WO2012155467A1 - 一种连续流内循环拟流化床树脂离子交换与吸附反应器 - Google Patents

一种连续流内循环拟流化床树脂离子交换与吸附反应器 Download PDF

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Publication number
WO2012155467A1
WO2012155467A1 PCT/CN2011/082012 CN2011082012W WO2012155467A1 WO 2012155467 A1 WO2012155467 A1 WO 2012155467A1 CN 2011082012 W CN2011082012 W CN 2011082012W WO 2012155467 A1 WO2012155467 A1 WO 2012155467A1
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WIPO (PCT)
Prior art keywords
reactor
diameter
resin
water
main body
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
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PCT/CN2011/082012
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English (en)
French (fr)
Inventor
龙超
范俊
李爱民
双陈冬
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Nanjing University
Nanjing Tech University
Nanjing University Yancheng Environmental Protection Technology and Engineering Research Institute
Original Assignee
Nanjing University
Nanjing Tech University
Nanjing University Yancheng Environmental Protection Technology and Engineering Research Institute
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Application filed by Nanjing University, Nanjing Tech University, Nanjing University Yancheng Environmental Protection Technology and Engineering Research Institute filed Critical Nanjing University
Priority to US14/117,486 priority Critical patent/US8758608B2/en
Publication of WO2012155467A1 publication Critical patent/WO2012155467A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B01D15/02—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor with moving adsorbents
    • 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
    • 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
    • B01J47/11—Ion-exchange processes in general; Apparatus therefor with moving ion-exchange material; with ion-exchange material in suspension or in fluidised-bed form in rotating beds
    • 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
    • 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
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/308—Dyes; Colorants; Fluorescent agents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/002—Construction details of the apparatus
    • C02F2201/003—Coaxial constructions, e.g. a cartridge located coaxially within another
    • 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, more specifically to a continuous flow internal circulation quasi-fluidized resin ion exchange and adsorption reaction device, in particular to use a solid powder resin or magnetic powder having a diameter of 75-200 ⁇ m.
  • the continuous flow of the bulk resin is internally circulated in the ion exchange and adsorption reactor.
  • 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;
  • Nanjing Zhongdianlian Environmental Engineering Co., Ltd. has also developed a perforated hydrojet magnetic resin reactor; however, the above reactors are fully mixed with resin. In this way, 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, and it is necessary to develop a new reactor to improve the above problems.
  • the invention provides a continuous flow internal circulation quasi-fluidized resin ion exchange and adsorption reactor for the characteristics of small particle size, low density and excellent hydrodynamic performance of the powder resin or the magnetic powder resin, and is suitable for the resin of the resin. Ion exchange and adsorption reaction, The advantages of this type of resin can be fully utilized, and the resin continuous separation and regeneration operation of the resin reaction device can be realized.
  • the apparatus of the present invention that is, the reactor can be applied to the water treatment of the powder resin or the magnetic powder resin, and can also be applied to the deep treatment of the waste water, the biochemical tail water and the middle water of the powder resin or the magnetic powder resin.
  • a continuous flow internal circulation pseudo-fluidized bed resin ion exchange and adsorption reactor comprising a reactor main body shell, a inclined pipe separator, a water collecting weir, an inlet pipe, an outlet pipe, a variable diameter fluidization tank, a deflector, Resin regeneration tank, resin discharge pipe, regenerated resin return pipe, water distribution jet; the bottom of the reactor main body is provided with an inlet pipe and a water distribution jet, the water distribution jet is connected with the inlet pipe, and the water distribution jet is disposed at the center of the reactor main body casing
  • the lower part of the variable diameter fluidization tank is connected, a baffle is arranged between the fluidized grooves of the main body casing of the reactor, a inclined pipe separator is arranged between the outer casing of the reactor main body and the deflector, and a water collecting tank is arranged above the inclined pipe separator.
  • the water collecting tank is connected to the water outlet pipe
  • the resin regeneration tank is connected to the bottom of the reactor and the variable diameter fluidizing tank
  • the upper part of the reactor main body is 2/3 ⁇ 3/4, which is an open cylinder.
  • the lower part is 1/3 ⁇ 1/4, which is a cone.
  • the slope of the cone is 35° ⁇ 10°.
  • the variable diameter fluidization tank is a combined hollow rotary body, and its axial center is consistent with the reactor main body.
  • the bottom end of the variable diameter fluidization tank is 0.2 to 0.8 m from the bottom end of the reactor main body casing, and the upper end is 0.5 to 1.0 m from the top end of the reactor main body casing.
  • the lower part of the radial fluidization tank is 1/4 ⁇ 1/3, which is a hollow cylinder, and the upper part 3/4 ⁇ 2/3 is a hollow circular platform structure;
  • the diameter of the cylinder is 1/5 ⁇ 1/3 of the outer diameter of the reactor, and the lower end of the circular platform
  • the diameter is the same as the diameter of the cylinder, and the diameter of the upper end of the circular table body is 1/4 ⁇ 1/2 of the outer diameter of the reactor;
  • the agitator provided in the variable diameter fluidization tank adopts the propeller blade type, and the diameter of the agitating groove is the lower cylinder of the variable diameter fluidization groove.
  • the section diameter is 1/4 ⁇ 1/3, and the stirrer speed is adjustable from 10-60r/min.
  • the water distribution jet is composed of a water distributor and a combined jet of 2 to 4 circular jet tubes, and the single jet tube is evenly distributed in the radial direction at a distance of 0.2 to 1.0 m from the bottom end of the lower cylindrical body of the variable diameter fluidization tank;
  • the diameter is 1/20 ⁇ 1/8 of the diameter of the lower cylinder of the variable diameter fluidization tank, and the angle between the central axis of the jet tube and the central axis of the variable diameter fluidization tank is 10° ⁇ 60°.
  • the deflector is a hollow cylinder, the axis of which is identical to the reactor body, the diameter of which 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 from the bottom of the reactor. 1.0 ⁇ 1.5m.
  • the water collecting raft consists of 4 ⁇ 12 sets of water collecting weirs, which are installed in the form of spokes between the reactor shell and the deflector and 0.3 ⁇ 0.5m below the top of the reactor.
  • the water collecting raft can adopt zigzag water collecting raft or The orifice collects water.
  • the inclined pipe separator is composed of a single pipe with a diameter of 50mm ⁇ 80mm.
