Tower type catalytic ozonation reactor

Abstract

The utility model discloses a tower type catalytic ozonation reactor which comprises a reactor body, the reactor body comprises a plurality of catalytic units which are sequentially communicated from bottom to top, the number of the catalytic units can be increased or decreased, each catalytic unit comprises a catalyst whole building filler and a sieve plate, and the sieve plate is arranged at the bottom of the catalyst whole building filler. Gas distribution devices are arranged in part of the catalytic units, a gas inlet and a first water through hole are formed in the bottom of the reactor body, a gas outlet and a second water through hole are formed in the top of the reactor body, and the water inlet and the water outlet are interchangeable. According to the scheme, the rising of bubbles is delayed, ozone dissolution is promoted, and meanwhile it can be guaranteed that ozone which is rapidly dissolved in the initial stage has enough standing time in a catalyst area, so that effective decomposition of ozone and the yield of. OH are guaranteed; 2, the treatment efficiency of the reactor can be greatly improved only by replacing the positions of the water inlet, the water outlet and the air inlet, the operation is simple, and the effect is obvious; 3, working condition optimization can be realized by only adding one or two sets of ozone distribution devices, the investment cost is slightly increased, and the operation cost can be greatly reduced; and 4, when the inlet water quality and quantity change, the position of the air inlet can be changed through water quality analysis, the operation is convenient, and the working condition elasticity is high.

Description

Technical Field

[0001] The utility model belongs to the technical field of catalytic ozonation equipment, and particularly relates to a tower-type catalytic ozonation reactor. Background Art

[0002] As an advanced oxidation technology, the catalytic ozonation method is becoming more and more widely used. Its main advantages are as follows: no chemical agents need to be added, no sludge and salt are produced, and it has almost no harm to the environment, which is a clean and green process. The invention of the iron-based catalyst integral packing has greatly improved the efficiency of catalytic ozonation and significantly reduced the cost of the catalyst, and has been applied to the deep treatment process of large-scale industrial wastewater.

[0003] With the in-depth research on the engineering of ozone catalytic oxidation, the importance of the flow pattern has been increasingly emphasized. Ozone generates bubbles through the air distribution device. When the bubble size is medium or small, the bubble rising speed is relatively fast, and the time for the bubble to pass through the water layer (gas path time) is less, which affects the dissolution ratio of ozone in the bubble. If the water flows downward, that is, the gas-liquid countercurrent flow, it can extend the residence time of the bubble in the water layer and strengthen mass transfer, which is beneficial to the dissolution of ozone; and it also extends the residence time of the dissolved ozone in the catalyst area, increasing the proportion of the effective decomposition of the dissolved ozone and the generation of ·OH. However, when the bubble is a microbubble, the bubble rising speed is very small. At this time, if the gas-liquid countercurrent flow is adopted, although it will also strengthen the dissolution of ozone and promote the effective decomposition of the dissolved ozone in the upper part of the catalyst area and the generation of ·OH; but at this time, the dissolution of gaseous ozone is no longer the main contradiction, and the microbubble itself already has the condition for rapid ozone dissolution, and ozone is more soluble than oxygen, and its solubility is 13 times that of oxygen. Research shows that the dissolution rate of ozone is very fast. Under the condition of strongly turbulent microbubbles, most of the ozone can be dissolved even in 1 second. At this time, a new contradiction arises: the ozone rapidly dissolved below the catalyst will be carried downward by the water flow and will not pass through the catalyst area, resulting in waste of ozone. When this contradiction is serious to a certain extent, it can be solved by changing the flow pattern, that is, changing to gas-liquid co-current flow. However, usually, by changing the amount of the catalyst placed above and below the air distribution device, it is a more flexible and optimized solution. Summary of the Utility Model

[0004] In view of this, the purpose of the present utility model is to provide a tower-type catalytic ozonation reactor to solve the deficiencies in the prior art.

[0005] In order to achieve the above purpose, the present utility model is realized through the following technical solutions:

[0006] Provided is a tower-type catalytic ozonation reactor, which comprises a reactor body. The reactor body includes a plurality of catalytic units connected in sequence from bottom to top, the number of the catalytic units can be increased or decreased, each catalytic unit includes a catalyst monolithic packing and a sieve plate, the sieve plate is arranged at the bottom of the catalyst monolithic packing, a gas distribution device is arranged in some of the catalytic units, an air inlet and a first water inlet are arranged at the bottom of the reactor body, an air outlet and a second water inlet are arranged at the top of the reactor body. When the first water inlet is a water inlet, the second water inlet is a water outlet; when the first water inlet is a water outlet, the second water inlet is a water inlet.

[0007] For the tower-type catalytic ozonation reactor as described above, the gas distribution device is a microporous gas distribution device, the microporous gas distribution device is arranged at the bottom of the catalyst area composed of all the catalyst monolithic packings, and the first water inlet is a water inlet.

[0008] For the tower-type catalytic ozonation reactor as described above, the microporous gas distribution device is a fine titanium disc or a fine titanium rod.

[0009] For the tower-type catalytic ozonation reactor as described above, the gas distribution device is a small-hole gas distribution device or a medium-hole gas distribution device, the catalyst monolithic packing is arranged at the top and bottom of the small-hole gas distribution device or the medium-hole gas distribution device, and the first water inlet is a water outlet.

[0010] For the tower-type catalytic ozonation reactor as described above, the small-hole gas distribution device is a conventional titanium disc or a conventional titanium rod, and the medium-hole gas distribution device is a sand core disc or a sand core rod.

[0011] For the tower-type catalytic ozonation reactor as described above, the reactor body includes six sections of the catalytic units, and the small-hole gas distribution device or the medium-hole gas distribution device is arranged under the catalyst monolithic packing in the second or third section from bottom to top.

[0012] For the tower-type catalytic ozonation reactor as described above, both the first water inlet and the second water inlet are cross-shaped.

[0013] The beneficial effects of the technical solution of the present utility model are as follows:

[0014] 1. Solve the problem of delaying the rise of bubbles, promoting the dissolution of ozone, and at the same time ensuring that the initially rapidly dissolved ozone also has sufficient residence time in the catalyst area to ensure the effective decomposition of ozone and the yield of ·OH; 2. Only need to change the positions of the water inlet, water outlet and air inlet, and the treatment efficiency of the reactor can be greatly improved, the operation is simple, and the effect is obvious; 3. Only need to add one or two sets of ozone gas distribution devices to realize the optimization of working conditions, the investment cost increases very little, and the operating cost can be greatly reduced; 4. When the water quality and water volume of the influent change, the position of the air inlet can be adjusted through water quality analysis, the operation is convenient, and the working condition flexibility is large. Description of the Drawings

[0015] To further illustrate the above objects, structural features, and effects of the present utility model, the present utility model will be described in detail below with reference to the accompanying drawings.

[0016] Figure 1 Schematic diagram of the overall structure of a preferred embodiment of the present utility model;

[0017] Figure 2 Schematic diagram of the sieve plate structure of a preferred embodiment of the present utility model;

[0018] Figure 3 Schematic diagram of the gas distribution device structure of a preferred embodiment of the present utility model;

[0019] Figure 4 Schematic diagram of the structure of the first water inlet (second water inlet) of a preferred embodiment of the present utility model;

[0020] In the figure: 1, catalytic unit; 2, catalyst monolithic packing; 3, sieve plate; 4, gas distribution device; 41, microporous gas distribution device; 42, small-hole gas distribution device; 43, medium-hole gas distribution device; 5, first water inlet; 6, air outlet; 7, second water inlet. Detailed implementation manners

[0021] The term "utility model" used in this specification, as well as "the present utility model", are intended in a broad sense to refer to all the subject matters of this specification and any subsequent patent claims. Statements containing these terms should not be construed as limiting the subject matter described herein or the meaning or scope of any subsequent patent claims. In addition, this specification does not attempt to describe or limit the subject matter covered by any specific component, paragraph, statement, or claim of this application. The subject matter should be understood with reference to the entire specification, all the drawings, and any subsequent claims. The present utility model may have other embodiments and may be practiced or implemented in other ways. Moreover, it should be understood that the wording and terms used herein are for illustrative purposes and should not be considered limiting.

[0022] Details of the present utility model will now be discussed with reference to the drawings of the present utility model, which are provided by way of example only. In the drawings, like features or components may be labeled with the same reference numerals.

[0023] The use of the terms "comprising", "having", and "including" and their variants herein means including the items listed hereinafter, their equivalents, and additional items. Although directions such as above, below, upward, downward, backward, bottom, top, front, and rear may be referred to in the description of the drawings for convenience, reference is made to the drawings. These directions are not intended to be literally accepted or limit the present utility model in any way. In addition, terms such as "first", "second", "third", etc. are used herein for illustrative purposes and are not intended to indicate or imply importance or significance.

[0024] See Figure 1 As shown, the tower-type catalytic ozonation reactor of the present utility model includes a reactor body, which from bottom to top includes a number of catalytic units 1 connected in sequence, and the number of catalytic units 1 can be increased or decreased. The catalytic unit 1 includes a catalyst monolithic packing 2 and a sieve plate 3, the sieve plate 3 is arranged at the bottom of the catalyst monolithic packing 2, and the structure of the sieve plate 3 is shown in Figure 2 As shown. In some of the catalytic units 1, there is an air distribution device 4, and the structure of the air distribution device 4 is shown in Figure 3 As shown. At the bottom of the reactor body, there are an air inlet and a first water inlet 5, and at the top of the reactor body, there are an air outlet 6 and a second water inlet 7. When the first water inlet 5 is the water inlet, the second water inlet 7 is the water outlet, and when the first water inlet 5 is the water outlet, the second water inlet 7 is the water inlet, that is, the inlet and outlet water ports in this case can be replaced to form a co-current or counter-current of gas and liquid.

[0025] Since in actual operation, the concentration of influent organic matter fluctuates to a certain extent, and the water volume to be treated and the gas supply volume of the ozone generator can both be adjusted within a certain range, the flow pattern of the reactor should have multiple choices to optimize the reaction conditions and ensure the production rate of ·OH.

[0026] In a preferred embodiment, still referring to the figure, the air distribution device 4 is a microporous air distribution device 41, and the microporous air distribution device 41 is arranged at the bottom of the catalyst area composed of all the catalyst monolithic packings 2. At this time, the first water inlet 5 is the water inlet. Only when using the microporous air distribution device 41 and the ozone dissolution rate can reach more than 99%, can the co-current of gas and liquid be adopted.

[0027] In another preferred embodiment, the air distribution device 4 is a small-hole air distribution device 42 or a medium-hole air distribution device 43, and the catalyst monolithic packing 2 is arranged at the top and bottom of the small-hole air distribution device 42 or the medium-hole air distribution device 43. At this time, the first water inlet 5 is the water outlet. For the medium- and small-hole air distribution devices, the formed bubbles are larger, and improving the ozone dissolution conditions is an important task of the working conditions. At this time, the counter-current of gas and liquid can be adopted; and catalyst packings are installed above and below the air distribution device to ensure that after the ozone gas forms bubbles through the air distribution device, the ozone dissolved at different time periods has sufficient residence time in the catalyst area to catalyze the decomposition of ozone to form ·OH.

[0028] The catalyst monolithic packing 2 of this tower-type catalytic ozonation reactor is arranged in multiple sections along the elevation to solve the problems of promoting ozone dissolution and ensuring the residence time of dissolved ozone in the catalyst area. The height of the air distribution device in the catalyst area can be optimized through debugging. The reactor body is generally set in six sections, labeled as 1# to 6# packing from bottom to top. The air distribution device 4 can be arranged under the 2# or 3# packing to ensure that 1 / 6 to 1 / 3 (<1 / 2) of the height of the packing is below the air distribution device 4. In this way, the ozone dissolved within the first 1 / 6 gas path time (generally about 1 / 3 of the total ozone amount) can pass through 1 / 3 of the catalyst area when the air distribution device 4 is under the 2# packing; when the air distribution device 4 is under the 3# packing, it can pass through 1 / 2 of the catalyst area to ensure that the initially dissolved ozone is effectively decomposed by the catalyst.

[0029] According to the common specifications of current ozone air distribution devices, three types of air distribution devices 4 with different pore sizes are used in this case, which are divided into: fine titanium disks (rods) with a pore size of 5 μm, called "micro-pore air distribution device 41"; conventional titanium disks (rods) with a pore size of 20 μm, called "small-pore air distribution device 42"; and sand core disks (rods) with a pore size of 500 μm, called "medium-pore air distribution device 43" (the naming of pore sizes is not unified in different industrial fields).

[0030] See Figure 4 As shown, both the first water inlet 5 and the second water inlet 7 are cross-shaped.

[0031] The following further describes the examples of this tower-type catalytic ozonation reactor in conjunction with the attached drawings:

[0032] Example 1: The COD concentration of a certain printing and dyeing wastewater is only 60 mg / L, and it is required to reach 40 mg / L after ozonation treatment. Since the amount of COD to be removed is small and the amount of ozone gas required is small, it is decided to adopt co-current flow of gas and liquid - water inlet and air inlet at the bottom of the tower, and use the micro-pore air distribution device 41 for air distribution. The comparison of operating conditions shows that the COD removal rate of co-current flow can reach 50%, while that of counter-current flow can only reach 42%.

[0033] Example 2: The COD concentration of a certain coal chemical wastewater is relatively high, reaching 180 mg / L, and it is required to reach 100 mg / L after ozonation treatment. Considering that this wastewater is relatively easy to oxidize and a large amount of ozone gas is required, the medium-pore air distribution device 43 is adopted, and the gas-liquid counter-current flow. The comparison of operating conditions shows that the COD removal rate in this condition can reach more than 50%. If the bottommost layer of packing is missing, the COD removal rate can only reach 45%.

[0034] Example 3: The COD concentration of a certain chemical industrial wastewater is 150 mg / L, and it is required to reach below 80 mg / L after ozonation treatment. Considering that the required treatment degree of this wastewater is relatively high and a large amount of ozone gas is needed, a small-hole gas distribution device 42 is adopted, and the gas-liquid flows in reverse. The comparison of operating conditions shows that: the COD removal rate in this condition can stably reach 50%; if the lower two layers of packing below the gas distribution device 4 are missing, the COD removal rate can only reach 40%.

[0035] The above are only the preferred embodiments of the present invention, and do not limit the implementation manners and protection scope of the present invention accordingly. For those skilled in the art, it should be able to realize that all the equivalent replacements and obvious changes made by using the description and illustration content of the present invention should be included in the protection scope of the present invention.

Claims

1. A tower-type catalytic ozonation reactor, characterized in that, It includes a reactor body, which from bottom to top includes a number of catalytic units connected in sequence. The number of the catalytic units can be increased or decreased. The catalytic unit includes a catalyst monolithic packing and a sieve plate. The sieve plate is arranged at the bottom of the catalyst monolithic packing. A gas distribution device is provided in some of the catalytic units. An air inlet and a first water inlet are provided at the bottom of the reactor body. An air outlet and a second water inlet are provided at the top of the reactor body. When the first water inlet is the water inlet, the second water inlet is the water outlet. When the first water inlet is the water outlet, the second water inlet is the water inlet.

2. The tower-type catalytic ozonation reactor according to claim 1, wherein The gas distribution device is a microporous gas distribution device. The microporous gas distribution device is arranged at the bottom of the catalyst area composed of all the catalyst monolithic packings. The first water inlet is the water inlet.

3. The tower-type catalytic ozonation reactor according to claim 2, characterized in that, The microporous gas distribution device is a fine titanium disc or a fine titanium rod.

4. The tower-type catalytic ozonation reactor according to claim 1, characterized in that, The gas distribution device is a small-hole gas distribution device or a medium-hole gas distribution device. The catalyst monolithic packing is arranged at the top and bottom of the small-hole gas distribution device or the medium-hole gas distribution device. The first water inlet is the water outlet.

5. The tower-type catalytic ozonation reactor according to claim 4, characterized in that, The reactor body includes six sections of the catalytic units. The small-hole gas distribution device or the medium-hole gas distribution device is arranged under the second or third section of the catalyst monolithic packing from bottom to top.

6. The tower-type catalytic ozonation reactor according to claim 1, characterized in that, Both the first water inlet and the second water inlet are cross-shaped.

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