CN110559842A - propylene gas catalytic deoxidation device and method with temperature and tail oxygen concentration control - Google Patents
propylene gas catalytic deoxidation device and method with temperature and tail oxygen concentration control Download PDFInfo
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Abstract
The invention discloses a propylene gas catalytic deoxidation device with temperature and tail oxygen concentration control and a method, and relates to the technical field of chemical tail gas treatment. After heat exchange of raw material propylene tail gas by a heat exchanger, further heating the raw material propylene tail gas to a reaction operation temperature by an electric heater, entering a deoxygenation reactor, wherein a catalyst bed layer is arranged in the deoxygenation reactor, after heat exchange of gas after deoxygenation reaction and raw material gas, cooling the gas by an air condenser, entering a gas-liquid separation tank, separating a liquid phase generated in the reaction process, boosting the gas phase by a compressor, entering a noncondensable gas separation tower, separating the noncondensable gas from the gas phase, and obtaining pure propylene from the liquid phase; and a tail oxygen analyzer is arranged on the fourth outlet pipeline, can detect the content of tail oxygen, and carries out reflux treatment through the fourth outlet branch pipeline if the content of tail oxygen is higher than a normal value. The invention is especially suitable for the process treatments of bed temperature runaway, tail oxygen content overproof and the like which are possibly generated due to oxygen content fluctuation, catalyst activity reduction and the like in the olefin deoxidation process.
Description
Technical Field
the invention relates to the technical field of chemical tail gas treatment, in particular to a propylene gas catalytic deoxidation device and method with temperature and tail oxygen concentration control.
Background
Oxygen-containing organic hydrocarbon gas or tail gas is common gas in the processes of chemical production, storage and transportation at present, for example, organic tail gas in oxidation and peroxidation processes, tail gas of a tank area communication system, landfill gas and the like, and the explosion risk is often caused due to high oxygen content; and SH 3009-. Therefore, in order to reduce the risk of explosion, recycle the organic gas, or ensure that the oxygen-containing organic tail gas meets the emission requirements, the oxygen-containing organic gas or tail gas needs to be deoxidized. For propylene oxide devices, including traditional chlorohydrination propylene oxide devices and hydrogen peroxide method propylene oxide devices applied in recent years, the oxygen content in propylene tail gas fluctuates within the range of 0.5-8%, the oxygen content of the propylene tail gas cannot be discharged into a combustible gas discharge system according to the requirements of the specifications, and the oxygen content needs to be reduced to be below 0.5% for discharge or reduced to be below 0.1% for recycling.
The deoxidation technology in the prior art mainly comprises pressure swing adsorption deoxidation, chemical adsorption deoxidation, activated carbon combustion deoxidation and catalytic combustion deoxidation, wherein the physical and chemical adsorption deoxidation load is small, the deoxidation technology is suitable for removing trace oxygen, the activated carbon deoxidation temperature is high, and the energy consumption is high. The existing catalytic deoxidation technology basically needs to add H2The reducing gas is equal, and the separation of the reducing gas becomes a problem which is difficult to solveTo give a title. Currently, the catalytic oxidation deoxidation technology for organic gas in the prior art is mainly used for methane-containing gas such as coal bed gas, landfill gas and the like, and the deoxidation technology for olefins such as ethylene, propylene and the like is only suitable for removing ppm-level trace oxygen, and the catalytic deoxidation technology for olefins such as ethylene, propylene and the like is not available.
disclosure of Invention
The invention aims to provide a propylene gas catalytic deoxidation device and method with temperature and tail oxygen concentration control, which do not need to add H2the reducing gas is equal, and propylene and oxygen are directly reacted to generate CO2And H2O, the purpose of propylene tail gas deoxidation is achieved, the reaction device is safe, environment-friendly and energy-saving, and the device is particularly suitable for solving the problems of temperature runaway of a catalytic bed layer, overproof tail oxygen content and the like possibly caused by oxygen content fluctuation, catalyst activity reduction and the like in the olefin deoxidation process.
