CN111249859A - Low-temperature absorption-low-temperature catalytic oxidation method waste gas recovery treatment process - Google Patents
Low-temperature absorption-low-temperature catalytic oxidation method waste gas recovery treatment process Download PDFInfo
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- CN111249859A CN111249859A CN202010097257.9A CN202010097257A CN111249859A CN 111249859 A CN111249859 A CN 111249859A CN 202010097257 A CN202010097257 A CN 202010097257A CN 111249859 A CN111249859 A CN 111249859A
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- 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
- B01D53/14—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 absorption
- B01D53/1487—Removing organic compounds
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- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8668—Removing organic compounds not provided for in B01D53/8603 - B01D53/8665
Abstract
The invention discloses a waste gas recovery treatment process by a low-temperature absorption-low-temperature catalytic oxidation method, which comprises a low-temperature absorption part and a low-temperature catalytic oxidation part; the low-temperature absorption part comprises a first cooler, a second cooler, an absorption tower and a condensate tank, wherein the first cooler is connected to the top of the absorption tower, and the second cooler is connected to the bottom of the absorption tower; the low-temperature catalytic oxidation part comprises a buffer tank, a heat exchanger, a heater and a reactor which are connected, wherein an outlet of the buffer tank is connected to an inlet of the heat exchanger, an outlet of the heat exchanger is connected with an inlet of the heater, an outlet of the heater is connected to an inlet of the reactor, and an outlet of the reactor is connected with an inlet of the heat exchanger. The invention adopts the mode of combining low-temperature absorption and low-temperature catalytic oxidation, can thoroughly treat the mixed gas containing the styrene, eliminates the problem of violent self-polymerization heat release of the styrene, achieves the aim of safe production, and simultaneously can recover a large amount of organic substances, save energy consumption and improve benefits.
Description
Technical Field
The invention relates to the technical field of waste gas treatment, in particular to a waste gas recovery treatment process by a low-temperature absorption-low-temperature catalytic oxidation method.
Background
At present, the petrochemical enterprise tank deck organic waste gas breathes, and the mixed gas such as oil gas, benzene and easy polymeric styrene that volatilize among the in-process such as loading, shipment, volatilizees the loss of these waste gases not only brings economic loss for the enterprise, still can cause environmental pollution, probably causes the fire hidden danger even and arouses the incident.
With the increasing shortage of energy sources and the increasingly stringent environmental protection requirements, the regulations on the recovery treatment standards of the gases become more and more strict, the traditional combined process cannot treat the gases thoroughly, and the recovery utilization rate of waste gas is low, so that a new process which mainly aims at the mixed gases of oil gas, benzene, easily polymerized styrene and the like volatilized in the processes of tank top organic waste gas respiration, loading, shipping and the like of petrochemical enterprises and meets the environmental protection requirements is urgently needed to be developed.
Patent 201510770073.3 discloses a styrene waste gas treatment method, which is mainly characterized in that potassium permanganate solution is sprayed and absorbed, styrene gas is treated only, the treatment effect of mixed gas containing styrene is poor, and the mixed gas outlet index is difficult to meet the condition that the total hydrocarbon content of methane is lower than 15mg/m3Benzene content less than 1mg/m3Styrene less than 5mg/m3If the above criteria are to be met, other processes need to be combined.
Patent 201710339150.9 discloses a method and a device for treating refinery VOCs waste gas, wherein the main technical route is "activated carbon adsorption-desorption", which is suitable for volatile oil gas such as gasoline and diesel oil, but for mixed gas containing styrene, the styrene self-polymerization is violent and the heat release is easy to cause high-temperature ignition of activated carbon, so that the potential safety hazard is high.
Disclosure of Invention
The invention discloses a waste gas recovery treatment process by a low-temperature absorption-low-temperature catalytic oxidation method, aiming at solving the technical problems of incomplete treatment and low recovery rate in the waste gas recovery treatment process.
In order to achieve the purpose, the invention adopts the following technical scheme:
a low-temperature absorption-low-temperature catalytic oxidation method waste gas recovery treatment process comprises a low-temperature absorption part and a low-temperature catalytic oxidation part; wherein the content of the first and second substances,
the low-temperature absorption part comprises a first cooler, a second cooler, an absorption tower and a condensate tank, wherein the first cooler is connected to the top of the absorption tower, an absorbent is sent into the first cooler through a first oil pump for cooling, the cooled absorbent is sent into the top of the absorption tower, the second cooler is connected to the bottom of the absorption tower, the mixed gas enters the second cooler for cooling, the cooled gas part is sent into the bottom of the absorption tower, and the condensed liquid enters the condensate tank; the rich liquid after low-temperature absorption in the absorption tower is conveyed to the desorption tower through a second oil pump;
the low-temperature catalytic oxidation part comprises a buffer tank, a heat exchanger, a heater and a reactor which are connected, a mixer is further arranged on a pipeline connecting an outlet at the top of the absorption tower with an inlet of the buffer tank, an outlet of the buffer tank is connected to an inlet of the heat exchanger, an outlet of the heat exchanger is connected with an inlet of the heater, an outlet of the heater is connected to an inlet of the reactor, and an outlet of the reactor is connected with an inlet of the heat exchanger; the gas absorbed at low temperature in the absorption tower is mixed with air in a mixer, the diluted low-concentration waste gas is buffered in a buffer tank and then enters a heat exchanger to recover reaction heat, and the gas is heated to the reaction temperature in a heater and then enters a reactor for low-temperature catalytic oxidation.
As a further preferable mode of the present invention, an oil gas fan is further disposed on a pipeline connecting the second cooler and the bottom of the absorption tower, and the cooled mixed gas is sent into the absorption tower through the oil gas fan adjusted by frequency conversion, and is in countercurrent contact with the low temperature absorbent from the top of the absorption tower.
As a further preferred aspect of the present invention, the second cooler is further connected to a condensate tank, and liquid generated by condensing the mixed gas by the second cooler enters the condensate tank to be periodically discharged.
As a further preferable aspect of the present invention, the first cooler and the second cooler are both connected to a condensing unit, the cold source for cooling enters the inlet of the first cooler and the inlet of the second cooler from the outlet of the refrigerant main pipe of the condensing unit, and after cooling, the cold source is returned to the inlet of the refrigerant main pipe of the condensing unit from the outlet of the first cooler and the outlet of the second cooler.
As a further preferred aspect of the present invention, the mixer is further connected to an air blower controlled by a variable frequency, the exhaust gas absorbed by the absorption tower enters the mixer from the top of the tower, the exhaust gas is mixed with the air delivered by the air blower in the mixer, and the exhaust gas is diluted to below 25% of the lower explosion limit and then is delivered to the buffer tank.
As a further preferred aspect of the present invention, an on-line concentration analyzer is further installed on a pipeline connecting the mixer and the buffer tank to monitor the concentration of the diluted exhaust gas.
As a further preference of the invention, the combustion temperature in the reactor is controlled to be less than 320 ℃, if the heat released by catalytic combustion reaches the temperature required by the reaction, the heater can stop working, and when the catalytic combustion temperature does not reach the requirement, the heater is started again to supplement the heat.
As a further optimization of the invention, the heat exchanger is also connected with an exhaust funnel to discharge the gas reaching the standard.
In a further preferred embodiment of the present invention, the rich oil fed into the desorption tower is subjected to removal of organic matters with a low boiling point, the treated lean oil is fed into the absorption tower again to form an absorbent circulation, and the desorbed exhaust gas is fed into a fuel gas system or a flare system.
The invention has the advantages that the mode of combining low-temperature absorption and low-temperature catalytic oxidation is adopted, so that the mixed gas containing styrene can be thoroughly treated, the self-polymerization violent heat release of the styrene in the treatment process is eliminated, the aim of safe production is fulfilled, meanwhile, a large amount of organic substances can be recovered, the energy consumption is saved, and the economic benefit is improved; the exhaust emission index of the waste gas treated by the method can meet the strictest national standard, industrial standard and local standard, meet the latest national standard and industrial standard requirements, and the total hydrocarbon of non-methane is less than or equal to 15mg/m3The removal rate is more than or equal to 97 percent, and the benzene content is less than or equal to 1mg/m3Styrene is less than or equal to 5mg/m3。
Drawings
FIG. 1 is a schematic structural view of the present invention;
wherein, 1, an air fan; 2. a first cooler; 3. a first oil pump; 4. a second cooler; 5. an oil-gas fan; 6. a condensate tank; 7. a second oil pump; 8. an absorption tower; 9. a mixer; 10. a buffer tank; 11. a heat exchanger; 12. a heater; 13. a reactor; 14. an exhaust funnel; 15. an on-line concentration analyzer.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
As shown in the figure, the process for recycling and treating the waste gas by the low-temperature absorption-low-temperature catalytic oxidation method comprises a low-temperature absorption part and a low-temperature catalytic oxidation part, and can be used for recycling and treating mixed gas such as oil gas, benzene and easily polymerized styrene volatilized in the processes of tank top organic waste gas size respiration, loading, shipment and the like of petrochemical enterprises.
The low-temperature absorption part comprises a first cooler 2, a second cooler 4, an absorption tower 8 and a condensate tank 6, wherein the first cooler 2 is connected to the top of the absorption tower 8, an absorbent is sent into the first cooler 2 through a first oil pump 3 for cooling, the cooled absorbent is sent into the top of the absorption tower 8, the second cooler 4 is connected to the bottom of the absorption tower 8, the mixed gas enters the second cooler 4 for cooling, the cooled gas part is sent into the bottom of the absorption tower 8, and the condensed liquid enters the condensate tank 6; the absorbent and the mixed gas are in countercurrent contact in an absorption tower 8, the absorption tower 8 is filled with packing, and the rich solution subjected to low-temperature absorption treatment in the absorption tower 8 is conveyed to a desorption tower through a second oil pump 7.
The low-temperature catalytic oxidation part comprises a buffer tank 10, a heat exchanger 11, a heater 12 and a reactor 13 which are connected, a mixer 9 is further arranged on a pipeline connecting an outlet at the top of the absorption tower 8 with an inlet of the buffer tank 10, an outlet of the buffer tank 10 is connected to an inlet of the heat exchanger 11, an outlet of the heat exchanger 11 is connected with an inlet of the heater 12, an outlet of the heater 12 is connected to an inlet of the reactor 13, and an outlet of the reactor 13 is connected with an inlet of the heat exchanger 11; the gas absorbed at low temperature in the absorption tower 8 is mixed with air in a mixer 9, the diluted low-concentration waste gas is buffered in a buffer tank 10 and then enters a heat exchanger 11 to recover reaction heat, and the gas is heated to the reaction temperature in a heater 12 and then enters a reactor 13 for low-temperature catalytic oxidation.
Particularly, an oil gas fan 5 is further arranged on a pipeline connected between the second cooler 4 and the bottom of the absorption tower 8, and the cooled mixed gas is sent into the absorption tower 8 through the oil gas fan 5 regulated by frequency conversion and is in countercurrent contact with the low-temperature absorbent from the top of the tower.
In a further preferred embodiment of the present invention, the second cooler 4 is further connected to a condensate tank 6, and the liquid generated by condensing the mixed gas in the second cooler 4 is periodically discharged into the condensate tank 6.
Particularly, the first cooler 2 and the second cooler 4 are both connected with a condensing unit, a cold source for cooling respectively enters an inlet of the first cooler 2 and an inlet of the second cooler 4 from an outlet of a refrigerant main pipe of the condensing unit, and is respectively connected back to the inlet of the refrigerant main pipe of the condensing unit from the outlet of the first cooler 2 and an outlet of the second cooler 4 after being cooled, so that the cold source is recycled.
Particularly, the mixer 9 is also connected with an air fan 1 which is controlled by frequency conversion, the waste gas absorbed by the absorption tower 8 enters the mixer 9 from the top of the tower, the waste gas is mixed with the air conveyed by the air fan 1 in the mixer 9, and the waste gas is diluted to be below 25% of the lower explosion limit and then is conveyed into a buffer tank 10.
In particular, an on-line concentration analyzer 15 is further installed on a pipeline connecting the mixer 9 and the buffer tank 10, and is used for monitoring and diluting the concentration of the waste gas, ensuring that the concentration is always below 25% of the lower explosion limit, detecting the concentration of the waste gas, and avoiding the explosion in the subsequent reaction.
Particularly, the combustion temperature in the reactor 13 is controlled to be less than 320 ℃, if the heat released by catalytic combustion reaches the temperature required by the reaction, the heater 12 can stop working, and when the catalytic combustion temperature does not meet the requirement, the heater 12 is started again to supplement the heat, so that the flexibility is strong, and the energy consumption is saved.