  • 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) Installed between the reactor shell and the deflector and 1.5 to 3.5 m below the top of the reactor.
  • the present invention has the following advantages: 1. It is especially suitable for ion exchange and adsorption reaction of powder resin or magnetic powder resin;
  • variable diameter fluidization tank the powder resin or magnetic powder resin is mainly concentrated in the variable diameter fluidization tank, so that the resin is in full contact with water, the time required for ion exchange and adsorption is short, and the required resin amount is small, accounting for Small area;
  • the main body of the reactor is an open atmospheric pressure vessel, which can be made of metal, organic composite or steel concrete, and the manufacturing cost is low;
  • the resin regeneration tank of the present invention sufficiently separates the powder resin or the magnetic powder resin from water, has a low loss rate, and has low operating cost;
  • the reactor of the invention can be continuously operated by the system design of each component, and the deactivated resin can be continuously removed and regenerated without stopping the water in the reactor, and the recycled resin can be continuously returned to the main body of the device, and the utilization rate of the device is high;
  • FIG. 1 is a schematic view showing the structure of a continuous flow internal circulation pseudo-fluidized bed resin ion exchange and adsorption reactor of the present invention: reactor main body casing 1, cylinder 2, vertebral body 3, jet 4, water distributor 5, variable flow The tank 6, the deflector 7, the inclined pipe separator 8, the water collecting dam 9, the agitator 10, the water inlet pipe 11, the water outlet pipe 12, the clean water zone 13, the resin regeneration tank 14, the resin discharge pipe 15, and the regenerated resin return pipe 16.
  • the continuous flow internal circulation quasi-fluidized bed resin ion exchange and adsorption reactor comprises a reactor main body casing 1, a inclined pipe separator 8, an overflow weir 9, an inlet pipe 11, and an outlet pipe 12, which are characterized by further including variable diameter fluidization.
  • An inclined pipe separator 8 is disposed between the flow plates 7, and a water collecting weir 9 is disposed above the inclined pipe separator 8, and the water collecting weir 9 is connected to the water discharge pipe 12, and the resin regeneration tank 14 passes through the resin discharge pipe 15 and the regenerated resin return pipe.
  • 16 is connected to the bottom of the reactor and the reducing fluidization tank 6, respectively.
  • the main body casing 1 of the reactor has a steel structure, and the upper part is an open cylinder 2 having a diameter of 8.5 m, a height of 4.5 m, a lower portion being a cone 3, a vertebral body 3 having a height of 2.5 m, a cone slope of 35°, and a variable diameter fluidization tank 6
  • the axial center thereof is identical to the reactor main body, and the bottom end of the variable diameter fluidization groove is 0.6 m from the bottom end of the reactor main body casing 1, and the upper end is 0.6 m from the top end of the reactor main body casing (1).
  • the lower part of the runoff tank is 1/3 hollow cylinder
  • the upper part 2/3 is hollow circular platform structure
  • the hollow cylinder is 1.5m in diameter
  • the diameter of the lower end of the round table body is the same as the diameter of the cylinder
  • the diameter of the upper end of the round table body is 4.25m
  • internal filling The variable diameter fluidization tank has a volume of 8% by volume of powder resin or magnetic powder resin, and the powder resin has a diameter of 75 to 200 rn.
  • the agitator provided in the variable diameter fluidization tank adopts a propeller blade type, and the diameter thereof is variable diameter fluidization.
  • the diameter of the cross section of the lower cylinder is 1/3
  • the stirrer speed is adjustable from 10-60 r/min.
  • the water distribution jet is composed of a water distributor 5 and three circular jet tube combined jets 4, and the single jet tube is evenly distributed in the radial direction 0.6 m from the bottom end of the lower cylindrical body of the variable diameter fluidization tank; the diameter of the single jet tube is The diameter of the lower cylinder of the variable fluidization tank is 1/10, and the angle between the central axis of the jet tube and the central axis of the variable diameter fluidization tank is 30°.
  • the incoming water enters the reactor from the inlet pipe 11, and the influent water is distributed into the jet pipe through the water distributor 5, and the mixing flow rate of the single jet pipe is adjusted by the valve and the rotation speed of the mixer in the variable diameter fluidization tank is adjusted to control the mixing intensity in the variable diameter fluidization tank.
  • the resin enters the bottom of the variable diameter fluidization tank with the rising water flow and vortexes upward, and the propeller stirrer 10 in the variable diameter fluidization tank 6 further
  • the water flow is lifted upwards, and the cross-sectional area of the upper portion of the variable-diameter fluidization tank 6 is gradually increased, and the rising water flow rate is gradually reduced, so that the resin is mainly concentrated in the variable-diameter fluidization tank 6, and the variable-size fluidization tank 6 is the main reaction of the resin and the water substance.
  • a negative pressure zone is formed at the bottom end of the variable flow fluidization tank 6 and the bottom end of the reactor, and the powder resin or magnetic powder resin deposited on the bottom of the reactor is sucked into the variable diameter fluidization tank 6, and is in full contact with water.
  • the flow rate of the liquid upflow in the lower cylinder of the runoff tank 6 is controlled at 10 m/h
  • the flow rate of the liquid upflow at the outlet of the upper round table of the variable diameter fluidization tank is controlled at 2m/h
  • the hydraulic retention time in the variable-fluidization tank is 40 minutes
  • various organic and inorganic substances in the water are enriched on the surface of the resin by ion exchange and adsorption.
  • the deflector 7 is a hollow cylinder, the axis of which is identical to the reactor body, the diameter is 2/3 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 1.0 m from the bottom end of the reactor.
  • the deflector 7 directs the resin and water mixture flowing out of the reducing fluidization tank 6 to the lower portion of the reactor, thereby achieving rapid sedimentation separation of the resin and recirculating into the variable diameter fluidization tank.
  • the inclined pipe separator consists of a single pipe with a diameter of 60 mm.
  • the inclined pipe has a dip angle of 60°, the inclined pipe has a length of lm, and the inclined pipe has a surface load of 4 m 3 /(m 2 ⁇ h). It is installed in the reactor casing and the deflector. 2m below the top of the reactor, the inclined pipe separator 8 further promotes the sedimentation separation of the resin in the water.
  • the upper part of the inclined pipe separator and the water collecting sluice are the clear water-free zone 13 without resin.
  • the water collecting weir 9 consists of 6 sets of water collecting weirs, which are installed in the form of spokes between the reactor shell and the deflector and 0.3 ⁇ 0.5m below the top of the reactor.
  • the water collecting tank can adopt the orifice water collecting tank, and the reaction
  • the effluent water is collected through the water collection enthalpy 9 between the reactor casing and the baffle at the top of the reactor and discharged out of the reactor through the outlet pipe 12, and the water flow velocity in the culvert is not more than 1.0 m/s.
  • the spent resin can be sent to the resin regeneration tank 14 through the reactor lower resin discharge pipe 15 for regeneration, and the regenerated resin is returned from the regeneration tank to the reducing fluidization tank of the reactor by the recycled resin return pipe 16; the amount of recycled resin is different according to different water quality Claim And the actual situation is adjusted, generally controlled at 10%.
  • the equipment is used as an advanced treatment device for the biochemical tail water of a printing and dyeing plant.
  • the water quality index and treatment capacity of the powder resin or magnetic powder resin before adsorption treatment are as follows:
  • the waste water is mixed with the regenerated reflow resin and then enters the variable-flow fluidization reaction tank of the reactor, and the amount of the resin is the volume of the variable-diameter fluidization tank.
  • the residence time of the wastewater in the variable fluidization tank is 40 min.
  • the resin and the wastewater are fully contacted by adjusting the rotation speed of the mixer, and the flow rate of the liquid upflow at the outlet of the upper circular table of the variable diameter fluidization tank is controlled at 2 m/h.
  • Part of the resin removed from the lower part of the reactor is sent to the regeneration reaction tank for dynamic regeneration.
  • the regeneration liquid is 10% NaCl solution, and the regenerated resin is refluxed to the reduced-flow fluidization reaction tank of the reactor.
  • the amount of resin removed is controlled in the reactor. 10% of the amount of the resin, the amount of the recycled resin to be replenished coincides with the amount of the resin which is removed and regenerated.
  • the reactor main body casing (1) is made of steel, and the upper part 3/4 is an open cylinder (2) with a diameter of 8.5 m and a height of 7.5 m, the lower part is 1/4 of a cone (3), and the vertebral body 3 is 2.5 m high.
  • the cone slope is 45°, and the variable diameter fluidization tank 6 is a combined hollow rotary body whose axis is identical to the reactor main body.
  • the bottom end of the variable diameter fluidization tank is 0.8 m from the bottom end of the reactor main body casing (1), and the upper end is spaced from the reactor.
  • the top of the main body casing (1) is 1.0m, the lower part of the variable diameter fluidization tank is 1/3, and the upper part is 3/3.
  • the hollow cylinder is 3m in diameter.
  • the diameter of the lower end of the circular table is the same as the diameter of the cylinder.
  • the upper end of the body has a diameter of 4.25m, and the inside is filled with a volume resin having a volume of 10% by volume of a volume resin or a magnetic powder resin.
  • the powder resin has a diameter of 75 to 200 ⁇ m, and the agitator provided in the variable diameter fluidization tank is used.
  • the propeller blade type has a diameter of 1/3 of the cross-sectional diameter of the lower cylinder of the variable-flow fluidization tank, and the agitator rotation speed is adjustable from 10-60 r/min.
  • the water distribution jet is composed of a water distributor 5 and four circular jet tube combined jets 4, and the single jet tube is evenly distributed at a distance of 1.0 m from the bottom end of the lower cylindrical body of the variable diameter fluidization tank; the diameter of the single jet tube is The diameter of the lower cylinder of the variable fluidization tank is 1/8, and the angle between the central axis of the jet tube and the central axis of the variable diameter fluidization tank is 60°.
  • the incoming water enters the reactor from the inlet pipe 11, and the influent water is distributed into the jet pipe through the water distributor 5, and the mixing flow rate of the single jet pipe is adjusted by the valve and the rotation speed of the mixer in the variable diameter fluidization tank is adjusted to control the mixing intensity in the variable diameter fluidization tank.
  • the flow rate of the liquid in the variable flow fluidization tank while controlling the reflux ratio of the resin reaction, the resin enters the bottom of the variable diameter fluidization tank with the rising water flow and vortexes The upward flow, while the propeller agitator 10 in the variable-diameter fluidization tank 6 further lifts the water flow upward.
  • variable-diameter fluidization tank 6 As the cross-sectional area of the upper portion of the variable-diameter fluidization tank 6 is gradually increased, the rising water flow rate is gradually reduced, so that the resin is mainly concentrated in the variable-path flow.
  • the variable-diameter fluidization tank 6 is a main reaction zone of the resin and the water substance; at the same time, a negative pressure zone is formed at the bottom end of the variable-flow fluidization tank 6 and the bottom end of the reactor, and the powder resin or magnetic deposit deposited at the bottom of the reactor The powder resin is sucked into the reducing fluidization tank 6, and is in full contact with the water.
  • the flow rate of the liquid upflow in the lower cylinder of the variable diameter fluidization tank 6 is controlled at 2 m/h, and the flow rate of the liquid upward flow at the outlet of the upper circular orifice of the variable diameter fluidization tank is controlled at lm. /h, the hydraulic retention time in the variable fluidization tank is 0.3h, and various organic and inorganic substances in the water are enriched on the surface of the resin by ion exchange and adsorption.
  • the deflector 7 is a hollow cylinder, the axis of which is identical to the reactor body, the diameter is 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 1.5 m from the bottom end of the reactor.
  • the deflector 7 directs the resin and water mixture flowing out of the reducing fluidization tank 6 to the lower portion of the reactor, thereby achieving rapid sedimentation separation of the resin and recirculating into the variable diameter fluidization tank.
  • the inclined pipe separator consists of a single hole with a diameter of 80mm.
  • the inclined pipe has a inclination of 60°, the inclined pipe has a length of 1.2m, and the inclined pipe has a surface load of 6m 3 /(m 2 * h). It is installed in the reactor shell and the deflector. At a distance of 3.5 m from the top of the reactor, the inclined tube separator 8 further promotes the sedimentation separation of the resin in the water.
  • the upper portion of the inclined tube separator and the water collecting bowl are a clear water-free zone 13 without resin.
  • the water collecting raft 9 is composed of 4 ⁇ 12 sets of water collecting weirs, and is installed in the form of spokes between the reactor shell and the deflector and 0.3 ⁇ 0.5m below the top of the reactor.
  • the water collecting raft can adopt the zigzag water collecting raft.
