CN109942065B - Reduction fluidized bed and application and use method thereof - Google Patents
Reduction fluidized bed and application and use method thereof Download PDFInfo
- Publication number
- CN109942065B CN109942065B CN201711394357.2A CN201711394357A CN109942065B CN 109942065 B CN109942065 B CN 109942065B CN 201711394357 A CN201711394357 A CN 201711394357A CN 109942065 B CN109942065 B CN 109942065B
- Authority
- CN
- China
- Prior art keywords
- layer
- fluidized bed
- reducing
- ejector
- reducing agent
- 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.)
- Active
Links
- 230000009467 reduction Effects 0.000 title claims abstract description 25
- 238000000034 method Methods 0.000 title claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 66
- 239000007787 solid Substances 0.000 claims abstract description 44
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 43
- 239000007788 liquid Substances 0.000 claims abstract description 39
- 238000009826 distribution Methods 0.000 claims abstract description 25
- 238000005243 fluidization Methods 0.000 claims abstract description 18
- 238000005352 clarification Methods 0.000 claims abstract description 6
- 230000000149 penetrating effect Effects 0.000 claims abstract description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 33
- 229910052742 iron Inorganic materials 0.000 claims description 13
- 238000001514 detection method Methods 0.000 claims description 6
- 239000000843 powder Substances 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 239000010802 sludge Substances 0.000 claims 2
- 230000005465 channeling Effects 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 238000005299 abrasion Methods 0.000 abstract description 6
- 238000009991 scouring Methods 0.000 abstract description 3
- 238000006722 reduction reaction Methods 0.000 description 19
- 230000003197 catalytic effect Effects 0.000 description 15
- 239000007789 gas Substances 0.000 description 13
- 238000003756 stirring Methods 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 10
- 230000000694 effects Effects 0.000 description 7
- 238000002347 injection Methods 0.000 description 7
- 239000007924 injection Substances 0.000 description 7
- 238000007254 oxidation reaction Methods 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 230000000630 rising effect Effects 0.000 description 6
- 239000012028 Fenton's reagent Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 230000003647 oxidation Effects 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 238000005260 corrosion Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 230000008859 change Effects 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 238000007086 side reaction Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 239000002638 heterogeneous catalyst Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses a reduction fluidized bed, and application and a using method thereof. The reduction fluidized bed comprises the following components sequentially connected from top to bottom: a clarification layer, a diversion layer and a fluidization layer; the clarifying layer comprises a liquid collecting area, a three-phase separator and a buffer area which are sequentially connected from top to bottom, a double-layer overflow weir is annularly arranged on the inner wall of the liquid collecting area, and a reducing agent feeder is arranged in the middle of the clarifying layer in a penetrating manner; the outer wall of the guide layer is gradually reduced in size from top to bottom; at least one sprayer is vertically arranged at the bottom of the fluidization layer, and a plurality of solid distribution plates are arranged around the sprayer; the ejector is provided with a water suction port, one end of the solid distribution plate is connected with the lower end of the water suction port, and the other end of the solid distribution plate is connected with the wall surface of the fluidized layer or another adjacent ejector. The reduction fluidized bed has high mixing efficiency and low operation energy consumption, does not generate the condition of mechanical scouring, and can reduce the abrasion of the structure.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a reduction fluidized bed and application and a using method thereof.
Background
In the field of sewage treatment, fenton oxidation technology is a high-grade oxidation technology applied to sewage treatment, and has the characteristics of simple equipment, strong oxidation capacity, high removal rate of chemical oxygen demand COD (Chemical Oxygen Demand) and the like, and has wide application in the fields of pretreatment and advanced treatment of industrial wastewater. The Fenton oxidation mechanism is Fe 2+ And H is 2 O 2 On the one hand, the Fenton reagent generates a large amount of hydroxyl free radicals under the acidic condition, and the high oxidization property of the Fenton reagent is utilized to degrade macromolecular organic pollutants in the wastewater into micromolecular organic matters, and the micromolecular organic matters can be further oxidized into CO 2 And H 2 O; on the other hand, fenton reagent can produce Fe (OH) 3 Flocculent colloid is removed by flocculation and adsorptionPart of the organic matters.
However, the Fenton oxidation technology has the greatest side effect, the generated iron mud amount is increased in proportion with the increase of the Fenton reagent amount, if the iron mud is not treated correspondingly, a great amount of secondary pollution is generated, most of the iron-containing mud in the field of industrial water treatment is considered as dangerous waste, the treatment cost is higher than that of general waste, and the cost also tends to be increased gradually.