The technical solution comprises:
A propylene gas catalytic deoxidation device with temperature and tail oxygen concentration control comprises a heat exchanger, an electric heater, a deoxidation reactor, an air condenser, a gas-liquid separation tank, a compressor and a separation tower, wherein the heat exchanger is provided with a first inlet, a second inlet, a first outlet and a second outlet, the first inlet is opposite to the second outlet, the first inlet is connected with a first inlet pipeline, and the first inlet pipeline is used for feeding raw material propylene tail gas into the heat exchanger; the outlet is connected with a first outlet pipeline;
The other end of the first outlet pipeline is connected with the inlet end of the electric heater, and the outlet end of the electric heater is connected with the inlet end of the deoxygenation reactor;
The outlet end of the deoxygenation reactor is connected with a second outlet pipeline, the other end of the second outlet pipeline is connected to the second inlet, a first temperature monitor is arranged on the second outlet pipeline, and the first temperature monitor is used for monitoring the temperature of gas discharged through the second outlet pipeline;
The second outlet is connected with a third outlet pipeline, the third outlet pipeline is connected with the inlet end of the air condenser, the outlet end of the air condenser is connected with the inlet end of the gas-liquid separation tank, the gas-liquid separation tank is provided with a third outlet and a fourth outlet, the third outlet is used for discharging gas phase, the fourth outlet is used for discharging liquid phase, the third outlet is connected with a fourth outlet pipeline, a fourth outlet branch pipeline is arranged on the fourth outlet pipeline, the other end of the fourth outlet branch pipeline is connected with the first inlet pipeline, and the fourth outlet branch pipeline is used for sending the discharged overproof tail oxygen gas into the heat exchanger for reflux treatment;
A tail oxygen analyzer is arranged on the fourth outlet pipeline, and a second temperature monitor is arranged on the electric heater;
the other end of the fourth outlet pipeline is connected to the inlet end of the compressor, the outlet end of the compressor is connected to the inlet end of the separation tower, the separation tower is provided with an outlet five and an outlet six, the outlet five is used for discharging a gas phase, and the outlet six is used for discharging a liquid phase.
In a preferred embodiment of the present invention, the propylene gas has the following composition in terms of volume percentage concentration: 0.5 to 8 percent of oxygen, 20 to 95 percent of propylene and the balance of nitrogen, carbon dioxide and hydrogen.
as another preferable scheme of the invention, the deoxygenation reactor is a fixed bed adiabatic reactor, the operation pressure is 0-4 MPa, and the reaction operation temperature is 100-430 ℃.
Further, a catalyst bed layer is arranged in the deoxygenation reactor, the outlet temperature of the catalyst bed layer is 200-600 ℃, and the space velocity of the propylene gas in the catalyst bed layer is 500-50000hr-1。
furthermore, the catalyst selected by the catalyst bed layer comprises a main catalyst and an auxiliary catalyst, the main catalyst is a noble metal catalyst, and the auxiliary catalyst is one or a mixture of more of oxides of soil, alkali metals or alkaline earth metals.
furthermore, the noble metal catalyst contains one or more active components of Pt, Pd, Ru, Rh, Ag and Ir.
Furthermore, the carrier selected by the catalyst is alumina balls, silica balls, titanium dioxide, molecular sieve, active carbon or carbon nano tubes.