  • the reactor effluent is collected by the water collection tank 9 between the reactor shell and the baffle at the top of the reactor and discharged out of the reactor through the outlet pipe 12, and the water flow velocity in the water collection tank is not more than 1.0 m/so.
  • the spent resin can be sent to the resin regeneration tank 14 through the reactor lower resin discharge pipe 15 for regeneration, and the regenerated resin is returned from the regeneration tank to the reducing fluidization tank of the reactor by the recycled resin return pipe 16; the amount of recycled resin is different according to different water quality The requirements and actual conditions are adjusted and controlled at 20%.
  • the equipment is used as an advanced treatment device for the biochemical tail water of a printing and dyeing plant, and the water quality and quantity of the powder resin or magnetic powder resin adsorbed into the tail water
  • the waste water is mixed with the regenerated reflow resin and then enters the variable-flow fluidization reaction tank of the reactor, and the amount of the resin is the volume of the variable-diameter fluidization tank.
  • the residence time of wastewater in the variable diameter fluidization tank is 30min, and the resin and wastewater are realized by adjusting the speed of the mixer. Fully contact, and maintain the flow rate of the liquid upflow at the outlet of the upper circular table of the variable flow fluidization tank at 2m/h.
  • Part of the resin removed from the lower part of the reactor is sent to the regeneration reaction tank for dynamic regeneration.
  • the regeneration liquid is 10% NaCl solution, and the regenerated resin is refluxed to the reduced-flow fluidization reaction tank of the reactor.
  • the amount of resin removed is controlled in the reactor. Amount of resin
  • the amount of regenerated resin added is consistent with the amount of resin removed.
  • the reactor main body casing (1) is made of steel, and the upper part 2/3 is an open cylinder (2) with a diameter of 8.5 m, a height of 4.5 m, a lower part of 1/3 being a cone (3), and a vertebral body 3 being 1.5 m high.
  • the cone slope is 25°
  • the variable diameter fluidization tank 6 is a combined hollow rotary body whose axis is identical with the reactor main body.
  • the bottom end of the variable diameter fluidization tank is 0.2 m from the bottom end of the reactor main body casing (1), and the upper end is spaced from the reactor.
  • the top of the main body casing (1) is 0.5m
  • the lower part of the variable diameter fluidization tank is 1/4 hollow cylinder
  • the upper part 3/4 is hollow circular platform structure
  • the diameter of the hollow cylinder is 1/5 of the outer diameter of the reactor
  • the diameter of the lower end of the circular table body The diameter of the upper end of the circular table body is 1/4 of the outer diameter of the reactor, and the internal volume of the fluidized groove is 2% by volume of the powder resin or magnetic powder resin.
  • the diameter of the powder resin is between 75 ⁇ 200 rn
  • the agitator set in the variable diameter fluidization tank adopts the propeller blade type, and its diameter is 1/4 of the cross-sectional diameter of the lower cylinder of the variable-diameter fluidization tank, and the agitator rotation speed is adjustable from 10-60 r/min.
  • the water distribution jet is composed of a water distributor 5 and two circular jet tube combined jets 4, and the single jet tube is evenly distributed at a distance of 0.2 m from the bottom end of the lower cylindrical body of the variable diameter fluidization tank; the diameter of the single jet tube is The diameter of the lower cylinder of the variable fluidization tank is 1/20, and the angle between the central axis of the jet tube and the central axis of the variable diameter fluidization tank is 10°.
  • the incoming water enters the reactor from the inlet pipe 11, and the influent water is distributed into the jet pipe through the water distributor 5, and the mixing flow rate of the single jet pipe is adjusted by the valve and the rotation speed of the mixer in the variable diameter fluidization tank is adjusted to control the mixing intensity in the variable diameter fluidization tank.
  • the resin enters the bottom of the variable diameter fluidization tank with the rising water flow and vortexes upward, and the propeller stirrer 10 in the variable diameter fluidization tank 6 further
  • the water flow is lifted upwards, and the cross-sectional area of the upper portion of the variable-diameter fluidization tank 6 is gradually increased, and the rising water flow rate is gradually reduced, so that the resin is mainly concentrated in the variable-diameter fluidization tank 6, and the variable-size fluidization tank 6 is the main reaction of the resin and the water substance.
  • a negative pressure zone is formed at the bottom end of the variable flow fluidization tank 6 and the bottom end of the reactor, and the powder resin or magnetic powder resin deposited on the bottom of the reactor is sucked into the variable diameter fluidization tank 6, and is in full contact with water.
  • the flow rate of the liquid upflow in the lower cylinder of the runoff tank 6 is controlled at 20 m/h
  • the flow rate of the liquid upflow at the outlet of the upper round table of the variable diameter fluidization tank is controlled at 5m/h
  • the hydraulic retention time in the variable-flow fluidization tank is 1.0h
  • various organic and inorganic substances in the water are enriched on the surface of the resin by ion exchange and adsorption.
  • the deflector 7 is a hollow cylinder, the axis of which is identical to the reactor body, the diameter of which is 1/2 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 1.0 m from the bottom end of the reactor.
  • the deflector 7 guides the resin and water mixture flowing out of the reducing fluidization tank 6 to the lower portion of the reactor, thereby achieving rapid sedimentation separation of the resin and recirculating into the variable diameter fluidization tank. Medium.
  • the inclined pipe separator consists of a single pipe with a diameter of 50mm.
  • the inclined pipe has a inclination of 45°, the inclined pipe has a length of 0.8m, and the inclined pipe has a surface load of 3m 3 /(m 2 * h). It is installed in the reactor shell and the deflector. Between 1.5m below the top of the reactor, the inclined pipe separator 8 further promotes the sedimentation separation of the resin in the water.
  • the upper portion of the inclined pipe separator and the water collecting sluice are the clear water-free zone 13 without resin.
  • the water collecting weir 9 consists of 4 ⁇ 12 sets of water collecting weirs, which are installed in the form of spokes between the reactor shell and the deflector and 0.3m below the top of the reactor.
  • the water collecting weir can adopt the zigzag water collecting weir.
  • the effluent water is collected through the water collection enthalpy 9 between the reactor casing and the baffle at the top of the reactor and discharged out of the reactor through the outlet pipe 12, and the water flow velocity in the culvert is not more than 1.0 m/s.