There are many techniques currently on the market for optimizing and improving Fenton process, including but not limited to photo Fenton method, electro Fenton method, heterogeneous catalyst fixed bed method and heterogeneous catalyst fluidized bed method (for example, patent document CN105000654A, CN102701392A, CN103755092A, CN105461103A, CN202139138U, CN205650179U, CN 101088936A). A new iron mud recycling system is available, which adopts ferric iron existing in iron mud to dissolve out, and then uses a reducing agent to reduce the ferric iron into Fe needed by Fenton reagent 2+ . The reducing agent commonly used in this process is a heterogeneous catalytic reducing agent. The reaction principle is Fe 3+ +reductant → Fe 2+ . The reduction reaction in this process is produced in the form of a reaction tank and stirring. The method is a conventional liquid-solid reaction mode in the fields of chemical industry and environmental protection. However, the heterogeneous catalytic reducer has certain hardness and can cause certain abrasion and corrosion to the stirring paddles; meanwhile, the heterogeneous catalytic reducer has a density far higher than that of water, and reactants are difficult to stir and mix uniformly by adopting a stirring paddle; in addition, the stirring paddle mode needs to use a high-power stirring motor, and the reaction duration needs to be increased to enable the reaction to be complete under the condition of low reaction mixing rate, which increases the operation energy consumption. This problem is to be solved.
Disclosure of Invention
The technical problems to be solved by the invention are that the defects that the heterogeneous catalytic reducer has certain hardness and can generate certain abrasion and corrosion on a stirring paddle, the heterogeneous catalytic reducer has density far higher than that of water, reactants are difficult to stir and mix uniformly by adopting a stirring paddle mode, and the operation energy consumption is increased by using a stirring paddle mode by using a high-power stirring motor are overcome in the prior art, and the reduction fluidized bed and the application and the use method thereof are provided. According to the invention, the stirring tank is replaced by the circulating fluidized bed, the mixing effect is improved, the flow of the circulating pump is regulated, the most energy-saving and stable fluidization state of heterogeneous catalytic reducing agents with different particle sizes is realized, the operation energy consumption is reduced, the circulating pump is used for enabling liquid to generate turbulent motion, the mixing main body is solid reducing agent and solution, the condition of mechanical scouring is not generated, and the possibility of structural abrasion is reduced.
The invention provides a reduction fluidized bed, which comprises the following components sequentially connected from top to bottom: a clarification layer, a diversion layer and a fluidization layer;
the device comprises a clarifying layer, a liquid collecting area, a three-phase separator and a buffer area, wherein the clarifying layer comprises the liquid collecting area, the three-phase separator and the buffer area which are sequentially connected from top to bottom, a double-layer overflow weir is arranged on the inner wall of the liquid collecting area in a surrounding mode, a reducing agent feeder penetrating through the liquid collecting area, the three-phase separator and the buffer area is further arranged in the middle of the clarifying layer, the upper part of the reducing agent feeder is higher than the double-layer overflow weir, and the lower part of the reducing agent feeder is higher than the bottom of the buffer area;
the flow guide layer is provided with a flow guide plate for reducing the axial upward flow energy of liquid, and the outer wall size of the flow guide layer gradually reduces from the clarifying layer to the fluidization layer;
wherein, the bottom of the fluidization layer is vertically provided with at least one sprayer, and a plurality of solid distribution plates which can enable powder to fall down in a tilting way are arranged around the sprayer; the ejector is provided with a water suction port, one end of the solid distribution plate is connected with the ejector, the connection position is positioned at the lower end of the water suction port, and the other end of the solid distribution plate is connected with the wall surface of the fluidization layer or another adjacent ejector.
In the present invention, the double-layered overflow weir is a double-layered overflow weir conventionally used in the art, and preferably, the double-layered overflow weir may have a circular structure or a rectangular structure around the edge of the tower body.
In the invention, the reducing agent feeder is a reducing agent feeder conventionally used in the field, preferably, the reducing agent feeder comprises a weight detection module, and the weight detection module is fed back to the variable frequency motor according to weight change to control feeding frequency.
