CN216005486U

CN216005486U - Circulating fluidized bed reactor

Info

Publication number: CN216005486U
Application number: CN202121796402.9U
Authority: CN
Inventors: 范世祥; 郑兴兴; 张悍; 韩雪刚
Original assignee: Harbin Huachunhua Environmental Protection Technology Development Co ltd
Current assignee: Harbin Huachunhua Environmental Protection Technology Development Co ltd
Priority date: 2021-08-03
Filing date: 2021-08-03
Publication date: 2022-03-11
Anticipated expiration: 2031-08-03

Abstract

The present invention provides a circulating fluidized bed reactor comprising: the container is separated into a regulating area, a reaction area and a settling area by a separator, the regulating area is provided with an inlet, and a sample entering through the inlet flows through the regulating area, the reaction area and the settling area in sequence; the reaction zone is provided with a dosing port, and the precipitation zone is provided with an outlet; the stirring module is arranged in the adjusting area; the aeration module is arranged in the reaction zone; the pipeline is used for communicating the sedimentation zone and the reaction zone, and the pump is arranged on the pipeline. The utility model has the advantages of simple structure, low operation cost and the like.

Description

Circulating fluidized bed reactor

Technical Field

The utility model relates to wastewater treatment, in particular to a circulating fluidized bed reactor.

Background

At present, in the advanced treatment process of high-concentration organic chemical wastewater, the more commonly used processes are as follows:

1. the two processes mainly utilize the higher oxidation potential of hydroxyl free radicals generated in the Fenton reaction or the higher oxidation potential of ozone to oxidize macromolecular organic matters in the wastewater into micromolecular inorganic matters, so that the effect of removing pollutants in the wastewater is achieved, wherein the COD of the wastewater is a main factor of the water quality condition. The disadvantages of these two processes are:

aiming at the Fenton method, according to the related policies and market situations of the state at present, a plurality of limiting factors exist in the purchase and use of hydrogen peroxide, the method can generate a large amount of waste iron mud, and the sludge is difficult to treat and needs to consume a large amount of financial resources. In the catalytic ozonation method, although secondary pollution such as sludge is not generated, the preparation cost of ozone is high, the utilization efficiency of ozone is low, and the requirement of treating a large amount of industrial wastewater is difficult to meet.

2. The adsorption method is to utilize active carbon and other adsorbent to adsorb pollutant in the pore structure on the surface or inside the adsorbent through physical adsorption or chemical adsorption and to eliminate pollutant with the elimination of the adsorbent to reach the effect of eliminating pollutant from waste water. The process has the following defects:

in the adsorption method, high-quality adsorbents such as activated carbon which have high pollutant adsorption capacity are frequently used at present, but the activated carbon is expensive and difficult to recycle or expensive in regeneration cost, so that the operation cost of the adsorption method is high.

SUMMERY OF THE UTILITY MODEL

In order to overcome the defects in the prior art, the utility model provides the circulating fluidized bed reactor which is simple in structure, low in operation cost and good in treatment effect.

The purpose of the utility model is realized by the following technical scheme:

a circulating fluidized bed reactor, the circulating fluidized bed reactor comprising:

the device comprises a container and a separator, wherein the container is separated into a regulating area, a reaction area and a settling area by the separator, the regulating area is provided with an inlet, and a sample entering through the inlet sequentially flows through the regulating area, the reaction area and the settling area; the regulating area and the reaction area are provided with dosing ports, and the settling area is provided with an outlet;

a stirring module disposed within the conditioning zone;

an aeration module disposed within the reaction zone;

the pipeline is used for communicating the sedimentation zone and the reaction zone, and the pump is arranged on the pipeline.

Compared with the prior art, the utility model has the beneficial effects that:

aiming at the problems in the prior art, the iron-carbon microelectrolysis process is introduced on the basis of the structural design, combines the advantages of electrocatalytic oxidation and adsorption methods, combines the microelectrolysis reaction with the adsorption reaction, and simultaneously reflows the medicament after the microelectrolysis reaction for recycling, so that the use efficiency of the medicament is improved, the amount of waste sludge is reduced, and the medicament cost of actual operation is reduced;

1. the operation cost is low;

the reduced iron powder and the active coke are used as medicaments, so that the medicaments are more smoothly purchased and used;

the micro-electrolysis reaction is accelerated by aeration and stirring, and meanwhile, oxygen in the air can participate in the micro-electrolysis reaction to form a small amount of hydroxyl free radicals, so that the efficiency of removing pollutants by micro-electrolysis is improved, and free air resources are fully utilized;

the result of the small test shows that when the reflux rate of the reagent after reaction is 50%, the cost of the reagent in the whole process can be saved by about 37%;

2. the structure is simple, and the applicability is good;

the pipeline, the stirring module, the aeration module, the pump, the partition plate and the like are conventional components, and the structure is simple;

the reactor can optimally select proper dosing amount, reflux amount and reflux ratio according to different water qualities, and has certain adaptability to different water qualities;

3. the treatment effect is good;

the effect of recycling the medicament is achieved by refluxing precipitates such as iron powder, active coke and the like after micro-electrolysis reaction, the use efficiency of the medicament is improved, and the generation of sludge is reduced;

and aeration is carried out in the reaction zone, on one hand, oxygen in the aeration participates in the micro-electrolysis reaction, so that the reaction efficiency is enhanced, and on the other hand, the wastewater is stirred, so that the medicament is fully mixed with the wastewater, and the micro-electrolysis reaction rate is improved.

Drawings

The disclosure of the present invention will become more readily understood with reference to the accompanying drawings. As is readily understood by those skilled in the art: these drawings are only for illustrating the technical solutions of the present invention and are not intended to limit the scope of the present invention. In the figure:

FIG. 1 is a schematic view of the structure of a circulating fluidized bed reactor in example 1 according to the present invention.

Detailed Description

Fig. 1 and the following description depict alternative embodiments of the utility model to teach those skilled in the art how to make and reproduce the utility model. Some conventional aspects have been simplified or omitted for the purpose of teaching the present invention. Those skilled in the art will appreciate that variations or substitutions from these embodiments will be within the scope of the utility model. Those skilled in the art will appreciate that the features described below can be combined in various ways to form multiple variations of the utility model. Thus, the present invention is not limited to the following alternative embodiments, but is only limited by the claims and their equivalents.

Example 1:

fig. 1 schematically shows a schematic view of a circulating fluidized bed reactor according to an embodiment of the present invention, which includes, as shown in fig. 1:

a stirring module disposed within the conditioning zone;

an aeration module disposed within the reaction zone;

In order to improve the reaction effect, the reaction area is further divided into a first part and a second part by a partition plate; the distance between the partition plate and the bottom wall of the reaction zone is greater than zero, and the first part and the second part are communicated through an area on the lower side of the partition plate;

the dosing ports are respectively arranged on the first portion and the second portion.

In order to accurately control dosing for two years, further, the circulating fluidized bed reactor further comprises:

a pH meter disposed within the conditioning zone and the second section, respectively.

In order to conveniently realize the communication, an overflow port is further arranged between the adjusting area and the first part, and an overflow port is arranged between the second part and the settling area.

In order to increase the sedimentation effect, the inner diameter of the sedimentation zone is further reduced from top to bottom.

In order to add different reaction medicines, the first part and the second part are further provided with two medicine adding openings respectively.

Example 2:

an example of application of the circulating fluidized bed reactor according to example 1 of the present invention in wastewater treatment.

