CN219571942U - High-concentration organic waste gas combined purification system - Google Patents
High-concentration organic waste gas combined purification system Download PDFInfo
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- CN219571942U CN219571942U CN202223509275.7U CN202223509275U CN219571942U CN 219571942 U CN219571942 U CN 219571942U CN 202223509275 U CN202223509275 U CN 202223509275U CN 219571942 U CN219571942 U CN 219571942U
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Abstract
The utility model discloses a high-concentration organic waste gas combined purification system, which comprises: the TO incinerator is provided with an organic waste gas inlet and a mixed gas inlet and is used for carrying out thermal oxidative decomposition on the organic waste gas and oxygen in the mixed gas at high temperature; the waste heat boiler is used for heating deoxygenated water by utilizing heat of tail gas discharged by the TO incinerator TO generate steam; the SCR denitration furnace is provided with a tail gas inlet and an ammonia inlet, and a catalyst is arranged in the SCR denitration furnace; the SCR denitration furnace is used for catalyzing the reaction of nitrogen oxides in the tail gas and ammonia gas by adopting a catalyst; the tail gas outlet of the SCR denitration furnace is communicated with the exhaust barrel through the heat exchanger, the economizer and the tail gas fan in sequence. The utility model can be applied to the working conditions of high waste gas concentration, solid matters containing tar and the like, can fully recycle heat energy while ensuring the waste gas purification efficiency, has simple operation and maintenance of the whole system and low operation cost, and is suitable for purifying the high-concentration waste gas in various industries.
Description
Technical Field
The utility model relates to the field of environmental protection, in particular to a high-concentration organic waste gas combined purification system.
Background
Volatile organic compounds are a common type of atmospheric pollutants and are generated in petrochemical industry, coating, packaging and printing industries, semiconductors and other industries. Because the waste gas has complex components and various kinds, different process combinations aiming at different waste gas components exist on the market, and compared with other processes, the incineration method has high treatment efficiency, so the application is the most widely, wherein the RTO process is used as a high-efficiency and low-energy-consumption treatment mode, and has universality at present, but when the working conditions of high waste gas concentration, halogen or tar and the like are met, the RTO incineration process has serious problems of corrosion, heat accumulator blockage, overtemperature, waste of heat energy and the like, seriously influences the safe operation of a system, and even causes safety accidents.
The petrochemical enterprises in China have a large quantity, a small average scale, a distributed layout, complex industry division and various production procedures. Therefore, the VOCs are various in types and emission links, and the waste gas produced in the petrochemical industry is characterized by high concentration and contains naphtha, light oil, dirty oil and other components. At present, for such exhaust gas, a combined process is generally adopted for treatment, and common processes include: "condensation+activated carbon adsorption and desorption", "oil wash+water wash+RTO", etc. The condensation method aims at the working conditions that the components are complex and far lower than the saturation concentration, has low recycling value and higher operation energy consumption, and can also generate secondary pollutants such as waste liquid; if RTO technology is adopted, the design air quantity is very large to ensure safe operation, the investment cost is huge, and safety risks such as over-temperature operation and the like are also existed.
Figure 2 of the accompanying drawings is a schematic diagram of a typical organic waste gas treatment system in the prior art, wherein the system adopts a combined process of oil washing, water washing and RTO to treat organic waste gas, the organic waste gas is pretreated by oil washing and water washing, when mixed gas is introduced into a washing tower from the middle part of the washing tower, due to product component liquid existing between tower plates, the product component gas is liquefied and simultaneously evaporates, impurities cannot be liquefied or solidified, and the impurities are fixed by the product component liquid when passing through the tower plates with the liquid, so that a washing effect is generated. And (3) removing part of particulate matters and organic matters in the waste gas after washing, then entering RTO incineration equipment, and enabling the waste gas to enter a chimney through a tail end fan for standard emission after incineration. This system has the following disadvantages:
(1) Oil washing and water washing can generate a large amount of wastewater; (2) For highly corrosive gases, RTO presents a risk of corrosion collapse; (3) The waste gas containing tar and particulate matters can cause the blockage of an RTO heat accumulator, influence the heat accumulation efficiency and cause the risk of shutdown and production stoppage; (4) for high concentration exhaust gas conditions, overtemperature risks exist; (5) The RTO switching valve needs to be frequently switched, and there is a risk of leakage and exceeding standards. (6) The RTO device has larger pressure loss and high energy consumption for system operation.
Disclosure of Invention
In view of the above-mentioned drawbacks of the prior art, the present utility model provides a high-concentration organic waste gas combined purification system, which utilizes a TO incinerator TO process organic matters and nitrogen oxides in organic waste gas in cooperation with an SCR denitration furnace, and recovers heat in the process of processing in various manners.
In order to achieve the above object, the present utility model provides a high concentration organic waste gas combined purification system comprising:
the TO incinerator is provided with an organic waste gas inlet and a mixed gas inlet and is used for carrying out thermal oxidative decomposition on the organic waste gas and oxygen in the mixed gas at high temperature;
the inlet of the waste heat boiler is connected with the outlet of the TO incinerator and is used for heating deoxygenated water by utilizing the heat of tail gas discharged by the TO incinerator TO generate steam;
the SCR denitration furnace is provided with a tail gas inlet and an ammonia inlet, a catalyst is arranged in the SCR denitration furnace, and the tail gas inlet is connected with a tail gas outlet of the waste heat boiler; the SCR denitration furnace is used for catalyzing nitrogen oxides in tail gas to react with the ammonia gas by adopting a catalyst;
the tail gas outlet of the SCR denitration furnace is communicated with the exhaust barrel through a heat exchanger, an economizer and a tail gas fan in sequence; the heat exchanger performs heat exchange with organic waste gas supplied TO the TO incinerator by utilizing tail gas discharged by the SCR denitration furnace so as TO preheat the organic waste gas; the economizer performs heat exchange with deoxygenated water supplied to the waste heat boiler by utilizing tail gas discharged by the heat exchanger so as to preheat the deoxygenated water.
The utility model further improves that: the pipeline for supplying the organic waste gas is sequentially connected with a system main valve, a main fan and a flame arrester in series, and the organic waste gas is conveyed into the heat exchanger for preheating.
The utility model further improves that: said conduit for supplying said organic waste gas is connected to a bypass conduit prior to said system main valve; the bypass pipeline is sequentially connected with a bypass valve, an emergency host and an activated carbon adsorption device, and finally is led into the exhaust funnel.
The utility model further improves that: the active carbon adsorption device is connected with a fire-fighting spray water pipeline.
The utility model further improves that: the TO incinerator is also connected with a reducing agent spraying system for spraying reducing agent into the TO incinerator; the reducing agent comprises one or more of ammonia water, ammonia gas and urea.
The scheme of the utility model has the following technical effects: (1) Almost can treat all organic waste gas and waste liquid, and can not generate the phenomena of catalyst poisoning, heat accumulator damage, blockage and the like; (2) The TO furnace has the design incineration temperature of more than 1100 ℃, the residence time of more than or equal TO 2s, meets the pyrolysis condition of dioxin, and can effectively inhibit the generation of dioxin in the combustion products of chlorine-containing organic waste gas; (3) For organic waste gas containing halogen and the like, the TO furnace operation temperature can decompose most halogen-containing compounds, and the TO furnace body is not in direct contact with combustion products, so that corrosion of the TO furnace body by secondary combustion products can be avoided; (4) For high-concentration organic waste gas, self-heating operation can be realized without adding fuel; (5) The waste gas with extra-high concentration (exceeding the upper explosion limit) can be directly used as fuel; (6) Organic waste gas with different air volumes (generally more than or equal to 500m 3/h) can be treated; (7) The method can adapt to the working condition (30-120% of design flow) with large fluctuation of the waste gas flow; (8) The dust and solid particle content in the waste gas is not required; (9) The combustion temperature has high elasticity and can stably run in the range of 700-1100 ℃ for a long time; (10) the purification efficiency is highest (can reach more than 99.9 percent); (11) The pressure drop across the plant is small (TO furnace plants are typically less than 1000 Pa); (12) The operation is simple, the operation is stable, the safety and reliability are high, and the service life of the device is long; (13) The inlet concentration of the waste gas is allowed to be high, the gas quantity is not required to be diluted aiming at the high-concentration waste gas treatment project, and the project investment is reduced.
The conception, specific structure, and technical effects of the present utility model will be further described with reference to the accompanying drawings to fully understand the objects, features, and effects of the present utility model.
Drawings
Fig. 1 is a schematic diagram of a high-concentration organic waste gas combined purification system of the present embodiment;
fig. 2 is a schematic diagram of a conventional organic exhaust gas purifying system.
Detailed Description
Other advantages and effects of the present utility model will become apparent to those skilled in the art from the following disclosure, which describes the embodiments of the present utility model with reference to specific examples. The utility model may be practiced or carried out in other embodiments that depart from the specific details, and the details of the present description may be modified or varied from the spirit and scope of the present utility model. It should be noted that the following embodiments and features in the embodiments may be combined with each other without conflict.
It should be noted that the illustrations provided in the following embodiments merely illustrate the basic concept of the present utility model by way of illustration, and only the components related to the present utility model are shown in the illustrations, not according to the number, shape and size of the components in actual implementation, and the form, number and proportion of each component in actual implementation may be arbitrarily changed, and the layout of the components may be more complex.
Some exemplary embodiments of the utility model have been described for illustrative purposes, it being understood that the utility model may be practiced otherwise than as specifically shown in the accompanying drawings.
As shown in fig. 1, an embodiment of the present utility model provides a high concentration organic exhaust gas combined purification system mainly including a TO incinerator 10, a waste heat boiler 11, and an SCR denitration furnace 12.
The TO incinerator 10 has an organic exhaust gas inlet and a mixture gas inlet for performing thermal oxidative decomposition of the organic exhaust gas with oxygen in a mixture gas (combustion air) by high temperature. In addition, the TO incinerator 10 has a fuel inlet for introducing GAS (GAS) so as TO heat the inside of the furnace TO a predetermined temperature. The TO incinerator 10 is provided with turbulence-enhancing means TO enhance the turbulence of the organic exhaust gas within the incinerator. The outer shell of the TO incinerator 10 is of a steel structure, the inner wall of the TO incinerator is made of high-quality refractory materials, and heat-insulating materials are lined between the steel plates and the refractory materials, so that heat is not easy TO transfer outwards. The TO incinerator 10 employs a low nitrogen combustion technique: the burner is a low nitrogen burner to reduce NOx emissions. The TO incinerator 10 can be designed TO be vertical, horizontal or L-shaped according TO actual requirements. When the concentration of the organic waste GAS is high and exceeds the upper explosion limit, the organic waste GAS can be used as fuel for the TO incinerator 10, and fuel GAS (GAS) does not need TO be introduced into the incinerator. In this embodiment, the TO incinerator 10 has the following safety mechanism:
| interlocking with each other | Alarm device |
| Flame extinction interlock; | flame extinction alarm; |
| the hearth temperature is Gao Liansuo; | alarming when the temperature of the hearth is high; |
| hearth pressure is Gao Liansuo; | alarming when the pressure of the hearth is high; |
| fault interlocking of combustion-supporting fans; | alarming when the fuel gas pressure is low; |
in addition, in the present embodiment, a reducing agent spraying system is also connected TO the TO incinerator 10 for spraying reducing agent into the TO incinerator 10. In the heating process, the reducing agent can ensure the full cracking in the organic waste gas and can reduce part of nitrogen oxides. The reducing agent can be one or more of ammonia water, ammonia gas and urea. In one embodiment, the reductant spraying system is an ammonia spraying system and the reductant is ammonia.
The TO incinerator 10 can oxidize and decompose organic waste gas containing VOCs under four combustion conditions of reasonable oxygen supply amount, combustion temperature, residence time and turbulence, and the purification efficiency can reach more than 99.9%.
An inlet of the exhaust-heat boiler 11 is connected TO an outlet of the TO incinerator 10 TO receive high-temperature exhaust gas discharged from the TO incinerator 10. The waste heat boiler 11 can heat deoxygenated water TO generate steam by utilizing the heat of the tail gas discharged from the TO incinerator 10.
After entering the boiler barrel of the waste heat boiler 11, water is mixed with saturated water in the boiler barrel, and enters the evaporator along the down tube below the boiler barrel to absorb heat and start to produce steam.
The steam-water mixture is separated from the evaporator and enters the upper boiler barrel to be separated by the steam-water separation equipment, water falls into the water space in the boiler barrel and enters the down pipe to continue absorbing heat and producing steam, and steam enters the superheater from the upper part of the boiler barrel to absorb heat so as to convert saturated steam into superheated steam.
The SCR denitration furnace 12 has an exhaust gas inlet and an ammonia inlet, and a catalyst is provided therein. The ammonia gas inlet is connected with the reducing agent spraying system. The tail gas inlet is connected with a tail gas outlet of the waste heat boiler 11. The SCR denitration furnace 12 is used for catalyzing the reaction of nitrogen oxides in the tail gas with the ammonia gas by using a catalyst.
In this embodiment, ammonia gas is sprayed into the flue at the upstream of the SCR denitration furnace 12 as a reducing agent through an ammonia spraying grid, so that the ammonia gas is fully mixed with the tail gas, and NO in the tail gas is generated under the action of a catalyst in the SCR denitration furnace 12 x Is reduced to N 2 . The reducing agent spraying system comprises an ammonia injection system, an ammonia storage and preparation system and the like.
The exhaust gas discharged from the SCR denitration furnace 12 still has a higher temperature, so that the exhaust gas outlet of the SCR denitration furnace 12 sequentially passes through the heat exchanger 14 and the economizer 15 to exchange heat, and passes through the exhaust gas fan and then is introduced into the exhaust funnel 13. The heat exchanger 14 performs heat exchange with the organic exhaust gas supplied TO the TO incinerator 10 using the exhaust gas discharged from the SCR denitration furnace 12 TO preheat the organic exhaust gas. The economizer 15 performs heat exchange with deoxygenated water supplied to the waste heat boiler 11 using the exhaust gas discharged from the heat exchanger 14 to preheat the deoxygenated water.
In this example, the pipeline for supplying the organic waste gas is connected in series with a system main valve, a main fan and a flame arrester in sequence, and the pipeline conveys the organic waste gas to the heat exchanger 14 for heating. The pipeline for supplying the organic waste gas is connected with a bypass pipeline in front of a system main valve; the bypass pipeline is connected with a bypass valve, an emergency host and an activated carbon adsorption device in sequence and finally is led into the exhaust funnel 13. The active carbon adsorption device is connected with a fire-fighting spray water pipeline.
The application method of the high-concentration organic waste gas combined purification system comprises the following steps of:
step 1: mixing the organic waste gas with the mixed gas by adopting a TO incinerator 10, and enabling organic matters in the organic waste gas TO react with oxygen in the mixed gas TO decompose at the temperature of more than 850 ℃;
step 2: the exhaust-heat boiler 11 performs heat exchange between the exhaust gas discharged from the TO incinerator 10 and water TO primarily cool the exhaust gas and obtain water vapor;
step 3: mixing ammonia with the primarily cooled tail gas by using the SCR denitration furnace 12, and catalyzing by using a catalyst to enable NO in the tail gas x Reduction to N 2 . The tail gas discharged from the SCR denitration furnace 12 is cooled by the heat exchanger and the economizer in sequence, and is conveyed into the exhaust barrel 13 by the tail gas fan for high-altitude discharge.