In the invention, the three-phase separator is a three-phase separator conventionally used in the field, preferably adopts a double-layer inverted triangle structure, and the person skilled in the art knows that the gas is collected through the top end of the triangle and can be periodically pumped out by detecting the volume of the gas through the gas volume detection module, and the gas is hydrogen generated by side reaction, so that the purity is higher, and the gas can be collected by using the gas storage tank; preferably, the top of the three-phase separator is provided with an outward exhaust pipe.
In the invention, the guide plate is a guide plate conventionally used in the field, the number of blades of the guide plate is set according to the number of diameters, the preferred number of blades is 3-8, preferably a spiral structure is adopted, and the inclination angle (the inclination angle is an included angle with the horizontal plane) of the blades of the guide plate can be 15-75 degrees, preferably 30-60 degrees; the guide plate can be positioned on the inner wall surface of the guide layer, and can also be suspended in the round table and fixed by a connecting rod; the arrangement of the guide plate can increase the rising flow state of the liquid cyclone, reduce the rising flow speed of the liquid, simultaneously increase the radial kinetic energy of the fluid, control the axial flow velocity of the liquid separated from the fluidized layer and reduce the gushing phenomenon.
In the invention, the ratio of the upper diameter to the lower diameter of the diversion layer is preferably 1.5-3:1; the diameter of the diversion layer is increased from bottom to top, so that the rising flow speed is reduced, the solid is changed from a critical flow state to a sinking state, and the flow state and the solid-liquid separation trend of the fluidized bed layer are maintained.
In the invention, preferably, the bottom of the fluidization layer is also provided with a water inlet distributor so as to realize the average distribution of the water inlet in each sprayer.
In the invention, the distance between the top of the jet pipe of the jet and the bottom of the diversion layer is more than or equal to 5cm, preferably 10cm-20cm; the height-diameter ratio of the jet pipe is more than or equal to 2, preferably 3-8:1.
In the present invention, the fluidized layer may be provided with 1 or more ejectors. When the number of the ejectors is multiple, the ejectors are uniformly distributed at equal intervals, and the solid distribution plates are uniformly distributed around the ejectors.
In the invention, the ejector adopts the venturi principle, and the liquid flowing through the pipeline rapidly in the axial direction generates a certain negative pressure effect on the water suction port to drive the solids near the water suction port to enter the ejector tube, so that the ejector is driven by water flow to float upwards, the fluidization state is achieved, and the liquid-solid reaction efficiency is improved.
In the invention, the inclination angle of the solid distribution plate is preferably 15-75 degrees, so that heterogeneous catalytic reducer is accumulated around the water suction port of the ejector along with the action of water flow, and meanwhile, due to the structure, the solid circulation frequency is improved, and the phenomenon of hardening of the heterogeneous catalytic reducer is reduced. The number of the solid distribution plates can be set according to the flow rate of the actual tower body and the diameter requirement of the tower body, but the number of the solid distribution plates is required to correspond to the number of the ejectors.
In the invention, the ratio of the height of the upper, middle and lower structures of the reduction fluidized bed can be adjusted according to actual needs, for example, the height ratio of the clarifying layer, the diversion layer and the fluidized layer can be (0.7-1.3): (0.7-1.3): (1.4-2.6), and is preferably 1:1:2.
In the invention, a circulating water pump and a circulating water tank are also arranged outside the reduction fluidized bed according to the conventional technology in the field.
The circulating water tank is connected with the double-layer overflow weir through a pipeline, and the circulating water tank is connected with the circulating water pump through a pipeline.
The circulating water tank is used for collecting liquid flowing out of the fluidized bed overflow weir, and then the liquid can be pumped into a corresponding pipeline by the metering pump.
The circulating water pump is preferably a chemical anti-corrosion pump, and an outlet pipeline of the circulating water pump is provided with a water outlet valve, so that the flow rate of the water entering the tower can be controlled; the inlet pipeline of the circulating water pump is connected with the circulating water tank, and the flow is controlled by a water inlet valve; the circulating water pump is connected with the tower inlet pipeline and the emptying pipe through a tee joint; the emptying pipe is provided with an emptying valve and is mainly used for periodical discharging and cleaning.
In the invention, the inlet water flow rate can be adjusted by adjusting the inlet water pipe valve, so that the turbulent fluidization state of the solid in the ejector is realized.
In the present invention, in general, the solid ratio in the reduction fluidized bed is 1% to 20%, and those skilled in the art know that the diameter and the height of the fluidized layer can be adjusted according to the solid-to-liquid ratio.