  • the spent resin can be sent to the resin regeneration tank 14 through the reactor lower resin discharge pipe 15 for regeneration, and the regenerated resin is returned from the regeneration tank to the reducing fluidization tank of the reactor by the recycled resin return pipe 16; the amount of recycled resin is different according to different water quality
  • the requirements and actual conditions are adjusted and controlled at 5%.
  • the equipment is used as an advanced treatment device for the biochemical tail water of a printing and dyeing plant, and the powder resin or magnetic powder resin is adsorbed.
  • the waste water is mixed with the regenerated reflow resin and then enters the variable-flow fluidization reaction tank of the reactor, and the amount of the resin is the volume of the variable-diameter fluidization tank.
  • variable-flow fluidization tank lh 5% volume fraction
  • residence time of wastewater in the variable-flow fluidization tank lh, the resin and wastewater are fully contacted by adjusting the rotation speed of the mixer, and the flow rate of the liquid upflow at the outlet of the upper circular table of the variable-diameter fluidization tank is controlled at 20m/h.
  • Part of the resin removed from the lower part of the reactor is sent to the regeneration reaction tank for dynamic regeneration.
  • the regeneration liquid is 10% NaCl solution, and the regenerated resin is refluxed to the reduced-flow fluidization reaction tank of the reactor.
  • the amount of resin removed is controlled in the reactor. 10% of the amount of the resin, the amount of the recycled resin to be replenished coincides with the amount of the resin which is removed and regenerated.

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Description

一种连续流内循环拟流化床树脂离子交换与吸附反应器 技术领域
本发明涉及一种树脂离子交换与吸附设备， 更具体的说是一种连续流内循环拟流化树脂离 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连续流 水力内循环离子交换与吸附反应器。
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， 有必要开发新型反应器改善上述问题。
发明内容
本发明所要解决的技术问题
针对粉体树脂或磁性粉体树脂的小粒径、 低密度、 流体力学性能优的特点， 本发明提供一种 连续流内循环拟流化树脂离子交换与吸附反应器， 适用于该类树脂的离子交换与吸附反应， 可以充分发挥该类树脂的优势， 并实现树脂反应装置的树脂连续分离再生运行。 本发明装置 即反应器既可适用于粉体树脂或磁性粉体树脂的给水处理， 也可适用于粉体树脂或磁性粉体 树脂的废水、 生化尾水及中水的深度处理。
技术方案
一种连续流内循环拟流化床树脂离子交换与吸附反应器， 包括反应器主体外壳、斜管分离器、 集水堰、 进水管、 出水管， 还包括变径流化槽、 导流板、 树脂再生槽、 树脂排出管、 再生树 脂回流管、 配水射流器； 反应器主体外壳底部设有进水管和配水射流器， 配水射流器与进水 管连接， 配水射流器与设置于反应器主体外壳中心的变径流化槽下部相连接， 反应器主体外 壳变径流化槽之间设置导流板， 反应器主体外壳与导流板之间设置斜管分离器， 斜管分离器 的上方设置集水堰， 集水堰与出水管相连接， 树脂再生槽通过树脂排出管和再生树脂回流管 分别与反应器底部、 变径流化槽相连接。
反应器主体外壳上部 2/3〜3/4为敞口圆柱体，下部 1/3〜1/4为锥体，锥体坡度 35° ± 10° 。 变径流化槽为组合空心回转体， 其轴心与反应器主体一致， 变径流化槽底端距反应器主体 外壳底端 0.2〜0.8m， 上端距反应器主体外壳顶端 0.5〜1.0m， 变径流化槽下部 1/4〜 1/3为空 心圆柱体,上部 3/4〜2/3为空心圆台体结构； 圆柱体直径为反应器外径的 1/5〜1/3， 圆台体下 端直径与圆柱体直径相同， 圆台体上端直径为反应器外径的 1/4〜1/2； 变径流化槽中设置的 搅拌器采用螺旋桨叶式， 其直径为变径流化槽下部圆柱体横截面直径的 1/4〜1/3， 搅拌器转 速 10-60r/min可调。
配水射流器由配水器与 2〜4支圆形射流管组合射流器构成，单支射流管沿径向均布于距变 径流化槽下部圆柱体底端 0.2〜1.0m 处； 单支射流管直径为变径流化槽下部圆柱体直径的 1/20〜1/8， 射流管中心轴与变径流化槽中心轴夹角为 10° 〜60° 。
导流板为空心圆柱体， 其轴心与反应器主体一致， 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， 下端距反应器底端 1.0〜1.5m。
集水堰由 4〜12组集水堰组成， 以轮辐形式安装于反应器外壳与导流板之间并距反应器顶 端下方 0.3〜0.5m处， 集水堰可采用锯齿形集水堰或孔口集水堰。
斜管分离器由单孔直径 50mm〜80mm的斜管构成，斜管倾角 45° 〜60° ，斜管管长 0.8m〜 1.2m, 斜管表面负荷 3〜6m3/(m2 · h)， 安装于反应器外壳与导流板之间并距反应器顶端下方 1.5〜3.5m处。
有益效果
本发明相对于现有技术， 具有以下有益之处： 1. 特别适合于粉体树脂或磁性粉体树脂的离子交换与吸附反应；
2. 通过改变射流器进水流量及搅拌器转速动态控制内循环量， 同时粉体树脂或磁性粉体树脂 与水接触程度较高；
3. 通过变径流化槽的设计， 使粉体树脂或磁性粉体树脂主要集中于变径流化槽， 使树脂与水 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；
4. 反应器主体外壳为敞口常压容器， 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. 通过本发明中的树脂再生槽， 使粉体树脂或磁性粉体树脂与水分离充分， 流失率低， 运行 成本低；
6. 本发明中反应器通过对各部件的系统设计， 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， 操作简便， 可方便实现自动化运行。 附图说明
附图 1是本发明一种连续流内循环拟流化床树脂离子交换与吸附反应器结构示意图： 反应 器主体外壳 1、 圆柱体 2、 椎体 3、 射流器 4、 配水器 5、 变径流化槽 6、 导流板 7、 斜管 分离器 8、 集水堰 9、 搅拌器 10、 进水管 11、 出水管 12、 清水区 13、 树脂再生槽 14、 树 脂排出管 15、 再生树脂回流管 16。
具体实施方式
连续流内循环拟流化床树脂离子交换与吸附反应器，包括反应器主体外壳 1、斜管分离器 8、 溢流堰 9、进水管 11、出水管 12，其特征在于还包括变径流化槽 6、导流板 7、树脂再生槽 14、 树脂排出管 15、 再生树脂回流管 16、 配水射流器； 反应器主体外壳 1底部设有进水管 11和 配水射流器， 配水射流器与进水管 11连接， 配水射流器与设置于反应器主体外壳 1中心的变 径流化槽 6下部相连接， 反应器主体外壳 1变径流化槽 6之间设置导流板 7， 反应器主体外 壳 1与导流板 7之间设置斜管分离器 8， 斜管分离器 8的上方设置集水堰 9， 集水堰 9与出水 管 12相连接， 树脂再生槽 14通过树脂排出管 15和再生树脂回流管 16分别与反应器底部、 变径流化槽 6相连接。
实施例 1
反应器主体外壳 1为钢制结构， 上部为敞口圆柱体 2直径为 8.5m， 高 4.5m， 下部为锥体 3， 椎体 3高 2.5m，锥体坡度 35° ，变径流化槽 6为组合空心回转体，其轴心与反应器主体一致， 变径流化槽底端距反应器主体外壳 1底端 0.6m， 上端距反应器主体外壳 （1 ) 顶端 0.6m， 变 径流化槽下部 1/3为空心圆柱体，上部 2/3为空心圆台体结构， 空心圆柱体直径为 1.5m， 圆台 体下端直径与圆柱体直径相同， 圆台体上端直径为 4.25m， 内部填充变径流化槽体积 8%体积 百分比的粉体树脂或磁性粉体树脂， 粉体树脂直径介于 75〜200 rn, 变径流化槽中设置的 搅拌器采用螺旋桨叶式， 其直径为变径流化槽下部圆柱体横截面直径的 1/3， 搅拌器转速 10-60r/min可调。
配水射流器由配水器 5与 3支圆形射流管组合射流器 4构成， 单支射流管沿径向均布于距 变径流化槽下部圆柱体底端 0.6m处； 单支射流管直径为变径流化槽下部圆柱体直径的 1/10， 射流管中心轴与变径流化槽中心轴夹角为 30° 。
来水由进水管 11进入反应器， 进水经配水器 5分配进入射流管， 通过阀门调节单根射流管 进水流量及调节变径流化槽内搅拌机转速可控制变径流化槽内混合剧烈程度及变径流化槽内 的液体上升流速， 同时控制树脂反应的回流比， 树脂随上升水流进入变径流化槽底部并涡旋 向上流动， 同时变径流化槽 6中的螺旋桨式搅拌器 10进一步将水流向上提升， 由于变径流化 槽 6上部横截面面积逐渐增大， 上升水流速逐渐变小， 使得树脂主要集中于变径流化槽 6中， 变径流化槽 6为树脂与水中物质的主要反应区； 同时在变径流化槽 6底端与反应器底端形成 负压区， 沉积于反应器底部的粉体树脂或磁性粉体树脂被吸入变径流化槽 6中， 与水充分接 触， 变径流化槽 6下部圆柱体内液体上升流流速控制在 10m/h， 变径流化槽上部圆台体出口 液体上升流流速控制在 2m/h， 变径流化槽内水力停留时间 40分钟， 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。
导流板 7为空心圆柱体， 其轴心与反应器主体一致， 直径为反应器主体直径的 2/3， 导流板 上端与反应器主体上端平齐， 下端距反应器底端 1.0m， 导流板 7将变径流化槽 6流出的树脂 与水混合物导流至反应器下部， 从而实现树脂的快速沉降分离， 并重新循环进入变径流化槽 中。
斜管分离器由单孔直径 60mm的斜管构成， 斜管倾角 60° ， 斜管管长 lm， 斜管表面负荷 4m3/(m2 · h)， 安装于反应器外壳与导流板之间并距反应器顶端下方 2m处， 斜管分离器 8， 进一步促进水中树脂的沉降分离， 斜管分离器上部与集水堰之间为不含树脂的清水区 13。 集水堰 9由 6组集水堰组成， 以轮辐形式安装于反应器外壳与导流板之间并距反应器顶端 下方 0.3〜0.5m处， 集水堰可采用孔口集水堰， 反应器出水经反应器顶部介于反应器外壳与 导流板之间的集水堰 9收集并经出水管 12排出反应器， 集水堰中水流速度不大于 1.0m/s。 失效树脂可通过反应器下部树脂排出管道 15送入树脂再生槽 14进行再生， 再生后的树脂 由再生树脂回流管 16从再生槽回流至反应器的变径流化槽中；再生树脂量根据不同水质要求 及实际情况进行调整， 一般控制在 10%。
采用该设备作为某印染厂废水生化后尾水的深度处理装置， 粉体树脂或磁性粉体树脂吸附 处理前水质指标及处理量如下：
进水尾水的水质水量
Figure imgf000007_0001
该废水与再生回流树脂混合后进入反应器的变径流化反应槽中， 树脂量为变径流化槽体积的
5%体积分数， 废水在变径流化槽中停留时间 40min， 通过调节搅拌机转速实现树脂与废水的 充分接触， 并保持变径流化槽上部圆台体出口液体上升流流速控制在 2m/h。
反应器下部移出的部分树脂输送至再生反应槽中动态再生， 再生液采用 10%NaCl溶液， 再 生后的树脂回流至反应器的变径流化反应槽中； 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。
处理后的出水水质 CODcr 35〜45mg/l 总氮 5〜8mg/l 总磷 0.1〜0.2mg/l色度 5-10倍。 实施例 2
反应器主体外壳 （1 ) 为钢制结构， 上部 3/4为敞口圆柱体 （2) 直径为 8.5m， 高 7.5m， 下部 1/4为锥体 （3)， 椎体 3高 2.5m， 锥体坡度 45° ， 变径流化槽 6为组合空心回转体， 其轴心 与反应器主体一致， 变径流化槽底端距反应器主体外壳 （1 ) 底端 0.8m， 上端距反应器主体 外壳（1 )顶端 1.0m， 变径流化槽下部 1/3为空心圆柱体，上部 2/3为空心圆台体结构， 空心圆 柱体直径为 3m， 圆台体下端直径与圆柱体直径相同， 圆台体上端直径为 4.25m， 内部填充变 径流化槽体积 10%体积百分比的粉体树脂或磁性粉体树脂，粉体树脂直径介于 75〜200 μ m， 变径流化槽中设置的搅拌器采用螺旋桨叶式， 其直径为变径流化槽下部圆柱体横截面直径的 1/3， 搅拌器转速 10-60r/min可调。
配水射流器由配水器 5与 4支圆形射流管组合射流器 4构成， 单支射流管沿径向均布于距 变径流化槽下部圆柱体底端 1.0m处； 单支射流管直径为变径流化槽下部圆柱体直径的 1/8， 射流管中心轴与变径流化槽中心轴夹角为 60° 。
来水由进水管 11进入反应器， 进水经配水器 5分配进入射流管， 通过阀门调节单根射流管 进水流量及调节变径流化槽内搅拌机转速可控制变径流化槽内混合剧烈程度及变径流化槽内 的液体上升流速， 同时控制树脂反应的回流比， 树脂随上升水流进入变径流化槽底部并涡旋 向上流动， 同时变径流化槽 6中的螺旋桨式搅拌器 10进一步将水流向上提升， 由于变径流化 槽 6上部横截面面积逐渐增大， 上升水流速逐渐变小， 使得树脂主要集中于变径流化槽 6中， 变径流化槽 6为树脂与水中物质的主要反应区； 同时在变径流化槽 6底端与反应器底端形成 负压区， 沉积于反应器底部的粉体树脂或磁性粉体树脂被吸入变径流化槽 6中， 与水充分接 触， 变径流化槽 6下部圆柱体内液体上升流流速控制在 2m/h， 变径流化槽上部圆台体出口液 体上升流流速控制在 lm/h， 变径流化槽内水力停留时间 0.3h， 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。
导流板 7为空心圆柱体， 其轴心与反应器主体一致， 直径为反应器主体直径的 3/4， 导流板 上端与反应器主体上端平齐， 下端距反应器底端 1.5m， 导流板 7将变径流化槽 6流出的树脂 与水混合物导流至反应器下部， 从而实现树脂的快速沉降分离， 并重新循环进入变径流化槽 中。
斜管分离器由单孔直径 80mm的斜管构成， 斜管倾角 60° ， 斜管管长 1.2m， 斜管表面负荷 6m3/(m2 * h)， 安装于反应器外壳与导流板之间并距反应器顶端下方 3.5m处， 斜管分离器 8， 进一步促进水中树脂的沉降分离， 斜管分离器上部与集水堰之间为不含树脂的清水区 13。 集水堰 9由 4〜12组集水堰组成， 以轮辐形式安装于反应器外壳与导流板之间并距反应器 顶端下方 0.3〜0.5m处， 集水堰可采用锯齿形集水堰， 反应器出水经反应器顶部介于反应器 外壳与导流板之间的集水堰 9 收集并经出水管 12 排出反应器， 集水堰中水流速度不大于 1.0m/s o
失效树脂可通过反应器下部树脂排出管道 15送入树脂再生槽 14进行再生， 再生后的树脂 由再生树脂回流管 16从再生槽回流至反应器的变径流化槽中；再生树脂量根据不同水质要求 及实际情况进行调整， 控制在 20%。
采用该设备作为某印染厂废水生化后尾水的深度处理装置， 粉体树脂或磁性粉体树脂吸附 进水尾水的水质水量
Figure imgf000008_0001
该废水与再生回流树脂混合后进入反应器的变径流化反应槽中， 树脂量为变径流化槽体积的
5%体积分数， 废水在变径流化槽中停留时间 30min， 通过调节搅拌机转速实现树脂与废水的 充分接触， 并保持变径流化槽上部圆台体出口液体上升流流速控制在 2m/h。
反应器下部移出的部分树脂输送至再生反应槽中动态再生， 再生液采用 10%NaCl溶液， 再 生后的树脂回流至反应器的变径流化反应槽中； 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。
处理后的出水水质 CODcr50〜60mg/l 总氮 6〜10mg/l 总憐 0.1〜0.2mg/l色度 15-30倍。 实施例 3
反应器主体外壳 （1 ) 为钢制结构， 上部 2/3为敞口圆柱体 （2) 直径为 8.5m， 高 4.5m， 下部 1/3为锥体 （3)， 椎体 3高 1.5m， 锥体坡度 25° ， 变径流化槽 6为组合空心回转体， 其轴心 与反应器主体一致， 变径流化槽底端距反应器主体外壳 （1 ) 底端 0.2m， 上端距反应器主体 外壳（1 )顶端 0.5m， 变径流化槽下部 1/4为空心圆柱体，上部 3/4为空心圆台体结构， 空心圆 柱体直径为反应器外径的 1/5， 圆台体下端直径与圆柱体直径相同， 圆台体上端直径为为反应 器外径的 1/4， 内部填充变径流化槽体积 2%体积百分比的粉体树脂或磁性粉体树脂， 粉体树 脂直径介于 75〜200 rn, 变径流化槽中设置的搅拌器采用螺旋桨叶式， 其直径为变径流化 槽下部圆柱体横截面直径的 1/4， 搅拌器转速 10-60r/min可调。
配水射流器由配水器 5与 2支圆形射流管组合射流器 4构成， 单支射流管沿径向均布于距 变径流化槽下部圆柱体底端 0.2m处； 单支射流管直径为变径流化槽下部圆柱体直径的 1/20， 射流管中心轴与变径流化槽中心轴夹角为 10° 。
来水由进水管 11进入反应器， 进水经配水器 5分配进入射流管， 通过阀门调节单根射流管 进水流量及调节变径流化槽内搅拌机转速可控制变径流化槽内混合剧烈程度及变径流化槽内 的液体上升流速， 同时控制树脂反应的回流比， 树脂随上升水流进入变径流化槽底部并涡旋 向上流动， 同时变径流化槽 6中的螺旋桨式搅拌器 10进一步将水流向上提升， 由于变径流化 槽 6上部横截面面积逐渐增大， 上升水流速逐渐变小， 使得树脂主要集中于变径流化槽 6中， 变径流化槽 6为树脂与水中物质的主要反应区； 同时在变径流化槽 6底端与反应器底端形成 负压区， 沉积于反应器底部的粉体树脂或磁性粉体树脂被吸入变径流化槽 6中， 与水充分接 触， 变径流化槽 6下部圆柱体内液体上升流流速控制在 20m/h， 变径流化槽上部圆台体出口 液体上升流流速控制在 5m/h， 变径流化槽内水力停留时间 1.0h， 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。
导流板 7为空心圆柱体， 其轴心与反应器主体一致， 直径为反应器主体直径的 1/2， 导流板 上端与反应器主体上端平齐， 下端距反应器底端 1.0m， 导流板 7将变径流化槽 6流出的树脂 与水混合物导流至反应器下部， 从而实现树脂的快速沉降分离， 并重新循环进入变径流化槽 中。
斜管分离器由单孔直径 50mm的斜管构成， 斜管倾角 45° ， 斜管管长 0.8m， 斜管表面负荷 3m3/(m2 * h)， 安装于反应器外壳与导流板之间并距反应器顶端下方 1.5m处， 斜管分离器 8， 进一步促进水中树脂的沉降分离， 斜管分离器上部与集水堰之间为不含树脂的清水区 13。 集水堰 9由 4〜12组集水堰组成， 以轮辐形式安装于反应器外壳与导流板之间并距反应器 顶端下方 0.3m处， 集水堰可采用锯齿形集水堰， 反应器出水经反应器顶部介于反应器外壳与 导流板之间的集水堰 9收集并经出水管 12排出反应器， 集水堰中水流速度不大于 1.0m/s。 失效树脂可通过反应器下部树脂排出管道 15送入树脂再生槽 14进行再生， 再生后的树脂 由再生树脂回流管 16从再生槽回流至反应器的变径流化槽中；再生树脂量根据不同水质要求 及实际情况进行调整， 控制在 5%。
采用该设备作为某印染厂废水生化后尾水的深度处理装置， 粉体树脂或磁性粉体树脂吸附
Figure imgf000010_0001
该废水与再生回流树脂混合后进入反应器的变径流化反应槽中， 树脂量为变径流化槽体积的
5%体积分数，废水在变径流化槽中停留时间 lh，通过调节搅拌机转速实现树脂与废水的充分 接触， 并保持变径流化槽上部圆台体出口液体上升流流速控制在 20m/h。
反应器下部移出的部分树脂输送至再生反应槽中动态再生， 再生液采用 10%NaCl溶液， 再 生后的树脂回流至反应器的变径流化反应槽中； 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。
处理后的出水水质 CODcr 55〜65mg/l 总氮 5〜9mg/l 总磷 0.1〜0.2mg/l色度 10-15倍。

Claims

1. 一种连续流内循环拟流化床树脂离子交换与吸附反应器， 包括反应器主体外壳 （1 )、 斜管 分离器 （8)、 集水堰 （9) 进水管 （11 )、 出水管 （12)， 其特征在于还包括变径流化槽 （6)、 导流板 （7 )树脂再生槽 （14)、 树脂排出管 （15)、 再生树脂回流管 （16)、 配水射流器； 反 应器主体外壳 （1 ) 底部设有进水管 （11 ) 和配水射流器， 配水射流器与进水管 （11 ) 连接， 配水射流器与设置于反应器主体外壳 （1 ) 中心的变径流化槽 （6 ) 下部相连接， 反应器主体 外壳 （1 ) 与变径流化槽 （6) 之间设置导流板 （7)， 反应器主体外壳 （1 ) 与导流板 （7 ) 之 间设置斜管分离器（8)， 斜管分离器（8 ) 的上方设置集水堰（9)， 集水堰（9)与出水管 (12) 相连接， 树脂再生槽 （14)通过树脂排出管 （15 ) 和再生树脂回流管 （16 ) 分别与反应器底 部、 变径流化槽 （6) 相连接。
2. 根据权利要求 1所述的一种连续流内循环拟流化床树脂离子交换与吸附反应器， 其特征是 反应器主体外壳（1 )上部 2/3〜3/4为敞口圆柱体（2)， 下部 1/3〜1/4为锥体（3)， 锥体坡度 35° ± 10° 。
3. 根据权利要求 2所述的一种连续流内循环拟流化床树脂离子交换与吸附反应器， 其特征是 变径流化槽为组合空心回转体， 其轴心与反应器主体一致， 变径流化槽底端距反应器主体外 壳（1 )底端 0.2〜0.8m， 上端距反应器主体外壳（1 )顶端 0.5〜1.0m， 变径流化槽下部 1/4〜 1/3为空心圆柱体，上部 3/4〜2/3为空心圆台体结构； 圆柱体直径为反应器外径的 1/5〜1/3， 圆 台体下端直径与圆柱体直径相同， 圆台体上端直径为反应器外径的 1/4〜1/2。
4. 根据权利要求 3所述的一种连续流内循环拟流化床树脂离子交换与吸附反应器， 其特征是 配水射流器由配水器（5 )与 2〜4支圆形射流管组合射流器（4)构成， 单支射流管沿径向均 布于距变径流化槽下部圆柱体底端 0.2〜1.0m处； 单支射流管直径为变径流化槽下部圆柱体 直径的 1/20〜1/8， 射流管中心轴与变径流化槽中心轴夹角为 10° 〜60° 。
5. 根据权利要求 1〜4中任一项所述的一种连续流内循环拟流化床树脂离子交换与吸附反应 器， 其特征是变径流化槽中设置的搅拌器 （10) 采用螺旋桨叶式， 其直径为变径流化槽下部 圆柱体横截面直径的 1/4〜1/3， 搅拌器转速 10-60r/min可调。
6. 根据权利要求 1〜4 中任一项所述的一种连续流内循环拟流化床树脂离子交换与吸附反应 器，其特征是导流板为空心圆柱体，其轴心与反应器主体一致，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， 下端距反应器底端 1.0〜1.5m。
7. 根据权利要求 1〜4 中任一项所述的一种连续流内循环拟流化床树脂离子交换与吸附反应 器， 其特征是集水堰由 4〜12组集水堰组成， 以轮辐形式安装于反应器外壳与导流板之间并 距反应器顶端下方 0.3〜0.5m处， 集水堰可采用锯齿形集水堰或孔口集水堰。
8. 根据权利要求 1〜4 中任一项所述的一种连续流内循环拟流化床树脂离子交换与吸附反应 器， 其特征是斜管分离器由单孔直径 50mm〜80mm的斜管构成， 斜管倾角 45° 〜60° ， 斜 管管长 0.8m〜1.2m， 斜管表面负荷 3〜6m3/(m2 · h)， 安装于反应器外壳与导流板之间并距反 应器顶端下方 1.5〜3.5m处。
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