CN220656950U - Tail gas purifying and recycling equipment - Google Patents
Tail gas purifying and recycling equipment Download PDFInfo
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- CN220656950U CN220656950U CN202322011512.5U CN202322011512U CN220656950U CN 220656950 U CN220656950 U CN 220656950U CN 202322011512 U CN202322011512 U CN 202322011512U CN 220656950 U CN220656950 U CN 220656950U
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- exhaust gas
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- 238000004064 recycling Methods 0.000 title abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000011084 recovery Methods 0.000 claims abstract description 16
- 238000000926 separation method Methods 0.000 claims abstract description 7
- 238000001035 drying Methods 0.000 claims description 22
- 238000001179 sorption measurement Methods 0.000 claims description 19
- 238000011144 upstream manufacturing Methods 0.000 claims description 18
- 239000007788 liquid Substances 0.000 claims description 12
- 230000008929 regeneration Effects 0.000 claims description 12
- 238000011069 regeneration method Methods 0.000 claims description 12
- 239000003463 adsorbent Substances 0.000 claims description 11
- 238000003795 desorption Methods 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 8
- 238000003912 environmental pollution Methods 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 103
- 238000000034 method Methods 0.000 description 27
- 239000012855 volatile organic compound Substances 0.000 description 21
- 238000010586 diagram Methods 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 8
- 238000003860 storage Methods 0.000 description 7
- 230000007613 environmental effect Effects 0.000 description 6
- 239000006096 absorbing agent Substances 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- SCYULBFZEHDVBN-UHFFFAOYSA-N 1,1-Dichloroethane Chemical compound CC(Cl)Cl SCYULBFZEHDVBN-UHFFFAOYSA-N 0.000 description 4
- 239000003507 refrigerant Substances 0.000 description 4
- 238000013461 design Methods 0.000 description 3
- 230000001788 irregular Effects 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 150000002894 organic compounds Chemical class 0.000 description 2
- 239000003513 alkali Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- -1 small molecule halogenated hydrocarbons Chemical class 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Abstract
The utility model provides an exhaust gas purifying and recycling device, which comprises: the device comprises an exhaust gas cooler, a first adsorber, a second adsorber and an exhaust gas negative pressure fan; the system comprises a resolving primary cooler, a resolving secondary cooler, a recovery oil-water separation tank and a delivery pump; fresh air blower and air heater; the apparatus includes a first adsorber connection state and a second adsorber connection state. The equipment provided by the utility model realizes effective control and standard emission of tail gas, effectively reduces environmental pollution, realizes green and environment-friendly tail gas treatment, can realize effective recycling of resources, improves economic benefits of enterprises, and can realize automatic tail gas treatment.
Description
Technical Field
The application belongs to the technical field of environmental protection, and in particular relates to tail gas purifying equipment.
Background
In various chemical production, a large amount of exhaust gas to be treated is generated, and a specially designed exhaust gas purifying apparatus is required. For example, during the production and storage of oxychlorination devices in the chlor-alkali industry, in particular during the material input of dichloroethane (EDC) storage tanks, a large amount of gas must be discharged to balance the pressure in the tanks, and in addition, the partial pressure of the volatile EDC due to heat must be balanced during high-temperature seasons.
Due to the effective concentration of EDC in the EDC-rich effluent gas of up to 3000mg/m 3 Above, direct emissions can cause serious VOC emissions exceeding, which must be handled properly in advance to meet the requirements of the relevant environmental regulations. Meanwhile, the device is influenced by the input and output of the EDC tank materials at an irregular time, and the irregular fluctuation of the external exhaust gas quantity also seriously influences the normal operation of the device for treating the partial gas, and even causes irregular exceeding discharge.
The existing common tail gas treatment methods comprise a direct incineration method, a direct absorption method, a direct condensation method and an adsorption method, but the methods have various defects to be overcome in general, for example, the direct incineration method is suitable for treating the tail gas which is difficult to recycle or has no recycling value, and can generate corrosive gases such as HCl and the like after incineration, so that the requirements on equipment are high, and secondary pollution is easy to cause; the direct absorption method is to absorb harmful components in the tail gas by the absorbent and then separate the harmful components, and the difficulty is that the absorbent is screened and separated, and the emission reaching the standard is difficult to achieve; the direct condensation method is suitable for high-temperature gas phase recovery, is mainly used for recovering high-boiling point or high-concentration VOC, has limited application range, and is generally not used independently but used in the pretreatment stage of other processes; the adsorption method is to adsorb VOC in organic waste gas by using a porous structure of a porous adsorbent, the adsorption process is physical adsorption, and after the adsorption saturation of the adsorbent, the adsorbent is desorbed by hot air or water vapor, and the regenerated adsorbent can be reused, but the main treatment concentration of the adsorbent is VOC with medium and low concentration, and the adsorbent has quite limitations.
In addition, the prior art has a great deal of attention to the treatment of organic-containing exhaust gases generated by production plants, while the attention to the exhaust gas emissions from tank areas like material storage is significantly inadequate. With increasing importance of environmental protection, VOC emission standards are becoming stricter, and the automation degree of production control is improved, so that it is very desirable to develop a tail gas purifying and recovering system suitable for use in organic matter production or storage, for example, for tail gas purifying and recovering systems in dichloroethane production and storage, so that the treated waste gas reaches the emission standards, thereby not only realizing effective recycling of resources, improving economic benefits of enterprises, but also effectively reducing environmental pollution and meeting the requirements of environmental protection.
Disclosure of Invention
The application provides a tail gas purification recovery plant, equipment includes:
(i) The adsorption component comprises an exhaust gas cooler, a first adsorber, a second adsorber and an exhaust gas negative pressure fan;
(ii) The analysis regeneration assembly comprises an analysis primary cooler, an analysis secondary cooler, a recovery oil-water separation tank and a delivery pump;
(iii) The drying assembly comprises a fresh air fan and an air heater;
the apparatus includes a first adsorber connection state and a second adsorber connection state,
in the connection state of the first adsorber, the first adsorber is connected with an upstream tail gas condenser and a downstream tail gas negative pressure fan, the second adsorber is connected with the analysis regeneration assembly and is in an analysis state, or is connected with the drying assembly and is in a drying state, or is in a standby state,
and in the connection state of the second adsorber, the second adsorber is connected with an upstream tail gas condenser and a downstream tail gas negative pressure fan, and the first adsorber is connected with the analysis regeneration assembly to be in an analysis state, or is connected with the drying assembly to be in a drying state, or is in a standby state.
According to one embodiment of the present application, the first and second adsorbers each have a tail gas inlet at a bottom or lower portion thereof and a gas phase outlet at a top or upper portion thereof.
According to another embodiment of the present application, the first adsorber and the second adsorber are each fixed beds, which are packed with granular or pellet-shaped adsorbents.
According to another embodiment of the present application, the tail gas cooler, the resolving primary cooler and the resolving secondary cooler are tube array heat exchangers, and the air heater is a fin-and-tube heat exchanger.
According to another embodiment of the present application, the gas phase outlet of the resolving secondary cooler, downstream of the resolving secondary cooler or upstream of the recovery oil water separator tank is connected to the exhaust gas cooler or upstream of the exhaust gas cooler.
According to another embodiment of the application, a differential pressure gauge is arranged upstream of the exhaust gas cooler and upstream of the exhaust gas negative pressure fan, and the differential pressure gauge is in data connection with the exhaust gas negative pressure fan.
According to another embodiment of the application, a VOC on-line analysis device is arranged at the outlet of the exhaust negative pressure fan, said VOC on-line analysis device being in data connection with the first adsorber and the second adsorber, arranged to control the device to switch between a first adsorber connection state and a second adsorber connection state.
According to another embodiment of the present application, the primary cooler, the secondary cooler and the tail gas cooler are liquid cooling devices, and temperature sensors are arranged at respective outlets.
According to another embodiment of the present application, a liquid level controller is provided inside or outside the recovery oil-water separator tank.
According to another embodiment of the present application, the device comprises an automation control system, which is directly or indirectly data-connected with at least one component of the device.
In the following detailed description, processes and designs of the present application are described with reference to the accompanying drawings.
Drawings
FIG. 1 shows a schematic view of an exhaust gas purifying and recovering apparatus according to an embodiment of the present application;
FIG. 2 shows a schematic diagram of a normal tail gas treatment flow in an apparatus, according to one embodiment of the present application;
FIG. 3 shows a schematic diagram of an parsing process flow in a device according to one embodiment of the present application;
fig. 4 shows a schematic diagram of a post-resolution drying process in an apparatus according to one embodiment of the present application.
Detailed Description
"Range" is disclosed herein in the form of lower and upper limits. There may be one or more lower limits and one or more upper limits, respectively. The given range is defined by selecting a lower limit and an upper limit. The selected lower and upper limits define the boundaries of the particular ranges. All ranges that can be defined in this way are inclusive and combinable, i.e., any lower limit can be combined with any upper limit to form a range. For example, ranges of 60-120 and 80-110 are listed for specific parameters, with the understanding that ranges of 60-110 and 80-120 are also contemplated. Furthermore, if the minimum range values 1 and 2 are listed, and if the maximum range values 3,4 and 5 are listed, the following ranges are all contemplated: 1-3, 1-4, 1-5, 2-3, 2-4 and 2-5.
In the present utility model, unless otherwise indicated, the numerical range "a-b" represents a shorthand representation of any combination of real numbers between a and b, where a and b are both real numbers. For example, the numerical range "0-5" means that all real numbers between "0-5" have been listed throughout, and "0-5" is simply a shorthand representation of a combination of these values.
In the present utility model, all the embodiments mentioned herein and the preferred embodiments may be combined with each other to form new technical solutions, if not specifically described.
In the present utility model, all technical features mentioned herein and preferred features may be combined with each other to form new technical solutions, if not specifically stated.
In the present utility model, all the steps mentioned herein may be performed sequentially or randomly, but are preferably performed sequentially, unless otherwise specified. For example, the method comprises steps (a) and (b), meaning that the method may comprise steps (a) and (b) performed sequentially, or may comprise steps (b) and (a) performed sequentially. For example, the method may further include step (c), which means that step (c) may be added to the method in any order, for example, the method may include steps (a), (b) and (c), may include steps (a), (c) and (b), may include steps (c), (a) and (b), and the like.
In the present utility model, the term "comprising" as referred to herein means open or closed unless otherwise specified. For example, the term "comprising" may mean that other components not listed may also be included, or that only listed components may be included.
In the present utility model, when describing the spatial relationship of a particular element or object relative to other elements or objects, the terms "inner", "outer", "above", "below" and the like are used to denote that the former is located inside, outside, above or below the latter, either directly in contact with or at a distance from each other or separated by a third element or object.
It should be emphasized that the drawings and the following description illustrate only some embodiments of the utility model, and the scope of the utility model is not limited to these embodiments. The scope of the utility model is defined by the claims of the present utility model and may include any technical solution within the scope of the claims, including but not limited to further improvements and substitutions to these specific embodiments.
The present application provides an exhaust gas purifying and recovering apparatus which can be used for purifying and material recycling an exhaust gas containing organic substances, examples of which may include Volatile Organic Compounds (VOCs), more specifically, small molecule halogenated hydrocarbons, and hereinafter, the exhaust gas purifying and recovering apparatus of the present utility model will be described by taking an exhaust gas mainly containing dichloroethane (EDC) as an example.
Fig. 1 shows a schematic diagram of an apparatus according to an embodiment of the present application, the apparatus shown in the figure comprising: adsorption module, desorption regeneration module and drying module. The adsorption component comprises a tail gas cooler, a first adsorber, a second adsorber and a tail gas negative pressure fan. Fig. 2 shows a schematic diagram of the operation of the adsorption module, according to one embodiment, one of the first and second adsorbers is connected to an upstream exhaust cooler and a downstream exhaust negative pressure fan via a pipeline for adsorbing EDC in the exhaust, and the other adsorber is connected to the desorption regeneration module in a desorption state, or is connected to the drying module in a drying state, or is in a standby state. According to one embodiment of the present application, the first and second adsorbers are each fixed beds of adsorbent packing, and the adsorbent may be selected as desired, such as oleophilic pellet resin or granular activated carbon.
For example, when the first adsorber is operating normally, the exhaust gas containing EDC flows into the exhaust gas cooler, the temperature in the exhaust gas is adjusted as needed, and then the exhaust gas is transported to flow through the first adsorber, and a negative pressure exhaust fan is used to provide a pressure difference for the adsorption assembly, so that the exhaust gas treated in the adsorber flows downstream and is discharged into the atmosphere. According to one embodiment of the present application, the tail gas to be treated enters the first adsorber from the bottom of the first adsorber, EDC adsorption is performed therein, EDC contained in the tail gas is adsorbed by the adsorbent filled in the first adsorber during the process of passing through the first adsorber, and the tail gas after adsorption treatment is pumped and discharged to the atmosphere from the upper gas phase outlet of the first adsorber through the tail gas negative pressure fan. According to one embodiment of the application, differential pressure meters are arranged at the upstream of the tail gas cooler and the upstream of the tail gas negative pressure fan respectively, the differential pressure meters control the frequency conversion of the fan and the air draft flow, the normal use state of the adsorption assembly is ensured, and the flow of the tail gas in the adsorption assembly is ensured. According to another embodiment of the application, the exhaust negative pressure fan outlet is provided with a VOC on-line analysis device, and the VOC concentration in the exhaust gas is detected and recorded on line, for example, the concentration of EDC in the exhaust gas treated by the first adsorber is detected, so that the treated exhaust gas VOC meets the requirements of relevant laws or regulations and can reach the emission standards. The second adsorber is in a stand-by state, or in a desorption regeneration state or in a dry state.
In this application, the term "data connection" means that a wired or wireless connection is established between two devices by means of a data line, bluetooth, etc., and the two devices can perform data communication to complete the data exchange and control.
When the VOC concentration in the exhaust gas discharged from the outlet of the adsorber in normal operation reaches the set value, it indicates that the first adsorber has adsorbed enough EDC and needs to be analyzed and regenerated, at this time, the apparatus is switched from the first adsorber connection state to the second adsorber connection state, and the first adsorber is no longer connected to the upstream exhaust gas condenser and the downstream exhaust gas negative pressure fan, but the second adsorber is connected to the upstream exhaust gas condenser and the downstream exhaust gas negative pressure fan, and the exhaust gas containing EDC is treated by the second adsorber, and the connection manner and the operation principle of the second adsorber are as described above for the first adsorber. The first adsorber is connected with the analysis regeneration component and the drying component in sequence and is used for analyzing and regenerating the first adsorber.
Fig. 3 shows a schematic diagram of the analytical process flow in the apparatus, when the first adsorber or the second adsorber is switched to the analytical regeneration state, steam is introduced into the adsorber through the overhead steam inlet to perform analytical regeneration, so that EDC and other organic compounds (if any) adsorbed on the adsorber are flushed away, so that the adsorber recovers its adsorption capacity, and VOCs such as EDC are recovered. The cleaned regenerated gas (steam flow containing organic compounds) is discharged from the bottom of the absorber, flows through the first-stage resolving cooler and the second-stage resolving cooler in sequence, the condensate flows into the oil-water separating tank, after oil-water separation, the oil phase (mainly EDC) is pumped back to the crude EDC tank for recovery by the EDC conveying pump, and can also be conveyed to production equipment, storage equipment or refining equipment for reuse as required, and the water phase is conveyed to an organic wastewater pool of the production device for unified treatment.
According to one embodiment of the present application, during the resolving process, the gas phase outlet of the resolving secondary cooler, downstream of the resolving secondary cooler or upstream of the recovery oil water separator tank is connected to the exhaust gas cooler or to the exhaust gas cooler. The gas phase of the material flowing out of the analysis secondary cooler is conveyed to a tail gas cooler and is combined with the EDC-containing tail gas to be treated and conveyed to an adsorber.
Fig. 4 shows a schematic diagram of the drying process after the desorption in the apparatus, after the desorption is completed, the adsorber is put into a dry state, at which time the steam supply is cut off and the drying is performed instead using air. Specifically, fresh air is heated by a fresh air fan and then sent to the top of an absorber, flows out from the bottom of the absorber, passes through an analysis primary cooler and an analysis secondary cooler, and then gas phase returns to an inlet of a tail gas cooler to be combined with EDC-containing tail gas to be treated and then is sent to the absorber. And after the drying is finished, the absorber is in a standby state to be switched.
According to one embodiment of the present application, the tail gas cooler, the resolving primary cooler and the resolving secondary cooler are tube array heat exchangers and the air heater is a pin fin heat exchanger, such as a pin fin heat exchanger with dust cloth. According to another embodiment of the present application, the primary cooler, the secondary cooler and the tail gas cooler are liquid cooling devices, such as water cooling devices, and temperature sensors are arranged at respective outlets. According to one embodiment, the temperature control points are arranged at the gas phase outlets of the coolers and the heat exchangers, and the temperature control is realized by adjusting the flow of the refrigerant entering the heat exchangers. According to one embodiment, the tail gas cooler and the analysis primary cooler use circulating water as a refrigerant, and the analysis secondary cooler uses water at 5-7 ℃ as a refrigerant, so that most of the tail gas is ensuredSeparating EDC for recovery, and discharging gas phase EDC concentration less than or equal to 1mg/m 3 。
According to another embodiment, a liquid level control device is arranged inside or outside the recovery oil-water separation tank, so that automatic delivery of oil-water two phases is realized. The device of the utility model can be controlled manually, partly automatically or entirely in an automated manner. For example, the equipment comprises an automatic control system which is directly or indirectly connected with at least one component of the equipment in a data mode, steam for analysis and air for drying are used for analysis, all control loops and detection points are programmed into a PLC program, the whole process automatic control of adsorption, analysis, automatic switching and the like is achieved, and meanwhile key parameters are transmitted to a DCS from the PLC to be controlled in a central mode.
According to one embodiment, the following operations are performed in an automated manner: a differential pressure gauge is arranged in front of the tail gas cooler and in front of the tail gas negative pressure fan, and the differential pressure gauge controls the fan frequency conversion and the air draft flow, so that the whole set of treatment recovery system is ensured to be in a normal use state; the outlet of the tail gas negative pressure fan is provided with VOC on-line analysis equipment, and the concentration of VOC in the discharged gas is detected and recorded on line, so that the discharged gas VOC after being treated by the system is ensured to reach the standard for discharge; the temperature control points are arranged at the gas phase outlets of the coolers and the heat exchangers, and the temperature control of the gas phase outlets of the heat exchangers is realized by adjusting the flow of the refrigerant entering the heat exchangers; the recovery oil-water separation tank is provided with oil-water two-phase interface liquid level control, an EDC conveying pump is controlled to realize automatic start and stop, an upper water phase flows out from an overflow port, and the overflow pipe is provided with a liquid seal to prevent gas phase short circuit and realize automatic delivery of oil-water two phases; a signal for opening and closing a shut-off valve such as a steam for analysis or an air for drying, a shut-off valve and a regulating valve for each control circuit, a signal for detecting a temperature, a pressure, a liquid level and a flow rate, and the VOC detection data are all programmed into a PLC program and are controlled by an independent PLC system, so that the whole process automatic control of adsorption, analysis, automatic switching and the like is realized, and meanwhile, key parameters are transmitted to the DCS for central control by the PLC. By adopting the design of partial or complete automation, the automatic standard emission of the tail gas of the dichloroethane production facility or the storage tank area can be realized, and the unattended operation is realized.
The utility model has reasonable design of the process flow, realizes the automation of the whole process, furthest controls the total amount of VOC discharged to the atmosphere, furthest recovers EDC, saves resources, avoids environmental pollution, and has obvious economic benefit and environmental protection benefit.
Examples
Preferred embodiments of the present utility model are specifically illustrated in the following examples, but it should be understood that the scope of the present application is not limited thereto. All changes and modifications that come within the meaning and range of equivalency of the claims are to be embraced within their scope.
In the examples of the present application, the tail gas purifying and recovering apparatus of the present application was constructed according to the schematic diagram shown in fig. 1, and the respective device structures are as follows: the tail gas cooler is a liquid cooling cooler adopting a fin structure, and the heat exchange area of the tail gas cooler is 10 meters 2 The temperature of the cooler is set to 18 ℃ and the pressure is set to 0.25Mpa by controlling the flow rate of cooling water during operation. The first adsorber and the second adsorber are 3 m in volume 3 Adopts a vertical round tank, the working temperature is 150 ℃ and the pressure is 0.01Mpa. The tail gas negative pressure fan is a centrifugal fan, the wind pressure is 1000pa, and the wind quantity is 300m 3 /h。
The analytical primary cooler is a tube type liquid cooling cooler: its heat exchange area is 10m 2 The working temperature is 75 ℃ and the pressure is 0.25Mpa. The analytical secondary cooler is a tube type liquid cooling cooler with heat exchange area of 10 meters 2 The working temperature is 18 ℃ and the pressure is 0.25Mpa. The volume of the recovery oil-water separation tank is 0.1 meter 3 The working temperature is 30 ℃ and the pressure is less than 0.01Mpa. The flow rate of the delivery pump is more than 2m 3 And/s, the lift is more than 10m.
The fresh air fan is a centrifugal fan, the wind pressure is more than 1000pa, and the wind quantity is more than 300m 3 And/h. The air heater is a tubular liquid cooling heat exchanger with fins, and the heat exchange area is 10 meters 2 The working temperature is 110 ℃ and the pressure is 0.25pa.
The pair of devices described above was used to contain about 3000mg/m 3 The EDC industrial off-gas is treated and fed to the plant at a flow rate of 10m/s, the components of the plant operating under the conditions described above. First cool the first adsorber and the tail gasThe cooler is connected with the tail gas negative pressure fan, so that the tail gas flows through the first adsorber, and EDC in the tail gas is adsorbed by using the first adsorber. The adsorption treatment of the tail gas is continuously carried out by the first adsorber until the EDC concentration measured on line by a VOC on-line analysis device arranged at the downstream of the tail gas negative pressure fan reaches 1mg/m 3 At this time, the first adsorber is switched to an analysis state, and the second adsorber is switched to be connected to the exhaust gas cooler and the exhaust gas negative pressure fan, and the exhaust gas containing EDC is adsorbed by the second adsorber.
The desorption time was continued for about 115 minutes by feeding steam through the first adsorber by means of a steam generator at a flow rate of about 0.5 ton/hour, then switched to a drying mode, fresh air was fed through the air heater using a fresh air fan, and then through the first adsorber at a flow rate of 10m/s for a drying process duration of about 80 minutes.
The whole process of the utility model realizes automation, effectively controls VOC discharged to the atmosphere, effectively recovers EDC, saves resources, avoids environmental pollution, and has obvious economic benefit and environmental protection benefit.
Claims (10)
1. An exhaust gas purifying and recovering apparatus, characterized by comprising:
i. the adsorption component comprises an exhaust gas cooler, a first adsorber, a second adsorber and an exhaust gas negative pressure fan;
a desorption regeneration assembly comprising a desorption primary cooler, a desorption secondary cooler, a recovery oil-water separation tank and a delivery pump;
a drying assembly comprising a fresh air fan and an air heater;
the apparatus includes a first adsorber connection state and a second adsorber connection state,
in the connection state of the first adsorber, the first adsorber is connected with an upstream tail gas condenser and a downstream tail gas negative pressure fan, the second adsorber is connected with the analysis regeneration assembly and is in an analysis state, or is connected with the drying assembly and is in a drying state, or is in a standby state,
and in the connection state of the second adsorber, the second adsorber is connected with an upstream tail gas condenser and a downstream tail gas negative pressure fan, and the first adsorber is connected with the analysis regeneration assembly to be in an analysis state, or is connected with the drying assembly to be in a drying state, or is in a standby state.
2. The apparatus of claim 1, wherein the first adsorber and the second adsorber each have a tail gas inlet at a bottom or lower portion thereof and a gas phase outlet at a top or upper portion thereof.
3. The apparatus of claim 1, wherein the first adsorber and the second adsorber are each a fixed bed packed with a particulate or pellet-shaped adsorbent.
4. The apparatus of claim 1, wherein the tail gas cooler, the resolving primary cooler, and the resolving secondary cooler are tubular heat exchangers and the air heater is a pin heat exchanger.
5. The apparatus of claim 1, wherein the gas phase outlet of the resolving secondary cooler, downstream of the resolving secondary cooler or upstream of the recovery oil-water separator tank is connected to the exhaust gas cooler or upstream of the exhaust gas cooler.
6. The apparatus of claim 1, wherein a differential pressure gauge is disposed upstream of the exhaust cooler and upstream of the exhaust negative pressure fan, and the differential pressure gauge is in data connection with the exhaust negative pressure fan.
7. The apparatus of claim 1, wherein a VOC on-line analysis device is provided at the exhaust negative pressure fan outlet, the VOC on-line analysis device in data connection with the first adsorber and the second adsorber, configured to control the apparatus to switch between a first adsorber connection state and a second adsorber connection state.
8. The apparatus of claim 1, wherein the primary cooler, the secondary cooler, and the tail gas cooler are liquid cooling devices, and temperature sensors are disposed at respective outlets.
9. The apparatus of claim 1, wherein a level controller is provided inside or outside the recovery oil-water separator tank.
10. The apparatus of claim 1, wherein the apparatus comprises an automated control system that is directly or indirectly data-connected with at least one component of the apparatus.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322011512.5U CN220656950U (en) | 2023-07-28 | 2023-07-28 | Tail gas purifying and recycling equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322011512.5U CN220656950U (en) | 2023-07-28 | 2023-07-28 | Tail gas purifying and recycling equipment |
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| Publication Number | Publication Date |
|---|---|
| CN220656950U true CN220656950U (en) | 2024-03-26 |
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| CN202322011512.5U Active CN220656950U (en) | 2023-07-28 | 2023-07-28 | Tail gas purifying and recycling equipment |
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| CN (1) | CN220656950U (en) |
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2023
- 2023-07-28 CN CN202322011512.5U patent/CN220656950U/en active Active
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