The invention also provides application of the reduction fluidized bed in Fenton iron mud recovery.
The invention also provides a Fenton iron mud recycling method matched with the reduction fluidized bed, which comprises the following steps:
reducing agent is added into a reducing agent feeder, fenton iron mud enters a fluidized layer and then is sprayed upwards by an ejector, the Fenton iron mud enters a clarification layer after passing through a guide plate, and liquid flowing out of a double-layer overflow weir after solid-liquid separation is recycled.
On the basis of conforming to the common knowledge in the field, the above preferred conditions can be arbitrarily combined to obtain the preferred examples of the invention.
The invention has the positive progress effects that:
the reduction fluidized bed has the advantages of improved mixing effect, stable control of feeding amount, optimized fluidized bed structure, reduced volume, adjustable external circulation amount according to the flow of incoming liquid, low operation energy consumption, turbulent flow motion of liquid generated by a circulating pump, no mechanical scouring of the mixed main body of solid reducer and solution, and reduced possibility of structural abrasion.
Drawings
FIG. 1 is a schematic view showing the configuration of 1 number of ejectors in a reduction fluidized bed according to example 1 of the present invention.
Fig. 2 is a schematic perspective view of a 3-leaf baffle in embodiment 1 of the present invention.
FIG. 3 is a cross-sectional view of the fluidized zone of the reduction fluidized bed of example 2 of the present invention when there are a plurality of ejectors.
FIG. 4 is a schematic view showing the structure of the fluidized zone in the reduction fluidized bed according to example 2 of the present invention when the number of ejectors is plural.
Fig. 5 is a schematic perspective view of a 6-leaf baffle in embodiment 2 of the present invention.
Fig. 6 is a top view of a 6-leaf baffle in example 2 of the present invention.
Fig. 7 is a top view of a 3-leaf baffle in example 3 of the present invention.
The reference numerals are as follows:
clarifying layer 1
Liquid collecting zone 11
Three-phase separator 12
Buffer zone 13
Double-layer overflow weir 14
Reducing agent feeder 15
Exhaust pipe 16
Diversion layer 2
Fluidized layer 3
Ejector 31
Solid distribution plate 32
Suction port 33
Solid collection zone 34
Inlet water distributor 35
Circulating water pump 4
Circulating water tank 5
Circulation pump flow valve 41
Drain valve 42
Detailed Description
The invention is further illustrated by means of the following examples, which are not intended to limit the scope of the invention.
Example 1
In this embodiment, as shown in FIG. 1, the reducing agent is a heterogeneous catalytic reducing agent (such as aluminum powder) with particle diameter of 0.15-10mm, and the main reaction in the fluidized bed is Fe 3+ +reductant → Fe 2+ The main side reaction is reducing agent +H + →H 2 . The ratio of heterogeneous catalytic reducing agent to liquid added to the fluidized bed per unit time was 5:95.
The fluidized bed comprises a fluidized bed body which is sequentially connected from top to bottom: the high ratio of the clarifying layer 1, the diversion layer 2 and the fluidization layer 3 is 1:1:2; the clarifying layer 1 comprises a liquid collecting area 11, a three-phase separator 12 and a buffer area 13 which are sequentially connected from top to bottom, a double-layer overflow weir 14 is arranged on the inner wall of the liquid collecting area in a surrounding manner, a reducing agent feeder 15 penetrating through the liquid collecting area 11, the three-phase separator 12 and the buffer area 13 is further arranged in the middle of the clarifying layer 2, the upper part of the reducing agent feeder 15 is higher than the double-layer overflow weir 12, and the lower part of the reducing agent feeder is higher than the bottom of the buffer area 13; the top of the three-phase separator 12 is provided with an outward exhaust pipe 16;
the flow guiding layer 2 is provided with a 3-leaf flow guiding plate (see fig. 2), the 3-leaf flow guiding plate is fixed at the middle part and used for reducing the axial upward flow energy of liquid, the outer wall size of the flow guiding layer 2 is gradually reduced along the clarifying layer 1 to the fluidization layer 3, and the ratio of the upper diameter to the lower diameter of the flow guiding layer is 1.5:1;
wherein, the bottom of the fluidized layer 3 is vertically provided with an ejector 31, and a plurality of solid distribution plates 32 which can enable powder to fall down in a tilting way are arranged around the ejector 31 to form a solid collecting area 34; the ejector 31 is provided with a water suction port 33, one end of the solid distribution plate 32 is connected with the ejector 31, the connection position is horizontal to the water suction port 33, no dead space can be formed for accumulation of solids, and the other end of the solid distribution plate 32 is connected with the wall surface of the fluidized layer 3.
The top overflow weir is of an annular structural design, and the first layer of water outlet weir can be regularly checked and cleaned, so that the water outlet of the second layer of water outlet weir is completely clarified, and the influence of the impurities in the later period on the normal operation of the pump is avoided. The reducer feeder 15 adopts timing quantitative continuous feeding, the feeder comprises a weight detection module, and a weight change signal is fed back to the variable frequency motor through a PLC. The variable frequency motor is connected with the material conveying rod, and the feeding frequency is controlled through the change of the rotating speed of the motor, so that stable and continuous feeding is realized; the three-phase separator 12 adopts a double-layer inverted triangle structure, gas is collected through the top end of the triangle and the volume of the gas is detected by the gas volume detection module, and the gas is periodically pumped out, so that the gas is hydrogen generated by side reaction, has higher purity and can be collected by using a gas storage tank. The heterogeneous catalytic reducer reduction method is used for realizing upward liquid, sinking solid and extracting gas through polymerization; the guide plate adopts a 3-leaf spiral structure, and the inclination angle of the guide plate is set to be 15 degrees so as to convert rising kinetic energy into radial kinetic energy; the injectors 31 are arranged in an equidistant manner in a plane, and the solids distribution plate 32 is designed so that the solids of the entire cross section can be collected uniformly around the individual injectors 31, with an inclination of 45 °. The distance from the top of the jet pipe of the jet 31 to the bottom of the guide layer 3 was 10cm; the ratio of the height to the diameter of the jet pipe is 3:1.
The outside of the reduction fluidized bed is also provided with a circulating water pump 4 and a circulating water tank 5. Wherein the circulating water tank 5 is connected with the double-layer overflow weir 14 through a pipeline, and the circulating water tank 5 is connected with the circulating water pump 4 through a pipeline. The circulating water tank 5 is used for collecting liquid flowing out of the overflow weir of the fluidized bed, and then the liquid can be pumped into a corresponding pipeline by a metering pump. The circulating water pump 4 adopts a chemical anti-corrosion pump, and a circulating pump flow valve 41 is arranged on an outlet pipeline of the circulating water pump 4 and can control the flow of the incoming tower; an inlet pipeline of the circulating water pump 4 is connected with a circulating water tank 5, and a water inlet valve is used for controlling the flow; the circulating water pump 4 is connected with a tower inlet pipeline and an emptying pipe through a tee joint, and the emptying pipe comprises an emptying valve 42 and is mainly used for periodical discharge cleaning.
The circulating water tank 5 stores liquid overflowed from the upper layer of the fluidized bed, the liquid is pumped into the Fenton process through a metering pump, and the rest of the solution enters the water inlet pipe of the fluidized bed through a circulating branch pipe and a circulating water pump 4. The inlet circulation pump flow valve 41 is adjusted to adjust the inlet water flow rate to achieve a turbulent fluidization of the solids in the ejector tube of the ejector 31. Because the cross-sectional area of the injection pipe is much smaller than that of the fluidized layer 3 at the lower layer of the fluidized bed, the circulating water pump 4 can enable the heterogeneous catalytic reducer in the injection pipe to be in an injection flow state only by small flux, and the operation energy consumption of the pump is much more energy-saving than that of the existing fluidized bed technology. The solid sprayed out of the spray pipe has larger upward flow kinetic energy, namely, the heterogeneous catalytic reducer can enter the diversion layer 2 to convert part of upward flow kinetic energy into radial kinetic energy, so that the heterogeneous catalytic reducer can generate downward kinetic energy through self gravity and hydraulic flow, return to the fluidized layer 3 and fall on the solid distribution plate 32. Thereafter, the liquid around the solid distribution plate 32 is sucked into the injection pipe due to the negative pressure of the water suction opening 33 of the injection pipe, and the heterogeneous catalytic reducing agent is entrained into the injection pipe to form the next injection cycle.
In this embodiment, the flow rate of the circulating water pump is related to the upflow rate, the density of the solid particles and the particle size. Since the solid has the phenomenon that the particle size is continuously reduced along with the progress of the reaction, the calculation of the rising flow speed of the circulating flow pump is carried out by taking the diameter of the fluidized layer 3 as the basis, and the calculation formula is as follows:
wherein, V critical current rising speed, Q pump flow, R fluidized bed radius. The V critical flow rate is obtained through a pilot experiment according to the relation between the actual solid density and the particle size.
Example 2
The ratio of the upper diameter to the lower diameter of the guide layer of the reduction fluidized bed in the embodiment is 3:1, the guide plate is 6 blades (see fig. 5 and 6), and the inclination angle of the guide plate is 75 degrees; the fluidized layer 3 is provided with 28 injectors 31 and the bottom of the fluidized layer 3 is further provided with a water inlet distributor 35 (see fig. 4) to achieve an even distribution of the water inlet in the individual injectors, the inclination of the solids distribution plate 32 being 15 deg.. The rest of the structure was the same as that of the reduction fluidized bed in example 1. FIG. 3 is a cross-sectional view showing the fluidized zone in the case of reducing the number of ejectors in the fluidized bed in example 2, and FIG. 4 is a schematic view showing the structure of the fluidized zone.
Example 3
The baffle plate of the reduction fluidized bed in this embodiment adopts the structure shown in fig. 7, and the other structures are the same as in embodiment 1.
Compared with the traditional reaction tank, the invention has the advantages of good mixing effect, low operation energy consumption and no abrasion to equipment structure. Meanwhile, the spray pipe structure is preferably designed, so that the liquid-solid mixing effect is improved, and the conditions of solid accumulation and dead ends are reduced.
The present invention is not limited to the above-described embodiments, and any changes in shape or structure thereof are within the scope of the present invention. The scope of the present invention is defined by the appended claims, and those skilled in the art can make various changes or modifications to these embodiments without departing from the principle and spirit of the present invention, but these changes and modifications fall within the scope of the present invention.
Claims (12)
1. A reduction fluidized bed, characterized in that it comprises, from top to bottom, successively connected: a clarification layer, a diversion layer and a fluidization layer;
the device comprises a clarifying layer, a liquid collecting area, a three-phase separator and a buffer area, wherein the clarifying layer comprises the liquid collecting area, the three-phase separator and the buffer area which are sequentially connected from top to bottom, a double-layer overflow weir is arranged on the inner wall of the liquid collecting area in a surrounding mode, a reducing agent feeder penetrating through the liquid collecting area, the three-phase separator and the buffer area is further arranged in the middle of the clarifying layer, the upper part of the reducing agent feeder is higher than the double-layer overflow weir, and the lower part of the reducing agent feeder is higher than the bottom of the buffer area;
the flow guide layer is provided with a flow guide plate for reducing the axial upward flow energy of liquid, and the outer wall size of the flow guide layer gradually reduces from the clarifying layer to the fluidization layer;
wherein, the bottom of the fluidization layer is vertically provided with at least one sprayer, and a plurality of solid distribution plates which can enable powder to fall down in a tilting way are arranged around the sprayer; the ejector is provided with a water suction port, one end of the solid distribution plate is connected with the ejector, the connection position is positioned at the lower end of the water suction port, and the other end of the solid distribution plate is connected with the wall surface of the fluidization layer or another adjacent ejector.
2. The reducing fluidized bed of claim 1, wherein the double-layer overflow weir is in a ring-shaped or rectangular structure around the edge of the tower;
the reducing agent feeder comprises a weight detection module;
the three-phase separator adopts a double-layer inverted triangle structure;
the top of the three-phase separator is provided with an outward exhaust pipe.
3. The reducing fluidized bed of claim 1, wherein the number of vanes of the baffle is 3-8;
the blades of the guide plate adopt a spiral structure;
the inclination angle of the blades of the guide plate is 15-75 degrees;
the guide plate is positioned on the inner wall surface of the guide layer or is fixed in the guide layer by a hanging connecting rod;
the ratio of the upper diameter to the lower diameter of the diversion layer is 1.5-3:1.
4. A reducing fluidised bed as claimed in claim 3, wherein the vanes of the deflector are inclined at an angle of 30 ° to 60 °.