Another task of the present invention is to provide a catalytic deoxygenation method for propylene gas with temperature and tail oxygen concentration control, which adopts the catalytic deoxygenation device, wherein the deoxygenation method comprises:
a, propylene gas enters a heat exchanger through a first inlet pipeline, is discharged from a first outlet after being subjected to heat exchange by the heat exchanger, and enters the electric heater through a first outlet pipeline;
The propylene gas comprises the following components in percentage by volume: 0.5 to 8 percent of oxygen, 20 to 95 percent of propylene, and the balance of nitrogen, carbon dioxide and a small amount of hydrogen;
b, heating the mixture to a temperature required by the reaction by an electric heater, and reacting the mixture in a deoxygenation reactor, wherein the operating pressure in the deoxygenation reactor is 1-3 MPa, and the reaction operating temperature is 100-430 ℃;
c, discharging the gas after the deoxidation reaction through a second outlet pipeline, measuring the temperature of the discharged gas through a first temperature monitor, feeding the gas after the deoxidation reaction into the heat exchanger, exchanging heat with the feed gas, cooling through an air condenser, feeding the gas into the gas-liquid separation tank, and separating a liquid phase generated in the reaction process through an outlet;
d, separating out a gas phase through an outlet, analyzing the tail oxygen content through a tail oxygen analyzer, controlling gas backflow through a valve on a fourth branch pipeline when the tail oxygen content is larger than or equal to 0.15%, cutting off backflow until the tail oxygen content is smaller than 0.15%, boosting the gas phase through a compressor, then feeding the gas phase into a separation tower, separating out noncondensable gas through the gas phase, and obtaining pure propylene through a liquid phase.
Further, the gas phase reflux amount is controlled by the temperature measured by the first temperature monitor.
Further, when the temperature measured by the first temperature monitor is greater than or equal to 550 ℃ and less than 560 ℃, controlling 10% of gas reflux; when the temperature measured by the first temperature monitor is higher than or equal to 560 ℃ and lower than 570 ℃, controlling 15% of gas reflux; when the temperature measured by the first temperature monitor is greater than or equal to 570 ℃ and less than 580 ℃, controlling 20% of gas to flow back; when the temperature measured by the first temperature monitor is greater than or equal to 580 ℃ and less than 590 ℃, controlling 30% of gas reflux; when the temperature measured by the first temperature monitor is greater than or equal to 590 ℃ and less than 600 ℃, controlling 40% of gas reflux; when the temperature measured by the first temperature monitor is more than or equal to 600 ℃, 50 percent of gas reflux is controlled.
in the prior art, the catalytic oxidation deoxidation technology for organic gas mainly aims at methane-containing gas such as coal bed gas, landfill gas and the like, and the deoxidation technology for olefin such as ethylene, propylene and the like is only suitable for removing ppm-level trace oxygen, and the catalytic deoxidation technology for olefin such as ethylene, propylene and the like is not available, but carbon deposition is easily generated on the surface of a catalyst at a certain temperature by olefin.
the invention relates to a propylene gas catalytic deoxidation method with temperature and tail oxygen concentration control, which does not need to add H2The reducing gas is equal, and propylene and oxygen are directly reacted to generate CO2And H2And O, the generation of carbon deposition on the surface of the catalyst and the generation of a byproduct CO can be inhibited, and the aim of deoxidizing the propylene tail gas is fulfilled. The invention provides a propylene gas catalytic deoxidation reaction device with automatic control and a method thereof, which are researched aiming at the problems of bed temperature runaway, excessive tail oxygen content and the like possibly caused by oxygen content fluctuation, catalyst activity reduction and the like in the olefin deoxidation process.
Drawings
The invention is further described below with reference to the accompanying drawings:
FIG. 1 is a flow chart of the catalytic deoxygenation process of propylene gas according to the present invention;
In the figure, 1-heat exchanger, 2-electric heater, 3-deoxygenation reactor, 4-air condenser, 5-gas-liquid separation tank, 6-compressor and 7-noncondensable gas separation tower.
Detailed Description
The invention provides a propylene gas catalytic deoxidation device with temperature and tail oxygen concentration control and a method thereof, and in order to make the advantages and technical scheme of the invention clearer and more clear, the invention is described in detail with reference to specific embodiments.
the raw material propylene tail gas of the invention comprises: the volume percentage concentration of the oxygen is 0.5-8%; the volume percentage concentration of the propylene is 20-95 percent, and the rest is nitrogen, carbon dioxide, a small amount of hydrogen and organic gas.
The deoxygenation reactor is a fixed bed adiabatic reactor, the operating pressure is 0-4 MPa, the reaction operating temperature is 100--1。
Percentage concentration of oxygen in reaction tail gas<0.2%, selectivity to CO<0.5％，CO2Selectivity is>98％。
the catalyst is a noble metal catalyst and contains one or more active components of Pt, Pd, Ru, Rh, Ag and Ir, the cocatalyst is one or more of rare earth, alkali metal or alkaline earth metal oxides which are combined in any proportion, and the carrier is alumina balls, silica balls, titanium dioxide, molecular sieves, active carbon or carbon nano tubes and the like.
as shown in figure 1, the propylene gas catalytic deoxidation device with temperature and tail oxygen concentration control comprises a heat exchanger 1, an electric heater 2, a deoxidation reactor 3, an air condenser 4, a gas-liquid separation tank 5, a compressor 6 and a non-condensable gas separation tower 7, wherein the heat exchanger is provided with a first inlet, a second inlet, a first outlet and a second outlet, the first inlet is opposite to the first outlet, the first inlet is connected with a first inlet pipeline, and the first inlet pipeline is used for feeding raw material propylene tail gas into the heat exchanger; the outlet is connected with a first outlet pipeline; the other end of the first outlet pipeline is connected with the inlet end of the electric heater, and the outlet end of the electric heater is connected with the inlet end of the deoxygenation reactor; the outlet end of the deoxygenation reactor is connected with a second outlet pipeline, the other end of the second outlet pipeline is connected to the second inlet, a first temperature monitor is arranged on the second outlet pipeline, and the first temperature monitor is used for monitoring the temperature of gas discharged through the second outlet pipeline; a third outlet pipeline is connected to the second outlet, the third outlet pipeline is connected to the inlet end of the air condenser, the outlet end of the air condenser is connected to the inlet end of the gas-liquid separation tank, the gas-liquid separation tank is provided with a third outlet and a fourth outlet, the third outlet is used for discharging gas phase, the fourth outlet is used for discharging liquid phase, the third outlet is connected with a fourth outlet pipeline, a fourth outlet branch pipeline is arranged on the fourth outlet pipeline, the other end of the fourth outlet branch pipeline is connected to the first inlet pipeline, and the fourth outlet branch pipeline is used for sending the discharged excessive tail oxygen into the heat exchanger for treatment; a tail oxygen analyzer is arranged on the fourth outlet pipeline, and a second temperature monitor is arranged on the electric heater; the other end of the fourth outlet pipeline is connected with the inlet end of the compressor, the outlet end of the compressor is connected with the inlet end of the separation tower, the separation tower is provided with an outlet five and an outlet six, the outlet five is used for discharging gas phase, and the outlet six is used for discharging liquid phase.
The deoxidation process flow of the invention is briefly described as follows:
the method comprises the following steps of after heat exchange of raw material propylene tail gas by a heat exchanger, further heating the raw material propylene tail gas to a reaction operation temperature by an electric heater, entering a deoxygenation reactor, after heat exchange of gas after deoxygenation reaction and raw material gas, cooling the gas to 20 ℃ by an air condenser, entering a gas-liquid separation tank, separating a liquid phase generated in the reaction process, boosting the gas phase by a compressor, entering a non-condensable gas separation tower, separating the non-condensable gas from the gas phase, and obtaining pure propylene from the liquid phase.
Aiming at the problems of bed temperature runaway, excessive tail oxygen content and the like possibly caused by oxygen content fluctuation, catalyst activity reduction and the like in the olefin deoxidation process, two control loops are designed: the temperature of the outlet of the reactor and the temperature of the reaction inlet are controlled by tail gas circulation to control the oxygen content of the reaction tail gas.
Reactor outlet temperature control: after the temperature of the outlet of the reactor reaches 550 ℃, a reflux regulating valve is opened, and 10% of gas is controlled to reflux; when the temperature reaches 560 ℃, the reflux regulating valve is opened, and 15% of gas is controlled to reflux; when the temperature reaches 570 ℃, the reflux regulating valve is opened, and 20% of gas is controlled to reflux; when the temperature reaches 580 ℃, a reflux regulating valve is opened, and 30% of gas is controlled to reflux; when the temperature reaches 590 ℃, a reflux regulating valve is opened, and 40% of gas is controlled to reflux; when the temperature reaches 600 ℃, a reflux regulating valve is opened, and 50% of gas is controlled to reflux; the temperature is lower than 500 ℃, and the reflux is cut off.
