CN109395580A - The processing method of the oxygen-containing tail gas of ethylene oxide-glycol unit - Google Patents
The processing method of the oxygen-containing tail gas of ethylene oxide-glycol unit Download PDFInfo
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Abstract
The present invention relates to a kind of processing method of oxygen-containing tail gas of ethylene oxide-glycol unit, mainly solve the problems, such as that oxygen-containing vent gas treatment is at high cost, energy consumption is high, safety is lower in the prior art, environmental pollution.The present invention by using a kind of oxygen-containing tail gas of ethylene oxide-glycol unit processing method, after the ethylene that the oxygen-containing tail gas of ethylene oxide-glycol unit removes in oxygen-containing tail gas through ethylene recovery unit, enter shell and tube reactor by gas-gas heat exchanger, under the action of noble metal catalyst, catalytic oxidation occurs in pipe side, so that the oxygen in tail gas is sufficiently reacted with ethylene, remove oxygen therein, then tail gas after treatment is cooling by cooler, into liquid separation tank, the technical solution that tail gas after treatment goes fuel gas pipe network or flare system to carry out subsequent processing preferably solves the above problem, it can be used in the processing of the oxygen-containing tail gas of ethylene oxide-glycol unit.
Description
Technical field
The present invention relates to a kind of processing methods of oxygen-containing tail gas of ethylene oxide-glycol unit.
Background technique
Ethylene oxide (Ethylene Oxide, EO), also known as ethylene oxide are colourless gas under room temperature, with water, alcohol,
Ether is mutually immiscible.Chemical property is active, easily carries out opening with the compound containing active hydrogen, generates a series of
Derivative.Common epoxyethane derivative mainly has ethylene glycol, polyethylene glycol, glycol ether, ethanol amine etc..Currently, global
There are about 70% ethylene oxide for producing ethylene glycol and diethylene glycol, and about 11% for producing polyether-type nonionic surface-active
Agent, there is also about 19% for producing the intensive processing product such as ethanol amine, glycol ether, choline chloride.
Producing glycol by virtue of hydration of ethylene oxide (EG) is the most important application of ethylene oxide.Ethylene glycol is that a kind of purposes is extremely wide
Basic organic chemical raw material.It is mainly used in production polyester fiber, unsaturated polyester resin, plastics, antifreezing agent, film, profit
Lubrication prescription etc. is also largely used in a variety of chemical products such as production plasticizer, nonionic surfactant, desiccant.
In ethylene oxide-glycol unit, with the lasting progress of reaction, the product of inert gas is had in circulating air
It is tired, it needs periodically to discharge, oxygen-containing tail gas is then one gas extracted out from circulating air.
It is required according to " SH3009-2013 petrochemical industry imflammable gas exhaust system design specification ", oxygen content is greater than
The fuel gas of 2% (volume fraction) should not be discharged into full factory's fuel gas exhaust system, should be discharged into dedicated exhaust system or another
Row processing.So the processing problem of oxygen-containing tail gas is always a technological difficulties in ethylene oxide-glycol unit.
Since the oxygen content in tail gas is higher, full factory's fuel gas exhaust system, such as torch not can enter.Current processing
Method first is that the oxygen-containing tail gas extracted out from circulating air is sent into ethylene recovery unit, then the open fires equipment such as send to incinerator,
However, there are more drawbacks for this processing method.First, incinerator takes up a large area independently of device, and it is harsh to build condition；
Second, incinerator cost of investment is high, and for cost 10,000,000-1,500 ten thousand, economic rationality is poor；Third, incinerator will increase pollution
Object discharge amount causes to seriously endanger to environment.
In addition, also oxygen-containing tail gas can be sent to special nozzle, however, general cauldron distance has with device area farther out
Certain distance, pipe arrangement are complex.It is cross-device the problems such as need to considering safety interlocking, more numerous for safety perspective
It is trivial, and tailgas component is complicated.
Dilution method is also one of the method for handling oxygen-containing tail gas at present.In the prior art, oxygen-containing tail gas enters UF membrane list
Oxygen content before member is 5%-6%, the high oxygen content after UF membrane up to 10% or so, if by oxygen content be diluted to 2% with
Under, petrochemical industry imflammable gas exhaust system design specification is complied with, the methane of 6 times of left and right must be filled with, this is greatly increased
Consumption of raw materials.
Summary of the invention
The technical problem to be solved by the present invention is to oxygen-containing vent gas treatment is at high cost, energy consumption is high in the prior art, safety
The problem of lower, environmental pollution, provides a kind of processing method of new oxygen-containing tail gas of ethylene oxide-glycol unit, has gas
The advantage that bubble stability is good, good extinguishing effect, anti-re-ignition performance are good.
To solve the above problems, The technical solution adopted by the invention is as follows: a kind of oxygen-containing tail of ethylene oxide-glycol unit
The processing method of gas removes in oxygen-containing tail gas from the oxygen-containing tail gas of ethylene oxide-glycol unit through ethylene recovery unit
After ethylene, enter shell and tube reactor by gas-gas heat exchanger, under the action of noble metal catalyst, catalysis oxygen occurs in pipe side
Change reaction, so that the oxygen in tail gas is sufficiently reacted with remaining ethylene, removes oxygen therein, then tail gas after treatment
Cooling by cooler, into liquid separation tank, tail gas after treatment goes fuel gas pipe network or flare system to carry out subsequent processing.
In above-mentioned technical proposal, it is preferable that it is that raw material passes through hydration method that ethylene oxide-glycol unit, which is by ethylene oxide,
The device of ethylene glycol is produced, oxygen-containing tail gas is one gas extracted out from the ethylene oxide-glycol unit circulating air；Column
Catalytic oxidation occurs for tubular reactor pipe side, so that the oxygen in tail gas is removed with oxygen-containing tail gas through ethylene recovery unit
Remaining ethylene sufficiently reacts after ethylene；Catalytic oxidation in shell and tube reactor is isothermal reaction or adiabatic reaction.
In above-mentioned technical proposal, it is preferable that shell and tube reactor heat production is issued by drum, the reaction temperature of catalysis oxidation
It is controlled by the pressure of cooling drum.
In above-mentioned technical proposal, it is preferable that the oxygen volume content in oxygen-containing tail gas is 3~9%, the temperature of oxygen-containing tail gas
It is 20~100 DEG C.
In above-mentioned technical proposal, it is preferable that in oxygen-containing tail gas, the volume ratio of ethylene and oxygen is not less than 1:3, by processing
Oxygen volume content in tail gas afterwards by control catalytic oxidation temperature or passes through the oxygen in measurement tail gas less than 2%
Gas content controls the oxygen volume content in tail gas after treatment.
In above-mentioned technical proposal, it is preferable that from the oxygen-containing tail gas of ethylene oxide-glycol unit through ethylene recovery unit
After the ethylene removal in oxygen-containing tail gas to volumn concentration 2~30%, after gas-gas heat exchanger exchanges heat to 50~180 DEG C
Into shell and tube reactor.
In above-mentioned technical proposal, it is preferable that the operating condition in shell and tube reactor are as follows: 250~400 DEG C of operation temperature,
1~2MPaG of operating pressure.
In above-mentioned technical proposal, it is preferable that noble metal catalyst is silver, platinum or palladium, noble metal matter in noble metal catalyst
Measuring score is 0.05~15%.
In above-mentioned technical proposal, it is preferable that noble metal catalyst is silver.
In above-mentioned technical proposal, it is preferable that Set scale coefficient k, k=mSteam/ m, wherein m is the quality of oxygen-containing tail gas,
kg；mSteamFor the quality of steam that drum generates, kg；The value range of k is that 0.5-2 keeps it in by adjusting proportionality coefficient k
Reasonable value interval ensure that the cooling amount of shell and tube reactor, not allow runaway reaction.Since the amount of oxygen-containing tail gas is variation
, if during the reaction, the amount of fixed boiler feedwater will cause response not in time, catalytic oxidation be influenced, so ratio
Coefficient k is of great significance.The engineer in the field can formulate suitable control program on this basis.
The present invention uses new tail gas treatment process route, removes thermogenetic steam and is sent to device use, effectively reduces dress
Energy consumption is set, the energy-saving and emission-reduction requirement that current country is advocated is met；The oxygen-containing tail gas extracted out from circulating air, by ethylene recovery
Unit, then catalytic oxidation system is arrived, processed tail gas goes fuel gas pipe network or flare system again.This process flow is existing
It is transformed on the basis of process, workload is smaller, and oxygen depletion can be guaranteed tail gas subsequent processing by catalytic oxidation system
The safety of process.In the present invention, silver catalyst is can be used in catalytic oxidation, it can unify to recycle, and urge than conventional
It is low to change oxidation catalyst price.Further, it is also possible to use the versatilities VOC catalyst for catalytic oxidation such as palladium, platinum.Cooling in the present invention
There are two types of modes, is isothermal reaction and adiabatic reaction respectively.In the present invention, guarantee control of the oxygen content lower than 2% in tail gas
There are two types of methods, and one kind is temperature control method, and another kind is measurement of oxygen content method.By to technological design, equipment selection, it is various
The various aspects comprehensive consideration such as influence factor, realizes economical and efficient and energy-saving and environment-friendly basic demand and chemical products is reasonable
Change, the production process of safe and benefit, effectively oxygen-containing vent gas treatment is at high cost in the prior art, energy consumption is high, safety for solution
The problems such as property is lower, environmental pollution, achieves preferable technical effect.
Detailed description of the invention
Fig. 1 is the flow diagram of the method for the invention.
In Fig. 1,1 is drum, and 2 be shell and tube reactor, and 3 be gas-gas heat exchanger, and 4 be cooler, and 5 be liquid separation tank, and 6 be second
Alkene recovery unit, 7 be the oxygen-containing tail gas of reactor inlet, and 8 be the not oxygen-containing tail gas of reactor outlet, and 9 is oxygen-containing for heat exchanger exit
Tail gas, 10 be the not oxygen-containing tail gas of cooler outlet, and 11 is go fuel gas pipe network or flare system, and 12 be to go waste liquid fuel tank, 13
It is to remove hot water circuit for oxygen-containing tail gas, 14,15.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
[embodiment 1]
A kind of processing method of the oxygen-containing tail gas of ethylene oxide-glycol unit, as shown in Figure 1, oxygen-containing tail gas 13 is through ethylene
Recovery unit 6, by oxygen-containing tail gas ethylene remove, be then passed through gas-gas heat exchanger 3 enter shell and tube reactor 2, silver or
Under the action of the noble metal catalysts such as platinum, catalytic oxidation occurs in pipe side, so that the oxygen and ethylene in tail gas are sufficiently anti-
It answers, completely consumes, 2 heat production of shell and tube reactor is issued by drum 1, in addition, the reaction temperature of catalysis oxidation passes through cooling vapour
The pressure of packet 1 is controlled.Processed tail gas 9 is cooling by cooler 4, and into liquid separation tank 5, not oxygen-containing tail gas can remove fuel
Gas pipe network or flare system carry out subsequent processing.
25.2 DEG C of oxygen-containing exhaust temperature, mass flow 2397.72kg/hr, wherein with volume fraction, oxygen content
5.1%, ethylene contents 33.9%, methane content 52.8%, carbon dioxide content 1.5%, argon content 6.2%, nitrogen content
0.2%, water content 0.3% is changed the ethylene removal in oxygen-containing tail gas to 18.64% by gas gas by ethylene recovery unit
Hot device exchanges heat to after 70 DEG C, into shell and tube reactor, wherein shell-and-tube reactor heat production is issued by drum, in addition, catalysis oxygen
The reaction temperature of change process is controlled by the pressure of cooling drum, and 350 DEG C of reaction temperature, reaction pressure 1.5MPa (table
Pressure), in silver catalyst, (loaded catalyst 0.79924kg, silver-colored load capacity is 3.4% (quality) in catalyst, and carrier is
SiO2) under the action of, occur catalytic oxidation (for isothermal reaction), so that the oxygen in tail gas is sufficiently reacted with ethylene, oxygen
The conversion ratio of gas reaches 100%, and generates carbon dioxide and water, i.e., the oxygen volume content in tail gas after treatment is
0.02%.Later, the tail gas of oxygen is removed, temperature is 180 DEG C, after subcooler is cooling, into liquid separation tank, removes fuel gas pipe
Net or flare system carry out subsequent processing.Wherein, proportionality coefficient k=1.201.
Final result shows compared with prior art, handles oxygen-containing tail gas using this method, cost reduces by 13%, energy consumption
27% is reduced, and highly-safe, environmental pollution is minimum.
[embodiment 2]
According to condition described in embodiment 1 and step, 25.2 DEG C, mass flow 599.43kg/hr of oxygen-containing exhaust temperature,
In, with volume fraction, oxygen content 5.1%, ethylene contents 33.9%, methane content 52.8%, carbon dioxide content
1.5%, argon content 6.2%, nitrogen content 0.2%, water content 0.3% will be in oxygen-containing tail gas by ethylene recovery unit
Ethylene removal is to 17.98%, after gas-gas heat exchanger exchanges heat to 70 DEG C, into shell and tube reactor, wherein shell-and-tube reactor
Heat production is issued by drum, in addition, the reaction temperature of catalytic oxidation process is controlled by the pressure of cooling drum, reaction temperature
350 DEG C, reaction pressure 1.5MPa (gauge pressure) of degree, silver catalyst (loaded catalyst 0.1998kg, it is silver-colored negative in catalyst
Carrying capacity is 3.4% (quality), carrier SiO2) under the action of, occur catalytic oxidation (for isothermal reaction), so that in tail gas
Oxygen sufficiently reacted with ethylene, the conversion ratio of oxygen reaches 100%, and generate carbon dioxide and water, i.e., after treatment
Oxygen volume content in tail gas is 0.02%.Later, the tail gas of oxygen is removed, temperature is 180 DEG C, cooling through subcooler
Afterwards, into liquid separation tank, fuel gas pipe network or flare system is gone to carry out subsequent processing.Wherein, proportionality coefficient k=1.201.
Final result shows compared with prior art, handles oxygen-containing tail gas using this method, cost reduces by 11%, energy consumption
25% is reduced, and highly-safe, environmental pollution is minimum.
[embodiment 3]
According to condition described in embodiment 1 and step, 25.2 DEG C, mass flow 2397.72kg/hr of oxygen-containing exhaust temperature,
Wherein, with volume fraction, oxygen content 5.1%, ethylene contents 33.9%, methane content 52.8%, carbon dioxide content
1.5%, argon content 6.2%, nitrogen content 0.2%, water content 0.3% will be in oxygen-containing tail gas by ethylene recovery unit
Ethylene removal is to 26.1%, after gas-gas heat exchanger exchanges heat to 70 DEG C, into shell and tube reactor, wherein shell-and-tube reactor
Heat production is issued by drum, in addition, the reaction temperature of catalytic oxidation process is controlled by the pressure of cooling drum, reaction temperature
250 DEG C, reaction pressure 1.2MPa (gauge pressure) of degree, in palladium catalyst (loaded catalyst 0.59943kg, palladium in catalyst
Load capacity is 0.98% (quality), carrier SiO2) under the action of, occur catalytic oxidation (for isothermal reaction), so that tail
Oxygen in gas is sufficiently reacted with ethylene, and the conversion ratio of oxygen reaches 100%, and generates carbon dioxide and water, i.e., by processing
Oxygen volume content in tail gas afterwards is 0.02%.Later, the tail gas of oxygen is removed, temperature is 130 DEG C, cold through subcooler
But after, into liquid separation tank, fuel gas pipe network or flare system is gone to carry out subsequent processing.Wherein, proportionality coefficient k=1.287.
Final result shows compared with prior art, handles oxygen-containing tail gas using this method, cost reduces by 10%, energy consumption
23% is reduced, and highly-safe, environmental pollution is minimum.
[embodiment 4]
According to condition described in embodiment 1 and step, 25.2 DEG C, mass flow 2397.72kg/hr of oxygen-containing exhaust temperature,
Wherein, with volume fraction, oxygen content 3.5%, ethylene contents 41.49%, methane content 46.53%, carbon dioxide content
2.1%, argon content 5.8%, nitrogen content 0.18%, water content 0.4% will be in oxygen-containing tail gas by ethylene recovery unit
Ethylene removal to 26.8%, after gas-gas heat exchanger exchanges heat to 70 DEG C, into shell and tube reactor, wherein tubulation reaction
Device heat production is issued by drum, in addition, the reaction temperature of catalytic oxidation process is controlled by the pressure of cooling drum, reaction
350 DEG C of temperature, reaction pressure 1.5MPa (gauge pressure), in silver catalyst (loaded catalyst 0.79924kg, silver in catalyst
Load capacity be 3.4% (quality), carrier SiO2) under the action of, occur catalytic oxidation (for isothermal reaction), so that tail
Oxygen in gas is sufficiently reacted with ethylene, and the conversion ratio of oxygen reaches 100%, and generates carbon dioxide and water, i.e., by processing
Oxygen volume content in tail gas afterwards is 0.02%.Later, the tail gas of oxygen is removed, temperature is 180 DEG C, cold through subcooler
But after, into liquid separation tank, fuel gas pipe network or flare system is gone to carry out subsequent processing.Wherein, proportionality coefficient k=0.7647.