5. The reducing fluidized bed of claim 1, wherein a bottom of the fluidized layer is provided with a water inlet distributor;
the distance between the top of the jet pipe of the jet and the bottom of the diversion layer is more than or equal to 5cm;
the height-diameter ratio of the jet pipe is more than or equal to 2;
the number of the ejectors is at least one;
the inclination angle of the solid distribution plate is 15-75 degrees;
the number of the solid distribution plates corresponds to the number of the ejectors.
6. The reducing fluidized bed of claim 5, wherein the top of the ejector tube of the ejector is a distance of 10cm to 20cm from the bottom of the deflector layer;
the height-diameter ratio of the jet pipe is 3-8:1.
7. The reducing fluidized bed of claim 1, wherein the ratio of the heights of the clarification layer, the channeling layer, and the fluidization layer is (0.7-1.3): 1.4-2.6.
8. The reducing fluidized bed of claim 1, wherein the elevation ratio of the clarifier layer, the flow directing layer, and the fluidized layer is 1:1:2.
9. The reducing fluidized bed according to claim 1, wherein a circulating water pump and a circulating water tank are provided outside the reducing fluidized bed.
10. The reducing fluidized bed of claim 9, wherein the circulating water tank is connected to the double-layer overflow weir by a pipe, and the circulating water tank is connected to the circulating water pump by a pipe.
11. Use of a reduction fluidised bed as claimed in any one of claims 1 to 10 in the recovery of Fenton iron sludge.
12. A method of using the reduction fluidised bed as claimed in any one of claims 1 to 10 in the recovery of Fenton iron sludge comprising the steps of:
reducing agent is added into a reducing agent feeder, fenton iron mud enters a fluidized layer and then is sprayed upwards by an ejector, the Fenton iron mud enters a clarification layer after passing through a guide plate, and liquid flowing out of a double-layer overflow weir after solid-liquid separation is recycled.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711394357.2A CN109942065B (en) | 2017-12-21 | 2017-12-21 | Reduction fluidized bed and application and use method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711394357.2A CN109942065B (en) | 2017-12-21 | 2017-12-21 | Reduction fluidized bed and application and use method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109942065A CN109942065A (en) | 2019-06-28 |
| CN109942065B true CN109942065B (en) | 2024-04-12 |
Family
ID=67005411
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711394357.2A Active CN109942065B (en) | 2017-12-21 | 2017-12-21 | Reduction fluidized bed and application and use method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109942065B (en) |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2154859Y (en) * | 1993-03-17 | 1994-02-02 | 王振声 | Multifunction aerobic organism fluidied bed |
| KR19980072360A (en) * | 1997-03-04 | 1998-11-05 | 한상배 | Stirring and chemical injection method and device for water treatment |
| CN1932236A (en) * | 2006-09-28 | 2007-03-21 | 侯华业 | Method and apparatus for directly dispersing polymer dry powder by hydraulic jet |
| CN101631881A (en) * | 2007-03-16 | 2010-01-20 | 奥图泰有限公司 | Method to enhance clarification in a mixing reactor and said mixing reactor |
| CN202297249U (en) * | 2011-10-12 | 2012-07-04 | 林长青 | Inner-circulated anaerobic fluidize bed reactor |
| CN104261622A (en) * | 2014-09-29 | 2015-01-07 | 中国电建集团中南勘测设计研究院有限公司 | Fenton sewage treatment process and equipment thereof |
| CN104445605A (en) * | 2014-11-24 | 2015-03-25 | 南京大学 | Mechanical internal circulation jet-flow anaerobic reactor and wastewater treatment method thereof |
| CN104973631A (en) * | 2015-07-23 | 2015-10-14 | 浙江奇彩环境科技有限公司 | Technique for preparing ferrous sulfate by reducing iron mud with SO2 |
| CN105237409A (en) * | 2014-06-05 | 2016-01-13 | 中国石油化工股份有限公司 | Method used for reductive amination using jet reactor |
| CN106892497A (en) * | 2017-04-14 | 2017-06-27 | 上海电气集团股份有限公司 | Fenton iron mud regeneration device, Fenton methods sewage disposal system and its method |
| CN207918512U (en) * | 2017-12-21 | 2018-09-28 | 上海电气集团股份有限公司 | A kind of reduction fluid bed |
-
2017
- 2017-12-21 CN CN201711394357.2A patent/CN109942065B/en active Active
