CN108452637B - Serial-type rotating wheel high-efficiency purification system and serial-type rotating wheel high-efficiency purification method - Google Patents

Serial-type rotating wheel high-efficiency purification system and serial-type rotating wheel high-efficiency purification method Download PDF

Info

Publication number
CN108452637B
CN108452637B CN201710086333.4A CN201710086333A CN108452637B CN 108452637 B CN108452637 B CN 108452637B CN 201710086333 A CN201710086333 A CN 201710086333A CN 108452637 B CN108452637 B CN 108452637B
Authority
CN
China
Prior art keywords
desorption
gas
adsorption
volatile organic
rotating wheel
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
Application number
CN201710086333.4A
Other languages
Chinese (zh)
Other versions
CN108452637A (en
Inventor
张丰堂
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
JG Environmental Technology Co Ltd
Original Assignee
JG Environmental Technology Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by JG Environmental Technology Co Ltd filed Critical JG Environmental Technology Co Ltd
Priority to CN201710086333.4A priority Critical patent/CN108452637B/en
Publication of CN108452637A publication Critical patent/CN108452637A/en
Application granted granted Critical
Publication of CN108452637B publication Critical patent/CN108452637B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/708—Volatile organic compounds V.O.C.'s
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/14—Gaseous waste or fumes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/10—Nitrogen; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/20—Sulfur; Compounds thereof
    • 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

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)

Abstract

A series-connection type rotating wheel high-efficiency purification system comprises a first rotating wheel, a second rotating wheel and incineration equipment. The first rotating wheel is provided with a first adsorption area and a first desorption area, and the first adsorption area is used for adsorbing VOCs and sending out a first adsorption treatment gas; the first desorption area is used for desorbing the VOCs and sending a first desorption treatment gas. The second rotating wheel is provided with a second adsorption area and a second desorption area, and the second adsorption area is used for adsorbing VOCs in the first adsorption treatment gas. The incineration equipment is used for incinerating VOCs in the first desorption treatment gas to generate incinerated gas. The invention is characterized in that the tail gas at the adsorption end of the first rotating wheel is subjected to secondary adsorption treatment by the second rotating wheel, so that the concentration of VOCs in the tail gas at the adsorption end of the second rotating wheel can be greatly reduced, and the aim of high-efficiency treatment is fulfilled.

Description

Serial-type rotating wheel high-efficiency purification system and serial-type rotating wheel high-efficiency purification method
Technical Field
The present invention relates to a system and a method for treating volatile organic compounds, and more particularly, to a system and a method for treating volatile organic compounds using a rotating wheel and an incineration facility.
Background
Organic solvents are widely used in many industries, some of which are Volatile to gases at room temperature and are therefore called Volatile Organic Compounds (VOCs), most of which are biologically toxic and therefore need to be disposed of before being discharged.
Incineration of volatile organic compounds using incineration plants is a common treatment; wherein, for the waste gas source with low content of volatile organic compounds, the absorption/desorption rotating wheel is often matched to carry out concentration treatment on the volatile organic compounds. The treatment efficiency of the existing high-efficiency rotating wheel to the volatile organic compounds can reach 90-95%, the concentration ratio can reach 10-25 times, namely, the concentration of the volatile organic compounds carried by desorption gas is 10-25 times higher than that of the gas to be treated, the desorption gas is subsequently introduced into incineration equipment, and the treatment efficiency of the existing incineration equipment to the volatile organic compounds can reach 95-99%. However, considering that the desorption gas contains volatile organic compounds with a concentration ratio as high as 10-25 times, the incineration exhaust gas of the incineration facility actually still contains many volatile organic compounds.
Because environmental regulations are becoming stricter and emission standards are gradually improved, the existing exhaust gas treatment system cannot completely meet the reduction standard of the air pollutant total amount control plan, so how to improve the treatment efficiency of the volatile organic compound treatment system is really worth thinking of people in the field.
On the other hand, after the volatile organic compound waste gas is incinerated by an incineration facility, volatile organic compounds with low concentration are still discharged, and if the volatile organic compounds containing nitrogen, sulfur, halogen or high boiling point are treated, derived pollutants such as nitrogen oxides, sulfur oxides SOx or derived particulate matters SS are generated after the treatment; however, the air quality monitoring data shows that the volatile organic compounds and the derivative pollutants such as NOx, SOx or SS replace the suspended particles to become the main pollutants affecting the air pollution index (PSI), and is one of the reduction standard items of the air pollutant total amount control plan, so the emission of the volatile organic compounds and the derivative pollutants such as NOx, SOx or SS must be intensively controlled, and these requirements must be considered comprehensively.
In order to effectively treat the volatile organic compounds, a new patent of TW M444870 "secondary volatile organic compound concentration treatment system" is proposed, which discloses a technique of treating the tail gas at the desorption end of a first rotating wheel by using a second rotating wheel (as shown in the second figure) or more rotating wheels (as shown in the fourth figure) in order to improve the disadvantages of the prior art incinerator for treating the tail gas at the desorption end of the first rotating wheel (as shown in the first figure), while the tail gas at the desorption end of the second rotating wheel is still treated by the incinerator (not shown in the figure); in other words, the technique disclosed by TW M444870 still involves the use of an incinerator. However, since the efficiency of removing the volatile organic compounds by the rotating wheel is generally lower than that of the incinerator, TW M444870 attempts to treat the desorption-end tail gas of the first rotating wheel by using the second rotating wheel instead of the conventional incinerator, but since the efficiency of removing the volatile organic compounds by the second rotating wheel is low, the concentration of the volatile organic compounds contained in the adsorption-end tail gas is rather higher than that of the incineration tail gas of the incinerator shown in the first figure. Therefore, the TW M444870 not only increases the equipment cost (additional rotating wheel is needed), but also the concentration of the volatile organic compounds in the exhaust gas is not decreased or increased, and obviously the aforementioned problems cannot be solved.
Disclosure of Invention
In view of the fact that the conventional VOC processing technology is not meeting the standards of the air pollutant total amount control program, the main object of the present invention is to provide a high-efficiency VOC processing system and method.
In order to achieve the above and other objects, the present invention provides a series-connected rotating wheel high efficiency purification system for treating a gas to be treated containing volatile organic compounds, which comprises a first rotating wheel, a second rotating wheel and an incineration device. The first rotating wheel is provided with a first adsorption area and a first desorption area, the first adsorption area is used for introducing the gas to be treated and adsorbing at least one part of volatile organic compounds in the gas to be treated and sending out a first adsorption treatment gas; the first desorption area is used for introducing a first desorption gas for desorbing the volatile organic compound adsorbed by the first rotating wheel and sending a first desorption treatment gas. The second rotating wheel is provided with a second adsorption area and a second desorption area, the second adsorption area is used for introducing the first adsorption treatment gas, adsorbing at least one part of volatile organic compounds in the first adsorption treatment gas and sending out a second adsorption treatment gas; the second desorption area is used for introducing a second desorption gas for desorbing the volatile organic compounds adsorbed by the second rotating wheel and sending a second desorption treatment gas. The incineration equipment is provided with an incineration unit, an air inlet and an exhaust port, wherein the air inlet and the exhaust port are communicated with the incineration unit, the air inlet is used for introducing first desorption treatment gas, the incineration unit is used for incinerating volatile organic compounds in the first desorption treatment gas to generate incinerated gas, and the exhaust port is used for exhausting at least part of the incinerated gas.
In order to achieve the above and other objects, the present invention further provides a serial-type rotating wheel high efficiency purification method, which can be applied to the serial-type rotating wheel high efficiency purification system, and comprises the following operations:
a first adsorption operation procedure: introducing a gas to be treated containing volatile organic compounds to the first adsorption area, adsorbing at least a part of the volatile organic compounds through the first adsorption area, and then sending out a first adsorption treatment gas;
a second adsorption operation procedure: introducing the first adsorption treatment gas into the second adsorption zone, and delivering a second adsorption treatment gas after at least a part of the volatile organic compounds are adsorbed by the second adsorption zone;
a first desorption operation procedure: introducing a first desorption gas to the first desorption area, wherein the first desorption gas desorbs the volatile organic compound adsorbed by the first rotating wheel from the first rotating wheel and sends a first desorption treatment gas;
a second desorption operation procedure: introducing a second desorption gas to the second desorption area, wherein the second desorption gas desorbs the volatile organic compounds adsorbed by the second rotating wheel from the second rotating wheel and sends a second desorption treatment gas; and
incineration operation procedure: the first desorption treatment gas is led into the incineration unit through the air inlet, and the volatile organic compounds in the first desorption treatment gas are incinerated through the incineration unit to generate an incinerated gas, and at least one part of the incinerated gas is discharged through the air outlet. Wherein the first adsorption operation procedure, the second adsorption operation procedure, the first desorption operation procedure and the second desorption operation procedure are performed substantially simultaneously.
Based on the above design, the present invention is characterized in that the tail gas from the adsorption end of the first rotor (i.e. the first adsorption process gas) is subjected to the second adsorption process by the second rotor, so that the concentration of the volatile organic compound in the tail gas from the adsorption end of the second rotor (i.e. the second adsorption process gas) can be substantially lower than the emission concentration of the conventional technology, thereby achieving the purpose of efficiently treating the volatile organic compound.
In other embodiments of the present invention, the incinerated gas discharged from the incinerating equipment is further introduced into the adsorption end of the first or second rotating wheel for reprocessing or is introduced into the desorption end of the first or second rotating wheel as desorption gas, so that the discharge flow rate of the incinerated gas to the outside is reduced or even not discharged to the outside, thereby further reducing the total discharge amount of volatile organic compounds.
In another embodiment of the present invention, the incinerated gas discharged from the incinerator is further purified by a reprocessing reactor to further remove the emission of volatile organic compounds, NOx, SOx, or SS derived pollutants from the incinerated gas.
Drawings
Fig. 1 is a schematic configuration diagram of a first embodiment of the present invention.
FIG. 2 is a front schematic view of a rotor suitable for use in the present invention.
Fig. 3 is a schematic configuration diagram of a second embodiment of the present invention.
Fig. 4 is a schematic configuration diagram of a third embodiment of the present invention.
Fig. 5 is a schematic configuration diagram of a fourth embodiment of the present invention.
Fig. 6 is a schematic configuration diagram of a fifth embodiment of the present invention.
FIG. 7 is a front schematic view of another rotor suitable for use in the present invention.
Fig. 8 is a schematic configuration diagram of a sixth embodiment of the present invention.
Fig. 9 is a schematic configuration diagram of a seventh embodiment of the present invention.
Fig. 10 is a schematic configuration diagram of an eighth embodiment of the present invention.
Detailed Description
Referring to fig. 1, there is shown a first embodiment of a tandem rotor high efficiency purification system (hereinafter referred to as purification system 1) according to the present invention, which comprises a first rotor 10, a second rotor 20, an incineration apparatus 30, a first heat exchanger 40, a second heat exchanger 50 and an exhaust stack 60, wherein the purification system 1 can be used to treat a gas to be treated containing volatile organic compounds, such as but not limited to petrochemical process waste gas, process waste gas using organic solvents and combustion waste gas, and the volatile organic compounds can be but not limited to toluene, xylene, p-xylene, ethylbenzene, styrene, formaldehyde, acetaldehyde, Isopropanol (IPA), Propylene Glycol Methyl Ether Acetate (PGMEA), Hexamethyldisilazane (HMDS), Trichloroethylene (TCE), Monoethanolamine (MEA) and dimethyl sulfoxide (DMSO), other possible volatile organic compounds are alkanes, aromatic hydrocarbons, alkenes, halogenated hydrocarbons, esters, aldehydes and ketones.
Referring to fig. 2, when the first rotating wheel 10 rotates in a rotating direction during operation, the wheel surface of the first rotating wheel 10 can be divided into a first adsorption region 11, a first desorption region 12 and a first cooling isolation region 13 according to the operation purpose, wherein the first cooling isolation region 13 is disposed between the first adsorption region 11 and the first desorption region 12, so that the adsorbing material carried by the first rotating wheel 10 sequentially passes through the first adsorption region 11, the first desorption region 12 and the first cooling isolation region 13 during operation, the used adsorbing material depends on the volatile organic compound to be adsorbed, and the adsorbing material can be, but is not limited to, hydrophilic or super-hydrated zeolite, activated carbon, activated alumina, silica gel or a combination thereof, wherein the hydrophilic zeolite is, for example, MCM a type, 13X type or low silica-alumina type Y zeolite, the super-alumina is, for example, ZSM-5 type, Mobil composite of zeolite or high silica-alumina type Y zeolite, the MCM-type zeolite may be, for example, zeolite of the M41S family such as MCM-41 having a hexagonal crystal structure (hexagonal), MCM-48 having a cubic structure (cubic), or MCM-50 having a layered structure (lamellar).
Similar to the first runner 10, the wheel surface of the second runner 20 can be divided into a second adsorption region, a second desorption region and a second cooling isolation region according to the working purpose, the front view thereof is equivalent to that shown in fig. 2, the second cooling isolation region is disposed between the second adsorption region and the second desorption region, so that the adsorption material carried by the second runner 20 sequentially passes through the second adsorption region, the second desorption region and the second cooling isolation region during the working, and the second runner can use the same or different adsorption material as the first runner, and depends on the volatile organic compound to be adsorbed. In addition, the first and second rotors 10 and 20 may also include other components such as rotor supports, axles, and supports that do not substantially participate in the absorption and desorption actions, which are not shown in the drawings.
The incineration apparatus 30 has an incineration unit 31, an air inlet 32 and an air outlet 33. In the present invention, applicable incineration apparatuses include, but are not limited to, regenerative direct-fired incinerators, such as double-tank regenerative thermal incinerators, triple-tank regenerative thermal incinerators, and rotary valve regenerative thermal incinerators. In this embodiment, the incineration equipment 30 is a dual-tank thermal storage incinerator, so the incineration unit 31 has two thermal storage tanks 311, 312 and a combustion chamber 313 communicated between the two thermal storage tanks 311, 312, each of the two thermal storage tanks 311, 312 has one air inlet 32 and one air outlet 33, a control valve set (not shown) is disposed on a pipeline connecting the air inlets 32, 33, one of the thermal storage tanks 311, 312 opens only the air inlet 32, and the other opens only the air outlet 33, the control valve set controls the opening and closing of the air inlet 32, the air outlet 33 to periodically adjust the direction of the air flow, so that the air flow can sequentially flow through the thermal storage tank 311, the combustion chamber 313 and the thermal storage tank 312, or sequentially flow through the thermal storage tank 312, the combustion chamber 313 and the thermal storage tank 311. The regenerators 311, 312 are filled with a heat medium (heat medium) for exchanging heat with the gas flowing through the incinerator 30, and suitable heat medium may be, but not limited to, Alumina ceramic (Alumina Oxide porcellain), porous Mullite (Mullite), Cordierite (Cordierite), porous Cordierite, and other heat-storing ceramic or gravel.
The first and second heat exchangers 40, 50 are each used for heat exchange of two gas streams, i.e., transferring heat from a hot fluid to a cold fluid, and suitable heat exchangers can be, but are not limited to, coiled plate heat exchangers, and shell and tube heat exchangers. A portion of the incinerated gases of the incineration facility 30 may be diverted from the combustion chamber 313 of the incineration unit 31 to the first and second heat exchangers 40, 50 as the hot fluid. In this embodiment, the incinerated gas as the hot fluid flows through the first and second heat exchangers 40 and 50 in sequence.
The above-described purification system 1 can be applied to a tandem type rotating wheel high efficiency purification method (hereinafter referred to as purification method) including the following operation procedures:
a first adsorption operation procedure: introducing the gas to be treated containing the volatile organic compounds into the first adsorption zone 11 of the first rotating wheel 10, adsorbing at least a part of the volatile organic compounds by the adsorbing materials in the first adsorption zone 11, and sending the treated gas as a first adsorption treatment gas from the other side of the first rotating wheel 10.
A second adsorption operation procedure: the first adsorption-treated gas is reintroduced into the second adsorption zone of second wheel 20, at least a portion of the volatile organic compounds are adsorbed by the adsorbent material in the second adsorption zone, and the treated gas is delivered from the other side of second wheel 20 as a second adsorption-treated gas. The second adsorption process gas after the two adsorption processes usually contains only a very small amount of volatile organic compounds, and can be pumped to the exhaust stack 60 by the blower 71 or used for other applications.
A first desorption operation procedure: the adsorbing material of the first rotor 10 adsorbs a considerable amount of the volatile organic compounds during the first adsorbing operation, so that the operation introduces the first desorption gas into the first desorption region 12 of the first rotor 10, so that the first desorption gas can desorb the volatile organic compounds adsorbed by the first rotor 10, and then the gas containing high concentration of volatile organic compounds is sent out from the other side of the first rotor 10 as the first desorption treatment gas; in order to improve the desorption efficiency, the first desorption gas can be raised to a higher temperature, so in this embodiment, the first desorption gas is first introduced into the first cooling isolation region 13 for preheating before entering the first desorption region 12, and then introduced into the first heat exchanger 40 for heat exchange with the incinerated gas; in this embodiment, the first desorption gas is composed of clean air and a portion of the gas to be treated, but not limited thereto.
A second desorption operation procedure: the adsorbing material of the second rotating wheel 20 adsorbs a considerable amount of volatile organic compounds in the second adsorption process, so that the process introduces a second desorption gas into the second desorption region of the second rotating wheel 20, so that the second desorption gas can desorb the volatile organic compounds adsorbed by the second rotating wheel 20, and then the gas containing higher concentration volatile organic compounds is sent out from the other side of the second rotating wheel 20 as a second desorption process gas; in order to improve the desorption efficiency, the second desorption gas can also be raised to a higher temperature, so in this embodiment, the second desorption gas is further introduced into the second cooling isolation region for preheating before entering the second desorption region, and then introduced into the second heat exchanger 50 for heat exchange with the incinerated gas; in this embodiment, the second desorption gas is branched from a portion of the first adsorption process gas; in addition, since the content of the volatile organic compounds in the second desorption process gas is equivalent to that of the gas to be treated, the gas to be treated can be merged and then introduced into the first adsorption zone 11 of the first rotor 10 to perform the first adsorption process again, and the residual heat of the second desorption process gas can raise the temperature of the gas to be treated before entering the first adsorption zone 11, reduce the relative humidity, and thus increase the removal rate of the volatile organic compounds in the first rotor 10, in which case the first rotor 10 preferably uses a hydrophobic zeolite adsorbent.
Incineration operation procedure: the first desorption treatment gas containing high concentration of volatile organic compounds is extracted by another fan 72 and introduced into the incineration unit 31 through the air inlet 32, the volatile organic compounds in the first desorption treatment gas are incinerated by the incineration unit 31 to generate an incinerated gas, a part of the incinerated gas is discharged from the air outlet 33, the other part of the incinerated gas is branched from the combustion chamber 313 of the incineration unit 31 to be used as a heat exchange gas, and the incinerated gas after heat exchange is further merged with the incinerated gas discharged from the air outlet 33 and is discharged through the discharge chimney 60 or used for other applications.
The first adsorption operation procedure, the second adsorption operation procedure, the first desorption operation procedure, and the second desorption operation procedure are substantially simultaneous based on the operating characteristics of the runner. In the usual case, the incineration process also takes place substantially simultaneously.
In one numerical simulation, the purification system 1 was fed with 2000SCMM (m3/min) of gas to be treated, wherein the voc content was 20ppmv, and after the gas to be treated was combined with 100SCMM of second desorption-treated gas, 1975SCMM was fed into the first adsorption zone of the first rotor 10 for the first adsorption operation sequence, and 125SCMM of gas to be treated was fed into the first desorption zone as the first desorption gas for the first desorption operation sequence; wherein, the volatile organic compound removal rate of the first rotating wheel 10 is 95%, the concentration ratio is about 16 times, the volatile organic compound removal rate of the second rotating wheel 20 is 90%, the concentration ratio is about 17 times, and the volatile organic compound removal rate of the incineration equipment 30 is 98%; under these conditions, the voc content of the 1975SCMM first adsorptive process gas may be reduced to 1ppmv, wherein 1875SCMM first adsorptive process gas is directed to the second adsorption zone of second wheel 20 for the second adsorption operation, and the voc content of the treated second adsorptive process gas may be further reduced to 0.1ppmv, and directed to exhaust stack 60 at a flow rate of 1875 SCMM; on the other hand, the first 100SCMM desorption process gas is introduced into the second desorption zone of the second runner 20 as a second desorption gas and subjected to a second desorption operation procedure, and then the 100SCMM second desorption process gas is sent out, the concentration of volatile organic compounds of which is about 17ppmv, and is mixed with the gas to be treated, so that the temperature is increased and the relative humidity is reduced; in addition, the concentration of the volatile organic compounds in the first desorption treatment gas sent by the first desorption operation procedure is about 320ppmv, and the first desorption treatment gas is introduced into the incineration equipment 30 for incineration operation procedure at a flow rate of 125SCMM, wherein the high-temperature incinerated gas of 15SCMM is sequentially guided to the first heat exchanger 40 and the second heat exchanger 50 for heat exchange, and then is merged with the rest gas of 110SCMM after incineration, so that the incinerated gas with a total flow rate of 125SCMM and a volatile organic compound concentration of about 6.4ppmv is sent to the emission chimney, and finally the emission chimney emits the incinerated tail gas with a total amount of 2000SCMM and a volatile organic compound concentration of about 0.5 ppmv. In other words, the total removal rate of volatile organic compounds in the purification system can reach 97.5%, which is a quite excellent treatment efficiency.
Compared with the conventional purification system, the purification system and the purification method can obviously reduce the concentration of the volatile organic compounds in the exhaust gas without additionally adding incineration equipment, and can fully recover heat energy, thereby realizing the effect of energy conservation.
Referring to fig. 3, a second embodiment of the purification system of the present invention is shown, which is mostly the same as that shown in the first embodiment, and the difference is that the purification system 100 of the second embodiment further comprises a re-purification reactor 180 and an ozone supply unit 190, the ozone supply unit 190 is used for supplying ozone to the incinerated gas, the re-purification reactor 180 has a reaction chamber 181 and a water supply unit 182 disposed in the reaction chamber 181, the water supply unit 182 is, for example, a sprayer and can be used for increasing the moisture content in the reaction chamber 181, and the reaction chamber 181 can be further provided with a catalyst adsorption material 183; thus, a re-purification process can be performed, in which ozone is introduced into the reaction chamber 181, so that ozone and water vapor can act in the reaction chamber 181 to generate high-activity hydroxyl radicals, and further, NOx (insoluble in water) possibly present in the incinerated gas can be purified and reacted into nitric acid (highly water-soluble), SOx (insoluble in water) possibly present can be purified and reacted into sulfuric acid (highly water-soluble), or organic suspended particles SS (having a high boiling point) possibly present can be purified and reacted into carbon dioxide and water, and finally a purified gas is discharged.
In a numerical simulation, the incinerated gas had 4.24ppmv volatile organic compounds, 100ppmv NOx, 5ppmv SOx, and 1mg/Nm3 SS, which could be purified to only 0.424ppmv volatile organic compounds, 20ppmv NOx, 0.5ppmv SOx, and 0.5mg/Nm3 SS after a re-purification treatment. Therefore, the concentration of the air pollutants in the exhaust gas is further reduced.
Referring to fig. 4, a third embodiment of the purification system 200 of the present invention is mainly different from the first embodiment in that the incinerated gas containing low concentration of volatile organic compounds is combined with the gas to be treated, the waste heat of the incinerated gas can be used to raise the temperature of the gas to be treated and lower the relative humidity thereof, and the gas can have higher adsorption efficiency when being introduced into the first adsorption zone of the first rotating wheel 210 for the first adsorption process again. In other words, only the second adsorption treatment gas treated by the second rotating wheel 220 is discharged, and the incinerated gas is not discharged, so that the content of the volatile organic compounds in the exhaust gas can be further reduced.
In one numerical simulation, the purification system 200 was fed 2000SCMM of gas to be treated, with a 20ppmv voc concentration, and the concentration of voc was about 17.6ppmv after the gas to be treated was combined with 100scm of second desorption gas and 125scm of incinerated gas, wherein 2100scm was fed into the first adsorption zone of the first rotor 210 for the first adsorption process and 125scm of gas to be treated was fed into the first desorption zone as the first desorption gas for the first desorption process; wherein, the volatile organic compound removal rate of the first rotating wheel 210 is 95%, the concentration ratio is about 18 times, the volatile organic compound removal rate of the second rotating wheel 220 is 90%, the concentration ratio is about 19 times, and the volatile organic compound removal rate of the incineration equipment 230 is 98%; under these conditions, the voc content of the 2100SCMM first adsorptive process gas may be reduced to 0.88ppmv, wherein the 2000SCMM first adsorptive process gas is directed to the second adsorption zone of the second rotating wheel 220 for the second adsorption operation, and the voc content of the treated second adsorptive process gas may be further reduced to about 0.09ppmv, and directed to the discharge stack 260 at a flow rate of 2000 SCMM; on the other hand, the first 100SCMM desorption process gas is introduced into the second desorption zone of the second runner 220 as a second desorption gas and subjected to a second desorption operation procedure, and then the 100SCMM second desorption process gas is sent out, the concentration of volatile organic compounds of which is about 17ppmv, and is mixed with the gas to be treated, so that the temperature is increased and the relative humidity is reduced; in addition, the concentration of the volatile organic compounds in the first desorption process gas sent by the first desorption process is about 320ppmv, and the first desorption process gas is introduced into the incineration equipment 230 for incineration process at a flow rate of 125SCMM, wherein the high-temperature incinerated gas of 15SCMM is sequentially introduced into the first and second heat exchangers 240 and 250 for heat exchange, and then is merged with the rest gas of 110SCMM after incineration to form an incinerated gas with a total flow rate of 125SCMM and a concentration of the volatile organic compounds of about 6.4ppmv, and then is mixed with the gas to be treated for retreatment.
Finally, the exhaust stack is externally exhausted by exhaust tail gas with the total amount of 2000SCMM and the concentration of volatile organic compounds of about 0.09ppmv, namely, the total removal rate of the volatile organic compounds of the purification system can reach more than 99.5 percent, and the treatment efficiency is very excellent.
Referring to fig. 5, a fourth embodiment of the purification system 400 of the present invention is shown, which mainly differs from the third embodiment in that the second heat exchanger is omitted, and a part of the second adsorbed process gas is branched off and merged with the incinerated gas after heat exchange to be used as the second desorption gas, and then introduced into the second desorption zone of the second wheel 420 for the second desorption process. The embodiment has the advantages of further saving the construction and maintenance cost of one heat exchanger, more fully utilizing the heat energy and realizing the purpose of energy saving.
In one numerical simulation, the purification system 400 was fed 2000SCMM of gas to be treated having a voc content of 20ppmv, and the concentration of voc was about 17.6ppmv after the gas to be treated was combined with 115scm of second desorption gas and 110scm of incinerated gas, wherein 2100scm was fed into the first adsorption zone of the first rotor 410 for the first adsorption process and 125scm of gas to be treated was fed into the first desorption zone as the first desorption gas for the first desorption process; wherein the first rotating wheel 410 has a voc removal rate of 95% and a concentration ratio of about 18 times, the second rotating wheel 420 has a voc removal rate of 90% and a concentration ratio of about 19 times, and the incineration apparatus 430 has a voc removal rate of 98%; under these conditions, the volatile organic compound content of the 2100SCMM first adsorptive process gas may be reduced to 0.88ppmv and subsequently introduced into the second adsorption zone of second wheel 420 for the second adsorption operation, and the volatile organic compound content of the treated second adsorptive process gas may be further reduced to about 0.09ppmv and introduced into discharge stack 460 at a 2000SCMM flow rate; on the other hand, the 100SCMM second adsorption process gas and the 15SCMM incinerated gas after heat exchange process are merged to be used as a second desorption gas, and are introduced into a second desorption region of the second runner 420 for a second desorption operation procedure, and then the 115SCMM second desorption process gas is sent out, the concentration of volatile organic compounds is about 17ppmv, and then the second desorption process gas is mixed with the gas to be processed, so that the temperature of the gas to be processed is increased and the relative humidity of the gas to be processed is reduced; in addition, the concentration of the volatile organic compounds in the first desorption process gas from the first desorption process is about 320ppmv, and the volatile organic compounds are introduced into the incineration facility 430 at a flow rate of 125SCMM for incineration, wherein the high-temperature incinerated gas of 15SCMM is guided to the first heat exchanger 440 for heat exchange, and then combined with the second adsorption process gas of 100SCMM to be used as the second desorption gas. On the other hand, the remaining 110SCMM, incinerated gas having a concentration of about 6.4ppmv volatile organic compounds, is mixed with the gas to be treated and reintroduced into the first wheel 410 for the first adsorption process.
Finally, the exhaust stack was vented to the outside in a total of 2000SCMM with a voc concentration of about 0.09ppmv, i.e., the present example was similar to the third example in high efficiency treatment, with one heat exchanger omitted.
Referring to fig. 6, a fifth embodiment of the purification system 500 of the present invention is shown, wherein the purification system 500 comprises a first rotating wheel 510, a second rotating wheel 520, an incineration apparatus 530, a heat exchanger 540, a re-purification reactor 550 and an ozone supply unit 560.
Referring to fig. 7, when the first wheel 510 rotates in a rotation direction during operation, the wheel surface of the first wheel 510 can be divided into a first adsorption area 511 and a first desorption area 512 according to the purpose of the operation, so that the adsorption material carried by the first wheel 510 sequentially passes through the first adsorption area 511 and the first desorption area 512 during operation. In this embodiment, the first rotor 510 substantially consists of only the first adsorption region 511 and the first desorption region 512, but does not include a cooling isolation region, but the first rotor 510 may further include other components such as a rotor holder, a wheel shaft, a support frame, etc. that do not substantially participate in the adsorption and desorption actions, which are not shown in the drawings.
The second wheel 520 may be divided into a second adsorption region, a second desorption region and a second cooling isolation region according to the working purpose, the front view of which is similar to that of fig. 2, the second cooling isolation region is disposed between the second adsorption region and the second desorption region, so that the adsorption material carried by the second wheel 520 sequentially passes through the second adsorption region, the second desorption region and the second cooling isolation region during working.
The incineration apparatus 530 has an incineration unit 531, an air inlet 532 and an air outlet 533. In this embodiment, the incineration apparatus 530 is a rotary valve type thermal storage incinerator, so the incineration unit 531 comprises a rotary valve 5311, a plurality of thermal storage tanks 5312 filled with thermal storage material, and a combustion chamber 5313, the thermal storage tanks 5312 are connected between the rotary valve 5311 and the combustion chamber 5313, and the air inlets 532 and the air outlets 533 are disposed on the rotary valve 5311.
The heat exchanger 540 is used for heat exchange of two gas streams, which is to transfer heat from a hot fluid to a cold fluid, and a portion of the incinerated gas in the incinerator 530 can be diverted from the combustion chamber 5313 of the incinerator unit 531 to the heat exchanger 540 as the hot fluid.
The ozone supply unit 560 is used for supplying ozone to the incinerated gas, and the re-purification reactor 550 has a reaction chamber 551 and a water supply unit 552 disposed in the reaction chamber 551, wherein the water supply unit 552 is a sprayer for increasing the moisture content in the reaction chamber 551, and a catalyst material 553 is disposed in the reaction chamber 551.
The above-described decontamination system 500 may be applied to a decontamination method comprising the following procedures:
a first adsorption operation procedure: the gas to be treated containing the volatile organic compounds is introduced into the first adsorption zone 511 of the first rotary wheel 510, at least a part of the volatile organic compounds are adsorbed by the adsorbent in the first adsorption zone 511, and the treated gas is sent out from the other side of the first rotary wheel 510 as a first adsorption treatment gas.
A second adsorption operation procedure: the first adsorption-treated gas is reintroduced into the second adsorption zone of the second wheel 520, at least a portion of the volatile organic compounds are adsorbed by the adsorbent material in the second adsorption zone, and the treated gas is delivered from the other side of the second wheel 520 as a second adsorption-treated gas. The second adsorption process gas after the two adsorption processes usually contains only a very small amount of volatile organic compounds, and can be pumped to the exhaust stack by the fan 571 or used for other applications.
A first desorption operation procedure: since the adsorbing material of the first rotor 510 adsorbs a considerable amount of the voc during the first adsorbing operation, the operation introduces the first desorption gas into the first desorption region 512 of the first rotor 510, so that the first desorption gas can desorb the voc adsorbed by the first rotor 510, and then the gas containing high concentration of the voc is discharged from the other side of the first rotor 510 as the first desorption process gas.
A second desorption operation procedure: the adsorbing material of the second wheel 520 adsorbs a considerable amount of the volatile organic compounds during the second adsorption process, so that the process introduces the second desorption gas into the second desorption region of the second wheel 520, so that the second desorption gas can desorb the volatile organic compounds adsorbed by the second wheel 520, and then the gas containing the volatile organic compounds with higher concentration is sent out from the other side of the second wheel 520 as the second desorption process gas; in order to improve the desorption efficiency, the second desorption gas can be raised to a higher temperature, so in this embodiment, the second desorption gas is further introduced into the second cooling isolation region for preheating before entering the second desorption region, and then introduced into the heat exchanger 540 for heat exchange with the incinerated gas; in this embodiment, the second desorption gas is branched from a portion of the first adsorption gas, and the second desorption gas still has a higher temperature, so that the second desorption gas can be directly introduced into the first desorption region 512 of the first rotor 510 to be used as the first desorption gas.
Incineration operation procedure: the first desorption process gas containing high concentration of volatile organic compounds is extracted by another fan 572 and introduced into the incineration unit 531 through the gas inlet 532, the volatile organic compounds in the first desorption process gas are incinerated by the incineration unit 531 to generate an incinerated gas, a part of the incinerated gas is discharged from the gas outlet 533, the other part of the incinerated gas is branched from the combustion chamber 5313 of the incineration unit 531 to be used as a heat exchange gas, the incinerated gas passing through the heat exchanger 540 contains a small amount of volatile organic compounds, and thus can be introduced into the first adsorption region 511 of the first rotary wheel 510 for reprocessing, and the incinerated gas can be mixed with the gas to be processed before being introduced into the first rotary wheel 510.
A re-purification operation procedure: ozone is introduced into the reaction chamber 551, so that ozone and water vapor can act in the reaction chamber 551 to generate high-activity hydroxyl radicals, and further NOx (insoluble in water) possibly existing in the incinerated gas can be purified and reacted into nitric acid (high water solubility), SOx (insoluble in water) possibly existing in the incinerated gas can be purified and reacted into sulfuric acid (high water solubility), or organic suspended particles SS (high boiling point) possibly existing in the incinerated gas can be purified and reacted into carbon dioxide and water, and finally a purified gas is sent out.
The first adsorption operation procedure, the second adsorption operation procedure, the first desorption operation procedure, and the second desorption operation procedure are substantially simultaneous based on the operating characteristics of the runner. In the usual case, the incineration process and the re-decontamination process also take place substantially simultaneously.
Based on the above design, both the second adsorption process gas delivered by the second wheel 520 and the purified gas delivered by the re-purification chamber 550 in this embodiment contain only a trace amount of volatile organic compounds, and can be directly discharged as the exhaust gas. Compared with the conventional purification system, the purification system and the purification method greatly reduce the concentration of volatile organic compounds in the exhaust gas without additionally adding incineration equipment, and can fully recover heat energy to realize the effect of energy conservation.
Referring to fig. 8, a sixth embodiment of the purification system of the present invention is shown, and the purification system 600 of the present embodiment is mostly similar to the fifth embodiment, except that the incinerated gas flowing through the heat exchanger 640 is not guided to the first adsorption region of the first rotary wheel 610, and the purification system 600 further includes a thermometer 671, a control valve 672 and a controller 673, the controller 673 is in signal connection with the thermometer 671 and the control valve 672 respectively, the thermometer 671 is used for detecting the temperature of the first desorption gas, the control valve 672 is used for adjusting the flow rate of the heat-exchanged incinerated gas merged to the second desorption process gas, the controller 673 controls the control valve 672 to adjust the flow rate according to the temperature detected by the thermometer 671, and the incinerated gas not merged with the second desorption process gas is merged with the incinerated gas discharged from the exhaust port 633.
Accordingly, if the temperature of the first desorption gas measured by the thermometer 671 is lower than the default operating temperature, the controller 673 controls the control valve 672 to increase the flow rate of the incinerated gas flowing to the second desorption process gas, and since the temperature of the incinerated gas is higher than the temperature of the second desorption process gas, the temperature of the flow-adjusted first desorption gas can be increased until the temperature is increased to the default operating temperature.
Referring to fig. 9, a seventh embodiment of the purification system of the present invention is shown, and the purification system 700 of the present embodiment is mostly the same as the second embodiment, and the main difference is that the incineration facility 730 is a three-tank type regenerative thermal incinerator, and the incinerated gas flowing through the first heat exchanger 740 is not guided to another heat exchanger, but directly joins with the incinerated gas exhausted from the exhaust port 733; alternatively, the purification system 700 further comprises a temperature raising device 770 for raising the temperature of the second desorption gas, wherein the temperature raising device 770 can be, but is not limited to, another type of heat exchanger, and the heat source can be steam, hot oil, hot air or electric heat.
Referring to fig. 10, a purification system 800 according to an eighth embodiment of the present invention is mainly the same as the seventh embodiment, and the main difference is that the incinerated gas is merged with the first adsorption treatment gas and then introduced into the second adsorption zone of the second wheel 820 to perform the second adsorption operation procedure, so as to further reduce the concentration of the volatile organic compounds before being discharged.
Finally, it should be noted that the components disclosed in the above embodiments are only for illustrative purposes and are not intended to limit the scope of the present disclosure, and other equivalent components may be substituted or modified and shall be covered by the claims of the present disclosure.

Claims (2)

1. An in-line rotary high efficiency purification system for treating a gas to be treated containing volatile organic compounds, comprising:
a first rotating wheel, which is provided with a first adsorption area and a first desorption area, wherein the first adsorption area is used for introducing the gas to be treated, adsorbing at least a part of volatile organic compounds in the gas to be treated and sending out a first adsorption treatment gas; the first desorption area is used for introducing a first desorption gas for desorbing the volatile organic compound adsorbed by the first rotating wheel and sending a first desorption treatment gas;
a second rotating wheel having a second adsorption region and a second desorption region, the second adsorption region being used for introducing the first adsorption treatment gas, adsorbing at least a part of volatile organic compounds in the first adsorption treatment gas and sending out a second adsorption treatment gas; the second desorption area is used for introducing a second desorption gas for desorbing the volatile organic compound adsorbed by the second rotating wheel and sending a second desorption treatment gas; and
an incineration device, having an incineration unit, an air inlet and an exhaust port, wherein the air inlet and the exhaust port are both communicated with the incineration unit, the air inlet is used for leading in the first desorption treatment gas, the incineration unit is used for incinerating volatile organic compounds in the first desorption treatment gas to generate an incinerated gas, the exhaust port is used for discharging at least a part of the incinerated gas, and at least a part of the incinerated gas is led into the first adsorption area, the first desorption area, the second adsorption area or the second desorption area;
wherein the second desorption treatment gas delivered from the second desorption zone is introduced into the first adsorption zone of the first rotating wheel;
wherein the second wheel further has a second cooling isolation region between the second adsorption region and the second desorption region, and the second desorption gas is introduced into the second cooling isolation region before being introduced into the second desorption region.
2. A serial runner high-efficiency purification method is applied to a serial runner high-efficiency purification system, the serial runner high-efficiency purification system comprises a first runner, a second runner and incineration equipment, the first runner is provided with a first adsorption area and a first desorption area, the second runner is provided with a second adsorption area and a second desorption area, the incineration equipment is provided with an incineration unit, an air inlet and an air outlet, the air inlet and the air outlet are both communicated with the incineration unit, the serial runner high-efficiency purification method comprises the following operation procedures:
a first adsorption operation procedure: introducing a gas to be treated containing volatile organic compounds to the first adsorption area, adsorbing at least a part of the volatile organic compounds through the first adsorption area, and then sending out a first adsorption treatment gas;
a second adsorption operation procedure: introducing the first adsorption treatment gas into the second adsorption zone, and delivering a second adsorption treatment gas after at least a part of the volatile organic compounds are adsorbed by the second adsorption zone;
a first desorption operation procedure: introducing a first desorption gas to the first desorption area, wherein the first desorption gas desorbs the volatile organic compound adsorbed by the first rotating wheel from the first rotating wheel and sends a first desorption treatment gas;
a second desorption operation procedure: introducing a second desorption gas to the second desorption area, wherein the second desorption gas desorbs the volatile organic compounds adsorbed by the second rotating wheel from the second rotating wheel and sends a second desorption treatment gas; and
incineration operation procedure: introducing the first desorption treatment gas into the incineration unit through the gas inlet, and incinerating volatile organic compounds in the first desorption treatment gas through the incineration unit to generate incinerated gas, wherein at least one part of the incinerated gas is discharged through the gas outlet, and at least one part of the incinerated gas is introduced into the first adsorption area, the first desorption area, the second adsorption area or the second desorption area;
wherein the first adsorption operation procedure, the second adsorption operation procedure, the first desorption operation procedure and the second desorption operation procedure are performed substantially simultaneously;
wherein the second desorption treatment gas delivered from the second desorption zone is introduced into the first adsorption zone of the first rotating wheel.
CN201710086333.4A 2017-02-17 2017-02-17 Serial-type rotating wheel high-efficiency purification system and serial-type rotating wheel high-efficiency purification method Active CN108452637B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201710086333.4A CN108452637B (en) 2017-02-17 2017-02-17 Serial-type rotating wheel high-efficiency purification system and serial-type rotating wheel high-efficiency purification method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201710086333.4A CN108452637B (en) 2017-02-17 2017-02-17 Serial-type rotating wheel high-efficiency purification system and serial-type rotating wheel high-efficiency purification method

Publications (2)

Publication Number Publication Date
CN108452637A CN108452637A (en) 2018-08-28
CN108452637B true CN108452637B (en) 2020-05-05

Family

ID=63229096

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201710086333.4A Active CN108452637B (en) 2017-02-17 2017-02-17 Serial-type rotating wheel high-efficiency purification system and serial-type rotating wheel high-efficiency purification method

Country Status (1)

Country Link
CN (1) CN108452637B (en)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
TWI686233B (en) * 2018-10-30 2020-03-01 華懋科技股份有限公司 Runner system with high temperature desorption and its method
CN110465159A (en) * 2019-07-25 2019-11-19 江苏苏净集团有限公司 A kind of processing exhaust gas adsorption runner device
CN115445387A (en) * 2022-08-23 2022-12-09 江苏中电创新环境科技有限公司 Treatment system and method for high-air-volume low-concentration organic waste gas

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5167679A (en) * 1990-03-31 1992-12-01 Taikisha Ltd. Rotary gas treating apparatus
CN101963359B (en) * 2009-07-24 2014-01-15 杰智环境科技股份有限公司 Energy saving device of incineration treatment system for nitrogen nitrogen- or/and sulphur-containing volatile organic matters
CN203315969U (en) * 2013-03-29 2013-12-04 无锡中舜成环保科技有限公司 Zero-energy consumption purifying device for volatile organic compounds
CN104107618B (en) * 2014-08-07 2017-02-08 石家庄天龙环保科技有限公司 Low-concentration large-air-volume waste gas concentration and wind reduction system
CN105597490B (en) * 2014-11-20 2020-12-01 杰智环境科技股份有限公司 Organic waste gas adsorption, desorption, concentration and purification system and method thereof
CN205127672U (en) * 2015-09-22 2016-04-06 江苏中研宜普科技有限公司 Two energy -saving concentrated runners and RTO's organic waste gas processing system
CN205252836U (en) * 2015-11-13 2016-05-25 惠州市环发环保科技有限公司 Runner adsorbs concentrated RTO waste gas treatment system
CN205481039U (en) * 2016-02-04 2016-08-17 杰智环境科技股份有限公司 Use concentrated purification treatment system of waste gas of incinerator heat recovery
CN106139821A (en) * 2016-08-31 2016-11-23 霍普科技（天津）股份有限公司 A kind of zeolite runner Adsorption Concentration purifier
CN206715626U (en) * 2017-02-17 2017-12-08 杰智环境科技股份有限公司 Runner high efficiency cleaning system

Also Published As

Publication number Publication date
CN108452637A (en) 2018-08-28

Similar Documents

Publication Publication Date Title
TWI629092B (en) High efficiency purification system and method using series-connected rotary wheels
US11014044B2 (en) Waste gas purification system and method
CN105749695B (en) A kind of low concentration, Wind Volume, high peculiar smell exhaust gas concentration energy equipment and its technique
CN103331086A (en) Movable integrated device for treating organic waste gas
CN206715626U (en) Runner high efficiency cleaning system
CN108452637B (en) Serial-type rotating wheel high-efficiency purification system and serial-type rotating wheel high-efficiency purification method
US20080063581A1 (en) Systems and methods for removing materials from flue gas via regenerative selective catalytic reduction
JP5810488B2 (en) Wastewater treatment system
TWM548246U (en) Rolling-wheel ultra-efficient purification system
US20230356142A1 (en) Voc treatment rotor system and voc treatment method
CN207153400U (en) A kind of organic exhaust gas regenerative oxidation device
KR20160012277A (en) Apparatus for Treating Waste Gas comprising VOCs From Pretreatment system
JP2010214285A (en) Gas treatment method
KR100889639B1 (en) Apparatus for destruction of volatile organic compounds
KR20160140533A (en) Apparatus for Treating Waste Gas comprising VOCs From Pretreatment system
TWM614915U (en) Tail gas nitrogen oxide re-purification device and exhaust gas purification system of incineration unit
CN213132566U (en) Molecular sieve runner system for treating waste gas of gravure printing
TWM619713U (en) High performance waste gas purification system
TWI779384B (en) Organic waste gas adsorption, desorption, concentration and purification system and method capable of increasing temperature and controlling humidity
CN208194032U (en) Waste gas catalytic combustion processing unit
TWI836468B (en) High-efficiency exhaust gas purification system and high-efficiency exhaust gas purification method
CN218794966U (en) Purification treatment system for waste gas containing volatile organic compound
TWI789962B (en) Green house gas purification system
CN216395815U (en) High-effect waste gas purification system
TWM634456U (en) High performance waste gas purification system

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant
TR01 Transfer of patent right

Effective date of registration: 20221109

Address after: Taoyuan County, Taiwan, China Longtan District, Gaoping village, Feng Road, Gaoping section 8

Patentee after: JG ENVIRONMENTAL TECHNOLOGY Co.,Ltd.

Address before: No. 8, Gaoping Section, Zhongfeng Road, Gaoping Village, Longtan District, Taoyuan City

Patentee before: JG ENVIRONMENTAL TECHNOLOGY Co.,Ltd.

Patentee before: Zhang Fengtang

TR01 Transfer of patent right