body 1.
  • the bell-shaped reaction tank 4 is a combined hollow rotary body whose axis is identical to the reactor main body 1.
  • the upper portion of the bell-shaped reaction tank 4 is a hollow cylinder, and the lower portion
  • the hollow circular table body structure is provided with a water blocking baffle between the hollow cylinder and the circular table body, and the water blocking baffle is opened at the center;
  • the bell-shaped reaction tank 4 is equipped with a turbine water mixing agitator 5, and the turbine water mixing agitator 5 is
  • the turbine 7, the turbine upper agitating paddle 8, and the turbine lower agitating paddle 6 are configured.
  • the deflector 9 is a hollow cylinder whose axis coincides with the reactor body 1.
  • a water collecting weir 12 and a inclined pipe separator 11 are installed between the flow plates 9, and the water collecting weir 12 is installed in the form of spokes between the outer casing of the reactor main body 1 and the deflector 9, and the water outlet pipe 14 is installed in the water collecting weir 12 At the office.
  • An annular resin collecting hopper 10 is provided at a lower portion between the outer casing of the reactor main body 1 and the deflector 9.
  • the reactor is provided with an inlet pipe 13 which is installed in the truncated body region at the lower portion of the bell-shaped reaction vessel 4; the resin removal pipe 16 is connected to the resin collecting hopper 10 and the resin desorption tank 17, respectively, and the regenerated resin return pipe 15 leads to The truncated cone body region in the lower portion of the bell-shaped reaction tank 4.
  • the baffle plate 9 provided in the reactor main body 1 guides the resin and water mixture flowing out of the bell-shaped reaction tank 4 to the lower portion of the reactor main body 1, thereby realizing rapid sedimentation separation of the resin and recirculating into the bell-shaped reaction tank. 4 in.
  • a inclined tube precipitator 11 is disposed between the outer casing of the reactor body 1 and the deflector 9, which further promotes sedimentation and separation of the resin in the water.
  • the reactor effluent passes through the top of the reactor body 1 and is collected and discharged from the water collection weir 12 between the outer casing of the reactor body 1 and the baffle 9.
  • the spent resin is collected in the annular resin collecting hopper 10 of the reactor, pumped into the resin desorption tank 17 for regeneration, and the regenerated resin flows from the regenerated resin return pipe 1 to the bell-shaped reaction vessel 4.
  • the invention relates to a mechanically stirred internal circulation resin ion exchange and adsorption reactor.
  • the upper part 2/3 of the reactor main body 1 is an open cylinder 3, the lower part 1/3 is a cone 2, and the cone 2 has a slope of 20°, and the reaction
  • the main body 1 is made of steel.
  • the stirrer installed in the bell-shaped reaction tank 4 has a rotational speed of lOr/min; the diameter of the turbine 7 is 1/4 of the cross-sectional diameter of the upper hollow cylinder of the bell-shaped reaction tank 4, and the linear velocity of the outer edge of the turbine 7 is 0.5 m/s.
  • the upper turbine agitating paddle 8 and the lower agitating paddle 6 are each composed of two blades, and the outer edge linear velocity of the agitating paddle blade is 0.5 m/s.
  • the cylindrical baffle 9 installed in the reactor main body 1 has a diameter of 1/2 of the diameter of the reactor main body 1; the upper end of the baffle 9 is flush with the upper end of the reactor main body 1, and the lower end is 1.5 m from the bottom end of the reactor main body 1. .
  • the water collecting weir 12 is disposed 0.3m below the top end between the outer casing of the reactor main body 1 and the deflector 9, and the water collecting weir 12 is composed of 6 sets of water collecting weirs 12, and is installed in the spoke form on the outer casing and the guide of the reactor main body 1. Between the flow plates 9, the water collecting weir 12 adopts a zigzag water collecting weir.
  • the inclined pipe separator 11 is disposed 1.5 m below the top end between the outer casing of the reactor main body 1 and the deflector 9, and the inclined pipe separator 11 is composed of a single pipe having a diameter of 50 mm, and the inclined pipe is a PP having a pipe length of lm. Material, inclined tube inclination angle 45°, inclined tube length 0.8m, inclined tube surface load 3m 3 /(m 2 ⁇ h).
  • the bottom of the annular resin collecting hopper 10 is 0.5 m from the bottom of the reactor, the total height of the annular resin collecting hopper 10 is 0.5 m, and the diameter of the upper ring of the annular resin collecting hopper 10 is 1/8 of the diameter of the reactor main body 1.
  • the reactor is provided with an inlet pipe 13 which is provided in the truncated body region at the lower portion of the bell-shaped reaction tank 4; the outlet pipe 14 is provided at the outlet of the sump 12; the resin removal pipe 16 is connected to the resin hopper 10 and the resin, respectively.
  • the desorption tank 17, the regenerated resin return pipe 15 leads to the truncated body region at the lower portion of the bell-shaped reaction vessel 4.
  • the equipment is used as an advanced treatment device for the biochemical tail water of a printing and dyeing park, and is treated by solid powder resin adsorption treatment.
  • the wastewater is mixed with the regenerated reflow resin and then enters the bell-shaped reaction tank 4 of the reactor.
  • the amount of the resin is 5% by volume of the volume of the bell-shaped reaction tank, and the residence time of the wastewater in the bell-shaped reaction tank 4 is 30 min. Adjust the speed of the mixer to achieve sufficient contact between the resin and the wastewater, and maintain the flow rate of the upper part of the bell-shaped reaction tank 4 at a flow rate of 3 m/h.
  • the resin collected from the reactor annular resin collecting bucket 10 is piped to the resin desorption tank 17 for dynamic regeneration, the regeneration liquid is 10% NaCl solution, and the regenerated resin is returned to the counter bell-shaped reaction tank 4; the removed resin
  • the amount control ratio is 10% of the amount of resin in the reactor, and the amount of regenerated resin to be replenished coincides with the amount of resin removed.
  • Table 2 Water quality indicators after treatment
  • Example 2 The invention relates to a mechanically stirred internal circulation resin ion exchange and adsorption reactor.
  • the upper part 4/5 of the reactor main body 1 is an open cylinder 3, the lower part 1/5 is a cone 2, and the cone 2 has a slope of 30°, and the reaction
  • the main body 1 is made of steel.
  • the upper part 1/2 of the bell-shaped reaction tank 4 is a hollow cylinder, and the lower part 1/2 is a hollow truncated cone structure; the bottom end of the bell-shaped reaction tank 4 is 0.6 m from the bottom end of the reactor main body 1, and the upper end of the bell-shaped reaction tank 4
  • the diameter of the hollow cylinder is 1/4 of the outer diameter of the reactor body 1.
  • the diameter of the lower end of the circular table body is the same as the diameter of the hollow cylinder.
  • the diameter of the upper end of the circular table body is 1/ of the outer diameter of the reactor body 1. 3; a water blocking baffle is arranged between the hollow cylinder and the circular table body, and the water blocking baffle is opened at the center, and the opening diameter is 1/3 of the diameter of the hollow cylinder.
  • the stirrer installed in the bell-shaped reaction tank 4 has a rotational speed of 35 r/min; the diameter of the turbine 7 is 1/3 of the cross-sectional diameter of the upper hollow cylinder of the bell-shaped reaction tank 4, and the linear velocity of the outer edge of the turbine 7 is 1.0 m/min. s;
  • the upper agitating paddle 8 and the lower agitating paddle 6 of the turbine are each composed of four blades, and the outer edge linear velocity of the agitating paddle blade is 1.0 m/s.
  • the cylindrical baffle 9 installed in the reactor main body 1 has a diameter of 2/3 of the diameter of the reactor main body 1; the upper end of the baffle 9 is flush with the upper end of the reactor main body 1, and the lower end is 2.0 m from the bottom end of the reactor main body 1. .
  • the water collecting weir 12 is disposed 0.4m below the top end between the outer casing of the reactor main body 1 and the deflector 9, and the water collecting weir 12 is composed of 8 sets of water collecting weirs 12, and is installed in the spoke form on the outer casing and the guide of the reactor main body 1. Between the flow plates 9, the water collecting weir 12 adopts an orifice water collecting weir.
  • the bottom of the annular resin collecting hopper 10 is 1.0 m from the bottom of the reactor, the total height of the annular resin collecting hopper 10 is 0.8 m, and the diameter of the upper ring of the annular resin collecting hopper 10 is 1/6 of the diameter of the reactor main body 1.
  • Others are the same as in the first embodiment, and the processing results are the same as those in Table 2.
  • Example 3 Example 3:
  • the invention relates to a mechanically stirred internal circulation resin ion exchange and adsorption reactor.
  • the upper part of the reactor main body 1 is an open cylinder 3, the lower part 1/5 is a cone 2, and the cone 2 has a slope of 40°.
  • the main body 1 is made of steel.
  • the upper part 1/2 of the bell-shaped reaction tank 4 is a hollow cylinder, and the lower part 1/2 is a hollow truncated cone structure; the bottom end of the bell-shaped reaction tank 4 is 0.8 m from the bottom end of the reactor main body 1, and the upper end of the bell-shaped reaction tank 4 1.0m from the top of the reactor body 1; the diameter of the hollow cylinder is 1/3 of the outer diameter of the reactor body 1, the diameter of the lower end of the truncated cone is the same as the diameter of the hollow cylinder, and the diameter of the upper end of the truncated cone is 1/ of the outer diameter of the reactor body 1. 2; a water blocking baffle is arranged between the hollow cylinder and the circular table body, and the water blocking baffle is opened at the center, and the opening diameter is 1/2 of the diameter of the hollow cylinder.
  • the stirrer installed in the bell-shaped reaction tank 4 has a rotation speed of 45 r/min; the diameter of the turbine 7 is 1/3 of the cross-sectional diameter of the upper hollow cylinder of the bell-shaped reaction tank 4, and the outer edge speed of the turbine 7 is 1.5 m/s.
  • the upper turbine agitating paddle 8 and the lower agitating paddle 6 are each composed of 6 blades, and the outer edge linear velocity of the agitating paddle blade is 1.5 m/s.
  • the cylindrical baffle 9 installed in the reactor main body 1 has a diameter of 3/4 of the diameter of the reactor main body 1; the upper end of the baffle 9 is flush with the upper end of the reactor main body 1, and the lower end is 2.5 m from the bottom end of the reactor main body 1. .
  • the water collecting weir 12 is disposed 0.5m below the top end between the outer casing of the reactor main body 1 and the deflector 9, and the water collecting weir 12 is composed of 10 sets of water collecting weirs 12, and is installed in the spoke form on the outer casing and the guide of the reactor main body 1. Between the flow plates 9, the water collecting weir 12 adopts an orifice water collecting weir.
  • the inclined pipe separator 11 is disposed between the outer casing of the reactor main body 1 and the deflector 9 at a distance of 3.0 m from the top end, and the inclined pipe separator 11 is composed of a single pipe with a diameter of 70 mm, and the inclined pipe is made of a fiberglass having a length of lm. Material, inclined pipe inclination angle 55°, inclined pipe length 1.2m, inclined pipe surface load 5m 3 /(m 2 ⁇ h).
  • the bottom of the annular resin collecting hopper 10 is 1.8 m from the bottom of the reactor, the total height of the annular resin collecting hopper 10 is 1.0 m, and the diameter of the upper ring of the annular resin collecting hopper 10 is 1/5 of the diameter of the reactor main body 1.
  • Others are the same as in the first embodiment, and the processing results are the same as those in Table 2.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Treatment Of Water By Ion Exchange (AREA)
  • Water Treatment By Sorption (AREA)

Description

一种机械搅拌内循环树脂离子交换与吸附反应器 技术领域
本发明为一种树脂离子交换与吸附设备， 特别涉及机械搅拌内循环树脂离子交换与吸附反 应设备， 尤其是采用直径 75-200 μ m实心粉体树脂或磁性粉体树脂的机械搅拌内循环离子交 换与吸附反应器， 属于水处理领域。
背景技术
在给水、各类废水及生化尾水的深度处理中， 常采用离子交换与吸附树脂对水中的有机物、 无机物进行富集分离， 以达到对水的脱色、 脱臭、 软化及去除微量有机物和重金属的目的。 然而采用普通离子交换树脂设备， 不但存在预处理工序复杂、 树脂用量多、 设备投资大、 运 行费用高的问题， 而且单体设备难以连续运行， 同时树脂再生液使用量大， 再生效率较低。 粉体树脂是一种颗粒平均粒径为 75-200 μ m的固体丙烯酸高分子材料， 含有丰富的孔结构和 离子基团， 具有电化学吸附及离子交换双重作用； 新型粉体树脂或磁性粉体树脂具有粒径小、 比表面积大、 反应动力学效能高的特点； 在实际应用中， 粉体树脂可与所需处理的废水混合 搅拌一定时间， 后将树脂与废水分离， 使其富集水中有机物、 无机物所需时间短、 树脂用量 少， 具有明显的抗污染、 使用寿命长、 脱附液产量少的优点。 然而， 由于粉体树脂或磁性粉 体树脂的粒径小且相对密度较小， 采用传统固定床或悬浮床时， 树脂床层阻力较大， 树脂易 压实、 破碎， 反洗时树脂易带出反应器， 且无法实现连续运行， 严重影响了粉体树脂性能的 发挥。 针对粉体树脂或磁性粉体树脂的小粒径、 低密度， 及优良的流体力学性能的特点， 有 必要开发出适用于该类树脂的新型树脂反应器， 以充分发挥该类树脂的优势。
目前， 澳大利亚 Orica公司开发的 MIEX ®树脂及其应用技术， 已广泛使用于给水的深度处 理； 其采用强碱离子交换丙烯酸树脂并使用机械搅拌及斜管分离方式对水中硝酸根、硫酸根、 磷酸根、 砷酸根等多种阴离子， 以及溶解性有机污染物去除具有良好的效果； 国内， 南京中 电联环保工程有限公司亦开发了穿孔水力射流磁性树脂反应器； 然而上述反应器采用树脂全 混方式， 树脂在反应器中分布较为平均， 反应器使用时树脂投加量较大， 且树脂分离出反应 器困难； 同时， 上述反应器单体处理水量较小， 在大型水处理时所需反应器数量较多， 所以 有必要开发新型反应器改善上述困难。
发明内容
1、 所要解决的技术问题
针对实心粉体树脂或磁性粉体树脂的小粒径、 低密度且流体力学性能优的特点， 本发明提供 一种机械搅拌内循环树脂离子交换与吸附反应器， 适用于粉体树脂的离子交换与吸附反应的 装置， 可以充分发挥该类树脂的优势， 并实现树脂反应装置的连续运行。 该反应器既可适用 于实心粉体树脂或磁性粉体树脂对废水、 生化尾水及中水的深度处理， 亦可用于给水的深度 处理。
2、 技术方案
本发明的技术方案如下： 本发明的一种机械搅拌内循环树脂离子交换与吸附反应器， 反应器 主体上部 2/3〜4/5为敞口圆柱体， 下部 1/5〜1/3为锥体， 锥体坡度为 30° ± 10° ； 反应器主 体中心设有钟罩形反应槽， 钟罩形反应槽内设有涡轮引水搅拌器； 反应器主体设有圆柱形导 流板； 反应器主体的外壳与导流板之间设置有集水堰和斜管分离器； 反应器主体的外壳与导 流板之间下部设有环形树脂收集斗； 反应器设有进水管， 进水管设在钟罩形反应槽下部的圆 台体区； 出水管设在集水堰出水处； 树脂移出管分别连接形树脂收集斗和树脂脱附槽， 再生 树脂回流管通向钟罩形反应槽下部的圆台体区。
所述的钟罩形反应槽为组合空心回转体， 其轴心与反应器主体一致， 该钟罩形反应槽上部 1/3〜1/2为空心圆柱体， 下部 1/2〜2/3为空心圆台体结构； 钟罩形反应槽底端距反应器主体 底端 0.2〜0.8m， 钟罩形反应槽上端距反应器主体顶端 0.5〜1.0m; 空心圆柱体直径为反应器 主体外径的 1/5〜1/3， 圆台体下端直径与空心圆柱体直径相同， 圆台体上端直径为反应器主 体外径的 1/4〜1/2； 空心圆柱体与圆台体之间设有隔水挡板， 隔水挡板中心开孔， 开孔直径 为空心圆柱体直径的 1/4〜1/2。
所述的钟罩形反应槽中设置的涡轮引水搅拌器由涡轮、 涡轮上部搅拌桨以及涡轮下部搅拌 桨构成， 搅拌器转速为 2~50r/min; 涡轮直径为钟罩形反应槽上部空心圆柱体横截面直径的 1/4〜1/3， 涡轮外缘线速度为 0.1〜1.5m/s; 涡轮上部搅拌桨和下部搅拌桨均由 2〜6片桨叶组 成， 搅拌桨桨叶外缘线速度为 0.2〜2.0m/s。
所述的导流板为空心圆柱体， 其轴心与反应器主体一致， 其直径为反应器主体直径的 1/2〜 3/4； 导流板上端与反应器主体上端平齐， 下端距反应器主体底端 1.5〜2.5m。 导流板用于改 变钟罩形反应槽 4出水水流方向， 并使树脂沉淀于反应器底部。
所述的集水堰设置在反应器主体的外壳与导流板之间距顶端下方 0.3〜0.5m处， 集水堰由 4〜12 组集水堰组成， 以轮辐形式安装于反应器主体外壳与导流板之间， 集水堰采用锯齿形 集水堰或孔口集水堰。
所述的斜管分离器设置在反应器主体的外壳与导流板之间距顶端下方 1.5〜3.5m处， 斜管 分离器由单孔直径 50mm〜80mm的斜管构成， 斜管采用 PP、 UPVC、 PE或玻璃钢材质中的 一种， 斜管倾角 45° 〜60° ， 斜管管长 0.8m〜1.2m， 斜管表面负荷 3〜6m3/(m2 · h)。
所述的环形树脂收集斗底距反应器底部 0.5〜2.0m， 环形树脂收集斗的总高为 0.5〜1.0m， 环形树脂收集斗上部环直径为反应器主体直径的 1/8〜1/4。
3、 有益效果
与现有技术相比， 本发明的有益效果是：
( 1 )本发明特别适合于小粒径的实心粉体树脂或磁性粉体树脂的离子交换与吸附反应， 能充 分发挥该类树脂的优势；
(2)实心粉体树脂或磁性粉体树脂与水接触程度及内循环量可通过改变涡轮引水搅拌器的转 速及进水流量进行动态控制；
( 3 )实心粉体树脂或磁性粉体树脂主要集中于钟罩形反应槽， 树脂与水接触充分， 离子交换 与吸附所需时间短， 所需树脂量少， 占地面积小， 处理水量较大；
(4) 反应器为敞口常压容器， 可采用金属、 有机复合材料或钢砼混凝土制造， 制造成本低；
( 5 ) 实心粉体树脂或磁性粉体树脂与水分离充分， 树脂流失率低， 设备运行成本低；
( 6)反应器可以连续运行， 失活树脂可以在反应器不停止进水情况下连续移出再生， 再生树 脂可连续回流至设备主体， 设备利用率高；
(7 )反应器工艺简单， 不需设置复杂的进水、 反洗管路等， 操作简便， 可方便实现自动化运 行。
附图说明
附图 1是本发明的一种机械搅拌内循环树脂离子交换与吸附反应器的结构示意图， 图中： 反应器主体 1、 锥体 2、 圆柱体 3、 钟罩形反应槽 4、 涡轮引水搅拌器 5、 下部搅拌 桨 6、涡轮 7、上部搅拌桨 8、 导流板 9、环形树脂收集斗 10、斜管分离器 11、集水堰 12、 进水管 13、 出水管 14、 再生树脂回流管 15、 树脂移出管 16、 树脂脱附槽 17。
具体实施方式
下面结合附图对本发明作进一步的描述。
本发明的一种机械搅拌内循环树脂离子交换与吸附反应器， 反应器主体 1上部为敞口圆柱 体 3， 下部为锥体 2。 反应器主体 1中心安装有钟罩形反应槽 4， 钟罩形反应槽 4为组合空心 回转体， 其轴心与反应器主体 1一致， 该钟罩形反应槽 4上部为空心圆柱体， 下部为空心圆 台体结构， 空心圆柱体与圆台体之间设有隔水挡板， 隔水挡板中心开孔； 钟罩形反应槽 4内 安装有涡轮引水搅拌器 5， 涡轮引水搅拌器 5由涡轮 7、涡轮上部搅拌桨 8以及涡轮下部搅拌 桨 6构成。 导流板 9为空心圆柱体， 其轴心与反应器主体 1一致。 反应器主体 1的外壳与导 流板 9之间安装有集水堰 12和斜管分离器 11， 集水堰 12以轮辐形式安装于反应器主体 1外 壳与导流板 9之间， 出水管 14安装在集水堰 12出水处。 反应器主体 1的外壳与导流板 9之 间下部设有环形树脂收集斗 10。 反应器设有进水管 13， 进水管 13安装在钟罩形反应槽 4下 部的圆台体区； 树脂移出管 16分别连接形树脂收集斗 10和树脂脱附槽 17， 再生树脂回流管 15通向钟罩形反应槽 4下部的圆台体区。
本发明的一种机械搅拌内循环树脂离子交换与吸附反应器的使用过程如下： 钟罩形反应槽 4内填充 2〜15%体积百分数的实心粉体树脂或磁性粉体树脂， 粉体树脂直径介于 75〜200 μ m。 来水通过进水管 14进入钟罩形反应槽 4下部圆台区， 沉积于反应器主体 1底部的实心粉 体树脂或磁性粉体树脂在搅拌浆作用下与水充分混合， 同时钟罩形反应槽 4中的涡轮 7进一 步将水与树脂混合液送入钟罩形反应槽 4上部圆柱区， 水中各类有机物与无机物通过离子交 换与吸附作用被富集于树脂表面。 通过调节涡轮引水搅拌器 5的转速可控制钟罩形反应槽 4 内混合剧烈程度及钟罩形反应槽 4内的液体上升流速， 同时控制树脂反应的回流比。
反应器主体 1中设置的导流板 9将钟罩形反应槽 4流出的树脂与水混合物导流至反应器主 体 1下部， 从而实现树脂的快速沉降分离， 并重新循环进入钟罩形反应槽 4中。 反应器主体 1外壳与导流板 9之间设有斜管沉淀器 11， 进一步促进水中树脂的沉降分离。 反应器出水经 反应器主体 1顶部， 从介于反应器主体 1外壳与导流板 9之间的集水堰 12收集排放。失效树 脂经反应器的环形树脂收集斗 10收集， 用泵送入树脂脱附槽 17进行再生， 再生后的树脂由 再生树脂回流管 1流至钟罩形反应槽 4中。
下面结合实施例对本发明作进一步的描述。
实施例 1 ：
本发明的一种机械搅拌内循环树脂离子交换与吸附反应器， 反应器主体 1上部 2/3为敞口圆 柱体 3， 下部 1/3为锥体 2， 锥体 2坡度为 20° ， 反应器主体 1为钢制结构。
钟罩形反应槽 4上部 1/3为空心圆柱体， 下部 2/3为空心圆台体结构； 钟罩形反应槽 4底端 距反应器主体 1底端 0.2m，钟罩形反应槽 4上端距反应器主体 1顶端 0.5m; 空心圆柱体直径 为反应器主体 1外径的 1/5， 圆台体下端直径与空心圆柱体直径相同， 圆台体上端直径为反应 器主体 1外径的 1/4; 空心圆柱体与圆台体之间设有隔水挡板， 隔水挡板中心开孔， 开孔直径 为空心圆柱体直径的 1/4。
钟罩形反应槽 4内安装的搅拌器转速为 lOr/min;涡轮 7直径为钟罩形反应槽 4上部空心圆 柱体横截面直径的 1/4， 涡轮 7外缘线速度为 0.5m/s; 涡轮上部搅拌桨 8和下部搅拌桨 6均由 2片桨叶组成， 搅拌桨桨叶外缘线速度为 0.5m/s。 反应器主体 1安装的圆柱形导流板 9， 其直径为反应器主体 1直径的 1/2; 导流板 9上端与 反应器主体 1上端平齐， 下端距反应器主体 1底端 1.5m。 集水堰 12设置在反应器主体 1的 外壳与导流板 9之间距顶端下方 0.3m处， 集水堰 12由 6组集水堰 12组成， 以轮辐形式安装 于反应器主体 1外壳与导流板 9之间， 集水堰 12采用锯齿形集水堰。 斜管分离器 11设置在 反应器主体 1的外壳与导流板 9之间距顶端下方 1.5m处， 斜管分离器 11由单孔直径 50mm 的斜管构成， 斜管采用管长为 lm的 PP材质， 斜管倾角 45° ， 斜管管长 0.8m， 斜管表面负 荷 3m3/(m2 · h)。
环形树脂收集斗 10底距反应器底部 0.5m， 环形树脂收集斗 10的总高为 0.5m，环形树脂收 集斗 10上部环直径为反应器主体 1直径的 1/8。 反应器设有进水管 13， 进水管 13设在钟罩 形反应槽 4下部的圆台体区； 出水管 14设在集水堰 12出水处； 树脂移出管 16分别连接形树 脂收集斗 10和树脂脱附槽 17， 再生树脂回流管 15通向钟罩形反应槽 4下部的圆台体区。 采用该设备作为某印染园区废水生化后尾水的深度处理装置， 采用实心粉体树脂吸附处理
Figure imgf000007_0001
该废水与再生回流树脂混合后进入反应器的钟罩形反应槽 4中， 树脂量为钟罩形反应槽 4体 积的 5%体积分数， 废水在钟罩形反应槽 4中停留时间 30min， 通过调节搅拌机转速实现树脂 与废水的充分接触， 并保持钟罩形反应槽 4上部出水流速 3m/h。
从反应器环形树脂收集斗 10收集的树脂经管道输送至树脂脱附槽 17内动态再生， 再生液 采用 10%NaCl溶液， 再生后的树脂回流至反钟罩形反应槽 4中； 移出的树脂量控制比例为反 应器中树脂量的 10%，补充的再生树脂量与移出再生的树脂量相一致。处理结果如表 2所示。 表 2处理后水质指标
Figure imgf000007_0002
实施例 2 ： 本发明的一种机械搅拌内循环树脂离子交换与吸附反应器， 反应器主体 1上部 4/5为敞口圆 柱体 3， 下部 1/5为锥体 2， 锥体 2坡度为 30° ， 反应器主体 1为钢制结构。
钟罩形反应槽 4上部 1/2为空心圆柱体， 下部 1/2为空心圆台体结构； 钟罩形反应槽 4底端 距反应器主体 1底端 0.6m，钟罩形反应槽 4上端距反应器主体 1顶端 0.8m; 空心圆柱体直径 为反应器主体 1外径的 1/4， 圆台体下端直径与空心圆柱体直径相同， 圆台体上端直径为反应 器主体 1外径的 1/3; 空心圆柱体与圆台体之间设有隔水挡板， 隔水挡板中心开孔， 开孔直径 为空心圆柱体直径的 1/3。
钟罩形反应槽 4内安装的搅拌器转速为 35r/min;涡轮 7直径为钟罩形反应槽 4上部空心圆 柱体横截面直径的 1/3， 涡轮 7外缘线速度为 l.Om/s; 涡轮上部搅拌桨 8和下部搅拌桨 6均由 4片桨叶组成， 搅拌桨桨叶外缘线速度为 1.0m/s。
反应器主体 1安装的圆柱形导流板 9， 其直径为反应器主体 1直径的 2/3; 导流板 9上端与 反应器主体 1上端平齐， 下端距反应器主体 1底端 2.0m。 集水堰 12设置在反应器主体 1的 外壳与导流板 9之间距顶端下方 0.4m处， 集水堰 12由 8组集水堰 12组成， 以轮辐形式安装 于反应器主体 1外壳与导流板 9之间， 集水堰 12采用孔口集水堰。 斜管分离器 11设置在反 应器主体 1的外壳与导流板 9之间距顶端下方 2.5m处， 斜管分离器 11由单孔直径 60mm的 斜管构成， 斜管采用管长为 lm的 PE材质， 斜管倾角 50° ， 斜管管长 1.0m， 斜管表面负荷 4m3/(m2 · h)。
环形树脂收集斗 10底距反应器底部 1.0m， 环形树脂收集斗 10的总高为 0.8m，环形树脂收 集斗 10上部环直径为反应器主体 1直径的 1/6。 其他同实施例 1， 处理结果同表 2所示。 实施例 3 ：
本发明的一种机械搅拌内循环树脂离子交换与吸附反应器， 反应器主体 1上部 4/5为敞口圆 柱体 3， 下部 1/5为锥体 2， 锥体 2坡度为 40° ， 反应器主体 1为钢制结构。
钟罩形反应槽 4上部 1/2为空心圆柱体， 下部 1/2为空心圆台体结构； 钟罩形反应槽 4底端 距反应器主体 1底端 0.8m，钟罩形反应槽 4上端距反应器主体 1顶端 1.0m; 空心圆柱体直径 为反应器主体 1外径的 1/3， 圆台体下端直径与空心圆柱体直径相同， 圆台体上端直径为反应 器主体 1外径的 1/2; 空心圆柱体与圆台体之间设有隔水挡板， 隔水挡板中心开孔， 开孔直径 为空心圆柱体直径的 1/2。
钟罩形反应槽 4内安装的搅拌器转速为 45r/min;涡轮 7直径为钟罩形反应槽 4上部空心圆 柱体横截面直径的 1/3， 涡轮 7外缘线速度为 1.5m/s; 涡轮上部搅拌桨 8和下部搅拌桨 6均由 6片桨叶组成， 搅拌桨桨叶外缘线速度为 1.5m/s。 反应器主体 1安装的圆柱形导流板 9， 其直径为反应器主体 1直径的 3/4; 导流板 9上端与 反应器主体 1上端平齐， 下端距反应器主体 1底端 2.5m。 集水堰 12设置在反应器主体 1的 外壳与导流板 9之间距顶端下方 0.5m处， 集水堰 12由 10组集水堰 12组成， 以轮辐形式安 装于反应器主体 1外壳与导流板 9之间， 集水堰 12采用孔口集水堰。 斜管分离器 11设置在 反应器主体 1的外壳与导流板 9之间距顶端下方 3.0m处， 斜管分离器 11由单孔直径 70mm 的斜管构成， 斜管采用管长为 lm的玻璃钢材质， 斜管倾角 55° ， 斜管管长 1.2m， 斜管表面 负荷 5m3/(m2 · h)。
环形树脂收集斗 10底距反应器底部 1.8m， 环形树脂收集斗 10的总高为 1.0m，环形树脂收 集斗 10上部环直径为反应器主体 1直径的 1/5。 其他同实施例 1， 处理结果同表 2所示。

Claims

权 利 要 求 书
1. 一种机械搅拌内循环树脂离子交换与吸附反应器， 其特征是： 反应器主体 （1 ) 上部 2/3〜 4/5为敞口圆柱体 （3)， 下部 1/5〜1/3为锥体 （2)， 锥体 （2)坡度为 30° ± 10° ； 反应器主 体 （1 ) 中心设有钟罩形反应槽 （4)， 钟罩形反应槽 （4) 内设有涡轮引水搅拌器 （5 ) ; 反应 器主体（1 ) 设有圆柱形导流板 （9); 反应器主体（1 ) 的外壳与导流板 （9)之间设置有集水 堰 （12)和斜管分离器 （11 ); 反应器主体 （1 ) 的外壳与导流板 （9)之间下部设有环形树脂 收集斗 （10); 反应器设有进水管 （13)， 进水管 （13 ) 设在钟罩形反应槽（4) 下部的圆台体 区； 出水管 （14)设在集水堰 （12) 出水处； 树脂移出管 （16) 分别连接形树脂收集斗 （10) 和树脂脱附槽 （17)， 再生树脂回流管 （15 ) 通向钟罩形反应槽 （4) 下部的圆台体区。
2. 根据权利要求 1所述的一种机械搅拌内循环树脂离子交换与吸附反应器， 其特征是钟罩形 反应槽（4) 为组合空心回转体， 其轴心与反应器主体 （1 )一致， 该钟罩形反应槽 （4) 上部 1/3〜1/2为空心圆柱体， 下部 1/2〜2/3为空心圆台体结构； 钟罩形反应槽（4)底端距反应器 主体（1 )底端 0.2〜0.8m， 钟罩形反应槽 （4)上端距反应器主体 （1 )顶端 0.5〜1.0m; 空心 圆柱体直径为反应器主体 （1 )外径的 1/5〜1/3， 圆台体下端直径与空心圆柱体直径相同， 圆 台体上端直径为反应器主体 （1 ) 外径的 1/4〜1/2； 空心圆柱体与圆台体之间设有隔水挡板， 隔水挡板中心开孔， 开孔直径为空心圆柱体直径的 1/4〜1/2。
3. 根据权利要求 1或 2所述的一种机械搅拌内循环树脂离子交换与吸附反应器， 其特征是钟 罩形反应槽（4) 中设置的涡轮引水搅拌器 （5 ) 由涡轮 （7)、 涡轮上部搅拌桨 （8 ) 以及涡轮 下部搅拌桨 （6) 构成， 搅拌器转速为 2~50r/min; 涡轮 （7 ) 直径为钟罩形反应槽 （4) 上部 空心圆柱体横截面直径的 1/4〜1/3，涡轮（7 )外缘线速度为 0.1〜1.5m/s;涡轮上部搅拌桨（8 ) 和下部搅拌桨 （6) 均由 2〜6片桨叶组成， 搅拌桨桨叶外缘线速度为 0.2〜2.0m/s。
4. 根据权利要求 1所述的一种机械搅拌内循环树脂离子交换与吸附反应器， 其特征是导流板 ( 9)为空心圆柱体， 其轴心与反应器主体（1 )一致， 其直径为反应器主体（1 )直径的 1/2〜
3/4； 导流板（9)上端与反应器主体（1 )上端平齐， 下端距反应器主体（1 )底端 1.5〜2.5m。
5. 根据权利要求 1所述的一种机械搅拌内循环树脂离子交换与吸附反应器， 其特征是， 集水 堰 （12) 设置在反应器主体 （1 ) 的外壳与导流板 （9) 之间距顶端下方 0.3〜0.5m处， 集水 堰（12)由 4〜12组集水堰（12)组成， 以轮辐形式安装于反应器主体（1 )外壳与导流板（9) 之间， 集水堰 （12) 采用锯齿形集水堰或孔口集水堰。
6. 根据权利要求 1所述的一种机械搅拌内循环树脂离子交换与吸附反应器， 其特征是， 斜管 分离器 （11 ) 设置在反应器主体 （1 ) 的外壳与导流板 （9) 之间距顶端下方 1.5〜3.5m处， 斜管分离器 （11 ) 由单孔直径 50mm〜80mm的斜管构成， 斜管采用 PP、 UPVC、 PE或玻璃
权 利 要 求 书
钢材质中的一种，斜管倾角 45° 〜60° ，斜管管长 0.8m〜1.2m，斜管表面负荷 3〜6m3/(m2 4 )。
7. 根据权利要求 1所述的一种机械搅拌内循环树脂离子交换与吸附反应器， 其特征是， 环形 树脂收集斗 （10) 底距反应器底部 0.5〜2.0m， 环形树脂收集斗 （10) 的总高为 0.5〜1.0m， 环形树脂收集斗 （10) 上部环直径为反应器主体 （1 ) 直径的 1/8〜1/4。
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20130298814A1 (en) * 2010-11-10 2013-11-14 Holger Militz Method for Treating Wood and Wood-Based Materials, and Wood and Wood-Based Materials Obtainable Therewith
CN109019750A (zh) * 2018-10-09 2018-12-18 江苏神洲环境工程有限公司 一种磁性树脂净水设备
CN110270286A (zh) * 2019-06-19 2019-09-24 江阴长盛化工有限公司 一种高纯度mpe热敏纸显色剂缩合系统

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102219284B (zh) 2011-05-16 2012-10-24 南京大学 一种机械搅拌内循环树脂离子交换与吸附反应器
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CN103265092A (zh) * 2013-05-21 2013-08-28 南京理工大学 磁性内循环流化床吸附器
JP6169903B2 (ja) * 2013-06-20 2017-07-26 前澤工業株式会社 水処理方法及び装置
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CN111807470A (zh) * 2020-07-13 2020-10-23 何礼君 一种反洗式离子交换软水机
CN114162893A (zh) * 2021-11-30 2022-03-11 华能营口热电有限责任公司 一种三层套筒式脱硫浆液闪蒸提热系统及其工作方法
US20230249993A1 (en) * 2022-02-10 2023-08-10 Avantech, Llc Apparatus and methods for treating water for removal of pfas

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004020349A1 (fr) * 2002-08-27 2004-03-11 Suez Environnement Procede et dispositif de traitement d'effluents, notamment de l'eau, par separation membranaire.
CN201321393Y (zh) * 2008-12-31 2009-10-07 南京中电联环保股份有限公司 磁性树脂吸附反应器
JP2010036130A (ja) * 2008-08-06 2010-02-18 Kurita Water Ind Ltd アミノ基を有する水溶性有機溶媒の回収方法及び装置
CN101708876A (zh) * 2009-12-25 2010-05-19 南京中电联环保工程有限公司 水力射流磁性树脂吸附反应器
CN101905931A (zh) * 2010-02-11 2010-12-08 南京大学 一种基于磁性树脂的生化尾水深度处理的方法
CN102219284A (zh) * 2011-05-16 2011-10-19 南京大学 一种机械搅拌内循环树脂离子交换与吸附反应器

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3084120A (en) * 1955-07-18 1963-04-02 Infilco Inc Apparatus and process for continuous ion exchange
DE1290118B (de) * 1961-12-04 1969-03-06 Alfred Dipl Ing Vorrichtung und Verfahren zur Durchfuehrung kontinuierlicher Trennungsoperationen in fluessiger Phase mit Hilfe von Ionenaustauschern oder Adsorptionsmitteln
HU905771D0 (en) * 1990-09-04 1991-03-28 Reanal Finomvegyszergyar Apparatus for establishing intensive contact between viscous liquids and low-density solid granulous materials
GB9022003D0 (en) * 1990-10-10 1990-11-21 Interox Chemicals Ltd Purification of hydrogen peroxide
JP2005169365A (ja) * 2003-12-05 2005-06-30 Catalysts & Chem Ind Co Ltd 流動床流通式イオン交換装置
CN102219285B (zh) * 2011-05-17 2013-01-02 南京大学 一种连续流内循环拟流化床树脂离子交换与吸附反应器

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004020349A1 (fr) * 2002-08-27 2004-03-11 Suez Environnement Procede et dispositif de traitement d'effluents, notamment de l'eau, par separation membranaire.
JP2010036130A (ja) * 2008-08-06 2010-02-18 Kurita Water Ind Ltd アミノ基を有する水溶性有機溶媒の回収方法及び装置
CN201321393Y (zh) * 2008-12-31 2009-10-07 南京中电联环保股份有限公司 磁性树脂吸附反应器
CN101708876A (zh) * 2009-12-25 2010-05-19 南京中电联环保工程有限公司 水力射流磁性树脂吸附反应器
CN101905931A (zh) * 2010-02-11 2010-12-08 南京大学 一种基于磁性树脂的生化尾水深度处理的方法
CN102219284A (zh) * 2011-05-16 2011-10-19 南京大学 一种机械搅拌内循环树脂离子交换与吸附反应器

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20130298814A1 (en) * 2010-11-10 2013-11-14 Holger Militz Method for Treating Wood and Wood-Based Materials, and Wood and Wood-Based Materials Obtainable Therewith
CN109019750A (zh) * 2018-10-09 2018-12-18 江苏神洲环境工程有限公司 一种磁性树脂净水设备
CN109019750B (zh) * 2018-10-09 2023-12-01 江苏神洲环境工程有限公司 一种磁性树脂净水设备
CN110270286A (zh) * 2019-06-19 2019-09-24 江阴长盛化工有限公司 一种高纯度mpe热敏纸显色剂缩合系统

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