Controlling the oxygen content of reaction tail gas: oxygen content of tail gas of CO2，CO2>after 0.15%, CO2Difference from 0.15% the reactor inlet temperature increase was controlled to 10 per 0.02% increaseuntil the temperature of a reaction inlet reaches 430 ℃ or the temperature of an outlet reaches 600 ℃; cO2<After 0.1%, the reaction inlet temperature was controlled to decrease by 10 ℃.
The present invention will be described in detail with reference to specific examples.
example 1:
The composition of the propylene tail gas is as follows: the oxygen volume percentage concentration is 5%; the concentration of propylene in percentage by volume is 90% and that of nitrogen is 5%. The reaction pressure is 1MPa, and the reaction space velocity is 10000hr-1. The propylene tail gas is subjected to heat exchange by a heat exchanger to 80 ℃, and then enters a deoxygenation reactor, wherein the outlet temperature of a reaction bed layer is 280 ℃. And exchanging heat between the gas after the deoxidation reaction and the feed gas to 80 ℃, cooling to 20 ℃ by an air condenser, and then feeding the gas into a gas-liquid separation tank to separate a liquid phase generated in the reaction process. The gas phase oxygen content was 0.1%, gradually increased to 0.17% during operation, and after increasing the reaction inlet temperature to 130 ℃, the gas phase oxygen content was brought to 0.14%, and operation was maintained under this operating condition.
Example 2:
the composition of the propylene tail gas is as follows: the oxygen volume percentage concentration is 3.5%; the concentration of propylene in percentage by volume is 90%, and the concentration of nitrogen is 6.5%. Reaction pressure of 3MPa and reaction space velocity of 30000hr-1. The propylene tail gas is subjected to heat exchange at 40 ℃ by a heat exchanger to 380 ℃, and then enters a deoxygenation reactor, wherein the outlet temperature of a reaction bed layer is 535 ℃. And exchanging heat between the gas after the deoxidation reaction and the feed gas to 120 ℃, cooling to 20 ℃ by an air 4 condenser, and then feeding the cooled gas into a gas-liquid separation tank to separate a liquid phase generated in the reaction process. The content of gas-phase oxygen is 0.18 percent, the temperature of a reaction inlet is increased to 390 ℃, the temperature of a reaction bed outlet is increased to 545 ℃, and the content of gas-phase oxygen is reduced to 0.16 percent; the temperature of the reaction inlet is continuously increased to 400 ℃, the temperature of the reaction bed outlet is increased to 555 ℃, the content of gas-phase oxygen is reduced to 0.12%, the temperature of the reactor outlet is controlled to be started, the reflux regulating valve is opened, 10% of gas is controlled to reflux, the temperature of the reactor outlet is reduced to 540 ℃, the content of gas-phase oxygen is 0.13%, and the operation is maintained under the operation condition.
Example 3:
The composition of the propylene tail gas is as follows: the oxygen volume percentage concentration is 4.6%;The concentration of propylene in percentage by volume is 90% and the nitrogen is 5.4%. Reaction pressure of 3MPa and reaction space velocity of 30000hr-1. The propylene tail gas is heated to 385 ℃ by the heat exchanger, and then enters a deoxygenation reactor, wherein the outlet temperature of a reaction bed layer is 595 ℃. Exchanging heat between the gas after the deoxidation reaction and the feed gas to 130 ℃, cooling to 20 ℃ by an air condenser, then feeding the gas into a gas-liquid separation tank, separating out a liquid phase generated in the reaction process, wherein the content of gas-phase oxygen is 0.11%, controlling the temperature of an outlet of the reactor to start, opening a reflux adjusting valve, controlling 40% of gas to reflux, controlling the temperature of the outlet of the reactor to 520 ℃ and the content of the gas-phase oxygen to 0.19%; adjusting the reaction temperature to 540 ℃, and adjusting the gas-phase oxygen content to 0.12%; operation was maintained under this operating condition.
Example 4:
The composition of the propylene tail gas is as follows: the oxygen volume percentage concentration is 1%; the concentration of propylene in volume percent was 96%, and the nitrogen was 4%. The reaction pressure is 2MPa, and the reaction space velocity is 40000hr-1. The propylene tail gas is subjected to heat exchange by a heat exchanger to 200 ℃, and then enters a deoxygenation reactor, wherein the outlet temperature of a reaction bed layer is 245 ℃. And exchanging heat between the gas after the deoxidation reaction and the feed gas to 75 ℃, cooling to 20 ℃ by an air condenser, and then feeding the gas into a gas-liquid separation tank to separate a liquid phase generated in the reaction process. The gas phase oxygen content was 0.20%, after increasing the reaction inlet temperature to 220 ℃, the gas phase oxygen content was brought to 0.09%, and operation was maintained under this operating condition.
The parts which are not described in the invention can be realized by taking the prior art as reference.
It is intended that any equivalents, or obvious variations, which may be made by those skilled in the art in light of the teachings herein, be within the scope of the present invention.
Claims (10)
1. the utility model provides a take gaseous catalytic deoxidation device of propylene of temperature, tail oxygen concentration control, its includes heat exchanger, electric heater, deoxidation reactor, air condenser, gas-liquid separation jar, compressor and knockout tower, its characterized in that: the heat exchanger is provided with a first inlet, a second inlet, a first outlet and a second outlet, the first inlet is opposite to the second outlet, the first inlet is connected with a first inlet pipeline, and the first inlet pipeline is used for feeding raw material propylene tail gas into the heat exchanger; the outlet is connected with a first outlet pipeline;
The other end of the first outlet pipeline is connected with the inlet end of the electric heater, and the outlet end of the electric heater is connected with the inlet end of the deoxygenation reactor;
The outlet end of the deoxygenation reactor is connected with a second outlet pipeline, the other end of the second outlet pipeline is connected to the second inlet, a first temperature monitor is arranged on the second outlet pipeline, and the first temperature monitor is used for monitoring the temperature of gas discharged through the second outlet pipeline;
the second outlet is connected with a third outlet pipeline, the third outlet pipeline is connected with the inlet end of the air condenser, the outlet end of the air condenser is connected with the inlet end of the gas-liquid separation tank, the gas-liquid separation tank is provided with a third outlet and a fourth outlet, the third outlet is used for discharging gas phase, the fourth outlet is used for discharging liquid phase, the third outlet is connected with a fourth outlet pipeline, a fourth outlet branch pipeline is arranged on the fourth outlet pipeline, the other end of the fourth outlet branch pipeline is connected with the first inlet pipeline, and the fourth outlet branch pipeline is used for sending the discharged overproof tail oxygen gas into the heat exchanger to be refluxed for treatment;
a tail oxygen analyzer is arranged on the fourth outlet pipeline, and a second temperature monitor is arranged on the electric heater;
The other end of the fourth outlet pipeline is connected to the inlet end of the compressor, the outlet end of the compressor is connected to the inlet end of the separation tower, the separation tower is provided with an outlet five and an outlet six, the outlet five is used for discharging a gas phase, and the outlet six is used for discharging a liquid phase.
2. the catalytic deoxygenator device for propylene gas with temperature and tail oxygen concentration control of claim 1, wherein: the propylene gas comprises the following components in percentage by volume: 0.5 to 8 percent of oxygen, 20 to 95 percent of propylene and the balance of nitrogen, carbon dioxide and hydrogen.
3. The catalytic deoxygenator device for propylene gas with temperature and tail oxygen concentration control of claim 2, wherein: the deoxygenation reactor is a fixed bed adiabatic reactor, the operating pressure is 0-4 MPa, and the reaction operating temperature is 100-430 ℃.
4. the catalytic deoxygenator device for propylene gas with temperature and tail oxygen concentration control of claim 3, wherein: a catalyst bed layer is arranged in the deoxygenation reactor, the outlet temperature of the catalyst bed layer is 200-600 ℃, and the space velocity of propylene gas in the catalyst bed layer is 500-50000hr-1。
5. The catalytic deoxygenator device for propylene gas with temperature and tail oxygen concentration control of claim 4, wherein: the catalyst selected by the catalyst bed layer comprises a main catalyst and an auxiliary catalyst, wherein the main catalyst is a noble metal catalyst, and the auxiliary catalyst is one or a mixture of more of earth, alkali metal or alkaline earth metal oxides.
6. The catalytic deoxygenator device for propylene gas with temperature and tail oxygen concentration control of claim 5, wherein: the noble metal catalyst contains one or more active components of Pt, Pd, Ru, Rh, Ag and Ir.
7. The catalytic deoxygenator device for propylene gas with temperature and tail oxygen concentration control of claim 4, wherein: the carrier selected by the catalyst is alumina ball, silicon dioxide ball, titanium dioxide, molecular sieve, active carbon or carbon nano tube.
8. a catalytic deoxidation method for propylene gas with temperature and tail oxygen concentration control is characterized in that: the catalytic deoxidation device for the propylene gas, which adopts the propylene gas, disclosed by the claim 1, comprises the following steps:
a, propylene gas enters a heat exchanger through a first inlet pipeline, is discharged from a first outlet after being subjected to heat exchange by the heat exchanger, and enters the electric heater through a first outlet pipeline;
The propylene gas comprises the following components in percentage by volume: 0.5 to 8 percent of oxygen, 20 to 95 percent of propylene, and the balance of nitrogen, carbon dioxide and a small amount of hydrogen;
b, heating the mixture to a temperature required by the reaction by an electric heater, and reacting the mixture in a deoxygenation reactor, wherein the operating pressure in the deoxygenation reactor is 1-3 MPa, and the reaction operating temperature is 100-430 ℃;
c, discharging the gas after the deoxidation reaction through a second outlet pipeline, measuring the temperature of the discharged gas through a first temperature monitor, feeding the gas after the deoxidation reaction into the heat exchanger, exchanging heat with the feed gas, cooling through an air condenser, feeding the gas into the gas-liquid separation tank, and separating a liquid phase generated in the reaction process through an outlet;
d, separating out a gas phase through an outlet, analyzing the tail oxygen content through a tail oxygen analyzer, controlling gas backflow through a valve on a fourth branch pipeline when the tail oxygen content is larger than or equal to 0.15%, cutting off backflow until the tail oxygen content is smaller than 0.15%, boosting the gas phase through a compressor, then feeding the gas phase into a separation tower, separating out noncondensable gas through the gas phase, and obtaining pure propylene through a liquid phase.
9. The catalytic deoxygenation method of claim 8, wherein the catalytic deoxygenation method comprises the following steps: the gas phase reflux amount is controlled by the temperature measured by the first temperature monitor.
10. The catalytic deoxygenation method of claim 9, wherein the catalytic deoxygenation method comprises the following steps: when the temperature measured by the first temperature monitor is greater than or equal to 550 ℃ and less than 560 ℃, controlling 10% of gas to flow back; when the temperature measured by the first temperature monitor is higher than or equal to 560 ℃ and lower than 570 ℃, controlling 15% of gas reflux; when the temperature measured by the first temperature monitor is greater than or equal to 570 ℃ and less than 580 ℃, controlling 20% of gas to flow back; when the temperature measured by the first temperature monitor is greater than or equal to 580 ℃ and less than 590 ℃, controlling 30% of gas reflux; when the temperature measured by the first temperature monitor is greater than or equal to 590 ℃ and less than 600 ℃, controlling 40% of gas reflux; when the temperature measured by the first temperature monitor is more than or equal to 600 ℃, 50 percent of gas reflux is controlled.
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