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2154859Y (en) * | 1993-03-17 | 1994-02-02 | 王振声 | Multifunction aerobic organism fluidied bed |
| KR19980072360A (en) * | 1997-03-04 | 1998-11-05 | 한상배 | Stirring and chemical injection method and device for water treatment |
| CN1932236A (en) * | 2006-09-28 | 2007-03-21 | 侯华业 | Method and apparatus for directly dispersing polymer dry powder by hydraulic jet |
| CN101631881A (en) * | 2007-03-16 | 2010-01-20 | 奥图泰有限公司 | Method to enhance clarification in a mixing reactor and said mixing reactor |
| CN202297249U (en) * | 2011-10-12 | 2012-07-04 | 林长青 | Inner-circulated anaerobic fluidize bed reactor |
| CN105237409A (en) * | 2014-06-05 | 2016-01-13 | 中国石油化工股份有限公司 | Method used for reductive amination using jet reactor |
| CN104261622A (en) * | 2014-09-29 | 2015-01-07 | 中国电建集团中南勘测设计研究院有限公司 | Fenton sewage treatment process and equipment thereof |
| CN104445605A (en) * | 2014-11-24 | 2015-03-25 | 南京大学 | Mechanical internal circulation jet-flow anaerobic reactor and wastewater treatment method thereof |
| CN104973631A (en) * | 2015-07-23 | 2015-10-14 | 浙江奇彩环境科技有限公司 | Technique for preparing ferrous sulfate by reducing iron mud with SO2 |
| CN106892497A (en) * | 2017-04-14 | 2017-06-27 | 上海电气集团股份有限公司 | Fenton iron mud regeneration device, Fenton methods sewage disposal system and its method |
| CN207918512U (en) * | 2017-12-21 | 2018-09-28 | 上海电气集团股份有限公司 | A kind of reduction fluid bed |
Non-Patent Citations (1)
| Title |
|---|
| 印染废水芬顿污泥原位资源化利用;黄思远;《净水技术》;第42卷(第S1期);第167-172页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109942065A (en) | 2019-06-28 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101193826B (en) | Anaerobic purification device | |
| US10814337B2 (en) | Composite ozone flotation integrated device | |
| CN103097307B (en) | Comprise the cleaner of solid separating device and the method for purification of waste water | |
| CN201777915U (en) | Chemical degreasing sediment separator | |
| JP7387656B2 (en) | Anaerobic treatment equipment and anaerobic treatment method | |
| CN103332784A (en) | Three-stage circulation aerobic reactor | |
| CN101475236B (en) | Pneumatic water pump pipe assembly and use thereof in water treatment technology | |
| CN109824186A (en) | Minerals sand, which is promoted, by negative pressure recycles high speed pellets pool process | |
| CN108689475B (en) | Fenton oxidation baffled reactor and organic wastewater treatment method | |
| CN206454320U (en) | The efficient clarifying reaction device of fine suspension in a kind of processing sewage | |
| CN212050745U (en) | Integrated sewage reactor | |
| CN102874910B (en) | Coagulation-precipitation integrated treatment method and device | |
| CN109942065B (en) | Reduction fluidized bed and application and use method thereof | |
| CN112573653A (en) | Internal circulation anaerobic reaction system with denitrification function | |
| CN105152324B (en) | Anaerobic ammonia oxidation reactor capable of classifying sludge through cyclone | |
| JP5666187B2 (en) | Waste water treatment apparatus and waste water treatment method | |
| CN101602553A (en) | A kind of method and stirring-granulating tank thereof of handling trade effluent | |
| CN201713366U (en) | Flow guide type tapered sedimentation tank | |
| CN203513389U (en) | Chemical oil removal inclined pipe precipitator | |
| CN207918512U (en) | A kind of reduction fluid bed | |
| CN202519078U (en) | Novel and effective integration reaction precipitation device | |
| CN202007150U (en) | Integrated energy-saving high-efficiency coagulating sedimentation water treatment facility | |
| CN103103215B (en) | Gradient circulation stirring method in marsh gas reactor and anaerobic reactor thereof | |
| CN212425543U (en) | Sludge gravity concentration tank | |
| CN110876861B (en) | Horizontal mud-water separator |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20190628 Assignee: Bluelight ecological environment technology (Fujian) Co.,Ltd. Assignor: Shanghai Electric Group Co.,Ltd. Contract record no.: X2019310000020 Denomination of invention: Reduction fluidized bed, as well as application and using method thereof License type: Common License Record date: 20191113 |
|
| EE01 | Entry into force of recordation of patent licensing contract | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |