CN213725643U - Circulation absorption formula exhaust-gas treatment system - Google Patents
Circulation absorption formula exhaust-gas treatment system Download PDFInfo
- Publication number
- CN213725643U CN213725643U CN202020841412.9U CN202020841412U CN213725643U CN 213725643 U CN213725643 U CN 213725643U CN 202020841412 U CN202020841412 U CN 202020841412U CN 213725643 U CN213725643 U CN 213725643U
- Authority
- CN
- China
- Prior art keywords
- tank
- aliphatic hydrocarbon
- absorption
- liquid aliphatic
- treatment system
- 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
- Treating Waste Gases (AREA)
Abstract
The application discloses circulation absorption formula exhaust-gas treatment system, this system include adsorption tanks, knockout drum and intercommunication the transfer line of adsorption tanks and knockout drum, wherein: the absorption tank is internally stored with liquid aliphatic hydrocarbon and is provided with an exhaust gas inlet and an exhaust gas outlet, and the absorption tank is provided with an aerator connected with the exhaust gas inlet; the separator tank is internally provided with a heater and is provided with a waste gas outlet; the conveying pipeline is used for conveying the liquid aliphatic hydrocarbon, and comprises a liquid supply pipeline for conveying the liquid aliphatic hydrocarbon in the absorption tank to the separation tank, and a return pipeline for conveying the liquid aliphatic hydrocarbon in the separation tank to the absorption tank. This application utilizes and is better and the liquid aliphatic hydrocarbon that the boiling point is higher than this organic matter with organic matter intersolubility as the medium, absorbs, transmits and separates this organic matter under high temperature to realize the collection of this organic matter, make things convenient for subsequent processing, for example burn or retrieve.
Description
Technical Field
The application relates to the technical field of environmental protection, more specifically relates to a cyclic absorption formula exhaust-gas treatment system.
Background
In some industrial manufacturing facilities (e.g., some chemical, environmental, or pharmaceutical industries), a certain amount of high concentration exhaust gas is generated during the process of manufacturing, testing, or conducting research experiments.
This exhaust gas is treated and then discharged to the atmosphere.
The inventors have found that the treatment method is different depending on the application field, and for example, it is suitable to treat the exhaust gas containing benzene or naphthalene vapor at a high concentration by the incineration method, and for the exhaust gas containing volatile organic solvents such as hydrocarbons and ethers, the treatment is carried out by the incineration method or the condensation method according to the conventional technical teaching in the art. The existing treatment methods have some defects, such as incineration method, i.e. incineration of waste gas, and the investment cost and the operation cost are high; whereas the condensation method requires deep refrigeration, i.e. the refrigeration temperature is low, which results in higher energy consumption.
SUMMERY OF THE UTILITY MODEL
In view of the above, an object of the present invention is to provide a recycling absorption type exhaust gas treatment system, which separates and collects substances to be separated from exhaust gas, facilitates subsequent treatment, such as incineration or recycling treatment, and is beneficial to reducing energy consumption.
The application discloses a circulation absorption formula exhaust-gas treatment system, including adsorption tank, knockout drum and intercommunication the transfer line of adsorption tank and knockout drum, wherein: the absorption tank is internally stored with liquid aliphatic hydrocarbon and is provided with an exhaust gas inlet and an exhaust gas outlet, and the absorption tank is provided with an aerator connected with the exhaust gas inlet; the separator tank is internally provided with a heater and is provided with a waste gas outlet; the conveying pipeline is used for conveying the liquid aliphatic hydrocarbon, and comprises a liquid supply pipeline for conveying the liquid aliphatic hydrocarbon in the absorption tank to the separation tank, and a return pipeline for conveying the liquid aliphatic hydrocarbon in the separation tank to the absorption tank.
Compared with the prior art, the technical scheme provided by the application ingeniously utilizes the liquid aliphatic hydrocarbon which is better in intersolubility with the organic matter and has a boiling point higher than that of the organic matter as a medium, absorbs, transmits and separates out the organic matter at high temperature, so that the collection of the organic matter is realized, and the subsequent further treatment, such as incineration or recovery, is facilitated.
In some embodiments, the exhaust system further comprises an after-treatment system for treating the exhaust gas output from the separation tank.
In some examples, the back end processing system includes, or may be, a combustion system.
In other embodiments, the back end processing system comprises an induced draft fan and a spray tower, wherein:
the induced draft fan is communicated with a waste gas outlet of the separation tank and introduces waste gas into the spray tower;
the spray tower is provided with a liquid outlet and a gas outlet, the gas outlet is communicated to the waste gas inlet of the absorption tank through a pipeline, after the spray tower sprays and cools the waste gas, the liquid is discharged through the liquid outlet, and the non-condensable gas enters the pipeline through the gas outlet and is conveyed to the waste gas inlet of the absorption tank.
This example need not to set up the system of burning and burns waste gas, but utilizes the insoluble in water characteristics of organic matter of waiting to separate, cools down to condense with the recovery, as the replenishment of raw materials, has reduced the loss of raw materials, has avoided combustion system's purchase and maintenance cost on the one hand from this, and on the other hand has reduced the loss of raw materials to the productivity effect of enterprise has been improved.
In other examples, a heat exchanger is disposed on the delivery line; a cooler is also arranged on the return pipeline; the liquid aliphatic hydrocarbon accounts for 50-80% of the volume of the absorption tank; the aerator is an aerator with the foaming diameter less than or equal to 3 mm; the aerator is a spray head aerator, a micro-porous aerator or a spiral-flow aerator.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present application, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
Fig. 1 is a schematic structural diagram of a cyclic absorption type exhaust gas treatment system according to an embodiment of the present application;
FIG. 2 is a schematic structural diagram of a cyclic absorption type exhaust gas treatment system according to another embodiment of the present application;
FIG. 3 is a schematic structural diagram of a cyclic absorption type exhaust gas treatment system according to yet another embodiment of the present application;
fig. 4 and 5 are schematic structural diagrams of a cyclic absorption type exhaust gas treatment system according to some other embodiments of the present application.
Detailed Description
During the work research, the inventor sees that some plants have problems to be solved when processing the exhaust gas, for example, when some chemical plants process the naphthalene-carrying exhaust gas, the incineration method is adopted, namely the naphthalene-carrying exhaust gas is directly incinerated, on one hand, an incineration system needs to be constructed, the equipment cost is increased, and on the other hand, a large amount of energy, such as liquefied natural gas, needs to be consumed when the chemical plants operate.
It can be seen that, in the specific use process, the incineration method and the condensation method have more or less defects, for example, the incineration method requires a large investment cost, the condensation method has higher energy consumption due to the problem of low refrigeration, and in addition, the existing methods have the defects that the analysis of the components of the waste gas is lacked, and the recovery treatment of the organic matters in the waste gas is lacked.
After further research, the inventor finds that certain organic components in the exhaust gas, such as benzene, naphthalene, and some hydrocarbons and ethers, are relatively soluble in aliphatic hydrocarbons, and have a boiling point generally lower than that of aliphatic hydrocarbons (especially some long-chain aliphatic hydrocarbons), so after research, analysis and test, an idea and a scheme of a recycling absorption type exhaust gas treatment system are formed.
As shown in fig. 1, a structure of a cyclic absorption type exhaust gas treatment system disclosed in an embodiment of the present application, the exhaust gas system includes an absorption tank 11 and a separation tank 21, and a transfer line connecting the absorption tank 11 and the separation tank 21, wherein:
the absorption tank 11 stores liquid aliphatic hydrocarbon 10 therein, the absorption tank 11 has an exhaust gas inlet 111 and an exhaust gas outlet 112, and the absorption tank 11 is provided with an aerator 113 connected to the exhaust gas inlet 111.
The separation tank 21 has an exhaust gas outlet 211 and a heater 212 is built therein.
The transfer line is used for transferring the liquid aliphatic hydrocarbon 10, and includes a supply line 311 for transferring the liquid aliphatic hydrocarbon 10 in the absorption tank 11 to the separation tank 21, and a return line 312 for transferring the liquid aliphatic hydrocarbon 10 in the separation tank 21 to the absorption tank 11.
The above-mentioned exhaust treatment system is when normal work:
industrial waste gas containing a substance to be separated (an organic substance such as benzene or naphthalene) enters the absorption tank 11 from the waste gas inlet 111, is dispersed into bubbles by the aerator 113, and is fully contacted with the liquid aliphatic hydrocarbon 10, wherein the substance to be separated is dissolved in the liquid aliphatic hydrocarbon 10, and waste gas containing other components is discharged from the waste gas outlet 112 of the absorption tank 11. The liquid aliphatic hydrocarbon 10 is delivered to the separation tank 21 through the liquid supply pipeline 311, the heater 212 disposed in the separation tank 21 heats the liquid aliphatic hydrocarbon 10 in the separation tank 21, when the liquid aliphatic hydrocarbon 10 is heated to a preset temperature, the substances to be separated in the liquid aliphatic hydrocarbon 10 are separated from the liquid aliphatic hydrocarbon 10 to form steam, the steam is discharged from the waste gas outlet 211 of the separation tank 21, and the liquid aliphatic hydrocarbon 10 is delivered to the absorption tank 11 through the return pipeline 312.
The specific value of the preset temperature is determined according to the boiling point of the substance to be separated, for example, if the substance to be separated is naphthalene, the preset temperature is above 218 ℃.
It can be seen that the operation of the exhaust gas treatment system comprises the following steps:
step S10, a waste gas absorption stage, in which the waste gas is absorbed by the liquid aliphatic hydrocarbon 10 (or is merged with the liquid aliphatic hydrocarbon 10) after entering the absorption tank 11;
step S20, in the waste gas transfer stage, the liquid aliphatic hydrocarbon 10 is conveyed from the absorption tank 11 to the separation tank 21 to realize the transfer of the waste gas;
step S30, in the waste gas collection phase, the heater 212 in the separation tank 21 heats the liquid aliphatic hydrocarbon 10 from the absorption tank 11, and after the preset temperature is reached, the substances to be separated are separated from the liquid aliphatic hydrocarbon 10 to form steam, and the steam is discharged (collected) through the waste gas outlet 211 of the separation tank 21; after separation, the liquid aliphatic hydrocarbon 10 is refluxed to the absorption tank 11.
The working process of the waste gas system continuously circulates from step S10 to step S20, the liquid aliphatic hydrocarbon 10 is used as a collection and transmission medium of substances (organic substances) to be separated in the waste gas, and circulates in the absorption tank 11 and the separation tank 21, so that the substances to be separated are conveniently collected, and the subsequent treatment is facilitated.
The gas discharged from the waste gas outlet 211 contains organic substances (i.e., the substances to be separated) at a higher concentration (compared to the original industrial waste gas), and thus the gas can be conveniently treated in a centralized manner. Another embodiment of the present application provides a structure, on the basis of fig. 1, a back-end processing system is added, as shown in fig. 2.
The back-end treatment system 41 is used to treat the gas discharged from the off-gas outlet 211 of the separation tank 21, for convenience of description, since the gas contains organic matter at a high concentration and has a high temperature, hereinafter referred to as organic matter vapor. The treatment may be a combustion or a further purification, two specific configurations being provided in fig. 3 and 4.
In fig. 3, the back-end treatment system 41 is a combustion system 411, i.e. the organic matter steam is directly combusted by the combustion system 411 to reduce or eliminate the organic matter in the exhaust gas.
In fig. 4, the back-end processing system 41 includes an induced draft fan 412 and a spray tower 413, wherein:
the induced draft fan 412 is communicated with the waste gas outlet 211 of the separation tank 21, the organic matter steam is introduced into the spray tower 413, and cold water spraying is carried out in the spray tower 413.
The spraying tower 413 is provided with a liquid outlet and a gas outlet, the gas outlet is communicated to the waste gas inlet 111 of the absorption tank 11 through a pipeline, after the spraying tower 413 sprays and cools the organic matter steam, organic matters in the organic matter steam are condensed and enter water, and the organic matters are gradually layered due to insolubility in water and can be discharged through the liquid outlet; the non-condensable gas enters the pipeline through the gas outlet and is conveyed to the waste gas inlet 111 of the absorption tank 11, so that on one hand, the pressure of the waste gas inlet 111 can be maintained to ensure the dispersion effect of the aerator 113 on the waste gas, and on the other hand, a small amount of organic matters possibly exist in the non-condensable gas, and the next round of separation treatment can be carried out to avoid direct discharge and pollution.
The specific structure and type of the induced draft fan 412 are not limited, for example, a roots fan may be used, and the rotation speed of the induced draft fan 412 is controlled so as to maintain a certain negative pressure, typically-10 kPa, in the separation tank 21.
The size of the spray tower 413 is set as required, in one example, the diameter of the spray tower 413 is 2 meters, and the height of the spray tower 413 is 5 meters; the spray tower 413 may consist of a tower top, a top water sprayer, a top gas outlet (i.e., gas outlet), a bottom gas sprayer, and a bottom water outlet (i.e., liquid outlet); the bottom gas ejector can be composed of a plurality of gas pipelines and a plurality of gas nozzles, the gas pipelines are communicated with the induced draft fan 412, organic matter steam from the waste gas outlet 211 of the separation tank 21 is introduced and is sprayed through the gas nozzles, and the organic matter steam moves upwards in the spray tower 413 after being sprayed; the top water sprayer sprays cold water to wash the gas to rapidly cool, wherein organic matters are condensed into solid particles, and the solid particles are discharged from a bottom water outlet of the spray tower 413 along with the water. In some examples, a filter (e.g., a bag filter) may be provided to filter and retain organic matter in the water, and the filtered water may be pumped to the top of the spray tower 413, continuing to spray water through the top water spray, and so forth. In this process, a small amount of noncondensable gas is discharged from the top vent, sent to the waste gas inlet 111 of the absorption tank 11, and separated again.
In the above embodiments, the material and size of the absorption tank 11 can be selected according to the requirement, for example, the absorption tank can be made of steel, and the shape of the absorption tank is designed to be a vertically placed cylinder with a diameter of 4 meters and a height of 3 meters. The liquid aliphatic hydrocarbon 10 is contained in the lower half of the absorption tank 11, and generally, the volume of the liquid aliphatic hydrocarbon 10 accounts for 50% to 80% of the volume of the absorption tank 11. The material, shape and size of the separation tank 21 may be similar to or the same as those of the absorption tank 11, the bottom of the separation tank contains the liquid aliphatic hydrocarbon 10, the heater 212 is immersed in the liquid aliphatic hydrocarbon 10, and the heater 212 may be a steam heater or an electric heater.
The aerator 113 is immersed in the liquid aliphatic hydrocarbon 10, and may be a shower head type aerator, i.e., composed of a gas input pipe, a gas branch pipe, a check valve and a shower head; the waste gas from the waste gas inlet 111 is divided into a plurality of paths of gas by each gas branch pipe after passing through the gas inlet pipe, and is sprayed into the liquid aliphatic hydrocarbon 10 by the spray head after passing through the check valve, so that a large number of bubbles are generated inside the liquid aliphatic hydrocarbon 10, and after the bubbles are fully contacted with the liquid aliphatic hydrocarbon 10, the substances (organic substances, such as benzene or naphthalene) to be separated therein are dissolved and absorbed by the liquid aliphatic hydrocarbon 10.
In some embodiments, the aerator 113 may also be of other configurations, such as a micro-porous aerator or a cyclonic aerator.
The inventors of the present invention conducted many experiments and analyses and found a phenomenon that the smaller the bubbles, the better the dissolution degree in the liquid aliphatic hydrocarbon 10, but the higher the exhaust gas pressure needs to be maintained, and the structure of the aerator may be more complicated, for example, for the micro-porous aerator, the pore size needs to be finer, the exhaust gas pressure needs to be increased (additional pressurizing means is needed); that is, the degree of dissolution of the substance to be separated in the liquid aliphatic hydrocarbon 10 is related to the structural complexity (cost) of the system, or contradictory, and after the study, the inventors found that the gas bubbles are greatly optimized at 3MM in the process of gradually reducing the gas bubbles to 3MM in a larger size, and if the gas bubbles are further reduced in size, a microporous aerator with a denser pore size and a smaller pore size is required, and a larger exhaust pressure is required, which inevitably increases the structural complexity of the exhaust system to a large extent, and increases the cost.
Therefore, in the general application environment, when the bubbles are maintained at 3MM, the obviously optimized dissolving degree of the substance to be separated in the liquid aliphatic hydrocarbon can be ensured without excessively increasing the complexity of the system.
In some embodiments, the liquid supply line 311 is provided with a liquid supply pump, and as shown in fig. 5, the liquid supply pump 3111 can increase the speed of transferring the liquid aliphatic hydrocarbon from the absorption tank 11 to the separation tank 21. The liquid supply pump 3111 may employ a chemical pump, such as a screw pump; the flow rate of the liquid feed pump 3111 is related to the volume of the liquid aliphatic hydrocarbon 10 in the tank (the absorption tank 11 or the separation tank 21) and the residence time of the liquid aliphatic hydrocarbon 10 in the tank, for example, if the volume of the liquid aliphatic hydrocarbon in the tank is 20 cubic meters and the residence time is 1 hour, the flow rate of the liquid feed pump 3111 is 20 cubic meters per hour.
In addition, the temperature of the liquid aliphatic hydrocarbon in the absorption tank 11 is low, and the temperature of the liquid aliphatic hydrocarbon in the separation tank 21 is high, taking naphthalene as an example of a substance to be separated, the temperature of the liquid aliphatic hydrocarbon in the absorption tank 11 is about 60 degrees celsius, and the temperature of the liquid aliphatic hydrocarbon in the separation tank 21 reaches more than 200 degrees celsius, so that the liquid aliphatic hydrocarbon flowing back to the absorption tank 11 needs to be cooled in many ways, for example, a return pipeline is extended, a heat exchanger can also be arranged, as shown in the figure, the heat exchanger 313 is arranged on a delivery pipeline, specifically, is arranged at a position on the liquid supply pipeline 311 close to the separation tank 11, and is arranged at a position on the return pipeline 312 close to the separation tank 11.
In this way, the high heat of the liquid aliphatic hydrocarbon output from the absorption tank 21 can be fully utilized to heat the liquid aliphatic hydrocarbon to be introduced into the absorption tank 21, i.e., the heat exchanger 313 is used for heat exchange between the return line 312 and the liquid supply line 311.
Since the liquid aliphatic hydrocarbon is heated in the separation tank 21, the temperature of the liquid aliphatic hydrocarbon output by the separation tank is higher, and the temperature of the return line 312 is higher, that is, the heat of the return line 312 can be used to heat the liquid supply line 311, so as to raise the temperature of the liquid aliphatic hydrocarbon in the liquid supply line 311, and simultaneously lower the temperature of the liquid aliphatic hydrocarbon in the return line 312. Equivalently, the liquid aliphatic hydrocarbon is preheated before entering the separation tank 21, thereby reducing the energy consumption of the heater 212 and realizing the full utilization of the heat energy.
The heat exchanger 313 may be a tubular heat exchanger, allowing high temperature liquid aliphatic hydrocarbon to flow on the tube side and low temperature (relatively speaking) liquid aliphatic hydrocarbon to flow on the shell side.
In addition, a cooler 3121 may be further disposed on the return line 312 between the heat exchanger 313 and the absorption tank 11, for further cooling the liquid aliphatic hydrocarbon subjected to heat exchange treatment by the heat exchanger 313. The cooler 3121 may be a jacketed heat exchanger, in which a cooling fluid (cooling water may be used) flows to cool the liquid aliphatic hydrocarbon in the return line 312. In specific work, the flow of cooling water can be controlled, a certain temperature can be kept while the temperature is reduced, and liquid aliphatic hydrocarbon is prevented from being solidified. The coolers with different heat exchange areas are manufactured or selected according to the requirements, and in some examples, the heat exchange area of the cooler 3121 is about 100 square meters.
The scheme described in the application can be applied to various industrial scenes which need to treat the waste gas and contain organic matters like benzene, naphthalene, hydrocarbons or ethers in the waste gas. For example, in an example that the present inventors have contacted, a chemical industry enterprise uses naphthalene as a raw material to produce, and a certain amount of residual raw material (naphthalene) is contained in the discharged exhaust gas, which cannot meet the emission standard, and a general treatment method adopts an incineration method, i.e., a combustion system is used to directly incinerate the exhaust gas, because the amount of naphthalene contained in the exhaust gas is relatively small, or relatively thin, and direct incineration requires a large amount of exhaust gas, a lot of energy is consumed, and thus the treatment cost is relatively high. In the scheme described in the application, the naphthalene-containing waste gas is absorbed by the liquid aliphatic hydrocarbon in the absorption tank, the naphthalene steam is dissolved in the liquid aliphatic hydrocarbon, then the liquid aliphatic hydrocarbon is conveyed and preheated, and after the liquid aliphatic hydrocarbon is heated to the set temperature (above 218 ℃) in the separation tank, the naphthalene steam is separated from the liquid aliphatic hydrocarbon, so that the energy consumption for burning is greatly reduced due to the concentrated collection of naphthalene even according to the conventional burning method.
Of course, if the burning method is not used, other methods are used, such as guiding the naphthalene vapor separated from the separation tank into a spray tower by an induced draft fan, spraying cold water by the spray tower, cooling the naphthalene vapor to condense into naphthalene solid, and gradually enriching. Because the mutual solubility of naphthalene and water is very low, the naphthalene gradually precipitates out. After standing, the naphthalene is separated out and can be recovered as a raw material. The liquid aliphatic hydrocarbon separated from the naphthalene vapor is handed out and preheated by the heat exchanger, cooled by the cooler and sent to the absorption tank for reuse, and the process is repeated. The mode does not need to burn, can also recover the raw materials, saves the raw material loss, has lower treatment cost and improves the production benefit of enterprises.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present application. Various modifications to these embodiments, as well as various combinations and applications of aerators, liquid feed pumps, heat exchangers, heaters, coolers, fans and cooling towers, and of these equipment components, of which various types or configurations or parameters are selected based on the disclosure herein, such as absorption tanks, separation tanks and transfer lines, will be readily apparent to those skilled in the art, and the generic principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the disclosure herein. Thus, the present application is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (9)
1. A cyclic absorption formula exhaust-gas treatment system, characterized by, includes adsorption tank, knockout drum and communicates the transfer line of adsorption tank and knockout drum, wherein:
the absorption tank is internally stored with liquid aliphatic hydrocarbon and is provided with an exhaust gas inlet and an exhaust gas outlet, and the absorption tank is provided with an aerator communicated with the exhaust gas inlet;
the separator tank is internally provided with a heater and is provided with a waste gas outlet;
the conveying pipeline is used for conveying the liquid aliphatic hydrocarbon, and comprises a liquid supply pipeline for conveying the liquid aliphatic hydrocarbon in the absorption tank to the separation tank, and a return pipeline for conveying the liquid aliphatic hydrocarbon in the separation tank to the absorption tank.
2. The system of claim 1, further comprising a back end treatment system for treating the exhaust output from the separator tank.
3. The cyclic absorption-type flue gas treatment system according to claim 2, wherein the back-end treatment system comprises an induced draft fan and a spray tower, wherein:
the induced draft fan is communicated with a waste gas outlet of the separation tank and introduces waste gas into the spray tower;
the spray tower is provided with a liquid outlet and a gas outlet, the gas outlet is communicated to the waste gas inlet of the absorption tank through a pipeline, after the spray tower sprays and cools the waste gas, the liquid is discharged through the liquid outlet, and the non-condensable gas enters the pipeline through the gas outlet and is conveyed to the waste gas inlet of the absorption tank.
4. The cyclic absorption exhaust treatment system of claim 2, wherein the back end treatment system comprises a combustion system.
5. A cyclic absorption-type exhaust gas treatment system according to any one of claims 1 to 4, wherein a heat exchanger is provided on the transfer line.
6. The system of claim 5, wherein a cooler is further disposed on the return line.
7. The cyclic absorption-type exhaust gas treatment system according to claim 5, wherein the liquid aliphatic hydrocarbon accounts for 50-80% of the volume of the absorption tank.
8. The cyclic absorption-type exhaust gas treatment system according to claim 5, wherein the aerator is an aerator having a bubble diameter of 3mm or less.
9. The system of claim 8, wherein the aerator is a jet aerator, a micro-porous aerator, or a cyclonic aerator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020841412.9U CN213725643U (en) | 2020-05-19 | 2020-05-19 | Circulation absorption formula exhaust-gas treatment system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020841412.9U CN213725643U (en) | 2020-05-19 | 2020-05-19 | Circulation absorption formula exhaust-gas treatment system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN213725643U true CN213725643U (en) | 2021-07-20 |
Family
ID=76813993
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202020841412.9U Active CN213725643U (en) | 2020-05-19 | 2020-05-19 | Circulation absorption formula exhaust-gas treatment system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN213725643U (en) |
-
2020
- 2020-05-19 CN CN202020841412.9U patent/CN213725643U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108947069A (en) | System and method based on micro passage reaction continuous processing organic wastewater | |
| CN110498398A (en) | A kind of waste hydrochloric acid differential pressure regeneration treatment system and regeneration treating method | |
| CN105601017B (en) | The near-zero release processing system and method for a kind of high concentrated organic wastewater and sludge | |
| CN206350977U (en) | Waste gas recovery processing unit | |
| WO2022041476A1 (en) | Salt-containing wastewater treatment apparatus | |
| US4213830A (en) | Method for the transfer of heat | |
| CN110054164A (en) | A kind of dilute sulfuric acid system for concentrating and recycling | |
| CN205442932U (en) | Near zero emission processing system of high concentration organic waste water and mud | |
| CN210786298U (en) | Pyrolysis gas grading treatment device | |
| CN203754482U (en) | Wet oxidation treatment device of wastewater | |
| CN213725643U (en) | Circulation absorption formula exhaust-gas treatment system | |
| CN109453573A (en) | Tail gas treatment process and processing unit for natural gas TEG dehydration device | |
| CN202538386U (en) | Alcohol recovery tower | |
| CN202246576U (en) | Low-temperature condensation absorption recycling device for oil gas | |
| CN208975204U (en) | A kind of system that organic matter recycles | |
| CN207430015U (en) | Integrated VOC exhaust treatment systems based on photocatalysis and membrane separation technique | |
| CN109796366A (en) | A kind of high concentration DMF or DMAC rectifying and purifying system and method | |
| CN209568026U (en) | A kind of high concentration DMF or DMAC rectifying and purifying system | |
| CN204873907U (en) | Hot pressing formula distilled water machine system | |
| CN103539215A (en) | Sewage treatment system and process | |
| CN209196830U (en) | A kind of boiler supply water deaerating processing system | |
| CN209242841U (en) | System based on micro passage reaction continuous processing organic wastewater | |
| CN210584416U (en) | Exhaust gas treatment device | |
| CN208711379U (en) | It is a kind of to absorb VOC and regeneration device using high boiling solvent | |
| CN203820495U (en) | Energy-saving deoxidation system of industrial boiler |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |