CN114455683B

CN114455683B - Carrier for loading precipitation, carrier preparation method and loading flocculation precipitation method

Info

Publication number: CN114455683B
Application number: CN202210135981.5A
Authority: CN
Inventors: 韩彦涛; 陈力辉
Original assignee: Zhenhe Huilian Zhejiang Environmental Technology Co ltd
Current assignee: Zhenhe Huilian Zhejiang Environmental Technology Co ltd
Priority date: 2022-02-15
Filing date: 2022-02-15
Publication date: 2022-12-13
Anticipated expiration: 2042-02-15
Also published as: CN114455683A

Abstract

The invention provides a carrier for loading precipitation, a carrier preparation method and a flocculation precipitation loading method, wherein the carrier comprises the following components: a kernel; the adsorption layer is coated on the periphery of the inner core and is a porous adsorption material; the kernel includes: a plurality of prefabricated particles which are particles composed of the exhaust gas recovery powder; the auxiliary agent is filled in gaps among the plurality of prefabricated particles and bonds the plurality of prefabricated particles together to form the inner core.

Description

Sediment-loaded carrier, carrier preparation method and flocculation sediment loading method

Technical Field

The invention relates to the field of sewage treatment, in particular to a carrier for loading precipitation, a carrier preparation method and a loading flocculation precipitation method.

Background

The loading flocculation precipitation is a method for adding carriers of high-density or magnetic insoluble particles such as fine sand, mineral particles, magnetic seeds and the like into sewage and accelerating the formation and precipitation of flocs by utilizing the adsorption capacity of the carriers and the gravity settling capacity or magnetic action of the carriers, so that the method can reduce the visual indexes such as turbidity, chromaticity and the like of raw water and remove various toxic and harmful substances in the water, and at present, the loading flocculation precipitation technology is widely applied to the water treatment industry.

When the carrier for loading the precipitate is selected, on one hand, the carrier is required to have higher density, so that better gravity settling capacity can be exerted, the particle size of the carrier is reduced, and the using amount of the carrier is reduced; on the other hand, the carrier is required to have good adsorption capacity so as to adsorb flocs more stably; in addition, the carrier is also required to have the characteristics of low price, easy preparation, reusability and the like so as to reduce the cost of sewage treatment and improve the convenience and efficiency of sewage treatment.

The current commonly used carriers comprise fine sand, mineral particles and the like, and the density and the adsorption capacity of the carriers are limited by the characteristics of the materials, so that the treatment effect and the treatment efficiency of the loading flocculation precipitation process on sewage are difficult to continuously improve; moreover, the current common loading flocculation precipitation process needs to be provided with a plurality of sedimentation tanks which are connected in series in sequence, such as a mixing tank, a flocculation tank, a floc curing tank, a floc sedimentation tank and the like, so that the engineering cost and the floor area of the loading flocculation precipitation process are extremely high, the application of the loading flocculation precipitation process in population gathering areas such as urban areas or narrow space areas is limited, and the application range of the loading flocculation precipitation process is difficult to widen and is not stopped for a long time; in addition, the stirring body in the sedimentation tank easily generates strong impact on the carrier and the floc in the stirring process, so that the floc is decomposed and the carrier is disintegrated, and the water treatment effect and the recycling frequency of the carrier are reduced.

Disclosure of Invention

The invention designs a loading and precipitating carrier, a carrier preparation method and a loading flocculation and precipitation method, and provides the loading and precipitating carrier which has the advantages of good flocculation and precipitation effect, low price, easy preparation, reusability, simple and efficient sewage treatment process, and low engineering cost and occupied area.

In order to solve the above problems, the present invention discloses a carrier for loading a precipitate, comprising:

a kernel;

the adsorption layer is coated on the periphery of the inner core and is a porous adsorption material;

the kernel includes:

a plurality of prefabricated particles which are particles composed of the exhaust gas recovery powder;

an auxiliary agent filling gaps between the plurality of preformed particles to bond the plurality of preformed particles together to form the inner core.

Furthermore, the average particle size of the inner core is 50-100 um, the average particle size of the prefabricated particles is 5-20 um, and the thickness of the adsorption layer is 3-10 um.

Further, the prefabricated particles are particles formed by waste gas recovery powder of a steel smelting plant.

A method for preparing a carrier, which is used for preparing the carrier, the method comprising the steps of:

s1, pressing prefabricated particles by adopting waste gas recovery powder;

s2, bonding a plurality of prefabricated particles together by adopting an auxiliary agent to form an inner core;

and S3, coating an adsorption layer on the outer surface of the inner core.

Further, the step S1 includes:

s11, waste gas recovery powder pretreatment: taking powder recovered from waste gas as a raw material, drying the powder to constant weight, and grinding the powder until the average particle size is less than or equal to 1um for later use;

s12, pressing the compact: placing the ground waste gas recovery powder in a die, and pressing into a compact with the relative density of more than or equal to 80%;

s13, crushing and granulating: putting the pressed briquette into a grinder to be ground into particles;

s14, high-temperature sintering: and placing the crushed particles into a sintering furnace, and sintering at 500-600 ℃ for 1-2 h to obtain the prefabricated particles.

Further, the step S2 includes: weighing a certain amount of auxiliary agent, uniformly mixing the auxiliary agent and the prefabricated particles, placing the mixture in a granulator for granulation, and drying to obtain an inner core; wherein the addition amount of the auxiliary agent is 10-30% of the mass of the prefabricated particles.

Further, the auxiliary agent is prepared according to the following processes: firstly weighing 50-80 parts by weight of saturated soft clay, placing the saturated soft clay in a closed container, heating to 65-85 ℃ under stirring, adding 5-10 parts by weight of PVA, stirring for 1-3 min to uniformly disperse and dissolve the PVA in the saturated soft clay, opening a container cover to volatilize water in the saturated soft clay, then adding medium-high temperature asphalt powder under continuous stirring at 60-70 ℃, heating and stirring until the water content of a mixed system reaches 25-30%, uniformly dispersing and dissolving 1-3 parts by weight of silane coupling agent in the mixed system to obtain the assistant.

Further, the step S3 includes: weighing a certain amount of raw materials of the adsorption layer, dissolving the raw materials of the adsorption layer in water to prepare slurry, spraying the slurry of the adsorption layer on the outer surface of the core in a spraying mode, stirring and mixing simultaneously, sintering and drying at 200-500 ℃ for 10-30 min after uniformly mixing to obtain the carrier loaded with the precipitate.

A loaded flocculation and precipitation method for sewage treatment by adopting the carrier is carried out by utilizing a loaded flocculation and precipitation device, and the loaded flocculation and precipitation device comprises the following steps:

a coagulant adding device, a carrier adding device, a coagulation reaction device, a coagulation assisting reaction barrel, a floc growth barrel, a sedimentation barrel and a sewage inlet;

the coagulation reaction device comprises an outer sleeve and an inner sleeve, and the outer sleeve is sleeved on the periphery of the inner sleeve;

the flocculation-assisting reaction barrel, the floc growth barrel and the sedimentation barrel are all cylindrical barrel-shaped structures, the flocculation-assisting reaction barrel, the floc growth barrel and the sedimentation barrel are coaxially arranged, the floc growth barrel is fixedly sleeved in the sedimentation barrel, the flocculation-assisting reaction barrel is rotatably sleeved in the floc growth barrel, and the internal spaces of the flocculation-assisting reaction barrel, the floc growth barrel and the sedimentation barrel are sequentially communicated;

the sewage import respectively with the device is put in to the coagulant and the carrier is put in the device and is connected, the reaction unit that thoughtlessly congeals respectively with the device is put in to the coagulant, the carrier is put in the device and is connected with the reaction vat that helps congealing, sewage import exhaust sewage can with coagulant and carrier in the carrier is put in the device are put in the coagulant and carrier in the device are put in carry into in the reaction unit that thoughtlessly congeals in the reaction unit behind the mixing in the reaction unit, flow through in proper order help congealing reaction vat, floc growth bucket and sedimentation bucket.