The organic exhaust gas is heat exchanged with the exhaust gas in a heat exchanger before being sent TO the TO incinerator 10.
The water heated by the waste heat boiler 11 is deoxidized water, the deoxidized water exchanges heat with tail gas discharged by the heat exchanger in the economizer before heating, and the absorbed heat is heated to a saturation temperature slightly lower than the drum pressure and enters the waste heat boiler 11.
The above embodiments are merely illustrative of the principles of the present utility model and its effectiveness, and are not intended to limit the utility model. Modifications and variations may be made to the above-described embodiments by those skilled in the art without departing from the spirit and scope of the utility model. Accordingly, it is intended that all equivalent modifications and variations of the utility model be covered by the claims, which are within the ordinary skill of the art, be within the spirit and scope of the present disclosure.
Claims (5)
1. A high concentration organic waste gas combined purification system, characterized by comprising:
a TO incinerator (10) having an organic waste gas inlet and a mixed gas inlet for thermally oxidative decomposition of the organic waste gas and oxygen in the mixed gas by high temperature;
an inlet of the waste heat boiler (11) is connected with an outlet of the TO incinerator (10) and is used for heating deoxygenated water TO generate steam by utilizing heat of tail gas discharged by the TO incinerator (10);
an SCR denitration furnace (12) provided with a tail gas inlet and an ammonia inlet, wherein a catalyst is arranged in the SCR denitration furnace, and the tail gas inlet is connected with a tail gas outlet of the waste heat boiler (11); the SCR denitration furnace (12) is used for catalyzing the reaction of nitrogen oxides in the tail gas and ammonia gas by adopting a catalyst;
the tail gas outlet of the SCR denitration furnace (12) is communicated with the exhaust barrel (13) through the heat exchanger (14), the economizer (15) and the tail gas fan in sequence; the heat exchanger (14) performs heat exchange with organic exhaust gas supplied TO the TO incinerator (10) by using tail gas discharged from the SCR denitration furnace (12) TO preheat the organic exhaust gas; the economizer (15) performs heat exchange with deoxygenated water supplied to the waste heat boiler (11) by utilizing the tail gas discharged from the heat exchanger (14) to preheat the deoxygenated water.
2. The high concentration organic waste gas combined purification system as claimed in claim 1, wherein: the pipeline for supplying the organic waste gas is sequentially connected with a system main valve, a main fan and a flame arrester in series, and the organic waste gas is conveyed into the heat exchanger (14) for preheating.
3. The high concentration organic waste gas combined purification system as claimed in claim 2, wherein: said conduit for supplying said organic waste gas is connected to a bypass conduit prior to said system main valve; the bypass pipeline is sequentially connected with a bypass valve, an emergency host and an activated carbon adsorption device, and finally is led into the exhaust funnel (13).
4. A high concentration organic waste gas combined purification system as claimed in claim 3, wherein: the active carbon adsorption device is connected with a fire-fighting spray water pipeline.
5. The high concentration organic waste gas combined purification system as claimed in claim 1, wherein: the TO incinerator (10) is also connected with a reducing agent spraying system, and is used for spraying reducing agent into the TO incinerator (10); the reducing agent comprises one or more of ammonia water, ammonia gas and urea.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223509275.7U CN219571942U (en) | 2022-12-28 | 2022-12-28 | High-concentration organic waste gas combined purification system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223509275.7U CN219571942U (en) | 2022-12-28 | 2022-12-28 | High-concentration organic waste gas combined purification system |
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| Publication Number | Publication Date |
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| CN219571942U true CN219571942U (en) | 2023-08-22 |
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| CN202223509275.7U Active CN219571942U (en) | 2022-12-28 | 2022-12-28 | High-concentration organic waste gas combined purification system |
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