Final result shows compared with prior art, handles oxygen-containing tail gas using this method, cost reduces by 14%, energy consumption
28% is reduced, and highly-safe, environmental pollution is minimum.
[embodiment 5]
According to condition described in embodiment 1 and step, 25.2 DEG C, mass flow 2397.72kg/hr of oxygen-containing exhaust temperature,
Wherein, with volume fraction, oxygen content 7.5%, ethylene contents 40.56%, methane content 44.32%, carbon dioxide content
3.22%, argon content 3.85%, nitrogen content 0.24%, water content 0.31%, by ethylene recovery unit, by oxygen-containing tail gas
In ethylene removal to 29.6%, after gas-gas heat exchanger exchanges heat to 70 DEG C, into shell and tube reactor, wherein tubulation is anti-
Device heat production is answered to issue by drum, in addition, the reaction temperature of catalytic oxidation process is controlled by the pressure of cooling drum, instead
350 DEG C of temperature, reaction pressure 1.5MPa (gauge pressure) are answered, in silver catalyst (loaded catalyst 0.79924kg, in catalyst
The load capacity of silver is 3.4% (quality), carrier SiO2) under the action of, occur catalytic oxidation (for isothermal reaction), so that
Oxygen in tail gas is sufficiently reacted with ethylene, and the conversion ratio of oxygen reaches 100%, and generates carbon dioxide and water, i.e., at
Oxygen volume content in tail gas after reason is 0.02%.Later, the tail gas of oxygen is removed, temperature is 180 DEG C, through subcooler
After cooling, into liquid separation tank, fuel gas pipe network or flare system is gone to carry out subsequent processing.Wherein, proportionality coefficient k=1.7272.
Final result shows compared with prior art, handles oxygen-containing tail gas using this method, cost reduces by 11%, energy consumption
23% is reduced, and highly-safe, environmental pollution is minimum.
[embodiment 6]
According to condition described in embodiment 1 and step, 25.2 DEG C, mass flow 2397.72kg/hr of oxygen-containing exhaust temperature,
Wherein, with volume fraction, oxygen content 5.1%, ethylene contents 33.9%, methane content 52.8%, carbon dioxide content
1.5%, argon content 6.2%, nitrogen content 0.2%, water content 0.3% will be in oxygen-containing tail gas by ethylene recovery unit
Ethylene removal is to 25.6%, after gas-gas heat exchanger exchanges heat to 70 DEG C, into shell and tube reactor, wherein shell-and-tube reactor
Heat production is issued by drum, in addition, the reaction temperature of catalytic oxidation process is controlled by the pressure of cooling drum, reaction temperature
300 DEG C, reaction pressure 1.35MPa (gauge pressure) of degree, in platinum catalyst (loaded catalyst 0.6850kg, platinum in catalyst
Load capacity is 1.2% (quality), carrier SiO2) under the action of, occur catalytic oxidation (for isothermal reaction), so that tail gas
In oxygen sufficiently reacted with ethylene, the conversion ratio of oxygen reaches 100%, and generates carbon dioxide and water, i.e., after treatment
Tail gas in oxygen volume content be 0.02%.Later, the tail gas of oxygen is removed, temperature is 165 DEG C, cooling through subcooler
Afterwards, into liquid separation tank, fuel gas pipe network or flare system is gone to carry out subsequent processing.Wherein, proportionality coefficient k=1.15.
Final result shows compared with prior art, handles oxygen-containing tail gas using this method, cost reduces by 9%, energy consumption drop
Low 18%, and it is highly-safe, environmental pollution is minimum.
Claims (10)
1. a kind of processing method of the oxygen-containing tail gas of ethylene oxide-glycol unit, oxygen-containing from ethylene oxide-glycol unit
After a part of ethylene that tail gas removes in oxygen-containing tail gas through ethylene recovery unit, enter tubular reaction by gas-gas heat exchanger
In pipe side catalytic oxidation occurs for device under the action of noble metal catalyst, so that oxygen and remaining ethylene in tail gas
Sufficiently reaction, removes oxygen therein, and then tail gas after treatment is cooling by cooler, into liquid separation tank, by processing
Tail gas afterwards goes fuel gas pipe network or flare system to carry out subsequent processing.
2. the processing method of the oxygen-containing tail gas of ethylene oxide-glycol unit according to claim 1, it is characterised in that epoxy second
It is device of the raw material by hydration method production ethylene glycol that alkane-glycol unit, which is by ethylene oxide, and oxygen-containing tail gas is from the ring
One gas extracted out in oxidative ethane-glycol unit circulating air；Catalytic oxidation occurs for shell and tube reactor pipe side, so that
Oxygen in tail gas with remaining ethylene sufficiently reacts after ethylene recovery unit removes ethylene in oxygen-containing tail gas；Tubular reaction
Catalytic oxidation in device is isothermal reaction or adiabatic reaction.
3. the processing method of the oxygen-containing tail gas of ethylene oxide-glycol unit according to claim 1, it is characterised in that shell and tube
Reactor heat production is issued by drum, and the reaction temperature of catalysis oxidation is controlled by the pressure of cooling drum.
4. the processing method of the oxygen-containing tail gas of ethylene oxide-glycol unit according to claim 1, it is characterised in that oxygen-containing tail
Oxygen volume content in gas is 3~9%, and the temperature of oxygen-containing tail gas is 20~100 DEG C.
5. the processing method of the oxygen-containing tail gas of ethylene oxide-glycol unit according to claim 1, it is characterised in that oxygen-containing tail
In gas, the volume ratio of ethylene and oxygen is not less than 1:3, and the oxygen volume content in tail gas after treatment passes through less than 2%
Control catalytic oxidation temperature controls the oxygen in tail gas after treatment by the oxygen content in measurement tail gas
Volume content.
6. the processing method of the oxygen-containing tail gas of ethylene oxide-glycol unit according to claim 1, it is characterised in that come from ring
The oxygen-containing tail gas of oxidative ethane-glycol unit is through ethylene recovery unit by the ethylene removal in oxygen-containing tail gas to volumn concentration
After 2~30%, shell and tube reactor is entered after gas-gas heat exchanger exchanges heat to 50~180 DEG C.
7. the processing method of the oxygen-containing tail gas of ethylene oxide-glycol unit according to claim 1, it is characterised in that shell and tube
Operating condition in reactor are as follows: 250~400 DEG C of operation temperature, 1~2MPaG of operating pressure.
8. the processing method of the oxygen-containing tail gas of ethylene oxide-glycol unit according to claim 1, it is characterised in that noble metal
Catalyst is silver, platinum or palladium, and noble metal mass fraction is 0.05~15% in noble metal catalyst.
9. the processing method of the oxygen-containing tail gas of ethylene oxide-glycol unit according to claim 8, it is characterised in that noble metal
Catalyst is silver.
10. the processing method of -9 oxygen-containing tail gas of ethylene oxide-glycol unit according to claim 1, which is characterized in that set
Set proportionality coefficient k, k=mSteam/ m, wherein m is the quality of oxygen-containing tail gas, kg；mSteamFor the quality of steam that drum generates, kg；K's
Value range is 0.5-2, by adjusting proportionality coefficient k, keeps it in reasonable value interval, ensure that shell and tube reactor
Cooling amount, do not allow runaway reaction.
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| CN111536419A (en) * | 2020-05-29 | 2020-08-14 | 连云港石化有限公司 | Treatment system and treatment method for high-oxygen-content tail gas |
| CN114405220A (en) * | 2022-02-22 | 2022-04-29 | 连云港石化有限公司 | Carbon dioxide tail gas treatment system and using method thereof |
| CN115382386A (en) * | 2021-05-24 | 2022-11-25 | 中国石油化工股份有限公司 | Method for treating oxygen-containing tail gas of industrial device |
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| CN111536419A (en) * | 2020-05-29 | 2020-08-14 | 连云港石化有限公司 | Treatment system and treatment method for high-oxygen-content tail gas |
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| CN115382386B (en) * | 2021-05-24 | 2024-05-07 | 中国石油化工股份有限公司 | Treatment method of oxygen-containing tail gas of industrial device |
| CN114405220A (en) * | 2022-02-22 | 2022-04-29 | 连云港石化有限公司 | Carbon dioxide tail gas treatment system and using method thereof |
| CN114405220B (en) * | 2022-02-22 | 2022-11-11 | 连云港石化有限公司 | Carbon dioxide tail gas treatment system and using method thereof |
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