Further, the loading flocculation precipitation method comprises the following steps:

p1, opening a sewage inlet, and respectively discharging sewage into the coagulant feeding device and the carrier feeding device, wherein the coagulant feeding device and the carrier feeding device generate negative pressure through a Venturi tube, a first one-way valve in the coagulant feeding device is automatically opened under the action of the negative pressure, a coagulant enters an inner sleeve in the coagulation reaction device along with the sewage, a second one-way valve in the carrier feeding device is automatically opened, and a carrier is discharged into the outer sleeve in the coagulation reaction device along with the sewage;

p2, the sewage and the carrier in the outer sleeve enter the inner sleeve, are mixed with the sewage and the coagulant in the inner sleeve for coagulation reaction, and are discharged into a coagulation assisting reaction barrel;

p3, controlling the coagulation reaction barrel to rotate at the speed of 100-600 revolutions per minute, putting a coagulant aid into the coagulation reaction barrel, carrying out flocculation reaction on sewage in rotary mixing, and enabling generated flocs to enter the floc growth barrel under the action of centrifugal force;

p4, after entering the floc growth barrel, the flocs are continuously rotated and mixed under the drive of the rotation of the coagulation-aiding reaction barrel, so that the flocs continue to grow and do centrifugal motion at the same time, and then enter the settling barrel under the action of centrifugal force;

and P7, realizing solid-liquid separation in the settling barrel through gravity settling and then discharging.

The carrier for loading precipitation, the carrier preparation method and the loading flocculation precipitation method have the advantages of being economical, efficient and convenient to use.

Drawings

FIG. 1 is a schematic diagram of the structure of a precipitate-loaded support according to the present invention;

FIG. 2 is a flow chart of a method for preparing a loaded precipitate support according to the present invention;

FIG. 3 is a schematic structural diagram of a loaded flocculation and sedimentation device according to the present invention;

fig. 4 is a partially enlarged view of the region M in fig. 3.

Description of the reference numerals:

a. an adsorption layer; b. a kernel; b1, preparing particles; b2, an auxiliary agent; 1. a coagulant adding device; 101. A coagulant storage tank; 102. a first negative pressure port; 103. a first venturi tube; 2. a carrier delivery device; 201. a carrier reservoir; 202. a second negative pressure port; 203. a second venturi tube; 3. a coagulation reaction device; 301. an outer sleeve; 302. an inner sleeve; 303. a first end; 304. a second end; 305. a first water passing opening; 306. a first water inlet; 307. a second water inlet; 308. a first water outlet; 4. a coagulation-assisting reaction barrel; 401. a rotating wall; 402. a second water passing opening; 403. a coagulant aid feeding port; 404. a third water inlet; 5. a floc growth barrel; 501. a fixed wall; 502. a third water passing hole; 503. an adjusting ring; 6. a settling barrel; 601. an outer wall; 602. a clean water discharge port; 603. a sediment discharge port; 7. and (6) a sewage inlet.

Detailed Description

In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in detail below.

As shown in fig. 1, a support loaded with a precipitate, the support comprising:

a kernel b;

the adsorption layer a is coated on the periphery of the inner core b and is a porous adsorption material;

the kernel b comprises:

a plurality of prefabricated particles b1, which are particulate matters composed of the exhaust gas recovery powder;

and an auxiliary agent b2 which fills gaps between the plurality of preformed particles b1 and bonds the plurality of preformed particles b1 together to form the inner core b.

Preferably, the prefabricated particles b1 are particles composed of waste gas recovery powder of a steel smelting plant.

The utility model provides an inside kernel b of carrier adopts waste gas recovery powder preparation to form, can make the bulk density of carrier is higher, and the setting of the outside adsorbed layer a of carrier then can form porous structure on the surface of carrier, makes the carrier possesses good adsorption efficiency. In addition, the carrier takes waste gas recovery powder as a main raw material, the cost of the carrier can be reduced through waste recovery, meanwhile, the raw material is prevented from being ground for a long time in the preparation process, the preparation process is simplified, the cost is reduced, and the preparation efficiency is improved.

Preferably, the average particle size of the inner core b is 50-100 um, and more preferably, the average particle size of the inner core b is 80-90 um, so that the prepared carrier has good adsorption capacity and sedimentation velocity. If the average particle size of the inner core b is too large, the prepared carrier has a small specific surface area and poor adsorption capacity; if the average particle size of the inner core b is too small, the sedimentation speed of the prepared carrier is obviously reduced.

Preferably, the average particle diameter of the preformed particle b1 is 5 to 20um, and more preferably, the average particle diameter of the preformed particle b1 is 6 to 13um. Thus, the density of the prepared inner core b is high, and the auxiliary agent b2 can stably bond a plurality of prefabricated particles b1 together to form the inner core b; if the average particle size of the prefabricated particles b1 is too large, the prepared inner core b is unstable in bonding and is easy to disintegrate in the using process; if the average particle diameter of the preformed particle b1 is too small, the density of the prepared core b is significantly reduced, which adversely affects the settling rate.

Preferably, the thickness of the adsorption layer a1 is about 3 to 10um, so that the outer surface of the inner core b can be uniformly covered by the adsorption layer a1, and the carrier can stably adsorb flocs in water.

In addition, as shown in fig. 2, the present application also provides a preparation method of a precipitate-loaded support, the preparation method being used for preparing the precipitate-loaded support, the preparation method comprising the steps of:

s1, pressing the prefabricated particles b1 by using waste gas recovery powder;

s2, bonding a plurality of prefabricated particles b1 together by adopting an auxiliary agent b2 to form an inner core b;

and S3, coating the adsorption layer a on the outer surface of the inner core b.

Specifically, the step S1 includes:

s13, crushing and granulating: putting the pressed blank blocks into a grinder to be ground into particles;

s14, high-temperature sintering: and placing the crushed particles obtained by crushing into a sintering furnace, and sintering for 1-2 h at 500-600 ℃ to obtain the prefabricated particles b1.

Preferably, in step S11, the preformed particle b1 is prepared by using waste gas recovery powder containing metal elements in waste gas of a steel smelting plant or the like as a raw material.

More preferably, in step S11, the preformed particle b1 is prepared by using waste gas recovery powder containing more than 30% by weight of metal elements in waste gas from steel smelting plants and the like as a raw material.

As some examples of this application, the powder that retrieves in the iron and steel smelting plant waste gas is the recovery powder that obtains through modes such as sack dust removal, filtration dust removal, adsorption dust removal.

Further, in the step S11, if the average particle size of the powder recovered from the exhaust gas is not greater than 1um, the powder may be dried and used without grinding.

In the prior art, some technologies using mill tailings, natural ores, modified composite materials and the like as carriers for loading precipitates have appeared, and certain effects are achieved, such as quartz (with the density of about 2.65 g/cm) in raw materials when the mill tailings or the natural ores are selected to prepare the carriers ³ ) Mica (density about 2.7-3.5 g/cm) ³ ) Medium density material with a density ratio of fine sand (density about 1.6 g/cm) ³ ) The ore is slightly heavy and can improve the settling velocity of the carrier, but the ore usually contains a lot of oxidized ores, the oxidized ores contain a lot of amorphous ores, the amorphous ores are easy to decompose and diffuse into water in the sewage treatment process, secondary pollution to water resources is caused, the specific gravity of the carrier is reduced, the precipitation is influenced, and in addition, the carrier prepared by tailings and natural ores has the problem of poor adsorption capacity; for example, when the modified composite material is used as a carrier for loading the precipitate, on one hand, the preparation process of the carrier is complex and the cost is high; on the other hand, the modifier on the surface of the composite material is easy to fall off in the stirring or centrifuging process, so that the composite material cannot be recycled and is difficult to regenerate.

The powder recovered from the waste gas is used as the raw material, so that the method has the following advantages:

firstly, the direct utilization of waste is realized, and the treatment of separation, purification and the like of powder recovered from waste gas is avoided;

secondly, the powder recovered from the waste gas has fine granularity and can be directly used or used through simple grinding, thereby avoiding the mining and long-time and high-energy consumption grinding of tailings or natural ores;

thirdly, the powder recovered from the waste gas has better oxidation resistance, and the subsequent sintering process can be directly carried out in high-temperature air, so that inert gas or vacuum protection is avoided, the process is simplified, and the cost is reduced;

fourthly, the powder recovered from the waste gas has higher density, and when the powder is used for loading a precipitated carrier, the settling speed of the floc can be effectively improved;

fifth, a dense sintered body can be formed by sintering while improving the bonding strength and density of the prefabricated particles.

Preferably, in the step S12, the ground exhaust gas-recovering powder may be placed in a mold and pressed into a compact having a relative density of 80% to 90%. The energy consumption in the pressing and sintering process can be reduced by controlling the relative density of the compact, if the relative density is too high, the energy consumption in the pressing and sintering process is too high, and the time consumption in the sintering process is greatly increased; if the relative density is too low, the strength of the sintered preformed particles b1 is insufficient, and the use requirement cannot be met.

Further, in step S13, the pressed briquettes are crushed into particles in a crusher, and then screened through a 500-mesh sieve, the undersize is collected and sintered at a high temperature, and the oversize is continuously crushed. By pressing, the density of the compact can be increased. The gas content in the particles is reduced, and a basis is provided for obtaining the prefabricated particles b1 with high density and high strength after subsequent sintering.

Further, in the step S14, the crushed particles obtained by crushing are placed in a sintering furnace, sintered at 500 to 600 ℃, such as 500 ℃, 520 ℃, 550 ℃ or 600 ℃, and heat preserved for 1 to 2 hours, so as to obtain the prefabricated particles b1.

The prefabricated particles b1 are prepared by directly pressing and molding waste gas recovery powder and then sintering, on one hand, no organic or inorganic binder is added in the preparation process, and the amount of air holes in the prefabricated particles b1 generated by volatilization of the organic or inorganic binder can be effectively reduced; meanwhile, solid particles in the prefabricated particles b1 can be bonded with each other through sintering, crystal grains grow up, the volume is shrunk, the density is increased, air holes are reduced, the density and the strength of the carrier are finally improved, and the settling speed and the stability are improved.

Further, the step S2 includes: weighing a certain amount of the auxiliary agent b2, uniformly mixing the auxiliary agent b2 and the prefabricated particles b1, placing the mixture in a granulator for granulation, and drying to obtain the inner core b.

As some embodiments of the present application, the step S2 includes: weighing a certain amount of the auxiliary agent b2, uniformly mixing the auxiliary agent b2 and the prefabricated particles b1, placing the mixture in a granulator for granulation, and drying at the temperature of 90-150 ℃ for 10-30 min to obtain the inner core b.

Furthermore, the addition amount of the auxiliary agent b2 is 10-30% of the mass of the prefabricated particles b1; preferably, the addition amount of the auxiliary b2 is 13 to 20 percent of the mass of the prefabricated particles b1.

Preferably, the auxiliary agent b2 comprises the following components in parts by weight:

preferably, the asphalt powder is medium-high temperature asphalt powder.

Further, the auxiliary agent b2 is prepared according to the following process: firstly weighing 50-80 parts by weight of saturated soft clay, placing the saturated soft clay in a closed container, heating to 65-85 ℃ under stirring, adding 5-10 parts by weight of PVA, stirring for 1-3 min to uniformly disperse and dissolve the PVA in the saturated soft clay, opening a container cover to volatilize water in the saturated soft clay, then adding medium-high temperature asphalt powder under continuous stirring at 60-70 ℃, heating and stirring until the water content of a mixed system reaches 25-30%, uniformly dispersing and dissolving 1-3 parts of silane coupling agent in the mixed system to obtain the assistant b2.

Preferably, the medium-high temperature asphalt powder is added in batches.

As some embodiments of the present application, the medium-high temperature asphalt powder may be equally divided into 3 to 5 parts, and added in batches, the time interval of adding the medium-high temperature asphalt powder each time is 5 to 15min, and the time interval of adding the medium-high temperature asphalt powder each time may be appropriately adjusted according to the water content of the mixed system, so that the water content in the finally prepared auxiliary agent b2 is 20 to 30%.

In the preparation process of the auxiliary agent b2, firstly, a support structure of the auxiliary agent b2 is constructed by utilizing an overhead structure and a honeycomb gap of the saturated soft clay, then PVA is added to increase the bonding capacity of the saturated soft clay, in the adding process of the PVA, the dissolving speed of the PVA is improved by adopting a closed stirring mode, the contact amount with air in the dissolving process of the PVA is reduced, the bubble amount generated in the dissolving process of the PVA is reduced, meanwhile, a small amount of bubbles generated in the dissolving process of the PVA are uniform and fine in size, the phenomenon that excessive and uneven bubbles generated in the dissolving process of the PVA generate adverse effects on the structure of the saturated soft clay is avoided, after the PVA is fully dissolved, a container cover is opened, so that the moisture in the saturated soft clay can be volatilized, and the moisture is evaporated.

In addition, the mode of adding the medium-high temperature asphalt powder in batches can uniformly disperse the medium-high temperature asphalt powder in the air holes in the saturated soft clay, so that the agglomeration or uneven distribution of the medium-high temperature asphalt powder in the saturated soft clay is avoided.

Moreover, the addition of the silane coupling agent can further improve the bonding capability of the auxiliary agent b2, and meanwhile, the auxiliary agent b2 has certain water-increasing property, so that the carrier is prevented from being disintegrated due to the entry of water in the use process.

In addition, the use of the saturated soft clay can also adhere to the surface of the preformed particle b1 after the carrier is disintegrated due to the fact that the recycling times exceed the design times, so that an adsorption structure on the surface of the preformed particle b1 is formed, and the preformed particle b1 has certain capacity of loading flocculation and precipitation.

The auxiliary agent b2 takes saturated soft clay as a main body, and a small amount of organic components are added, so that the cost of the carrier can be effectively reduced.

Further, the step S3 includes: weighing a certain amount of raw materials of the adsorption layer a, dissolving the raw materials of the adsorption layer a in water to prepare slurry, and then coating the slurry on the outer surface of the inner core b to obtain the carrier loaded with the precipitate.

As some embodiments of the application, the slurry of the adsorption layer a is sprayed on the outer surface of the inner core b in a spraying mode, and is stirred and mixed at the same time, and after uniform mixing, the carrier loaded with the precipitate is obtained by sintering and drying at 200-500 ℃ for 10-30 min.

Further, the raw materials of the adsorption layer a comprise the following components in parts by weight:

50-80 parts of a base material;

3-5 parts of pore-forming agent;

1-2 parts of a plant adhesive.

Preferably, the matrix material is one or more of diatomite, montmorillonite and bentonite.

More preferably, the matrix material is diatomite.

Preferably, the pore-forming agent is one or more of ammonium bicarbonate, urea and the like.

Preferably, the plant adhesive is one or more of dextrin, starch, cellulose and the like.

More preferably, the plant adhesive is B-cyclodextrin, and the B-cyclodextrin can be adhered to the surfaces of the air holes in the base material in a graft connection manner, so that the specific surface area of the adsorption layer a is further increased, and the adsorption effect of the adsorption layer a is improved; meanwhile, the B-cyclodextrin also has a certain high molecular effect and good environmental compatibility, and can adsorb organic pollutants in water.

The slurry of the adsorption layer a is prepared according to the following method: respectively weighing 50-80 parts by weight of a base material, 3-5 parts by weight of a pore-forming agent and 1-2 parts by weight of a plant adhesive according to the weight ratio, uniformly mixing, adding 30-40 parts by weight of water, uniformly stirring to obtain slurry of the adsorption layer a, spraying the slurry of the adsorption layer a on the outer surface of the inner core b in a spraying manner, simultaneously stirring and mixing, uniformly mixing, sintering at 200-500 ℃, and drying for 10-30 min to obtain the loaded and precipitated carrier.

Preferably, in the step S3, the weight ratio of the slurry of the adsorption layer a to the core b is 0.1 to 0.3:1.

in addition, the present application also provides a loaded flocculation and sedimentation method, according to which the above-mentioned loaded flocculation and sedimentation carrier is subjected to sewage treatment, the loaded flocculation and sedimentation method adopts a loaded flocculation and sedimentation device as shown in fig. 3 to 4 to perform sewage treatment, the loaded flocculation and sedimentation device comprises:

a coagulant adding device 1 for adding a coagulant into the coagulation reaction device 3;

a carrier feeding device 2 for feeding a carrier into the coagulation reaction device 3;

a coagulation reaction device 3, wherein the sewage is subjected to coagulation reaction in the coagulation reaction device 3;

the coagulation reaction barrel 4 is used for carrying out flocculation reaction on the sewage in the coagulation reaction barrel 4;

a floc growth barrel 5, wherein the floc grows into thick and dense floc in the floc growth barrel 5;

the sedimentation barrel 6 is used for settling the floc in the sedimentation barrel 6 to realize sewage purification treatment;

the flocculation-assisting reaction barrel 4, the floc growth barrel 5 and the sedimentation barrel 6 are all cylindrical barrel-shaped structures, the flocculation-assisting reaction barrel 4, the floc growth barrel 5 and the sedimentation barrel 6 are coaxially arranged, the floc growth barrel 5 is fixedly sleeved in the sedimentation barrel 6, the flocculation-assisting reaction barrel 4 is rotatably sleeved in the floc growth barrel 5, and the internal spaces of the flocculation-assisting reaction barrel 4, the floc growth barrel 5 and the sedimentation barrel 6 are sequentially communicated;

sewage import 7 respectively with device 1 is put in to the coagulant and device 2 is put in to the carrier is connected, coagulation reaction unit 3 respectively with device 1 is put in to the coagulant, the carrier is put in device 2 and is aided coagulation reaction barrel 4 and connect, sewage import 7 exhaust sewage can with coagulant put in device 1 in the coagulant and carrier put in the carrier in the device 2 and take into in coagulation reaction unit 3 in the mixing back in coagulation reaction unit 3 flows through in proper order help coagulation reaction barrel 4, flocculating constituent growth barrel 5 and sedimentation barrel 6.

Further, the coagulant adding apparatus 1 includes:

the system comprises a coagulant storage tank 101, a first valve and a second valve, wherein a coagulant is stored in the coagulant storage tank 101, a coagulant feeding port is arranged on the coagulant storage tank 101, and the first valve is arranged on the coagulant feeding port;

a first venturi tube 103 having a first negative pressure port 102;

the inlet of first venturi tube 103 is connected with sewage inlet 7, the liquid outlet with it connects to congeal reaction unit 3, sewage inlet 7 exhaust sewage passes through first venturi tube 103 gets into in the reaction unit 3 congeals, simultaneously first negative pressure mouth 102 department produces the negative pressure under the effect of first negative pressure mouth 102 department negative pressure, first check valve is opened, first negative pressure mouth 102 will the coagulant in the coagulant storage tank 101 is inhaled in first venturi tube 103, later with sewage in the first venturi tube 103 is discharged into in the lump in the reaction unit 3 congeals.

Preferably, the first one-way valve is a pressure automatic control valve, such as a duckbill valve.

Further, the carrier delivery apparatus 2 includes:

the carrier storage tank 201 is used for storing the carriers, a carrier feeding port is formed in the carrier storage tank 201, and a second one-way valve is arranged on the carrier feeding port;

a second venturi 203 having a second negative pressure port 202;

the inlet of second venturi 203 is connected with sewage inlet 7, the liquid outlet with it connects to congeal reaction unit 3, sewage inlet 7 exhaust sewage passes through second venturi 203 gets into in the reaction unit 3 congeals, simultaneously second negative pressure mouth 202 department produces the negative pressure under the effect of second negative pressure mouth 202 department negative pressure, the second check valve is opened, second negative pressure mouth 202 will carrier in the carrier storage tank 201 is inhaled in the second venturi 203, later along with sewage in the second venturi 203 arranges in the lump in the reaction unit 3 congeals.

Preferably, the second one-way valve is a pressure automatic control valve, such as a duckbill valve.

Further, the coagulation reaction apparatus 3 includes:

an outer sleeve 301, which is a tubular structure with two closed ends;

the inner sleeve 302 is a tubular structure with two open ends, and a first water passing port 305 is arranged on the side wall of the inner sleeve 302;

the outer sleeve 301 is sleeved on the periphery of the inner sleeve 302, and two open ends of the inner sleeve 302 respectively extend out from two end parts of the outer sleeve 301;

the coagulant adding device 1 is connected with one open end of the inner sleeve 302, the other open end of the inner sleeve 302 is connected with the coagulation reaction barrel 4, and sewage and coagulant discharged by the coagulant adding device 1 and sewage and carrier discharged by the carrier adding device 2 are mixed in the coagulation reaction device 3 and then discharged into the coagulation reaction barrel 4.

Furthermore, the coagulation reaction device 3 has a first end 303 and a second end 304 which are oppositely arranged, correspondingly, two open ends of the inner sleeve 302 are respectively marked as a first water inlet 306 and a first water outlet 308, the first water inlet 306 is located at the first end 303 of the coagulation reaction device 3, the first water outlet 308 is located at the second end 304 of the coagulation reaction device 3, the coagulant adding device 1 is connected with the first water inlet 306, the first water outlet 308 is connected with the coagulation assisting reaction barrel 4, sewage and coagulant discharged by the coagulant adding device 1 enter the inner sleeve 302 through the first water inlet 306, and are discharged into the coagulation assisting reaction barrel 4 through the first water outlet 308 after flowing through the inner sleeve 302.

Furthermore, a second water inlet 307 is arranged on the outer sleeve 301, and the carrier feeding device 2 is connected with the second water inlet 307, so that the sewage and the carrier discharged by the carrier feeding device 2 can enter the outer sleeve 301 through the second water inlet 304, and then enter the inner sleeve 302 through the first water passing opening 305, and are mixed with the sewage and the coagulant discharged by the coagulant feeding device 1 and then discharged into the coagulation assisting reaction barrel 4 through the first water outlet 308.

Preferably, the amount of sewage discharged by the coagulant adding device 1 is larger than the amount of sewage discharged by the carrier adding device 2. If the amount of the sewage discharged from the coagulant adding device 1 is 5 to 10 times of the amount of the sewage discharged from the carrier adding device 2, the coagulant and the sewage can be uniformly mixed, and the sewage in the coagulation reaction device 3 can be smoothly discharged through the first water outlet 308.

Preferably, as shown in fig. 3, when the distance between the second water inlet 307 and the first end 303 of the coagulation reactor 3 is denoted by W1, and the distance between the second water inlet 307 and the second end 304 of the coagulation reactor 3 is denoted by W2, the value of W2/(W1 + W2) is 0.3 to 0.4. The second water inlet 307 is disposed near the second end 304 and at a distance from the second end 304 such that the material discharged from the second water inlet 307 can be sufficiently convected and mixed with the material in the inner sleeve 302 before being discharged.

Preferably, as shown in fig. 3 to 4, the first water passing opening 305 is a through hole obliquely formed in the tube wall of the inner tube 302, and the first water passing opening 305 gradually inclines toward the first end 303 from the outside of the tube wall of the inner tube 302 to the inside of the tube wall, so that the flow direction of the substance in the outer tube 301 entering the inner tube 302 can be adjusted, and the substance discharged from the second water inlet 307 can be sufficiently mixed with the substance in the inner tube 302.

More preferably, as shown in fig. 4, when an included angle between the central axis of the first drainage port 305 and the pipe wall of the inner casing 302 is α, a value of α ranges from 15 ° to 55 °, so that the mixing effect is ensured, the speed of a substance flowing through the coagulation reaction device 3 can be increased, and the throughput of the coagulation reaction device 3 can be improved.

Further, help and congeal retort 4, floc growth bucket 5 and sedimentation bucket 6 and be cylindrical tubbiness structure, floc growth bucket 5 cover is established in sedimentation bucket 6, help and congeal retort 4 cover and establish in floc growth bucket 5, help and congeal retort 4, floc growth bucket 5 and the coaxial setting of sedimentation bucket 6, help and congeal retort 4 rotatable setting, floc growth bucket 5 and sedimentation bucket 6 are fixed, can not rotate the setting.

As some examples of the present application, the coagulation promoting reaction barrel 4, the floc growth barrel 5 and the sedimentation barrel 6 further have a bottom surface and a top cover, and the bottom surfaces and the top covers of the coagulation promoting reaction barrel 4, the floc growth barrel 5 and the sedimentation barrel 6 may or may not be on the same horizontal plane, and preferably, the bottom surfaces of the coagulation promoting reaction barrel 4, the floc growth barrel 5 and the sedimentation barrel 6 are on the same horizontal plane; the height of the top cover of the coagulation-assistant reaction barrel 4 is lower than that of the top covers of the floc growth barrel 5 and the sedimentation barrel 6.

As some embodiments of the present application, the bottom and the top cover of the coagulation-aiding reaction barrel 4 may or may not rotate synchronously with the coagulation-aiding reaction barrel 4.

Preferably, the bottom and the top of the coagulation reaction barrel 4 rotate synchronously with the coagulation reaction barrel 4.

Further, the coagulation reaction barrel 4 comprises:

a rotating wall 401 rotatably disposed within the floc growth tank 5;

a coagulant aid inlet 403 for introducing coagulant aid into the coagulation reaction tank 4;

a third water inlet 404 connected to the coagulation reaction device 3;

the rotating wall 401 is provided with a second water passing opening 402, and under the rotation action of the coagulation-promoting reaction barrel 4, the substances in the coagulation-promoting reaction barrel 4 enter the floc growth barrel 5 through the second water passing opening 402.

Preferably, a convex stirring rib is arranged on the inner side surface of the rotating wall 401, and the stirring rib accelerates the movement of the substances in the coagulation-promoting reaction barrel 4 and accelerates the speed of the substances entering the floc growth barrel 5 through the second water passing port 402.

As some embodiments of the present application, the stirring rib may be a protruding structure with 3 to 6 protrusions vertically disposed on the rotating wall 401, or may be a protruding structure spirally disposed on the rotating wall 401.

Further, the second water passing opening 402 is a through hole obliquely arranged on the rotating wall 401, from the inner side to the outer side of the rotating wall 401, and the second water passing opening 402 gradually extends obliquely downwards.

Preferably, as shown in fig. 3, an included angle between the central axis of the second water passing port 402 and the rotating wall 401 is represented as β, and a value of β is 30 to 80 °, so that after a substance in the coagulation promoting reaction barrel 4 enters the floc growth barrel 5 through the second water passing port 402, the substance can move centrifugally along with the coagulation promoting reaction barrel 4 at a proper speed and in a proper direction, and simultaneously, requirements of mixing and uniform mixing and timely discharging flocs which do not hinder growth and mature growth of the flocs from the floc growth barrel 5 are met.

Further, the floc growth tank 5 includes:

a fixed wall 501 which is fixedly arranged on the periphery of the coagulation-assistant reaction barrel 4 in an annular shape;

and a third water passing opening 502 which is a through hole arranged on the fixed wall 501, and the substances in the floc growth barrel 5 are driven by the coagulation-assistant reaction barrel 4 to be discharged through the third water passing opening 502.

Preferably, the third water passing opening 502 is a through hole obliquely arranged on the fixed wall 501, specifically, the third water passing opening 502 gradually extends obliquely and upwards along the inner side to the outer side of the fixed wall 501, so that the fluctuation of the rotation of the coagulation promoting reaction barrel 4 to the substances in the settling barrel 6 can be weakened, meanwhile, the settling height of flocs in the settling barrel 6 is prolonged, and the solid-liquid separation effect is improved.

More preferably, as shown in fig. 3, when an included angle between the central axis of the third water passing port 502 and the fixed wall 501 is denoted as γ, the value of γ ranges from 30 ° to 60 °.

Furthermore, an annular convex adjusting ring 503 is arranged inside the fixed wall 501, the third drainage port 502 penetrates through the adjusting ring 503, and the length of the third drainage port 502 is increased by the arrangement of the adjusting ring 503, so that the fluctuation of the rotation of the coagulation-promoting reaction barrel 4 on the substances in the sedimentation barrel 6 is further reduced; on the other hand, the cross-sectional area of the floc growth barrel 5 is changed, the pressure intensity of different height intervals in the floc growth barrel 5 is further changed, the descending speed of substances in the floc growth barrel 5 at different heights is finally changed, the mixing of substances at different radial positions is promoted, and the floc growth time and the mixing uniformity of the substances in the floc growth barrel 5 are improved.

Preferably, a plurality of convex adjusting rings 503 are provided at intervals inside the fixing wall 501.

More preferably, the adjusting ring 503 is disposed corresponding to the third water passing ports 502, such that each third water passing port 502 penetrates through the adjusting ring 503.

Further, the precipitation barrel 6 includes: the outer wall 601 is arranged around the periphery of the floc growth barrel 5, a clean water discharge port 602 and a precipitation discharge port 603 are arranged on the outer wall 601, the clean water discharge port 602 is positioned at the upper part of the precipitation barrel 6, the precipitation discharge port 603 is positioned at the lower part of the precipitation barrel 6, the precipitation discharge port 603 is connected with a cyclone, carriers and dirt in precipitation are separated through the cyclone, and then the carriers and the dirt are thrown into the carrier throwing device 2 again for recycling.

As some embodiments of the present application, an inclined plate sedimentation structure is arranged in the sedimentation barrel 6 to improve the sedimentation and solid-liquid separation effects.

The working process and the principle of the loading flocculation and precipitation device are as follows: firstly, opening the sewage inlet 7 to discharge sewage into a first venturi tube 103 in the coagulant adding device 1 and a second venturi tube 203 in the carrier adding device 2 respectively, generating negative pressure at the first negative pressure port 102 and the second negative pressure port 202 respectively, opening a first one-way valve of the coagulant adding port and a second one-way valve of the carrier adding port under the action of the negative pressure, sucking the coagulant in the coagulant adding device 1 through the first one-way valve and the first negative pressure port 102, mixing the coagulant with the sewage in the coagulant adding device 1, and then entering an inner sleeve 302 in the coagulation reaction device 3; meanwhile, the carrier in the carrier throwing device 2 is sucked through the second one-way valve and the second negative pressure port 202 and mixed with the sewage in the carrier throwing device 2, and then enters the outer sleeve 301 in the coagulation reaction device 3, the sewage and the carriers in the outer sleeve 301 enter the inner sleeve 302 through the first water passing opening 305, and form a counter flow with the sewage and the coagulant discharged by the coagulant feeding device 1, under the action of countercurrent, substances discharged by the coagulant adding device 1 and the carrier adding device 2 are subjected to convection, mixing and coagulation reaction, and finally, because the amount and the speed of the sewage discharged by the coagulant adding device 1 are larger, the substances in the coagulation reaction device 3 are discharged from the first water outlet 308 and enter the coagulation reaction barrel 4, meanwhile, the coagulant aid adding port 403 is opened to add coagulant aid into the coagulation aid reaction barrel 4, in the coagulation-aiding reaction barrel 4, along with the rotation of the coagulation-aiding reaction barrel 4, the substances in the coagulation-aiding reaction barrel 4 are mixed and generate flocculation reaction, meanwhile, the centrifugal motion is carried out, larger flocs move to the outer side of the coagulation-assistant reaction barrel 4 under the action of the centrifugal force and then enter the floc growth barrel 5 through the second water passing port 402, the substances in the floc growth barrel 5 are mixed with each other under the rotation driving action of the coagulation-assistant reaction barrel 4, the floc continues to grow, and simultaneously, the substances also do centrifugal motion, wherein, larger flocs move to the outer side of the floc growth barrel 5 under the action of centrifugal force and then enter the sedimentation barrel 6 through the third water passing port 502, after solid-liquid separation is realized in the sedimentation barrel 6 through gravity sedimentation, the solid-liquid separation is discharged through a sedimentation discharge port 603 and a clean water discharge port 602 respectively.

The working process and the principle of the loading flocculation and precipitation device can be known as follows: the loading flocculation and precipitation device avoids adopting a hard stirring body to directly and powerfully stir the sewage, the flocs and the carrier in the working process, and mixing the sewage, the flocs and the carrier in modes of countercurrent, centrifugation, up-and-down movement and the like, avoids the 'no-buffer' stirring of the carrier and the flocs, is not easy to cause the disintegration and the fracture of the carrier and the flocs, can effectively improve the service life of the carrier and the cycle use times, and is beneficial to the rapid growth of the flocs; simultaneously, for the overflow of pure among the prior art, this application has accelerated the processing speed of sewage through the mode of countercurrent mixing, centrifugation, and the helping of establishing cover in proper order congeals reaction tank 4, floc growth bucket 5 and precipitation bucket 6 and can effectively practice thrift sewage treatment plant's area, makes its applicable scene unrestricted, applicable scope wider.

p1, opening a sewage inlet 7, and respectively discharging sewage into the coagulant adding device 1 and the carrier adding device 2, wherein at the moment, the first one-way valve and the second one-way valve are automatically opened, the coagulant enters the inner sleeve 302 along with the sewage, and the carrier is discharged into the outer sleeve 301 along with the sewage;

p2, the sewage and the carrier in the outer sleeve 301 enter the inner sleeve 302 through the first water passing port 305, are mixed with the sewage and the coagulant in the inner sleeve 302, carry out coagulation reaction, and are discharged into the coagulation assisting reaction barrel 4;

p3, controlling the rotating wall 401 of the coagulation-aiding reaction barrel 4 to rotate at the speed of 100-600 rpm, simultaneously putting a coagulant aid into the coagulation-aiding reaction barrel 4, carrying out a flocculation reaction with sewage in a rotating mixing process, and allowing generated flocs to enter the floc growth barrel 5 through the second water passing port 402 under the action of centrifugal force;

p4, after entering the floc growth barrel 5, the flocs continue to grow and do centrifugal motion under the driving of the rotation of the coagulation-assistant reaction barrel 4, wherein larger flocs enter the sedimentation barrel 6 through the third water passing port 502 under the action of centrifugal force;

p7, after the solid-liquid separation is realized in the sedimentation barrel 6 through gravity sedimentation, solid and liquid substances are respectively discharged through a sedimentation discharge port 603 and a clean water discharge port 602.

The loading flocculation and precipitation method is simple in operation process, easy to realize automatic control and high in sewage treatment efficiency.

When the circulation frequency of the carrier reaches the design upper limit, for example, 30 to 100 times of circulation, the carrier discharged from the cyclone is cleaned and dried, a certain amount of auxiliary agent is weighed according to 3 to 7 percent of the mass of the carrier, and after the auxiliary agent and carrier particles are uniformly mixed, the carrier particles are placed in a granulator for granulation and drying to obtain an inner core; and then, the regeneration of the carrier can be realized after the adsorption layer coated in the step S3 is installed.

Example 1

A method of preparing a precipitate-laden support, the method comprising the steps of:

s1, pressing the prefabricated particles by adopting waste gas recovery powder: taking powder recovered from waste gas of a certain steel smelting plant as a raw material, drying the raw material to constant weight, grinding the raw material until the average particle size is less than or equal to 1um, placing the ground material in a mold, and pressing the ground material into a briquette with the relative density of 80%; placing the pressed compact blocks into a grinder to be ground into particles, then screening the particles by a 500-mesh sieve, collecting undersize products to be sintered at high temperature, and continuously grinding oversize products; sintering at high temperature in a sintering furnace for 2 hours at 500 ℃ to obtain prefabricated particles;

s2, bonding a plurality of prefabricated particles together by adopting an auxiliary agent to form an inner core: weighing a certain amount of auxiliary agent according to 10% of the mass of the prefabricated particles, uniformly mixing the auxiliary agent and the prefabricated particles, placing the mixture in a granulator for granulation, and drying the mixture at 90 ℃ for 30min to obtain a kernel;

s3, coating an adsorption layer on the outer surface of the inner core: weighing 80 parts by weight of a base material, 5 parts by weight of a pore-forming agent and 2 parts by weight of a plant adhesive according to the weight ratio, uniformly mixing, adding 40 parts by weight of water, uniformly stirring to obtain slurry of an adsorption layer, then weighing the slurry of the adsorption layer accounting for 10% of the weight of the inner core, spraying the slurry of the adsorption layer on the outer surface of the inner core in a spraying manner, simultaneously stirring and mixing, uniformly mixing, sintering at 500 ℃, and drying for 10min to obtain the loaded and precipitated carrier.

Example 2

s1, pressing prefabricated particles by adopting waste gas recovery powder: taking powder recovered from waste gas of a certain steel smelting plant as a raw material, drying the raw material to constant weight, grinding the raw material until the average grain diameter is less than or equal to 1um, placing the raw material in a mold, and pressing the raw material into a briquette with the relative density of 90%; placing the pressed compact blocks into a grinder to be ground into particles, then sieving the particles through a 500-mesh sieve, collecting undersize materials to be sintered at high temperature, and continuously grinding oversize materials; sintering at high temperature in a sintering furnace for 1h at 600 ℃ to obtain prefabricated particles;

s2, bonding a plurality of prefabricated particles together by adopting an auxiliary agent to form an inner core: weighing a certain amount of auxiliary agent according to 30% of the mass of the prefabricated particles, uniformly mixing the auxiliary agent and the prefabricated particles, placing the mixture in a granulator for granulation, and drying the mixture at 150 ℃ for 10min to obtain a kernel;

s3, coating an adsorption layer on the outer surface of the inner core: respectively weighing 50 parts by weight of a base material, 3 parts by weight of a pore-forming agent and 1 part by weight of a plant adhesive according to a weight ratio, uniformly mixing the base material, the pore-forming agent and the plant adhesive, adding 30 parts by weight of water, uniformly stirring to obtain slurry of an adsorption layer, then weighing 30% of the slurry of the adsorption layer by weight of an inner core, spraying the slurry of the adsorption layer on the outer surface of the inner core in a spraying manner, simultaneously stirring and mixing, uniformly mixing, sintering at 200 ℃ and drying for 30min to obtain the loaded and precipitated carrier.

Example 3

s1, pressing prefabricated particles by adopting waste gas recovery powder: taking powder recovered from waste gas of a certain steel smelting plant as a raw material, drying the raw material to constant weight, grinding the raw material until the average grain diameter is less than or equal to 1um, placing the raw material in a mold, and pressing the raw material into a briquette with the relative density of 84%; placing the pressed compact blocks into a grinder to be ground into particles, then sieving the particles through a 500-mesh sieve, collecting undersize materials to be sintered at high temperature, and continuously grinding oversize materials; sintering at high temperature in a sintering furnace for 1.3h at 550 ℃ to obtain prefabricated particles;

s2, bonding a plurality of prefabricated particles together by adopting an auxiliary agent to form an inner core: weighing a certain amount of auxiliary agent according to 20% of the mass of the prefabricated particles, uniformly mixing the auxiliary agent and the prefabricated particles, placing the mixture in a granulator for granulation, and drying the mixture at 100 ℃ for 15min to obtain a kernel;

s3, coating an adsorption layer on the outer surface of the inner core: respectively weighing 60 parts by weight of base material, 4 parts by weight of pore-forming agent and 1.5 parts by weight of plant adhesive according to the weight ratio, uniformly mixing the base material, the pore-forming agent and the plant adhesive, adding 35 parts by weight of water, uniformly stirring to obtain slurry of an adsorption layer, then weighing 20% of the slurry of the adsorption layer by weight of an inner core, spraying the slurry of the adsorption layer on the outer surface of the inner core in a spraying manner, simultaneously stirring and mixing, uniformly mixing, sintering at 300 ℃ for 20min, and drying to obtain the carrier loaded with the precipitate.

Example 4

The indexes of the sewage to be treated in a certain sewage treatment plant are as follows: COD _cr =178mg/L, chroma is 67 DEG, pH value is 5.7, and appearance is in a yellowish brown turbid state.

Introducing sewage to be treated into a sewage inlet 7 in the loading flocculation and precipitation device, opening the sewage inlet 7, and discharging the sewage into a coagulant adding device 1 and a carrier adding device 2 respectively, wherein the ratio of the sewage discharge amount in the coagulant adding device 1 to the sewage discharge amount in the carrier adding device 2 is 5; then, the sewage and the carrier in the outer sleeve 301 enter the inner sleeve 302, are mixed with the sewage and the coagulant in the inner sleeve 302, carry out coagulation reaction, and are discharged into the coagulation assisting reaction barrel 4; controlling the rotating wall 401 of the coagulation reaction barrel 4 to rotate at the speed of 100 revolutions per minute, simultaneously putting a coagulant aid into the coagulation reaction barrel 4, wherein the coagulant aid is polyacrylamide, the adding amount of the coagulant aid is 2mg/L, carrying out flocculation reaction on sewage in rotating mixing, and enabling generated flocs to enter the floc growth barrel 5 under the action of centrifugal force; after entering the floc growth barrel 5, the flocs continue to rotate and mix under the drive of the rotation of the coagulation assisting reaction barrel 4, so that the flocs continue to grow and do centrifugal motion at the same time, wherein larger flocs enter the sedimentation barrel 6 under the action of centrifugal force; finally, solid-liquid separation is realized in the sedimentation barrel 6 through gravity sedimentation, and then the solid-liquid separation is discharged.

Example 5

The present embodiment differs from embodiment 4 described above only in that: the sewage discharge amount ratio between the coagulant adding device 1 and the carrier adding device 2 is 10, the rotating speed of the rotating wall 401 of the coagulation-assistant reaction barrel 4 is 600 rpm, and the rest is the same as that of the embodiment 4, and the details are not repeated herein.

Example 6

The present embodiment differs from embodiment 4 described above only in that: the sewage discharge amount ratio between the coagulant adding device 1 and the carrier adding device 2 is 8, the rotating speed of the rotating wall 401 of the coagulation-assistant reaction barrel 4 is 300 revolutions/min, and the rest is the same as that of the embodiment 4, and the details are not repeated herein.

Comparative example 1

The present comparative example differs from example 4 above only in that: replacing the carrier with sandstone with the same granularity for sewage treatment, wherein the adding amount of the sandstone is 2g/L; the rest is the same as the above embodiment 4, and the description is omitted.

Comparative example 2

The present comparative example differs from example 4 above only in that: replacing the carrier with quartz stones with the same granularity for sewage treatment, wherein the adding amount of the quartz stones is 2g/L; the rest is the same as the above embodiment 4, and the description is omitted.

Comparative example 3

The present comparative example differs from example 1 above only in that:

in the step S1, powder recovered from waste gas of a certain steel smelting plant is used as a raw material, the raw material is dried to constant weight, the powder is ground until the average particle size is less than or equal to 1um, then high-temperature sintering is carried out in a sintering furnace, and the powder is sintered for 2 hours at 500 ℃ to obtain prefabricated particles.

The rest is the same as the above embodiment 1, and the description is omitted.

Test example 1

The carriers prepared in examples 1 to 3 and comparative example 3 were measured to obtain the following table 1:

TABLE 1 results of Carrier Property measurements

	Example 1	Example 2	Example 3	Comparative example 3
					Density of support (g/m) ³ )	5.21	5.34	5.58	4.29
Bulk specific gravity (g/m) ³ )	2.51	2.35	2.44	2.15
					Compressive strength (Mpa)	126	125	123	42

Test example 2

The water quality of the clean water obtained by the treatment of the examples 4 to 6 and the comparative examples 1 to 2 is measured to obtain the following table 2:

TABLE 2 Water quality measurement results

	Example 4	Example 5	Example 6	Comparative example 1	Comparative example 2
						Appearance of the product	Colorless and transparent	Colorless and transparent	Colorless and transparent	Colorless and transparent	Colorless and transparent
pH value	6.3	6.5	6.2	6.2	6.4
						Chroma (°)	31	32	35	52	43
COD _cr (mg/L)	66	73	71	109	89

Although the present invention is disclosed above, the present invention is not limited thereto. In the description herein, references to the description of the term "one embodiment," "some embodiments," "an illustrative embodiment," "an example," "a specific example," or "some examples" or the like mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Various changes and modifications may be effected by one skilled in the art without departing from the spirit and scope of the invention, as defined in the appended claims.

Claims

1. A loaded flocculation precipitation method, wherein the carrier for loading flocculation precipitation comprises:

a core (b);

the adsorption layer (a) is coated on the periphery of the inner core (b), and is a porous adsorption material;

the core (b) includes:

a plurality of prefabricated particles (b 1) which are particulate matters composed of an exhaust gas recovery powder;

an auxiliary agent (b 2) which fills gaps between the plurality of preformed particles (b 1) and bonds the plurality of preformed particles (b 1) together to form the inner core (b);

the carrier adopts loading flocculation and precipitation device to carry out sewage treatment, loading flocculation and precipitation device includes:

a coagulant adding device (1), a carrier adding device (2), a coagulation reaction device (3), a coagulation-aiding reaction barrel (4), a floc growth barrel (5), a sedimentation barrel (6) and a sewage inlet (7);

the coagulation reaction device (3) comprises an outer sleeve (301) and an inner sleeve (302), wherein the outer sleeve (301) is sleeved on the periphery of the inner sleeve (302);

the flocculation-assisting reaction barrel (4), the floc growth barrel (5) and the sedimentation barrel (6) are all cylindrical barrel-shaped structures, the flocculation-assisting reaction barrel (4), the floc growth barrel (5) and the sedimentation barrel (6) are coaxially arranged, the floc growth barrel (5) is fixedly sleeved in the sedimentation barrel (6), the flocculation-assisting reaction barrel (4) is rotatably sleeved in the floc growth barrel (5), the internal spaces of the flocculation-assisting reaction barrel (4), the floc growth barrel (5) and the sedimentation barrel (6) are sequentially communicated, and the rotation speed of the flocculation-assisting reaction barrel (4) is 100 to 600 revolutions per minute;

the sewage inlet (7) is respectively connected with the coagulant adding device (1) and the carrier adding device (2), the coagulation reaction device (3) is respectively connected with the coagulant adding device (1), the carrier adding device (2) and the coagulation assisting reaction barrel (4), the coagulant in the coagulant adding device (1) and the carrier in the carrier adding device (2) can be brought into the coagulation reaction device (3) by the sewage discharged from the sewage inlet (7), and the sewage sequentially flows through the coagulation assisting reaction barrel (4), the floc growth barrel (5) and the sedimentation barrel (6) after being uniformly mixed in the coagulation reaction device (3);

wherein the coagulation-aiding reaction barrel (4) comprises: the flocculating and coagulating reaction barrel comprises a rotating wall (401), a second water passing port (402) is arranged on the rotating wall (401), under the rotating action of the flocculating and coagulating reaction barrel (4), substances in the flocculating and coagulating reaction barrel (4) enter the floc growth barrel (5) through the second water passing port (402), the second water passing port (402) is a through hole obliquely arranged on the rotating wall (401), the second water passing port (402) gradually extends obliquely downwards from the inner side to the outer side of the rotating wall (401), an included angle between the central axis of the second water passing port (402) and the rotating wall (401) is recorded as beta, and the value range of the beta is 30-80 degrees;

the floc growth tank (5) comprises:

the fixed wall (501) is fixedly arranged on the periphery of the coagulation-aiding reaction barrel (4) in an annular shape;

the third water passing port (502) is a through hole formed in the fixed wall (501), substances in the floc growth barrel (5) are driven by the coagulation aid reaction barrel (4) to be discharged through the third water passing port (502), the third water passing port (502) gradually inclines and extends upwards along the inner side to the outer side of the fixed wall (501), an included angle between the central axis of the third water passing port (502) and the fixed wall (501) is recorded as gamma, and the value range of the gamma is 30 to 60 degrees;

an annular convex adjusting ring (503) is arranged on the inner side of the fixed wall (501), and the third water passing opening (502) penetrates through the adjusting ring (503).

2. The method for loaded flocculation and precipitation of claim 1, wherein the average particle size of the inner core (b) is 50 to 100um, the average particle size of the prefabricated particle (b 1) is 5 to 20um, and the thickness of the adsorption layer (a 1) is 3 to 10um.

3. A loaded flocculation and precipitation method according to claim 1, wherein said preformed particles (b 1) are particles consisting of waste gas recovery powders from steel smelting plants.

4. A loaded flocculation and precipitation method according to any of claims 1-3, wherein said carrier is prepared by a method comprising the steps of:

s1, pressing prefabricated particles by using waste gas recovery powder;

and S3, coating an adsorption layer on the outer surface of the inner core.

5. The loaded flocculation and sedimentation method according to claim 4, wherein said step S1 comprises:

s11, waste gas recovery powder pretreatment: taking powder recovered from waste gas as a raw material, drying the raw material to constant weight, and grinding the raw material until the average particle size is less than or equal to 1um for later use;

s12, pressing the compact: placing the ground waste gas recovery powder in a mould, and pressing into a billet with the relative density of more than or equal to 80%;

s14, high-temperature sintering: placing the crushed particles into a sintering furnace, and sintering at 500-600 ℃ for 1-2h to obtain prefabricated particles.

6. The loaded flocculation and sedimentation method according to claim 4, wherein said step S2 comprises: weighing a certain amount of auxiliary agent, uniformly mixing the auxiliary agent and the prefabricated particles, placing the mixture in a granulator for granulation, and drying to obtain an inner core; wherein the addition amount of the auxiliary agent is 10-30% of the mass of the prefabricated particles.

7. The loaded flocculation and sedimentation method of claim 6, wherein the auxiliary agent is prepared by the following process: firstly weighing 50 to 80 parts by weight of saturated soft clay, placing the saturated soft clay in a closed container, heating the saturated soft clay to 65 to 85 ℃ under stirring, adding 5 to 10 parts by weight of PVA, stirring for 1 to 3min to uniformly disperse and dissolve the PVA in the saturated soft clay, opening a container cover to volatilize water in the saturated soft clay, then adding medium-high temperature asphalt powder under continuous stirring at 60 to 70 ℃, heating and stirring until the water content of a mixed system reaches 25 to 30%, uniformly dispersing and dissolving 1 to 3 parts by weight of silane coupling agent in the mixed system to obtain the auxiliary agent.

8. The loaded flocculation and sedimentation method according to claim 4, wherein said step S3 comprises: weighing a certain amount of raw materials of the adsorption layer, dissolving the raw materials of the adsorption layer in water to prepare slurry, spraying the slurry of the adsorption layer on the outer surface of the inner core in a spraying mode, stirring and mixing at the same time, uniformly mixing, sintering at 200-500 ℃, and drying for 10-30min to obtain the carrier.

9. A loaded flocculation and precipitation method according to any of claims 1-3, comprising the steps of:

p1, opening a sewage inlet (7), and respectively discharging sewage into the coagulant adding device (1) and the carrier adding device (2), wherein at the moment, the coagulant adding device (1) and the carrier adding device (2) generate negative pressure through Venturi tubes, under the action of the negative pressure, a first one-way valve in the coagulant adding device (1) is automatically opened, a coagulant enters an inner sleeve (302) in the coagulation reaction device (3) along with the sewage, a second one-way valve in the carrier adding device (2) is automatically opened, and a carrier is discharged into an outer sleeve (301) in the coagulation reaction device (3) along with the sewage;

p2, the sewage and the carrier in the outer sleeve (301) enter the inner sleeve (302), are mixed with the sewage and the coagulant in the inner sleeve (302), carry out coagulation reaction and then are discharged into a coagulation assisting reaction barrel (4);

p3, controlling the coagulation reaction barrel (4) to rotate at a speed of 100 to 600 rpm, putting a coagulant aid into the coagulation reaction barrel (4), carrying out flocculation reaction on sewage in a rotating and mixing process, and enabling generated flocs to enter the floc growth barrel (5) under the action of centrifugal force;

p4, after entering the floc growth barrel (5), the flocs continuously rotate and mix under the drive of the rotation of the coagulation-assistant reaction barrel (4), so that the flocs continuously grow and do centrifugal motion at the same time, and then enter the sedimentation barrel (6) under the action of centrifugal force;

and P7, realizing solid-liquid separation in the settling barrel (6) through gravity settling and then discharging.