In particular, the heat exchanger 11 is also connected with an exhaust funnel 14 to discharge standard gas, and the waste gas after reaction is the standard gas.
In particular, the rich oil fed into the desorption tower is removed of organic matters with lower boiling points, the treated lean oil is fed into the absorption tower 8 again to form absorbent circulation, and the desorbed waste gas is fed into a fuel gas system or a flare system.
The working process of the invention is as follows:
the mixed gas is cooled by the second cooler 4, the liquid condensed in the cooling process enters the condensate tank 6 to be periodically discharged, the gas part enters the absorption tower 8 from the tower bottom, the absorbent enters the absorption tower 8 from the tower top after being cooled by the first cooler 2, the gas and the absorbent perform countercurrent mass transfer in the absorption tower 8, the rich liquid after absorption is discharged out of the absorption tower 8 from the outlet at the tower bottom and is sent to the analysis tower by the second oil pump 7, the gas after absorption is discharged from the tower top of the absorption tower 8 and enters the mixer 9 to be fully mixed with the air introduced by the air fan 1, and the concentration of the diluted waste gas is detected by the online concentration analyzer 15.
The diluted waste gas enters a buffer tank 10 for buffering pressure, enters a heat exchanger 11 for recovering waste heat, then enters a heater 12 for heating to a reaction temperature, enters a reactor 13 for catalytic oxidation reaction, when the heated waste gas reaches the catalytic reaction temperature, organic matters in the waste gas can be catalytically decomposed under the action of a catalyst, a large amount of heat is released by the catalytic oxidation reaction, and then enters the heat exchanger 11 again for heat exchange of the waste gas, when the heat released by the reaction is enough to support the catalytic oxidation reaction, the heater 12 can be turned off, energy is saved, when the temperature does not reach the catalytic combustion temperature requirement, the heater 12 is turned on again for supplementing energy, and the gas reaching the standard after the catalytic oxidation treatment is discharged out of the system through an exhaust funnel 14.
In addition, the rich liquid discharged from the absorption tower 8 is sent into a desorption tower, organic matters with lower boiling points are removed from the rich oil, the treated lean oil enters the absorption tower 8 again to form absorbent circulation, and the desorbed waste gas enters a fuel gas system or a flare system to complete the circulation treatment process of the rich liquid.
After the treatment by the process, the requirements of the latest national standard and industrial standard can be met, and the total non-methane hydrocarbon is less than or equal to 15mg/m3The removal rate is more than or equal to 97 percent, and the benzene content is less than or equal to 1mg/m3Styrene is less than or equal to 5mg/m3。
It is to be understood that the above description is not intended to limit the present invention, and the present invention is not limited to the above examples, and those skilled in the art may make modifications, alterations, additions or substitutions within the spirit and scope of the present invention.
Claims (9)
1. A low-temperature absorption-low-temperature catalytic oxidation method waste gas recovery treatment process is characterized by comprising a low-temperature absorption part and a low-temperature catalytic oxidation part; wherein the content of the first and second substances,
the low-temperature absorption part comprises a first cooler, a second cooler, an absorption tower and a condensate tank, wherein the first cooler is connected to the top of the absorption tower, an absorbent is sent into the first cooler through a first oil pump for cooling, the cooled absorbent is sent into the top of the absorption tower, the second cooler is connected to the bottom of the absorption tower, the mixed gas enters the second cooler for cooling, the cooled gas part is sent into the bottom of the absorption tower, and the condensed liquid enters the condensate tank; the rich liquid after low-temperature absorption in the absorption tower is conveyed to the desorption tower through a second oil pump;
the low-temperature catalytic oxidation part comprises a buffer tank, a heat exchanger, a heater and a reactor which are connected, a mixer is further arranged on a pipeline connecting an outlet at the top of the absorption tower with an inlet of the buffer tank, an outlet of the buffer tank is connected to an inlet of the heat exchanger, an outlet of the heat exchanger is connected with an inlet of the heater, an outlet of the heater is connected to an inlet of the reactor, and an outlet of the reactor is connected with an inlet of the heat exchanger; the gas absorbed at low temperature in the absorption tower is mixed with air in a mixer, the diluted low-concentration waste gas is buffered in a buffer tank and then enters a heat exchanger to recover reaction heat, and the gas is heated to the reaction temperature in a heater and then enters a reactor for low-temperature catalytic oxidation.
2. The process for recycling and treating the waste gas by the low-temperature absorption-low-temperature catalytic oxidation method according to claim 1, wherein an oil-gas fan is further arranged on a pipeline connecting the second cooler and the bottom of the absorption tower, and the cooled mixed gas is sent into the absorption tower through the oil-gas fan with variable frequency regulation and is in countercurrent contact with the low-temperature absorbent from the top of the absorption tower.
3. The process according to claim 2, wherein the second cooler is further connected to a condensate tank, and liquid generated by condensation of the mixed gas in the second cooler is periodically discharged into the condensate tank.
4. The process of claim 3, wherein the first cooler and the second cooler are both connected to a condenser unit, and the cooling source for cooling enters the inlet of the first cooler and the inlet of the second cooler from the outlet of the refrigerant manifold of the condenser unit, and is cooled and then returns to the inlet of the refrigerant manifold of the condenser unit from the outlet of the first cooler and the outlet of the second cooler.
5. The process for recycling and treating the waste gas by the low-temperature absorption-low-temperature catalytic oxidation method according to claim 1, wherein the mixer is further connected with an air fan which is controlled by frequency conversion, the waste gas absorbed by the absorption tower enters the mixer from the top of the tower, the waste gas is mixed with the air conveyed by the air fan in the mixer, and the waste gas is diluted to be below 25 percent of the lower explosion limit and then is conveyed into the buffer tank.
6. The process according to claim 5, wherein an on-line concentration analyzer is further installed on a pipeline connecting the mixer and the buffer tank to monitor and dilute the exhaust gas concentration.
7. The process for recovering and treating the waste gas generated by the low-temperature absorption-low-temperature catalytic oxidation method as claimed in claim 1, wherein the combustion temperature in the reactor is controlled to be less than 320 ℃, the heater can stop working if the heat released by catalytic combustion reaches the temperature required by the reaction, and the heater is turned on again to supplement the heat when the catalytic combustion temperature does not reach the requirement.
8. The process according to claim 1, wherein the heat exchanger is further connected to an exhaust stack for discharging the standard gas.
9. The process of claim 1, wherein the rich oil fed into the desorption tower is stripped of lower boiling point organic matter, the treated lean oil is fed into the absorption tower again to form absorbent circulation, and the desorbed waste gas is fed into fuel gas system or flare system.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112791582A (en) * | 2020-12-21 | 2021-05-14 | 广东申菱环境系统股份有限公司 | Oil gas catalytic oxidation processing apparatus |
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| CN208282134U (en) * | 2018-05-08 | 2018-12-25 | 上海力皇环保工程有限公司 | A kind of novel low temperature boosting absorption catalysis oxidation VOCs emission-control equipment |
| CN109304084A (en) * | 2017-11-16 | 2019-02-05 | 中国石油化工股份有限公司 | Method for organic waste gas recovery containing styrene in a kind of tank field and entrucking material |
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2020
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Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20050038290A1 (en) * | 2001-12-13 | 2005-02-17 | Mitsubishi Chemical Corporation | Process for producing (meth)acrolein or (meth)acrylic acid |
| US20140065040A1 (en) * | 2012-09-05 | 2014-03-06 | Basf Se | Process for separating off acid gases from a water-comprising fluid stream |
| CN105080278A (en) * | 2015-08-13 | 2015-11-25 | 中国石油化工股份有限公司 | Oil and gas recovery method |
| CN204865541U (en) * | 2015-08-13 | 2015-12-16 | 中国石油化工股份有限公司 | A processing apparatus for retrieving and it is gaseous to destroy VOCs |
| CN109304084A (en) * | 2017-11-16 | 2019-02-05 | 中国石油化工股份有限公司 | Method for organic waste gas recovery containing styrene in a kind of tank field and entrucking material |
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| CN112791582A (en) * | 2020-12-21 | 2021-05-14 | 广东申菱环境系统股份有限公司 | Oil gas catalytic oxidation processing apparatus |
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Application publication date: 20200609 |