CN116495875A - Biological sludge treatment system and method - Google Patents

Biological sludge treatment system and method Download PDF

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Publication number
CN116495875A
CN116495875A CN202310524098.XA CN202310524098A CN116495875A CN 116495875 A CN116495875 A CN 116495875A CN 202310524098 A CN202310524098 A CN 202310524098A CN 116495875 A CN116495875 A CN 116495875A
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China
Prior art keywords
ozone
biological sludge
reactor
gas
ozone oxidation
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Pending
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CN202310524098.XA
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Chinese (zh)
Inventor
明磊强
华志良
潘康红
张大海
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority to CN202310524098.XA priority Critical patent/CN116495875A/en
Publication of CN116495875A publication Critical patent/CN116495875A/en
Pending legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1205—Particular type of activated sludge processes
    • C02F3/1221—Particular type of activated sludge processes comprising treatment of the recirculated sludge
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/80—Mixing plants; Combinations of mixers
    • B01F33/834—Mixing in several steps, e.g. successive steps
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/06—Treatment of sludge; Devices therefor by oxidation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F2101/00—Mixing characterised by the nature of the mixed materials or by the application field
    • B01F2101/305—Treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
    • C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/04—Flow arrangements
    • C02F2301/046—Recirculation with an external loop
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/06—Sludge reduction, e.g. by lysis

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  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Microbiology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treatment Of Sludge (AREA)

Abstract

The application discloses a biological sludge treatment system and a method thereof. The gas rich in ozone in the gas-liquid mixer is primarily mixed with the biological sludge, and the proper residence time of the gas-liquid mixer and the biological sludge in the pipeline reactor is controlled. Not only improves the utilization rate of ozone, but also ensures that the reaction efficiency of ozone and biological sludge reaches the degree expected by people.

Description

Biological sludge treatment system and method
Technical Field
The application belongs to the technical field of sludge treatment, and relates to a biological sludge treatment system and a biological sludge treatment method. And more particularly to the use of ozone to reduce biosolids emissions after activated sludge treatment.
Background
The activated sludge process is a widely used biological wastewater treatment technology with activated sludge as the main body. This technique mixes and agitates the wastewater with microorganisms (activated sludge) and aerates them to decompose the organic substances in the wastewater. Biosolids (biosludge) are then separated from the treated wastewater. Finally, organic matters in the wastewater are degraded and removed, and the activated sludge is multiplied. However, the method brings more and more attention to the treatment problem of biological sludge (Bio-slurry).
The main components of the biological sludge comprise water, microorganisms, microorganism metabolites, organic matters, inorganic solids and the like. Landfill alone can render the land unusable. Incineration also has problems of excessive cost and environmental pollution. In addition, the use of ozone for treating biological sludge has been reported. Ozone has a strong oxidizing effect on the cell wall to lyse, and the integrity of the cell wall is destroyed. Lysis results in release of enriched intracellular organics. In this way, the problem of excessive biosolids emission can be solved, and the enriched organic material can be used for other target processes, such as anaerobic fermentation to produce biogas.
Conventional micro-porous aeration techniques may be used to diffuse ozone into the biological sludge to be treated. However, micropores with smaller size are easy to be blocked, micropores with larger size are easy to cause insufficient aeration pressure, the specific surface area is small, the bubble stabilizing time is shorter, and the diffusion effect is not ideal. In addition, the biological sludge closer to the micropores is fully contacted with ozone and even excessively oxidized due to the high oxidation reaction speed, and the biological sludge farther from the center of the micropores is less reacted, so that the reaction is incomplete.
Ozone oxidation systems commonly used today convert about 4-15% of the oxygen in a feed gas to ozone, wherein the feed gas comprises ambient air, oxygen enriched air, pure oxygen, or the like. Accordingly, the selection of ozone systems and techniques for use in biological sludge treatment plants also requires consideration of the overall investment and operating costs based on the ozone treatment system, and balances the benefits achieved by ozone treatment and consideration of regulatory directives on effluent emissions. It is particularly important to select an ozone technology that provides the best economic value. The method not only improves the utilization rate of ozone, but also ensures the reaction efficiency of ozone and biological sludge to reach the hope degree.
Disclosure of Invention
In order to overcome the technical problems, the application provides a biological sludge treatment system and a biological sludge treatment method.
To achieve the above object, the present application discloses a biological sludge treatment system comprising:
an ozone-enriched gas supply;
at least one gas-liquid mixer connected to the ozone-enriched gas supply source, the pipeline reactor and the ozone oxidation reactor, respectively, for promoting the preliminary mixing of the ozone-enriched gas and the biological sludge;
the pipeline reactor is used for controlling the residence time of the gas rich in ozone and the biological sludge; and
the ozone oxidation reactor is used for receiving the biological sludge and is respectively in fluid connection with the gas-liquid mixer and the pipeline reactor.
Further, the gas-liquid mixer further comprises a venturi device.
Further, the treatment system also comprises a circulation pipeline for reintroducing products after the ozone oxidation reaction occurring in the pipeline reactor into the ozone oxidation reactor.
Further, the ozone-enriched gas supply further comprises an ozone generator connected to an oxygen source.
Further, the ozone-enriched gas is ozone-enriched oxygen.
Further, the treatment system also includes a peristaltic pump that regulates the flow of the biological sludge output from the ozone oxidation reactor. To optimize the lysis of biosolids within the ozone oxidation reactor.
Further, the ozone oxidation reactor comprises a biological sludge inlet, a biological sludge outlet and a tail gas outlet.
Further, the VSS value of the biological sludge is in the range of 14-40 g/L.
The second aspect of the present invention provides a method for treating biological sludge, comprising the steps of:
(1) Introducing biological sludge into an ozone oxidation reactor;
(2) Operating an ozone generator to produce ozone-enriched gas;
(3) Delivering the biological sludge from the ozone oxidation reactor to a gas-liquid mixer so that ozone-enriched gas is primarily mixed with the biological sludge;
(4) The mixture after preliminary mixing enters a pipeline reactor, and the residence time of the gas rich in ozone and the biological sludge in the pipeline reactor is more than or equal to 2 seconds, preferably more than or equal to 3.6 seconds, more preferably more than or equal to 10 seconds, so as to carry out ozone oxidation reaction;
(5) Optionally, the product after the ozone oxidation reaction occurring in the pipeline reactor is again introduced into the ozone oxidation reactor, and steps (2) to (4) are repeated.
Further, the utilization rate of ozone by the treatment method is more than 92%.
Further, the volume of the biological sludge introduced into the ozone oxidation reactor is 20% to 60%, preferably 30% to 50% of the volume of the ozone oxidation reactor.
Further, the volume of the pipeline reactor is about 0.2 to 0.8%, preferably 0.3 to 0.6% of the volume of the ozone oxidation reactor.
Compared with the prior art, the technical scheme provided by the application has the following advantages:
1. aiming at the biological sludge with a certain range of VSS value, the treatment system and the treatment method can effectively improve the reaction efficiency of ozone and the biological sludge.
2. The gas-liquid mixer adopts the Venturi device to carry out preliminary gas-liquid mixing, the contact time of ozone and biological sludge is prolonged by the subsequent pipeline reactor, and the utilization rate of ozone is improved.
3. The sludge in the product after the ozone oxidation reaction can enter the ozone oxidation reactor again, and the cycle is repeated, so that the ozone can react with the cell walls in the biological sludge more fully, and better raw materials are provided for the subsequent target process.
Drawings
The advantages and spirit of the present application may be further understood by reference to the following detailed description of the invention and the accompanying drawings.
FIG. 1 shows a schematic diagram of a biological sludge treatment system provided herein;
FIG. 2 shows a schematic diagram of an ozone oxidation reactor provided herein;
FIG. 3 shows a schematic diagram of a microporous aeration ozone oxidation unit in a comparative example;
FIG. 4 shows a graph comparing SCOD release during sludge ozonation.
FIG. 5 shows a comparison of lysis efficiency during the ozone oxidation of sludge.
Figure 6 shows a graph of ozone utilization versus sludge ozone oxidation.
Detailed Description
Specific embodiments of the present application are described in detail below with reference to the accompanying drawings. However, the present application should be understood not to be limited to such an embodiment described below, and the technical idea of the present application may be implemented in combination with other known technologies or other technologies having functions identical to those of the known technologies.
In the following description of the specific embodiments, for the sake of clarity in explaining the structure and operation of the present application, description will be given by way of directional terms, but words of front, rear, left, right, outer, inner, outer, inner, axial, radial, etc. are words of convenience and are not to be construed as limiting terms.
In the following description of the specific embodiments, it should be understood that the terms "length," "width," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, merely to facilitate description of the present application and simplify the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operate in a specific orientation, and are therefore not to be construed as limiting the present application.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not intended to be limiting with respect to time sequence, number, or importance, but are not to be construed as indicating or implying a relative importance or implicitly indicating the number of features indicated, but merely for distinguishing one feature from another in the present disclosure. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present application, the meaning of "a plurality" is two or more, unless explicitly specified otherwise. Likewise, the appearances of the phrase "a" or "an" in this document are not meant to be limiting, but rather describing features that have not been apparent from the foregoing. Likewise, unless a particular quantity of a noun is to be construed as encompassing both the singular and the plural, both the singular and the plural may be included in this disclosure. Likewise, modifiers similar to "about" and "approximately" appearing before a number in this document generally include the number, and their specific meaning should be understood in conjunction with the context.
It should be understood that in this application, "at least one" means one or more, and "a plurality" means two or more. "and/or" is used to describe association relationships of associated objects, meaning that there may be three relationships, e.g., "a and/or B" may mean: only a, only B and both a and B are present, wherein a, B may be singular or plural. The character "/" generally indicates that the context-dependent object is an "or" relationship. "at least one of" or the like means any combination of these items, including any combination of single item(s) or plural items(s). For example, at least one (one) of a, b or c may represent: a, b, c, "a and b", "a and c", "b and c", or "a and b and c", wherein a, b, c may be single or plural.
The terms "unit", "article", "module" and "module" described in the present specification mean a unit for processing at least one function and operation, and may be implemented by hardware components or software components and combinations thereof.
"upstream" and "downstream" as described in this specification are defined with respect to the intended flow of fluid, the upstream end corresponding to the end closest to the inlet for introducing fluid into the device and the downstream end corresponding to the outlet from which fluid exits the device.
Each aspect or embodiment defined herein may be combined with any other aspect or embodiment unless clearly indicated to the contrary. In particular, any feature indicated as being preferred or advantageous may be combined with any other feature or features indicated as being preferred or advantageous.
A venturi mixer is an efficient mass transfer device. For wastewater treatment purposes, the transfer of ozone from the gas phase to the liquid phase is very important. The lateral inlet of the venturi can generate negative pressure to suck negative pressure, so that the negative pressure is fully mixed with liquid, and preliminary mixing of ozone and biological sludge is promoted. Venturi devices known to those skilled in the art may be used in the present application, and are not particularly limited.
Because ozone is extremely irritating and toxic above a certain concentration, ozone destruction systems or units are typically used to destroy any residual ozone in the exhaust gas in order to protect the personnel from exposure to ozone.
Herein, ozone-enriched gas may be produced from oxygen in air or high purity gaseous oxygen (> 99%). The dried oxygen or air stream is subjected to a high voltage/high density current to produce ozone.
Herein, the pipeline reactor provides a sufficient reaction space for the biological sludge and ozone. The internal structure of the pipeline reactor can be designed to enable the fluid to generate spiral flow so as to promote the full contact of the biological sludge and the ozone. Meanwhile, the inner surface of the pipeline reactor can be coated with a catalyst, so that the oxidation efficiency of ozone is improved.
Specific embodiments of the present application are described in detail below with reference to the accompanying drawings.
The inventors have found that the initial VSS (volatile suspended matter) of biological sludge affects the lysis effect of the sludge during ozone oxidation. When the initial VSS is lower, the microorganism content in the biological sludge is lower, the mineralization of ozone on organic matters is obvious, the lysis efficiency is lower, and the unnecessary loss of ozone is also caused. With the increase of VSS, the microorganism content in the biological sludge is increased, and the wall breaking and the lysis effects of ozone are dominant gradually.
The inventors classified biological sludge into low-concentration sludge (LS) and high-concentration sludge (HS) according to the level of VSS. Wherein the VSS value of the low-concentration sludge ranges from 0g/L to 13g/L, and the VSS value of the high-concentration sludge ranges from 14 g/L to 40g/L. Illustratively, the sludge treatment process herein is particularly suited for biological sludge having a VSS value in the range of 14 to 40g/L.
Larger solids are present in biological sludge. In order to meet the requirements of ozone oxidation equipment, prevent pipeline blockage, improve the contact effect of ozone and biological sludge, and remove solid particles with the diameter of more than 1cm in the biological sludge through a grid before reaction.
Fig. 1 shows a biological sludge treatment system as used in the present application. It includes oxygen source 101, first mass flowmeter 102, ozone generator 103, first ozone analyzer 104, second mass flowmeter 105, gas-liquid mixer 106, peristaltic pump 107, ozone oxidation reactor 108, second ozone analyzer 109, ozone destructor 110, pipeline reactor 111.
The concentration of ozone generated by the ozone generator 103 ranges from 0 to 170mg/L. The first ozone analyzer 104 is used to analyze the concentration of ozone delivered by the ozone generator 103. The first mass flow meter 102 controls the flow rate of ozone gas. The gas-liquid ratio in the gas-liquid mixer 106 was 3:25. Peristaltic pump 107 controls the flow of biological sludge.
A schematic of the structure of the ozone oxidation reactor 108 is shown in fig. 2. In this example, a batch reactor was used, which contained a stirrer (e) inside. The stirring rate of the stirrer (e) ranges from 0 to 400r/min. The volume of the biological sludge which is put into the ozone oxidation reactor once is 25 to 50 percent of the volume of the biological sludge. During the reaction, the stirrer (e) was continuously stirring and kept at a pressure of not more than 0.9MPa in the ozone oxidation reactor 108. The concentration of ozone generated by the ozone generator 103 is controlled to be 150-170 mg/L by adjusting the current of the ozone generator.
The top end of the batch reactor is provided with a tail gas outlet (b) and a pressure relief valve (a). The pressure relief valve (a) automatically relieves pressure when the internal pressure of the ozone oxidation reactor 108 is higher than 0.9MPa. The exhaust gas outlet (b) connects the second ozone analyzer 109 and the ozone destructor 110. The tail gas containing ozone is analyzed for ozone concentration in the tail gas by the second ozone analyzer 109 and then enters the ozone destructor 110 for treatment. The bottom end of the ozone oxidation reactor 108 is provided with a biological sludge inlet (c) and a biological sludge outlet (d). The pressure in the ozone oxidation reactor 108 is 0.6 to 0.9MPa. In the ozone oxidation reactor 108, a biological sludge feed valve (2) is located between the biological sludge outlet (d) and the tail gas outlet (b). The discharging valve (1) of the biological sludge is positioned at the upper end of the biological sludge inlet (c) and is respectively used for feeding before the ozone oxidation reaction and discharging after the ozone oxidation reaction.
The volume of the pipe reactor 111 was about 0.5% of the volume of the ozone oxidation reactor. The pipeline reactor can prolong the contact time of ozone and biological sludge and improve the utilization rate of ozone.
The biological sludge to be treated is fed into the ozone oxidation reactor 108 through the biological sludge inlet (c), and is fed from the biological sludge outlet (d) to the gas-liquid mixer 106 through the peristaltic pump 107 at a certain speed. While the gas-liquid mixer 106 draws in ozone. In the gas-liquid mixer, ozone and biological sludge are preliminarily mixed to form a mixture of ozone and biological sludge, and then enter the pipeline reactor 111. The mixture of ozone and biological sludge is left in the pipeline reactor for more than 2 seconds, preferably more than 3.6 seconds, more preferably more than 10 seconds, more preferably more than 20 seconds, and the ozone oxidation reaction is performed. Wherein the flow rate of ozone delivered to the gas-liquid mixer is controlled by the second mass flow meter 105 to meet the gas-liquid ratio requirement.
The gas-liquid mixer 106 may use a venturi mixer to promote efficient mixing of ozone with biological sludge.
Ozone utilization ratio was calculated according to the following manner, ozone utilization ratio= (reading of first ozone analyzer 104-reading of second ozone analyzer 109)/reading of first ozone analyzer 104. The ozone utilization rate is desirably 92% or more.
In order to improve the ozone utilization rate, the sludge in the product after the ozone oxidation reaction can enter the ozone oxidation reactor 108 again, and the cycle is repeated. At the same time, this allows the ozone to react more fully with the cell walls in the biological sludge without reacting excessively with the cytoplasm. Since the cytoplasmic component is mainly an organic substance, it is not suitable as a raw material for the subsequent target process if it is excessively oxidized to carbon dioxide or carbon.
The method of the invention enables the fluid containing biological sludge and the gas rich in ozone to be in effective gas-liquid contact, and the fluid is circularly and reciprocally passed through the multiple reactions in the tubular reactor, so that the cell walls in the biological sludge are dissolved, thereby realizing sludge reduction and higher ozone utilization rate.
The inventor selects the following two biological sludge from different sewage treatment plants as sources.
Low concentration sludge (LS): wherein the volatile suspended matter (VSS) was 7.00g/L, the Soluble Chemical Oxygen Demand (SCOD) was 208mg/L, and the Total Suspended Solids (TSS) was 12.65g/L.
High concentration sludge (HS): wherein the volatile suspended matter (VSS) was 21.30g/L, the Soluble Chemical Oxygen Demand (SCOD) was 427mg/L, and the Total Suspended Solids (TSS) was 35.65g/L.
The ozone adding amount is 320-6400 mg/L, calculated by the total volume of the biological sludge. The specific ozone addition amount can be determined according to the nature of the biological sludge and the desired oxidation effect.
Examples
The biological sludge treatment system in the application is used for respectively treating the two types of biological sludge to obtain SCOD, lysis efficiency and ozone utilization rate so as to explore ideal sludge concentration and pipeline reactor residence time.
In this example, the concentration of the ozone generator was set at 160mg/L. The ozone adding amount is 540mg/L, calculated by the total volume of the biological sludge. The volume of the ozone oxidation reactor was 15L. The volume of the biological sludge fed into the ozone oxidation reactor at a time is 5L. The volume of the pipe reactor was 75mL. The stirring rate of the stirrer in the ozone oxidation reactor was 200r/min. The pressure in the ozone oxidation reactor was 0.9MPa, and the reaction was carried out at room temperature.
The flow rate of the low-concentration sludge is 1250mL/min respectively. The flow rate of the high-concentration sludge is 1667mL/min. The residence time of the biological sludge in the pipeline reactor was set to 3.6S (VO-L condition) and 2.7S (VO-S condition), respectively.
Comparative example
A microporous aeration ozone oxidation device (called as 'FBO') is formed by adopting microporous aeration equipment to replace the gas-liquid mixer. The two biological sludge are respectively treated by the microporous aeration ozone oxidation device. The microporous aeration device can form smaller bubbles during aeration, thereby improving the dissolution speed of ozone in water.
The microporous aeration ozone oxidation apparatus is shown in fig. 3, and comprises an oxygen source 101, a first mass flow meter 102, an ozone generator 103, a first ozone analyzer 104, an ozone oxidation reactor 108 and an ozone destructor 110. Ozone generator 103 uses industrial oxygen (> 99%) as a source of gas. The concentration of ozone generated by the ozone generator 103 was set to 160mg/L.
The ozone flow rate was set to 0.3L/min. The ozone adding amount is 540mg/L, calculated by the total volume of the biological sludge. The volume of sludge in the ozone oxidation reactor is 50% of the effective volume of the ozone oxidation reactor. Ozone enters an ozone oxidation reactor through a micropore aeration device to react with biological sludge. The pressure in the ozone oxidation reactor was atmospheric pressure, and the reaction was carried out at room temperature. The stirring rate of the stirrer in the ozone oxidation reactor was 200r/min.
The results of SCOD release in the above examples and comparative examples are shown in FIG. 4. SCOD release of low-concentration sludge (LS) is lower than that of high-concentration sludge (HS) under the same ozone adding amount.
The SCOD release of the sludge with low concentration under the condition of VO-S is the greatest, 19.4% is improved compared with the SCOD under the condition of VO-L, and 36.2% is improved compared with the SCOD of the microporous aeration ozone oxidation device.
The SCOD release of the high-concentration sludge under the condition of VO-L is the greatest, which is increased by 6.5% compared with the VO-S condition and 166.0% compared with the microporous aeration ozone oxidation device.
As shown in fig. 5, the low concentration sludge had a lower lysis efficiency (SCOD release/VSS reduction) than the high concentration sludge under all conditions at the same ozone addition amount. The low-concentration sludge has highest lysis efficiency under the condition of VO-S, improves the lysis efficiency by 7.7 percent relative to the condition of VO-L, and increases by 20.7 percent relative to a microporous aeration ozone oxidation device. The high-concentration sludge has highest lysis efficiency under the condition of VO-L, which is improved by 25.1 percent compared with the lysis efficiency under the condition of VO-S and 130.0 percent compared with a microporous aeration ozone oxidation device.
Considering the economic cost of ozone, the utilization rate of ozone is an important reference index. As shown in fig. 6, the ozone utilization rate of the low-concentration sludge is lower than that of the high-concentration sludge under all conditions with the same ozone addition amount. Compared with a microporous aeration ozone oxidation device, the ozone utilization rate of the high-concentration sludge is increased from 83.8% to 93.3% under the condition of VO-L.
The results prove that under the same ozone adding amount, the ozone oxidation device used in the application is used for oxidizing high-concentration sludge and can obtain more ideal SCOD increment, lysis efficiency and ozone utilization rate improvement under the condition that a pipeline reactor stays for a certain time.
The preferred embodiments of the present application are described in this specification, which are intended to be illustrative of the technical aspects of the present application and not limiting. All technical solutions that can be obtained by logic analysis, reasoning or limited experiments according to the conception of the present application by a person skilled in the art are within the scope of the present application.

Claims (10)

1. A biological sludge treatment system comprising:
an ozone-enriched gas supply;
at least one gas-liquid mixer connected to the ozone-enriched gas supply source, the pipeline reactor and the ozone oxidation reactor, respectively, for promoting the preliminary mixing of the ozone-enriched gas and the biological sludge;
the pipeline reactor is used for controlling the residence time of the gas rich in ozone and the biological sludge; and
the ozone oxidation reactor is used for receiving the biological sludge and is respectively in fluid connection with the gas-liquid mixer and the pipeline reactor.
2. The treatment system of claim 1, wherein the gas-liquid mixer further comprises a venturi device.
3. The treatment system of claim 1, further comprising a recirculation line for reintroducing products of the ozone oxidation reaction occurring in the conduit reactor into the ozone oxidation reactor.
4. The treatment system of claim 1, wherein the ozone-enriched gas supply further comprises an ozone generator connected to an oxygen source.
5. The treatment system of claim 1, wherein the ozone-enriched gas is ozone-enriched oxygen.
6. The treatment system of claim 1, wherein the ozone oxidation reactor comprises a biological sludge inlet, a biological sludge outlet, and a tail gas outlet.
7. The treatment system of claim 1, wherein the biological sludge has a VSS value in the range of 14 to 40g/L.
8. A method for treating biological sludge, comprising the steps of:
(1) Introducing biological sludge into an ozone oxidation reactor;
(2) Operating an ozone generator to produce ozone-enriched gas;
(3) Delivering the biological sludge from the ozone oxidation reactor to a gas-liquid mixer so that ozone-enriched gas is primarily mixed with the biological sludge;
(4) The mixture after preliminary mixing enters a pipeline reactor, and the residence time of the gas rich in ozone and the biological sludge in the pipeline reactor is more than or equal to 2 seconds, preferably more than or equal to 3.6 seconds, more preferably more than or equal to 10 seconds, so as to carry out ozone oxidation reaction;
(5) Optionally, the product after the ozone oxidation reaction occurring in the pipeline reactor is again introduced into the ozone oxidation reactor, and steps (2) to (4) are repeated.
9. A treatment method according to claim 8, characterized in that the volume of the biological sludge introduced into the ozone oxidation reactor is 20-60%, preferably 30-50% of the volume of the ozone oxidation reactor.
10. A process according to claim 8, wherein the volume of the pipeline reactor is about 0.2 to 0.8%, preferably 0.3 to 0.6%, of the ozone oxidation reactor volume.
CN202310524098.XA 2023-05-09 2023-05-09 Biological sludge treatment system and method Pending CN116495875A (en)

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