In this application, as shown in fig. 1, the space inside the vessel is divided by the partition into the conditioning zone 6, the reaction zone 11 and the settling zone 17, the distance between the partition and the top wall of the vessel being greater than zero, i.e. the overflow ports 7, 16; in the reaction zone 11, a partition plate 23 is further arranged to divide the reaction zone 11 into a first part and a second part, and a gap is formed between the partition plate 23 and the bottom wall of the container; the adjusting area 6 is provided with a water inlet 2 and a dosing port 3, and the settling area 17 is provided with a water outlet 18;

a mechanical stirrer 5 and a pH meter 22 are arranged in the conditioning zone 6; the aeration module comprises a fan 1, an aeration pipeline 4 and aeration discs 12-13, wherein the aeration discs 12-13 are arranged at the bottom of the reaction zone; the first part is internally provided with an iron powder dosing port 8 and an active coke dosing port 9; the second part is internally provided with a liquid caustic soda dosing port 14, a PAM dosing port 15 and a PH meter 22; a slope is arranged in the settling zone 17, so that the collection of sediments is facilitated; the first pipeline 10 is communicated with the bottom of the settling zone 17 and the first part of the reaction zone 11, and a sludge discharge port 19 is arranged at the end part of the first pipeline 10; the pump 20 is arranged on the pipeline 10; the second conduit and the pump 21 communicate with said first conduit 10.

Application example 1

The effluent of the secondary sedimentation tank at the biochemical section of a certain coking plant is used as raw water, the pH value of the raw water is 6-8, and the COD is 160-200 mg/L. When the reactor of the embodiment 2 of the utility model is adopted for treatment, the pH value of the wastewater in the adjusting area is adjusted to about 3, the adding mass ratio of iron powder and active coke in the reaction area is 1.67 (wherein the adding amount of iron powder is 625ppm, and the adding amount of active coke is 375ppm), the hydraulic retention time in the reaction area is 60 min-120 min, the pH value at the rear end of the reaction area is adjusted to about 7.5, the reflux rate of the microelectrolysis agent after reaction is 50%, and the COD of the effluent is 30 mg/L-50 mg/L. The COD of the effluent reaches the direct discharge standard in the table 2 of GB 16171-2012 discharge Standard for pollutants from coking chemistry industry. According to rough calculation, a circulation reflux process is not adopted, the cost of the medicament is about 6-6.5 yuan/ton of water, after circulation reflux utilization, the cost of the medicament is about 3.75-4.25 yuan/ton of water, and the cost of the medicament is saved by about 36%.

Application example 2

The effluent of the secondary sedimentation tank at the biochemical section of a certain coking plant is used as raw water, the pH value of the raw water is 6-8, and the COD is 200-280 mg/L. When the reactor of the embodiment 2 of the utility model is adopted for treatment, the pH value of the wastewater in the adjusting area is adjusted to about 3, the adding mass ratio of the iron powder and the active coke in the reaction area is 0.66 (wherein the adding amount of the iron powder is 375ppm, and the adding amount of the active coke is 625ppm), the hydraulic retention time of the reaction area is 60 min-120 min, the pH value at the rear end of the reaction area is adjusted to about 7.5, the reflux rate of the microelectrolysis agent after reaction is 50%, and the COD of the effluent is 60 mg/L-90 mg/L. The COD of the effluent reaches the direct discharge standard in the table 2 of GB 16171-2012 discharge Standard for pollutants from coking chemistry industry. By rough calculation, the cost of the medicament is about 6 yuan/ton of water without adopting a circulation reflux process, and after circulation reflux utilization, the cost of the medicament is about 3.75 yuan/ton of water, so that the cost is saved by about 38%.

Claims

1. A circulating fluidized bed reactor, characterized in that the circulating fluidized bed reactor comprises:

a stirring module disposed within the conditioning zone;

an aeration module disposed within the reaction zone;

2. The circulating fluidized bed reactor of claim 1, wherein the reaction zone is divided into a first portion and a second portion by a partition; the distance between the partition plate and the bottom wall of the reaction zone is greater than zero, and the first part and the second part are communicated through an area on the lower side of the partition plate;

3. The circulating fluidized bed reactor of claim 2, further comprising:

4. A circulating fluidized bed reactor according to claim 2, wherein there is an overflow between the conditioning zone and the first portion and an overflow between the second portion and the settling zone.

5. The circulating fluidized bed reactor of claim 1, wherein the inner diameter of the settling zone becomes smaller from top to bottom.

6. The circulating fluidized bed reactor of claim 2, wherein the first portion and the second portion each have two dosing ports.