CN214611894U - Reaction system for treating high-concentration organic waste liquid - Google Patents
Reaction system for treating high-concentration organic waste liquid Download PDFInfo
- Publication number
- CN214611894U CN214611894U CN202023325178.3U CN202023325178U CN214611894U CN 214611894 U CN214611894 U CN 214611894U CN 202023325178 U CN202023325178 U CN 202023325178U CN 214611894 U CN214611894 U CN 214611894U
- Authority
- CN
- China
- Prior art keywords
- waste liquid
- reactor
- gas
- reaction system
- internal circulation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The utility model discloses a reaction system for treating high-concentration organic waste liquid, which belongs to the sewage treatment technology and comprises a pretreatment unit (14), a waste liquid water pump (15), a reactor (16), a heat exchanger (17), a gas-liquid separator (18) and a liquid storage tank (19) which are connected in sequence through pipelines; the gas inlet (3) of the reactor (16) is connected with the gas supply unit (20) through a pipeline, and the top of the gas-liquid separator (18) is connected with the gas purification device (23) through a pipeline. Can effectively degrade high-concentration organic waste liquid under the condition of high salt content, so that the treated waste liquid directly meets the national emission standard or meets the water inlet requirement of the subsequent common biochemical process.
Description
Technical Field
The utility model relates to an ecological environment protection sewage treatment field, especially high concentration difficult biodegradable organic waste water's reaction system.
Background
In industrial production, a large amount of waste liquid is generated, and particularly, in the production of emulsified oil, cutting fluid, electroplating solution, alkali washing, acid washing, phosphating and the like in the industries of oil refining, petrifaction, pharmacy, fine chemical manufacturing, metal processing and the like. These waste streams contain far greater concentrations of contaminants than the waste streams, some up to hundreds of thousands and high concentrations of salts. The waste liquid has: (1) the organic matter content is high, and the heat value is high; (2) the toxicity is high, and the environmental pollution is serious; (3) the components are complex, and the harmless difficulty is high; (4) is difficult to degrade, and the conventional sewage treatment method is difficult to effectively degrade organic matters in the waste liquid. Meanwhile, due to different components of the waste liquid, toxic gas and dangers such as heating and explosion are often accompanied in the treatment process, so that the properties of the waste liquid must be fully known before treatment.
High-concentration organic waste liquid is conventionally treated by a wet catalytic oxidation (CWO) method and a supercritical water oxidation (supercritical water oxidation) method. Catalytic Wet Oxidation (CWO)) is an advanced technology developed in 8O of the last 20 th century internationally for treating high-concentration organic wastewater difficult to biodegrade, has the characteristics of high purification efficiency, no secondary pollution, small occupied area and the like, and has attracted attention and engineering application in the industry. Supercritical water (T is more than or equal to 3740C, P is more than or equal to 22.1MPa) is a medium widely studied in chemistry and chemical engineering. Supercritical Water Oxidation (SCWO) technology is a new organic pollution treatment technology and has good application and development prospects. This process can be considered as a further development of the wet oxidation technique. In a supercritical state, hydrogen bonds in water are reduced, the dielectric constant and viscosity are reduced, the density is between a gas state and a liquid state, the ion product is sharply reduced, and the diffusion coefficient is increased. Organic matter and oxidant carry out the quick oxidation reaction in supercritical water medium, can make organic pollutant thoroughly oxidize and decompose into carbon dioxide, water and other small molecule organic matters within a few minutes even a few seconds. Compared with the conventional organic sewage treatment technology, the SCW0 has a series of advantages of high degradation efficiency, clean and non-secondary pollution of a reaction final product, no selectivity, wide application range, rapid reaction and the like. However, the supercritical water oxidation reaction has the problems of strong corrosivity, high material requirement, easy precipitation of inorganic salt, blockage of a reactor, a pipeline, a valve and the like, so that the industrial popularization and application of the technology and the process are hindered.
The existing wet catalytic oxidation reactor or supercritical water oxidation reactor generally adopts a fixed bed bubbling type reactor form, and in order to control the temperature at the tower top or the violent heat release (supercritical water oxidation) in the reaction process, the organic matter content (generally expressed by COD or TOC) of the waste liquid entering from the tower bottom needs to be controlled, so as to prevent the temperature at the tower top from exceeding the design temperature due to the heat release (14.7kJ/gCOD) in the reaction process. This design requirement for fixed bed bubble reactors is contradictory to the need to treat high concentration waste streams (typically COD in the hundreds of thousands).
SUMMERY OF THE UTILITY MODEL
To the problem that present high concentration organic waste liquid treatment is in, the utility model provides a subcritical fluidized bed reactor for high concentration organic waste liquid treatment can be under the high condition that contains salt in order to degrade the organic waste liquid of high concentration effectively for the waste liquid after the processing directly satisfies national emission standard or satisfies the requirement of intaking of follow-up ordinary biochemical technology.
The utility model discloses technical scheme as follows:
a subcritical fluidized bed reactor for treating high-concentration organic waste liquid comprises an outer cylinder (5) and at least two inner cylinders (24) arranged in the outer cylinder (5), wherein the top end and the bottom end of each inner cylinder (24) are both opened, the inside of each outer cylinder (5) is communicated with the inside of each inner cylinder (24), a cavity is reserved between the cylinder wall of each inner cylinder (24) and the cylinder wall of each outer cylinder (5) to form a down-flow area (11),
an upper end enclosure (6) is arranged at the top end of the outer barrel (5), a lower end enclosure (7) is arranged at the bottom end of the outer barrel, at least one waste liquid material inlet (1) is arranged at the middle upper part of the outer barrel, an air inlet (3) is arranged at the bottom of the outer barrel (5), and a treated material outlet (2) is arranged on the upper end enclosure (6);
the inner cylinders (24) are overlapped up and down to form a two-stage or multi-stage inner circulation section, a distance is reserved between two adjacent inner cylinders (24) up and down to form an overflow port, the bottom of the inner cylinder (24) at the lowest part is provided with an air distributor (4), and the air distributor (4) is connected with the air inlet (3) through a pipeline;
the inner part of the inner cylinder (24) is an upstream reaction area (12), the upper part of the uppermost inner cylinder (24) is a discharge reflux area (13), waste liquid enters the down-flow area (11) through a waste liquid material inlet (1) and then flows downwards, enters the upstream reaction area (12) from the bottom of the lowermost inner cylinder (24) and flows upwards under the action of gas discharged by the gas distributor (4).
Preferably, an inert filler layer (25) is arranged between the discharge return zone (13) and the upper head (6).
Preferably, a material emptying outlet (8) is arranged on the lower sealing head (7);
preferably, the upper seal head (6) and the lower seal head (7) are both convex seal heads; the number of the waste liquid material inlets (1) is two, and the two inlets are symmetrically arranged on the left and the right.
Preferably, the outer cylinder (5) and the inner cylinder (24) are both cylindrical cylinders and are arranged concentrically;
the number of the inner cylinders (24) is two, two secondary internal circulation sections are formed, and the two secondary internal circulation sections consist of a stage I internal circulation section (9) and a stage II internal circulation section (10).
Another aspect of the utility model provides a reaction system for high concentration organic waste liquid treatment, including the pretreatment unit (14), waste liquid water pump (15), above-mentioned arbitrary reactor (16), heat exchanger (17), vapour and liquid separator (18) and liquid storage pot (19) that connect gradually through the pipeline;
the gas inlet (3) of the reactor (16) is connected with the gas supply unit (20) through a pipeline, and the top of the gas-liquid separator (18) is connected with the gas purification device (23) through a pipeline.
Preferably, the heat exchanger (17) is a water-cooling heat exchanger, the heat exchanger is connected with a cooling water storage tank (22) through a pipeline, and a cooling water pump (21) is arranged on the pipeline.
Preferably, the air supply unit (20) provides oxygen or oxygen-enriched air, the waste liquid water pump (15) adopts a high-pressure pump group, and the pretreatment unit (14) performs precipitation and filtration treatment.
Another aspect of the present invention provides a method for treating high concentration organic waste liquid, which comprises the following steps:
after the waste liquid is conveyed to a pretreatment unit (14) for pretreatment, a waste liquid water pump (15) is started, a gas supply unit (20) is started to input gas into a reactor (16), the waste liquid enters the reactor (16), flows downwards from a down-flow area (11), then enters a lowermost inner cylinder (24) and flows upwards under the action of the gas, the waste liquid is fully reacted in the reactor (16) and then is output through a treated material outlet (2), the treated waste liquid is subjected to heat exchange and temperature reduction through a heat exchanger (17), then enters a gas-liquid separator (18) for gas-liquid separation, the separated liquid flows into a liquid storage tank (19), and the separated gas enters a gas purification device (23) and is purified and then discharged.
In the technical scheme, the working temperature in the reactor (16) is not higher than 350 ℃;
a catalyst accounting for 10-20% of the total volume of all the internal circulation sections is added into the reactor (16);
the pH value of the waste liquid is adjusted to 7.0-8.5 after the waste liquid is pretreated in a pretreatment unit (14).
Preferably, the internal circulation section is a two-stage internal circulation section, the peroxide coefficient is 1.5-3.0, and the reaction time is 40-120 min;
the preferable waste liquid treatment flow is 10m3/h。
Subcritical Water (Subcritical Water) means Water that remains in a liquid state when heated from a boiling point temperature at atmospheric pressure (100 ℃) to its supercritical point (374 ℃) under a certain pressure (≦ 22.05 MPa). In practical application, the temperature of subcritical water is generally above 200 ℃. In the subcritical state, as the thermal motion of water molecules increases, the following three characteristics can be changed: firstly, along with the rise of temperature, the self-ionization of water also rises, the ion product of water near a critical point is increased by more than 103 times compared with that of water in a room temperature state, and the concentration of H + and OH & lt- & gt is higher than that of water in normal temperature, so that subcritical water has the catalytic function of acid and alkali catalysts; ② the dielectric constant of water is lowered and the property similar to that of the organic solvent is exhibited. Water has a dielectric constant value of 78F/m at room temperature, but when the temperature is raised to 250 ℃, the dielectric constant value is reduced to 30F/m, which is similar to that of methanol or acetone, so that many weakly polar substances can be dissolved in subcritical water. ③ other parameters such as viscosity, surface tension and solubility parameters of water (solubility parameter) were also changed. Under subcritical conditions, the concentration of hydrogen and hydroxide ions increases due to increased ionic product, allowing water to act as both a solvent and to participate in chemical reactions in the form of acid/base catalysts or reactants. The chemical reaction in the subcritical water is usually a reaction catalyzed by an acid/base catalyst, and the chemical reaction rate is improved due to the action of high temperature and high pressure, but the reaction condition is milder than that of supercritical water oxidation, and the problems of inorganic salt deposition and the like are avoided.
The utility model discloses a subcritical fluidized bed reactor and reaction system, organic waste liquid are through deposit, simple preliminary treatment back such as filtration, and the normal atmospheric temperature directly gets into reactor down flow district, has avoided traditional adoption heat exchanger to heat the feeding outside the reactor just to get into the reactor behind reactor design operating temperature to cause the series problems such as the corruption of the heat exchanger that need set up special heat exchanger and probably cause, reduced the investment of equipment and the reliability of entire system operation. The position of the waste liquid material inlet on the reactor can be set to ensure that the material entering the reactor enters the down-flow area, and the inlet waste liquid is prevented from ascending to cause short circuit. The material entering the reactor at normal temperature is directly mixed with the high-temperature material in the discharge reflux zone, and the imported waste liquid is gradually heated to the set subcritical temperature in the downflow zone. The waste liquid entering the reactor at normal temperature is continuously and polar mixed with the high-temperature material from the reflux zone and the high-temperature material from the internal circulation zone in the downflow zone, so that the functions of heating the imported material to the designed subcritical temperature and diluting the imported material are achieved. Introducing a proper amount of oxygen or oxygen-enriched air into the bottom of the upflow reaction zone through an air distributor, and mainly aiming at (1) rapidly generating water oxidation reaction of organic pollutants in a subcritical state under the condition of introducing oxygen; (2) providing the power required by the internal circulation.
In the internal circulation section of the reactor inner cylinder, subcritical water oxidation reaction generated in the reaction zone can release a large amount of reaction heat (the generated heat is about 14.7kJ when COD is reduced by 1 g), in order to prevent the temperature at the top of each stage of internal circulation section from exceeding the designed working temperature of the reactor, an overflow port is arranged at the top of each stage of internal circulation section, high-temperature reaction products are led into a down-flow zone, the effects of reducing the top temperature of the internal circulation section and heating inlet materials are achieved, meanwhile, the effect of diluting the concentration of organic matters in the inlet materials is achieved, and the effect of severe overheating reaction is avoided. The secondary or multi-stage internal circulation section may be provided according to the concentration of organic matters in the material at the material inlet and the amount of organic matters to be removed in the reactor. By properly setting the distance between the top internal circulation section and the upper end enclosure flange, the waste liquid material entering the reactor is ensured not to directly enter the reflux zone, and meanwhile, a reaction product with a certain flow rate enters the down-flow zone to heat and dilute the inlet material. The material of the internal circulation section only needs to be a corrosion-resistant material in a subcritical water state, and the pressure-bearing material of the reactor can be a material which can bear pressure and is corrosion-resistant.
Compared with the prior art, the utility model has the advantages of it is following:
(1) the traditional heat exchanger which is arranged outside the reactor and heats the materials entering the reactor to the set temperature of the reactor is eliminated, the investment of the system is greatly reduced, and the reliability of the operation of the system is improved.
(2) The method directly heats the inlet material by using reaction heat release to gradually reach the designed reaction temperature and gradually dilute the concentration of organic matters in the inlet material, so that violent heat release possibly occurring in the subcritical water oxidation reaction process is prevented, and the damage to the reliability of the system is avoided.
(3) The secondary or multi-stage internal circulation section may be provided according to the concentration of the fed organic matter and the amount of the organic matter to be removed. The temperature at the top of each internal circulation section does not exceed the designed working temperature of the reactor, so that the phenomenon of overheating inside the reactor is prevented.
(4) The reactor takes the form of a novel reactor with multiple internal circulating fluidized beds to distinguish the traditional fixed bubbling beds. In the conventional fixed bubble-bed reactor, under the condition of high-concentration inlet materials, the overheating reaction is easy to occur at the top of the reactor. In order to prevent the overheating reaction at the top of the reactor, the amount of organic substances removed by the whole reactor (the amount of heat generated per 1g of COD removed is 14.7kJ) needs to be strictly controlled, so that the amount of organic substances removed by a single fixed-bed bubbling reactor is limited (generally, the amount is controlled to 20000 to 30000mg/L of COD). And the utility model discloses a COD volume that multiple fluidized bed reactor of inner loop can get rid of as required sets up the fine every section top of having avoided of multistage inner loop section and takes place overheat phenomenon.
(5) The utility model discloses a fluidized bed rather than traditional fixed bed reactor has increased the area of contact of catalyst with the material, the jam problem of the catalyst of having avoided for reaction rate has reduced the volume of reactor and the total investment of equipment.
(6) The designed working temperature of the reactor is controlled in a subcritical water oxidation section, the rising of ion product and the rising of hydrogen ion and hydroxyl ion concentration under the subcritical water condition are utilized, so that water can serve as a solvent, can also take the form of an acid/alkali catalyst or can participate in chemical reaction by reactants, and meanwhile, the subcritical water oxidation condition is utilized to be milder than the supercritical water oxidation condition, so that the problems of inorganic salt deposition and the like are avoided.
(7) The utility model discloses a subcritical multiple internal circulation fluidized bed reactor has solved the deposit of the inorganic salt that traditional supercritical water oxidation reactor faced and has probably aroused the jam problem of pipeline, valve, consequently the utility model discloses can effectual processing height contain the organic waste liquid of salt.
(8) The utility model discloses be the difficult biodegradable organic waste liquid of high concentration and under the lower condition of salt content imported the material, can upgrade to supercritical water oxidation reactor in a flexible way. Under the condition of not adding catalyst and letting in oxygen, the utility model can be changed into a subcritical/supercritical gasification reactor, thereby realizing the purpose of preparing hydrogen or combustible gas by gasifying organic waste liquid. Therefore, the utility model has wide universality.
(9) The utility model discloses a method of handling high concentration organic waste liquid (COD of waste liquid can reach hundreds of thousands mg/L) under the state of subcritical water, whole reaction is gone on in inclosed pressure vessel and subcritical water, can not produce secondary pollution like traditional method of burning.
Drawings
FIG. 1 is a schematic structural view of a subcritical fluidized bed reactor in a reaction system for treating high-concentration organic waste liquid according to the present invention;
FIG. 2 is a schematic structural view of a reaction system for treating high concentration organic waste liquid according to the present invention;
reference numerals: the device comprises a waste liquid material inlet 1, a treated material outlet 2, an air inlet 3, an air distributor 4, an outer cylinder 5, an upper sealing head 6, a lower sealing head 7, a material emptying outlet 8, a I-stage internal circulation section 9, a II-stage internal circulation section 10, a down-flow area 11, an up-flow reaction area 12, a discharge back-flow area 13, a pretreatment unit 14, a waste liquid water pump 15, a reactor 16, a heat exchanger 17, a gas-liquid separator 18, a liquid storage tank 19, an air supply unit 20, a cooling water pump 21, a cooling water storage tank 22, a gas purification device 23, an inner cylinder 24 and an inert filler layer 25.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings and examples. The following examples are given by way of illustration and description of the present invention and are not intended to limit the scope of the present invention.
EXAMPLE 1 subcritical fluidized bed reactor for treatment of high concentration organic waste liquid
As shown in fig. 1, a subcritical fluidized bed reactor for treating high concentration organic waste liquid comprises an outer cylinder 5 and at least two inner cylinders 24 disposed in the outer cylinder 5, wherein both the top end and the bottom end of the inner cylinders 24 are open, the inside of the outer cylinder 5 is communicated with the inside of the inner cylinders 24, a cavity is left between the cylinder wall of the inner cylinders 24 and the cylinder wall of the outer cylinder 5 to form a down flow region 11, and the inner cylinders 24 are fixed in the outer cylinder 5 (in the present invention, the inner cylinders are fixed by connecting support rods, and those skilled in the art can adopt other flexible forms);
the top end of the outer barrel 5 is provided with an upper end enclosure 6, the bottom end of the outer barrel 5 is provided with a lower end enclosure 7, the middle upper part of the outer barrel is provided with at least one waste liquid material inlet 1, the bottom of the outer barrel 5 is provided with an air inlet 3, and the upper end enclosure 6 is provided with a treated material outlet 2;
the inner cylinders 24 are overlapped up and down to form a two-stage or multi-stage internal circulation section, a distance is reserved between two adjacent inner cylinders 24 to form an overflow port, the bottom of the inner cylinder 24 at the lowest part is provided with an air distributor 4, and the air distributor 4 is connected with the air inlet 3 through a pipeline;
the inner cylinder 24 is internally provided with an upstream reaction zone 12, a discharging reflux zone 13 is arranged above the uppermost inner cylinder 24, waste liquid enters the down-flow zone 11 through a waste liquid material inlet 1 and then flows downwards, enters the upstream reaction zone 12 from the bottom of the lowermost inner cylinder 24 and flows upwards under the action of gas discharged by the gas distributor 4.
In some embodiments, as shown in fig. 1, an idler is disposed between the effluent recirculation zone 13 and the upper head 6
A layer of porous packing 25 prevents loss of catalyst inside the reactor 16.
In some embodiments, as shown in fig. 1, a material emptying outlet 8 is arranged on the lower head 7 to facilitate emptying of residue and waste liquid in the reactor during equipment maintenance;
preferably, the upper seal head 6 and the lower seal head 7 are both convex seal heads;
the number of the waste liquid material inlets 1 is two, and the two inlets are symmetrically arranged on the left and the right.
In some embodiments, as shown in fig. 1, the outer barrel 5 and the inner barrel 24 are both cylindrical barrels and are concentrically arranged; the number of the inner cylinders 24 is two, a two-stage internal circulation section is formed, and the two-stage internal circulation section consists of a stage I internal circulation section 9 and a stage II internal circulation section 10.
Example 2 reaction System for high concentration organic waste liquid treatment
As shown in fig. 2, the reaction system for treating the high-concentration organic waste liquid comprises a pretreatment unit 14, a waste liquid water pump 15, a reactor 16 of embodiment 1, a heat exchanger 17, a gas-liquid separator 18 and a liquid storage tank 19 which are connected in sequence through pipelines, wherein a gas inlet 3 of the reactor 16 is connected with a gas supply unit 20 through a pipeline, and the top of the gas-liquid separator 18 is connected with a gas purification device 23 through a pipeline.
In some embodiments, as shown in fig. 2, the heat exchanger 17 is a water-cooled heat exchanger, and the heat exchanger is connected to a cooling water storage tank 22 through a pipeline, and a cooling water pump 21 is disposed on the pipeline.
In some embodiments, as shown in fig. 2, the air supply unit 20 provides oxygen or oxygen-enriched air, the waste water pump 15 employs a high pressure pump set, and the pretreatment unit 14 performs a precipitation filtration process.
Example 3 method for high concentration organic waste liquid treatment
A method for treating a high concentration organic waste liquid using the reaction system of example 2, comprising the steps of:
after the waste liquid is conveyed to a pretreatment unit 14 for pretreatment, a waste liquid water pump 15 is started, a gas supply unit 20 is started to input gas into a reactor 16, the waste liquid enters the reactor 16 and flows downwards from a downflow area 11, then enters a lowermost inner cylinder 24 and flows upwards under the action of the gas, the waste liquid is fully reacted in the reactor 16 and then is output from a treated material outlet 2, the treated waste liquid is subjected to heat exchange and temperature reduction through a heat exchanger 17, then enters a gas-liquid separator 18 for gas-liquid separation, the separated liquid flows into a liquid storage tank 19, and the separated gas enters a gas purification device 23 and is purified and then discharged.
The working temperature in the reactor 16 is not higher than 350 ℃; a catalyst accounting for 10-20% of the total volume of all the internal circulation sections is added into the reactor 16; the pH value of the waste liquid is adjusted to 7.0-8.5 after the waste liquid is pretreated in the pretreatment unit 14.
In some embodiments, the internal circulation section is a two-stage internal circulation section, the peroxide coefficient is 1.5-3.0, the reaction time is 40-120 min, and the waste liquid treatment flow is 10m3/h。
The utility model discloses the method, the organic waste liquid of processing adopt the normal atmospheric temperature feeding, and the waste liquid gets into 16 back adoption subcritical water oxidation reaction's exothermic direct 11 gradual heating import materials to the operating temperature of design in the downwash district, need not set up traditional heat exchanger in order to be used for heating import materials at reactor 16. The material is subjected to Hydrolysis Reaction (Hydrolysis Reaction), thermal cracking Reaction (Pyrolysis Reaction) and thermal oxidation Reaction (thermal oxidation Reaction) in the downflow zone 11 along with temperature rise and in a relatively anoxic environment, so that the macromolecular organic matter is converted into the micromolecular organic matter, and then the subcritical water oxidation Reaction is rapidly performed in the upflow Reaction zone 12. The oxygen or oxygen-enriched air from the air supply unit 20 enters the oxygen or oxygen-enriched air amount of the upstream reaction zone 12 through the air distributor 4, and the oxygen demand of the subcritical water oxidation reaction and the air stripping amount required for ensuring the internal circulation of the materials need to be met.
In some preferred embodiments, two or more stages of internal circulation sections may be provided depending on the concentration of the feed organic waste stream and the design operating temperature of the reactor 16. The top temperature of the internal circulation section of each stage is no higher than the designed operating temperature of the reactor 16. The reactor 16 is designed to operate at a temperature of no greater than 350 c.
In some preferred embodiments, the distance between the stage I internal circulation section 9 and the stage II internal circulation section 10 is determined according to the concentration of organic matter in the feed waste liquid, so as to satisfy a certain amount of the reaction product in the stage I internal circulation section 9 for the dual purpose of lowering the temperature at the top of the stage I internal circulation section 9 and heating the inlet waste liquid material in the downflow zone 11.
In some preferred embodiments, it is necessary to set the appropriate area ratio of the cross sections of the downflow zone 11 and the upflow reaction zone 12 according to the concentration of the organic matter at the waste liquid material inlet, so as to determine the appropriate downflow rate of the downflow zone 11 and the upflow reaction zone 12.
In some preferred embodiments, the effluent recirculation zone 13 is sized to ensure that the inlet waste stream does not enter the effluent recirculation zone 13 directly.
In some preferred embodiments, the heat released by the reaction can be recovered by the heat exchanger 17 in the form of high-temperature and high-pressure water or high-temperature steam B, so as to achieve the purposes of harmless treatment and resource utilization of the waste liquid.
Application example 1:
the acrylonitrile waste liquid was treated by using the reaction system shown in FIG. 2, and the waste liquid mainly contained acrylonitrile, acetonitrile, hydrogen cyanide, propionitrile, methanol, methyl ester, ammonium sulfate, sulfuric acid and other main components, and had a COD value of 73360mg/L and a treatment flow rate of 10m3/h。
The sewage is adjusted to be neutral through a pH adjusting tank, the pH value is 7.0-8.5, and the sewage is directly input into a reactor 16 through a waste liquid material inlet 1 at normal temperature through a waste liquid water pump 15. The pressure of a high-pressure pump of the waste liquid water pump is 5-7 MPa. The reactor 16 is provided with two stages of internal circulation: a stage I internal circulation section 9 and a stage II internal circulation section 10. The waste liquid that gets into reactor 16 under the normal atmospheric temperature heats up to 200 ℃ to 240 ℃ after with the product of the reaction of I level and II level inner loop section overflow mouth backward flow gradually, gets into I level inner loop section 9's bottom, and the oxygen or the oxygen-enriched air that let in through air inlet 3 and gas distributor 4 carry out abundant mixture, and the peroxide coefficient adopts 2.0 (the utility model discloses the peroxide coefficient that other application examples adopted is between 1.5 ~ 3.0) to provide required oxygen of oxidation reaction and air stripping volume. The reactor 16 is thrown and is accounted for 12% (the utility model discloses other application examples throw the proportion and throw powder catalyst (the commodity of selling on the market) of I level inner loop section 9 and II level inner loop section 10 total volume 12%, reaction time 80min (the utility model discloses the reaction time of other application examples is between 40 ~ 120 min), export COD value is 12600mg/L, and the COD clearance is about 82.3%, and the B/C value is 0.39.
Claims (9)
1. A reaction system for treating high-concentration organic waste liquid is characterized in that: comprises a pretreatment unit (14), a waste liquid water pump (15), a reactor (16), a heat exchanger (17), a gas-liquid separator (18) and a liquid storage tank (19) which are connected in sequence through pipelines;
the reactor comprises an outer cylinder (5) and at least two inner cylinders (24) arranged in the outer cylinder (5), wherein the top end and the bottom end of each inner cylinder (24) are open, the inside of each outer cylinder (5) is communicated with the inside of each inner cylinder (24), and a cavity is reserved between the cylinder wall of each inner cylinder (24) and the cylinder wall of each outer cylinder (5) to form a down-flow area (11);
an upper end enclosure (6) is arranged at the top end of the outer barrel (5), a lower end enclosure (7) is arranged at the bottom end of the outer barrel, at least one waste liquid material inlet (1) is arranged at the middle upper part of the outer barrel, an air inlet (3) is arranged at the bottom of the outer barrel (5), and a treated material outlet (2) is arranged on the upper end enclosure (6);
two-stage or multi-stage internal circulation sections are formed by overlapping the inner cylinders (24) up and down, a distance is reserved between two adjacent inner cylinders (24) up and down to form an overflow port, the bottom of the inner cylinder (24) at the lowest part is provided with an air distributor (4), and the air distributor (4) is connected with the air inlet (3) through a pipeline;
the inner part of the inner cylinder (24) is provided with an upstream reaction area (12), the upper part of the uppermost inner cylinder (24) is provided with a discharging reflux area (13), waste liquid enters the down-flow area (11) through a waste liquid material inlet (1) and then flows downwards, enters the upstream reaction area (12) from the bottom of the lowermost inner cylinder (24) and flows upwards under the action of gas discharged by the gas distributor (4);
the gas inlet (3) of the reactor (16) is connected with the gas supply unit (20) through a pipeline, and the top of the gas-liquid separator (18) is connected with the gas purification device (23) through a pipeline.
2. The reaction system of claim 1, wherein: an inert filler layer (25) is arranged between the discharging reflux area (13) and the upper end enclosure (6).
3. The reaction system of claim 1, wherein: and a material emptying outlet (8) is formed in the lower end enclosure (7).
4. The reaction system of claim 3, wherein: the upper seal head (6) and the lower seal head (7) are both convex seal heads.
5. The reaction system of claim 1, wherein: the number of the waste liquid material inlets (1) is two, and the two inlets are symmetrically arranged on the left and the right.
6. The reaction system of claim 1, wherein: the outer cylinder (5) and the inner cylinder (24) are cylindrical cylinders and are arranged concentrically.
7. The reaction system of claim 1, wherein: the number of the inner cylinders (24) is two, two secondary internal circulation sections are formed, and the two secondary internal circulation sections consist of a stage I internal circulation section (9) and a stage II internal circulation section (10).
8. The reaction system of claim 1, wherein: the heat exchanger (17) is a water-cooling heat exchanger, the heat exchanger is connected with a cooling water storage tank (22) through a pipeline, and a cooling water pump (21) is arranged on the pipeline.
9. The reaction system of claim 1, wherein: the air supply unit (20) provides oxygen or oxygen-enriched air, the waste liquid water pump (15) adopts a high-pressure pump set, and the pretreatment unit (14) is used for carrying out precipitation filtration treatment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023325178.3U CN214611894U (en) | 2020-12-31 | 2020-12-31 | Reaction system for treating high-concentration organic waste liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023325178.3U CN214611894U (en) | 2020-12-31 | 2020-12-31 | Reaction system for treating high-concentration organic waste liquid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214611894U true CN214611894U (en) | 2021-11-05 |
Family
ID=78434588
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202023325178.3U Active CN214611894U (en) | 2020-12-31 | 2020-12-31 | Reaction system for treating high-concentration organic waste liquid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214611894U (en) |
-
2020
- 2020-12-31 CN CN202023325178.3U patent/CN214611894U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101254987B (en) | Handling method for advanced purification of little-volume refractory wastewater and operation equipment | |
| CN101209883A (en) | Technique for processing coking wastewater or organic wastewater by supercritical water oxidization technique | |
| CN103482835B (en) | Sludge hydrolysis device and hydrolysis process | |
| CN112661314B (en) | Subcritical fluidized bed reactor and method for treating high-concentration organic waste liquid | |
| KR102488891B1 (en) | Methods and apparatus used in acrolein reactor wastewater treatment | |
| CN114890611B (en) | Device and method for treating high-sulfur waste alkali liquor and high-salt high-nitrate nitrogen wastewater difficult to biochemically | |
| CN108383335B (en) | High-concentration organic wastewater treatment system and method | |
| CN214611894U (en) | Reaction system for treating high-concentration organic waste liquid | |
| CN201158601Y (en) | System for treating carbonized wastewater or organic waste water with supercritical water oxidization technique | |
| CN111675423B (en) | Treatment method and system for nicotinic acid medical intermediate wastewater | |
| CN105016527A (en) | High COD wastewater subcritical Fenton treatment system and treatment method | |
| CN100509661C (en) | Treating technique of polyether polyatomic alcohol producing sewage recovering and utilization | |
| CN110746050A (en) | Self-sufficient cyclic regeneration system for dyeing and printing desizing waste water energy and treatment process | |
| CN216472454U (en) | Step steady flow type anaerobic reaction system | |
| CN114349246B (en) | Combined treatment method of polycyclic aromatic hydrocarbon wastewater | |
| CN203486931U (en) | Sewage treatment unit for production of coal chemical industry | |
| CN210085221U (en) | Biochemical sludge treatment system | |
| CN106565009B (en) | Alkaline residue waste liquid catalytic treatment device and method based on waste heat utilization | |
| CN211871738U (en) | Treatment system for industrial hemp processing wastewater | |
| CN218521152U (en) | Bromine fire retardant class product waste water treatment device | |
| CN114057278B (en) | Waste alkali liquid treatment device and method | |
| CN110078326B (en) | Biochemical sludge treatment system and method | |
| CN112047575B (en) | Method for treating pyromellitic dianhydride production wastewater and special device | |
| CN211056912U (en) | Self-sufficient type cyclic regeneration system of printing and dyeing desizing waste water heat energy | |
| CN113501581A (en) | Step steady flow type anaerobic reaction system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |