KR810000776B1 - Gas mixing method - Google Patents

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Description

Gas mixing method

1 is a flow sheet showing an example in which the molecular oxygen gas mixing method according to the present invention is used for a method for producing ethylene oxide by an oxygen oxidation method.

2 is a flow sheet showing an example in which the mixing method according to the present invention is used for a method for producing ethylene oxide by air oxidation.

3 is a longitudinal sectional view showing one embodiment of a mixing apparatus according to the present invention.

4 is a cross-sectional view taken along the line IV-IV of FIG.

5 is an enlarged partial cross-sectional view taken along line V-V in FIG.

6 is a partial longitudinal sectional view showing another embodiment of the mixing apparatus according to the present invention.

7 is a cross-sectional view taken along the line VII-VII of FIG.

8 is an enlarged partial cross-sectional view taken along line VII-VII in FIG.

9 is a partial sectional view showing yet another embodiment of a mixing apparatus according to the present invention.

10 is a cross-sectional view taken along line X-X of FIG.

11 is an enlarged partial cross-sectional view taken along line IX-IX of FIG.

12 is a partial longitudinal cross-sectional view showing another embodiment of a mixing apparatus according to the present invention.

13 is a partial longitudinal sectional view showing still another embodiment of the mixing apparatus according to the present invention.

14 is a partial longitudinal sectional view showing yet another embodiment of a mixing apparatus according to the present invention.

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a hydrocarbon-containing gas and a method for containing molecular oxygen, and more particularly, to a catalytic gas phase oxidation reaction of hydrocarbons such as ethylene, propylene, benzene, ortho xylene, naphthalin, in particular ethylene by molecular oxygen. The present invention relates to a method of sufficiently mixing an ethylene-containing gas and a molecular oxygen-containing gas in a step of gas phase oxidation to produce ethylene oxide.

In the process of producing a ethylene oxide by contact phase oxidation of a hydrocarbon, oxidation reaction, for example, ethylene by contact phase oxidation of ethylene by molecular oxygen in the presence of a silver catalyst, saturated hydrocarbons such as methane and ethane, nitrogen, carbon dioxide, and argon The carbon-hydrogen-containing gas containing oxygen and the like and the molecular oxygen-containing gas of air, oxygen-enriched air, or pure oxygen are mixed at a predetermined ratio, and then charged with a silver catalyst. It is introduced into the reaction zone and the catalytic phase oxidation reaction is performed in this reaction zone. The reaction product gas containing ethylene oxide produced in this reaction zone is led to the bottom of the ethylene oxide absorption tower, and is introduced into the aqueous medium and countercurrent such as water, ethylene glycol aqueous solution, etc. introduced from the tower top of the tower. The ethylene oxide in this gas is absorbed and separated by contact. The absorbent liquid is discharged from the absorption tower bottom and transferred to the ethylene oxide dissipation tower so that the ethylene oxide is separated and the separated ethylene oxide is transferred to the purification process again. On the other hand, the gas that was not absorbed in the ethylene oxide absorption tower is introduced into the carbon oxide absorption tower as needed, carbon dioxide is absorbed by the aqueous alkali solution, and then supplied with ethylene and molecular phase to prepare a desired reaction raw material gas composition. Then it is recycled to the reaction zone.

It is preferable that the mixed gas circulated in any of the circulation steps of the reactor, the ethylene oxide absorption tower, and the carbon dioxide absorption tower in the ethylene oxide production step is out of the combustion range. However, in the mixing of hydrocarbon-containing gas and molecular oxygen-containing gas, there is often a local gas composition within the combustion range due to insufficient mixing and backflow. Therefore, the mixture of the hydrocarbon-containing gas and the molecular oxygen-containing gas is carried out as quickly as possible to reduce the area where the gas mixture is insufficient, and also prevents the reverse flow of the hydrocarbon-containing gas stream to the molecular oxygen-containing gas pipe. Eggplant improvements have been proposed. For example, in Japanese Patent Application Laid-Open No. 46-4362 and 47-16381, hydrocarbon-containing gas streams are provided with molecular oxygen-containing gas by means of a mixing device consisting of a ring having a plurality of tubes or pipes. The risk is reduced by adding a large amount of nitrogen to the molecular oxygen-containing gas in order to disperse the mixture in the mixture, to add and mix, and to prevent the hydrocarbon-containing gas stream from flowing back into the piping. However, in such a device, an unexpected or unexpected stop or restart of the device occurs due to regular repair failures, power failures, etc., and locally enough energy is generated to cause ignition in such an abnormal state. Accidents such as destruction occur.

In addition, there is an increased risk of explosion due to flame propagation due to local ignition energy generation or accumulation thereof due to an unexpected cause, and it is extremely difficult to eliminate such a risk even in a conventional apparatus. Therefore, the method of dissipating the ignition energy at the time of mixing the conventional hydrocarbon-containing gas and the molecular oxygen-containing gas is not sufficient yet, and the amount of nitrogen for preventing backflow is not enough.

Accordingly, an object of the present invention is to provide a novel and mixing method of hydrocarbon-containing gas streams and molecular coral-containing gas streams.

)을 마련하고, 이와 같이 하여 양자간에 형성되는 가스혼합역에 분자상의 산소 함유 가스류를 도입하여 탄화수소 함유 가스류와 충분히 혼합하는 것을 특징으로 하는 탄화수소 함유 가스류와 분자상 산소 함유가스류와의 혼합 방법에 의하여 달성된다.The purpose of this is to provide an aqueous medium seal through which at least one gas stream can pass by sealing the shaft into which the hydrocarbon-containing gas stream flows into the aqueous medium, and at the same time the flame which allows at least one of the gas stream to pass through the side of the gas stream. Radio wave shielding station

And a molecular oxygen-containing gas stream is introduced into the gas mixing zone formed therebetween so as to be sufficiently mixed with the hydrocarbon-containing gas stream. By the mixing method.

In addition, they are usually a discharge port and an introduction port of a hydrocarbon-containing gas stream provided on the upper body and a lower part of the main body, and an introduction port and an discharge port of an aqueous medium provided respectively on the upper and lower parts of the main body, and hydrocarbon-containing gas streams in the main body. Is provided on the side from which the gas flows and at least one aqueous medium holding means through which the gas flows in contact with the aqueous medium, and the gas flows on the side from which the hydrocarbon-containing gas flow in the main body is discharged. Hydrocarbon-containing gas and molecular acid-containing gas flow comprising at least one flame propagation shielding means, the retention means, and a molecular oxygen-containing gas introduction means provided in the gas mixing chamber formed between the shielding means. By means of a mixing device with.

In the gas mixing method according to the present invention, the hydrocarbon-containing gas is brought into countercurrent contact with the aqueous medium in a gas absorption tower or a container provided with an aqueous medium holding means such as a tray packing. On the other hand, the molecular oxygen-containing gas is brought into contact with the aqueous medium or separately supplied water in the aqueous medium retention zone and introduced into the gas mixing section to be mixed with the hydrocarbon-containing gas. The hydrocarbon-containing gas stream sufficiently mixed with the molecular oxygen-containing gas is passed to the reaction process through a demister provided at the top of the mixing apparatus, with or without passing through the aqueous medium retention zone again.

The gas mixing device according to the present invention is provided with at least one aqueous medium retention means therein, and a flame propagation shielding means such as an aqueous medium retention means or a demister at the top, and has the same structure as the gas absorption tower. . Therefore, the aqueous medium means is a tray such as a cap drain, a uniflux tray, a sieve tray, a ballast tray, a valve tray, a bantry tray, a turbo grid tray, a dual flow tray, a kittel tray, and the like. Furthermore, the filling of fillers, such as a raschici ring, a letsi ring, versadol, an interlock sadol, and the like can be used. As flame propagation means, an aqueous medium retention means such as a tray and a packed layer and a demister can be used. As the demister, any type can be used as long as it has a function as a mist separator. Among them, a wire mesh type is particularly suitable. As the aqueous medium retention means, a tray is preferable, and in particular, a tray of a particle flow contact type provided with a Daung kiln is most preferable. Thus, a tray top and a packed tower absorption tower are usually used as mixing devices, and in particular, a plurality of trays are used. The tray top provided is preferable. However, besides the absorption tower, it can be used as a mixing device having the above-described structure.

Thus, a hydrocarbon-containing gas inlet and an aqueous medium outlet are provided below the aqueous medium retention means of the mixing device, and hydrocarbon-containing gases (hydrocarbon-containing gas and molecular oxygen-containing gas are provided above the flame propagation shielding means). Outlet of the gaseous mixture). In addition, the aqueous medium inlet is provided above the flame propagation shielding means if it is an aqueous medium retention means, and below it if it is a demister.

In this way, the gas mixing chamber formed between the aqueous medium retention means and the flame propagation blocking means is provided with a molecular oxygen introduction soda as described later. Accordingly, the hydrocarbon-containing gas introduced at the inlet of the lower part of the mixing device rises through the layer of the aqueous medium on the tray where the aqueous medium introduced at the upper inlet remains, and when it reaches the gas mixing zone, Mixing with molecular oxygen introduced into the mixing zone through the aqueous medium is performed. It is then discharged out of the mixing device from the outlet through a flame propagation means such as a tray or a demister. On the other hand, the aqueous medium supplied to the mixing device is supplied from the inlet at the top of the uppermost tray of the mixing device and flows down the mixing device while passing through the tray at the bottom of the mixing device and finally discharged from the outlet. When using a gas absorption tower as a mixing device, it is simultaneously dissolved in an aqueous medium of a desired component and removed from the bottom of the gas absorption tower by exclusion. The flow rate ratio between the aqueous medium and the hydrocarbon-containing gas may be a ratio sufficient to remain in the liquid medium retention means in the aqueous medium retention means so that the gaseous liquid is sufficiently contacted without rising gas. This can be determined using the dragon's equation. Therefore, when the gas mixing device also serves as a gas absorption tower, the liquid gas ratio L / G is increased.

The aqueous medium used in the present invention is still not completely separated even after separating and recovering the circulated water and the predetermined component from the fresh water such as pure water, deionized water, and the absorption discharged from the bottom of the absorption tower. Or a circulating aqueous solution containing other components. As an example of said last thing, 0.1-30 weight% of ethylene glycol used at the time of absorbing and recovering the oxidation reaction product of ethylene at the time of ethylene oxide manufacture. In particular, the aqueous solution containing 1-20 weight% is mentioned.

Examples of the molecular oxygen-containing gas include pure oxygen diluted with a fluorine gas other than pure oxygen, air enriched with oxygen, and air. As the hydrocarbon-containing gas, in addition to ethylene, propylene isobutylene, benzene, orthoxylenenaphthalin, and the like, these hydrocarbons are obtained by contact gas oxidation of the above-mentioned molecular oxygen-containing gas and still contain unreacted hydrocarbons. . In particular, when a catalytic gas phase oxidation reaction gas containing unreacted hydrocarbons is used, mixing of molecular oxygen-containing gas is performed simultaneously with rare water due to absorption of a desired product.

Therefore, the mixing method and apparatus according to the present invention are ethylene oxide from ethylene, acrolein to propylene and acrylic acid or acryronitrile to benzene, maleic anhydride to benzene, ortho xylene or ethylene by contact gas phase oxidation with molecular oxygen-containing gas. It can be used conveniently in the process of manufacturing phthalic anhydride in naphthalin, naftquinone in naphthalin, etc. In particular, excellent results are obtained in the process of producing ethylene oxide by vapor-phase oxidizing ethylene with pure oxygen.

In the gas mixing method according to the present invention, a representative introduction method of the molecular oxygen-containing gas into the gas mixing region is as follows.

The injection type oxygen-containing gas introduction method of the first type diverges and connects a plurality of tube fluxes to a gas mixing zone formed between two aqueous medium retention means, for example, between a tray and another tray, and at each of its front ends. One or more orifices are provided. The tip in the tube is distributed evenly on the tray so as not to interfere with the operation of the tray and the orifice portion is immersed in a depth of 1 to 10 cm in the layer of aqueous medium staying on the tray. Each orifice is installed to meet the same level surface. As a whole, there is a high difference of about 0.1 to 3 cm in the entire retention zone. Therefore, when the flow rate of the molecular oxygen-containing gas is minute, it flows through only some orifices and from the remaining orifices. There is a fear that the flow back to the branch audience. In order to avoid this, an inert gas such as nitrogen is added to the molecular oxygen-containing gas which will surpass the differential pressure of the aqueous medium of 0.1 to 3 cm, and flows from the entire orifice at any flow rate. The molecular oxygen-containing gas ejected from the orifice at the tip of the branch pipe into the aqueous medium is mixed in contact with the hydrocarbon-containing gas in the gas mixing zone in this aqueous medium.

The second type of molecular coral-containing gas introduction method comprises an inner tube having a plurality of orifices in the gas phase of a gas mixing zone formed between two aqueous medium retention means, for example, between a tray and another tray, and an opening at the top. The double pipe which becomes an external appearance which has an external appearance is inserted and prepared substantially horizontally. Molecular oxygen-containing gas is continuously introduced into the inner tube and water is introduced into the outer tube. From the orifice provided in the lower portion of the inner tube, the molecular oxygen-containing gas is bubbled into the aqueous layer in the outer shell, and is discharged into the gas mixing zone together with water from the opening in the upper portion of the outer shell to be mixed with the hydrocarbon-containing gas. The amount of water used may be at least the sum of the amount saturated in the molecular oxygen-containing gas and the amount climbed. However, it is it is only to increase the It coast to futile to use excessive preferred that the gas volume of the used state using the water of 5 to 100ℓ per 1m ^3, the water that is used is due to the back flow of the oxygen-containing gas pipe the molecule In order to avoid contamination of organic matter, it is preferable to use pure or deionized water substantially free of organic halogen and the like.

The molecular oxygen-containing gas introduction method of the third type is a complex type of the first type and the second type, and gas mixing formed between two aqueous medium retention means, for example, between a tray and another tray. An inner tube having a plurality of orifices and a plurality of tube bundles communicating with the upper part are connected to each other, and a double tube is formed by inserting one or more orifices at the distal end of each branch pipe. The distal end of the tube is immersed in the aqueous medium remaining on the tray if it is uniformly arranged on the tray so as not to disturb the operation of the tray as in the case of the first type. The molecular oxygen-containing gas is continuously introduced into the inner tube and water into the outer tube. From the orifice provided in the lower portion of the inner tube, the molecular oxygen-containing gas is bubbled into the aqueous layer in the outer shell, and is discharged into the tray-like aqueous medium together with the water discharged from the outer shell through the branch pipe connected to the outer shell. Subsequently, the mixture is brought into contact with the hydrocarbon-containing gas at the gas mixing zone. At this time, the quantity and quality of water supplied to the external appearance are the same as in the case of the second mold, and the liquid depth and arrangement of the orifice portion are the same as in the case of the first mold.

The molecular oxygen-containing gas introduction method of the fourth type is described above except that the molecular oxygen-containing gas introduction means is provided in an aqueous medium retention zone, for example, a gas mixing zone formed between the tray and the demister. It is the same as the method of the first type.

The method of introducing the molecular oxygen-containing gas of the fifth type is described above except that the molecular oxygen-containing gas introduction means is provided in an aqueous medium retention zone, for example, a gas mixing zone formed between the tray and the demister. It is the same as the method of the second type.

The molecular oxygen-containing gas introduction method of the sixth type is described above except that the molecular oxygen-containing gas introduction means is provided in an aqueous medium retention zone, for example, a gas mixing zone formed between the tray and the demister. It is the same as the method of the third type.

According to the present invention, in the gas mixing zone, the hydrocarbon-containing gas introduction side is sealed by an aqueous medium on the aqueous medium retention means, and the hydrocarbon-containing gas (gas mixture with molecular oxygen-containing gas) is discharged by the aqueous medium retention means. Since it is sealed by an aqueous medium or shielded by a demister, ignition energy is generated for some reason, even if it is hard, the energy is absorbed by them and burns in a region that is likely to fall within the local combustion range. The flame is shielded in the seal area even if it is hard to produce, so that the flame does not propagate outside the gas mixing area. In addition, the molecular oxygen introduced into the gas mixing zone is mixed with the hydrocarbon-containing gas after contact with an aqueous medium or water, so that the pressure on the molecular oxygen-containing gas side is lowered, for example, the molecular oxygen gas is caused by water entering even if hard. There is no fear that the piping side will fall within the explosion limits. In addition, in the introduction methods of the second, third, fifth and sixth shapes, addition of an inert gas such as nitrogen is not required even when the molecular oxygen-containing gas flow rate is used. In addition, also in the introduction methods of the first and fourth molds, it is sufficient to add a small amount of inert gas sufficient to compensate for variations in the orifice liquid depth.

Next, a case where the gas mixing method and apparatus according to the present invention is used in the production process of ethylene oxide will be described with reference to the accompanying drawings, for example.

1 is a flow sheet showing the winry of the oxygen oxidation method, in which diluent gases such as ethylene supplied from line 1 and methane and ethane supplied from line 2 are mixed with ethylene and oxygen circulated in line 3 It is mixed with gas and subjected to catalytic gas phase oxidation in reactor 5 by line 4. The reaction product gas containing ethylene oxide exiting the reactor (5) is cooled to a predetermined temperature in the cooler (6), and then the ethylene oxide absorption tower (7) having a pressure of 2 to 40 kg / cm2 is introduced downward and introduced from the tower top. Ethylene oxide is absorbed by countercurrent contact with an absorbing liquid which is an aqueous solution of ethylene glycol having a temperature of 40 ° C. or less introduced through the line 9 from the bottom of the water or the ethylene oxide dissipation tower 8 having a temperature of 40 ° C. or less. The absorbent liquid is supplied from the column bottom to the ethylene oxide dissipation tower via line 10, where ethyl oxide is dissipated by heating and transferred from the column top to the purification process. The bottom liquid from which ethylene oxide has been substantially removed is circulated from the line 9 to the ethylene oxide absorption tower 7 as an absorbent liquid. On the other hand, pure oxygen is supplied to the ethylene oxide absorption tower 7 from the line 11 and mixed with unabsorbed gas (mixture of unreacted ethylene, oxygen, carbon dioxide, diluent gas, etc.) by a method described later, and a part of Is circulated from the line 12 to the reactor 5, and the remainder is countercurrently contacted with an alkaline absorbing liquid, for example, an aqueous potassium carbonate solution, which is led to the carbon dioxide gas and the absorption tower 13 and supplied from the carbon dioxide gas dissipation tower 14. To absorb and remove carbon dioxide gas. The absorbing liquid is transferred to the carbon dioxide dissipation tower 14 where carbon dioxide gas is dissipated and removed from the column top. The unabsorbed gas from the top of the carbon dioxide gas absorption tower 13 is transferred to the line 3 via the line 15 where it is mixed with freshly replenished ethylene, diluent gas and the like and circulated to the reactor 5.

2 is a flow chart showing the principle of the air oxidation method, in which the ethylene supplied in the line 21 is combined with a mixed gas of ethylene and air circulated from the line 23 and the first reactor 25a from the line 24. Is oxidized on the contactor. The reaction product gas containing the ethylene oxide exiting the first reactor 25a is cooled to a predetermined temperature in the cooler 26a and then introduced into the lower portion of the first absorption tower 27a at a pressure of 2 to 40 kg / cm 2. Here, ethylene oxide is absorbed by countercurrent contact with an absorbent liquid which is an aqueous solution of ethylene glycol having a temperature of 40 ° C. or less introduced from the column top or a temperature of 40 ° C. or less introduced via line 29a from the bottom of the dissipation tower 28 via line 29a. . Air is supplied from the line 31 to the first absorption tower 27a and mixed with unabsorbed gas (a mixture of unreacted ethylene, nitrogen, carbon gas, etc.) by a method described below, and part of the line 32 is line 32. After passing through the line 23 is mixed with freshly replenished ethylene and the like is circulated to the first reactor (25b). All of them are supplied to the second reactor 25b and subjected to contact gas phase conversion. The reaction gas containing ethylene oxide exiting the second reactor 25b is cooled to a predetermined temperature in the cooler 26b and then transferred to the second absorption tower 27b, the same method as in the case of the first absorption tower 27a. In countercurrent contact with water or aqueous ethylene glycol solution supplied from line 29b to absorb ethylene oxide. The unabsorbed gas is partly circulated to the second reactor and the remainder is sent to a purge process (not shown) or to a third reactor (not shown) to provide for contactor phase oxidation. The column bottom liquids of the first and second absorption towers 27a and 27b are transferred from the line 30 to the dissipation tower 28 where the ethyl oxide is dissipated by heating and transferred from the tower to the purification process.

3 to 5 show an example of the gas mixing device according to the present invention, which is a case where an ethylene oxide absorption tower is used. The mixing device is usually sealed by attaching the light plates 41 and 42 to the top and bottom of the main body 40, respectively, and the upper light plate 41 has a mixture outlet 43 of ethylene and oxygen, and a lower tube. An absorbent liquid outlet port 44 is provided at 42 with an absorbent liquid inlet port 45 at the upper part of the main body 40, and an oxidation reaction generation gas inlet port at the lower part of the main body. The main body 40 is provided with the demister 47 with respect to the uppermost part, and the several tray 48 (for example, 30 stage ballast tray) in the lower part. Thus, a gas mixing chamber 49 is formed between the tray 48 and the other tray 48, and a plurality of tube bundles 50 are separated by the oxygen introduction pipe 51 in the gas mixing chamber 49. Is connected and inserted. One or more orifices 52 are provided in the front-end | tip of a pipe | tube. Thus, an aqueous solution of 10 wt% ethylene glycol alcohol at the concentration of 10% by weight is supplied to the uppermost tray 48 from the inlet port 45 as an absorbing measure of the ethylene oxide absorption tower 7 (gas mixing device), and the ethylene oxidation reaction generating gas. While absorbing ethylene oxide through the down kiln (53) while absorbing the ethylene oxide in order to reach the bottom through the lower tray 48, it is transferred from the outlet 44 to the ethylene oxide dissipation tower (8). On the other hand, an oxygen-containing gas, such as pure oxygen, is introduced from the conduit 50 together with a small amount of nitrogen in the absorbent liquid 54 which is retained on the tray 48 at the orifice 52 of the branch pipe 50. It is ejected and mixed with the oxidation reaction product gas. The mixed gas is discharged from the discharge port 43 after passing through the demister 47. In addition, in FIG. 3, 60 is a spreading line, and 61 is a side. The side 61 is normally closed, but if an abnormality occurs in the oxygen inlet tube 51 due to some reason, the oxygen supply source becomes negative pressure when the oxygen supply source is abolished. Open (61). As a result, the gas in the mixing chamber flows in from the pressure equalizing line 60, so that the pressures are parallel and the liquid level is returned to the original state.

6 through 8 illustrate another embodiment of the present invention, and the absorbent liquid of the tray 148 is prevented from causing plading into the gas mixing chamber 149 formed by the tray 148 and the other tray 148. The inner tube 150 having a plurality of orifices 152 above the liquid level of 154 and a double tube consisting of an exterior 157 having an opening 155 at the top and a blocking plate 156 thereon are approximately horizontal. It is provided as an oxygen supply means. Oxygen-containing gas, such as pure oxygen, is introduced from the inner tube 150 and pure water is introduced from the outer tube 157. Oxygen is bubbled in the orifice 152 provided in the inner tube 150 to pass through the pure layer and at the same time to prevent the absorbent from entering the exterior 157 and the opening 155 of the exterior 157. It is discharged together with water from the gap of and the oxidation reaction gas is mixed.

9 through 11 illustrate another embodiment of the present invention, in which a plurality of orifices 252 are inserted into a gas mixing chamber 249 formed by a tray 248 and another tray 248. Branch pipe 250 and a plurality of pipes 258 communicated to the upper part are connected to each other, and a double pipe is formed by inserting an outer tube 257 provided with one or more orifices 259 at the distal end of each branch pipe. will be. Oxygen-containing gas, such as pure oxygen, is introduced from the inner tube 250 and pure water is introduced from the outer tube 257. Oxygen is bubbled in the orifice 252 provided in the inner tube 250, passes through the pure layer, is ejected from the orifice 259 of the branch tube 258 together with the pure water in the absorption liquid, and mixed with the oxidation reaction product gas. In Figures 9 and 10, 260 is a uniform line.

In the present invention, the installation point of the molecular oxygen-containing gas introduction means (Figs. 3 to 11) of the first to third types may be any tray shape in the gas mixing device using the absorption tower. It is preferable that the tray top from the top or the 5th stage to a low density is preferable.

12 is a view showing another embodiment of the present invention, wherein an oxygen inlet pipe 351 connecting a plurality of branch pipes 350 having an orifice at the front end thereof is provided between the uppermost tray 348 and the demister 347. Other than that is the same as the case of FIG.

FIG. 13 shows yet another embodiment of the present invention. As shown in FIG. 8, an inner tube 450 having a plurality of orifices and an outer portion 457 having an opening in the upper portion and a blocking plate 456 in the upper portion thereof. The same double tube as in the case of FIGS. 6 to 7 is provided except that the double tube is provided between the uppermost tray 448 and the demister 447 as the oxygen supply means.

FIG. 14 shows another embodiment of the present invention, in which an inner tube 550 having a plurality of orifices as shown in FIG. 11 and a plurality of pipe bundles 558 communicating therewith are branched and connected to each other. Except for providing the double tube which becomes the external appearance 557 by which the orifice was provided in the front-end part as an oxygen supply means between the tray 548 of the shortest part and the demister 547, it is completely the same as the case of FIGS. 9-11.

In addition, the diameter and the number of orifices of the oxygen-containing gas introduction tube in the present invention are determined by the pressure loss allowed in the production apparatus, and it is set so that the pressure loss is 0.1 to 3 kg / cm 2 in the steady state. desirable.

Claims (1)

Seal the hydrocarbon-containing gas stream inlet side with an aqueous medium to provide an aqueous medium seal zone through which at least one of the gas streams can pass, and provide a flame propagation shielding zone through which the at least one gas stream can pass through the gas stream outlet side. A method of mixing a hydrocarbon-containing gas and a molecular oxygen-containing gas, characterized by introducing a molecular oxygen-containing gas stream into a gas mixing zone formed therebetween to sufficiently mix with a hydrocarbon-containing gas stream.

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