JP2002220351A - Method for producing butane and propane, and device therefor - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a method and device for producing butane and propane where a large amount of butane and propane can be produced at low cost using inexpensive water and a solid carbon material as raw materials. SOLUTION: Synthesis gas is produced by catalytic reaction of water and a solid carbon material in the presence of a large amount of micro arc plasma in an arc plasma reactor APR. The synthesis gas is converted to methane in a methanization reactor MR, and the mixed gas of a specified ratio of methane and acetylene which is converted from methane is converted to n-butane by a super strong solid catalyst SC. The n-butane is then converted to propane by catalytic reaction using a zeolite catalyst.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

The present invention relates to a method and an apparatus for producing butane and propane, and more particularly to an industrial method for producing butane and propane and an apparatus therefor.

[0002]

2. Description of the Related Art Conventionally, butane and propane have been extracted as by-products of oil mining, and currently stay in high prices due to fluctuations in international oil prices. Difficult to maintain.

[0003] US Pat. Nos. 5,026,944 and 4,973,776 disclose using a solid superacid catalyst with a high selectivity of 99% from trace amounts of methane and acetylene.
Production method for conversion to butane and 83.2 from n-butane
A process for converting to propane with a high selectivity of% is disclosed.

[0004]

The conventional methods for producing butane and propane are extremely excellent, but the raw material costs are high because expensive natural gas and acetylene must be used as starting materials. Therefore, butane and propane cannot be economically mass-produced at low cost.

Accordingly, the present invention provides low-cost synthesis of methane and acetylene using inexpensive water and an inexpensive solid carbon material as starting materials, and continuously mass-produces butane and propane using these as intermediate materials at an extremely low cost. It is an object of the present invention to provide a method for producing butane and propane and an apparatus for producing the same.

[0006]

According to a first concept of the present invention, a method for producing butane and propane includes an insulating casing having a raw water supply port and a synthesis gas outlet, and an arc formed in the insulating casing. Preparing an arc plasma reactor having a plasma reaction chamber and an arc electrode disposed in the arc plasma reaction chamber; and filling a solid carbon material into the arc plasma reaction chamber to form a minute arc in a gap between the solid carbon materials. Forming a passage; supplying arc power to the arc electrode to generate a minute arc plasma in the minute arc passage; and feeding raw water or water vapor from the raw water supply port into the minute arc passage to produce the arc plasma. Reacting water vapor with the carbon of the solid carbon material in the presence of water to produce a synthesis gas containing hydrogen and carbon monoxide; Removing the synthesis gas from the mouth to cool the synthesis gas; introducing the synthesis gas into the methanation reactor to synthesize methane; irradiating methane with microwaves to produce acetylene; methane and acetylene With a solid superacid catalyst to produce n-butane; and contacting n-butane with a polymerization catalyst to convert it to propane.

[0007] According to a second concept of the present invention, a method for producing butane includes an insulating casing having a raw water supply port and a synthesis gas outlet, an arc plasma reaction chamber formed in the insulating casing, and an arc plasma reaction. Providing an arc plasma reactor having an arc electrode disposed in the chamber; filling a solid carbon material into the arc plasma reaction chamber to form a minute arc passage in a gap between the solid carbon materials; Supplying arc power to the electrodes to generate micro arc plasma in the micro arc passage; and passing raw water or water vapor through the micro arc passage from the raw water supply port to form water vapor and solid in the presence of the arc plasma. Producing a synthesis gas containing hydrogen and carbon monoxide by contacting and reacting the carbon of the carbon material; synthesizing the synthesis gas by extracting the synthesis gas from the synthesis gas outlet; Cooling methane; synthesizing methane by introducing synthesis gas into a methanation reactor; generating acetylene by irradiating methane with microwaves; contacting methane and acetylene with a solid superacid catalyst Reacting to synthesize n-butane;

According to a third concept of the present invention, an apparatus for producing butane and propane is formed in an insulating casing having a carbon material feed port, a feed water supply port, and a synthesis gas outlet, and in the insulating casing. An arc plasma reactor having an arc plasma reaction chamber, an arc electrode arranged in the arc plasma reactor, and a minute arc passage formed in a gap between carbon materials filled in the arc plasma reactor; A raw water supply pump for supplying the raw water inlet; a carbon material supply device for supplying the solid carbon material to the carbon raw material inlet; supplying arc power to the arc electrode to generate an arc plasma in the minute arc passage. And a multi-phase AC power source for generating a synthesis gas by causing a water vapor and a carbon material to contact and react in a minute arc passage; A methanation reactor for synthesizing methane from synthesis gas; an acetylene synthesis tower for irradiating methane with microwaves to produce acetylene; and a solid superacid catalyst column for synthesizing butane by contacting methane with acetylene to react. A polymerization catalyst column for converting butane into propane by contacting the butane with a polymerization reaction catalyst.

[0009]

According to the method and the apparatus for producing butane and propane of the present invention, the minute arc passage formed in the arc plasma reactor is constituted by a solid carbon material, and the minute arc by spark is formed in the minute arc passage. A large amount of plasma is generated, steam is introduced into the micro arc passage, and the steam reacts with the carbon of the carbon material in the presence of the arc plasma to form a sulfur-free monoxide as shown in the following equation. Efficiently generates synthesis gas consisting of carbon and hydrogen.

C + H ₂ O → Co + H ₂ (1) Co + H ₂ O → CO ₂ + H ₂ (2)

Next, the synthesis gas obtained by the reactions (1) and (2) is then fed to a methanation reaction tank, where it reacts with the methanation catalyst and reacts with the methane-containing gas as shown in the following formula. Generate.

Co + 3H ₂ → CH ₄ + H ₂ O (3) Co ₂ + 4H ₂ → CH ₄ + 2H ₂ O (4)

As shown in the above reaction formulas (3) and (4), the methane-containing gas contains product water as a by-product. However, the product water is separated and condensed from the methane-containing gas and recovered as condensed water. By recycling this as a raw material for the arc plasma reactor, it is possible to reduce the environmental burden without discharging the wastewater to the outside and at the same time to further reduce the raw material cost.

A portion of the methane gas from which water has been separated is subjected to microwave plasma reaction to be converted to acetylene with a maximum selectivity of 97%. Next, acetylene and methane are contact-reacted with a solid superacid catalyst to be converted into n-butane with a selectivity of up to about 99%, which is contacted with a polymerization catalyst to synthesize propane in high yield.

[0015]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, a butane / propane manufacturing apparatus according to a preferred embodiment of the present invention will be described with reference to the drawings. In FIG. 1, a butane / propane production apparatus 10 includes a carbon material input device 12 for supplying a solid carbon material, a water material supply device P1, and an arc plasma reactor APR that generates a synthesis gas from the carbon material and the water material. ,
A heat exchanger H for preheating the raw water by exchanging heat with the raw water and the syngas, and a cooler C1 for cooling the syngas.
A steam-water separator S, a compressor CM for pressurizing the synthesis gas, a methanation reactor MR filled with a methanation catalyst, a cooler C2 for cooling the methane gas, a pressure reducing valve V, and a gas-liquid separator. The apparatus includes a vessel S2, a methane supply line M, and a recycle line R for merging generated water with raw water via a circulation pump P2. Methane gas flow control valve CV
1, a super strong acid catalyst tower SC via CV2,
It is supplied to the acetylene synthesis tower AS. Acetylene synthesis tower AS is disclosed in JP-A-6-219970 and JP-A-10-139.
No. 6,932 and U.S. Pat. No. 5,205,912, a microwave generator for inducing a microwave plasma reaction and not absorbing microwaves, for example,
A microwave reactor including a reaction tube such as a quartz glass tube is provided. The microwave generation unit generates a microwave of 2.45 GH and irradiates the reaction tube via a waveguide while introducing methane at a linear velocity of 10 to 15 cm / min to cause a microwave plasma reaction. Preferably, it is converted to acetylene with a selectivity of 95% or more. Flow control valves CV1, C
V2 controls the flow rate of methane, respectively, and supplies it to the solid superacid catalyst tower SC and the acetylene synthesis tower AS. The flow rate of methane at that time is selected so as to be supplied to the solid superacid catalyst at a ratio of 0.05 to 5 mol per 100 acetylene. As the solid superacid catalyst, zirconia sulfate molded pellets sold by Japan Energy Co., Ltd. are used, and the pellets are filled in a fixed-bed reactor, and a mixed gas of acetylene and methane is filled into the reactor. 50 ° C, pressure 1-2
The reaction is carried out at 5 atm to convert n-butane, preferably with a selectivity of 95% or more. Next, n-butane is supplied to the polymerization catalyst tower PC to convert it into propane. As a polymerization catalyst, a zeolite catalyst known as ZSM-5 disclosed in U.S. Pat. No. 3,702,886 is used, packed in a reaction tower, and reacted at a reaction temperature of 200 to 300 ° C. and a reaction pressure of 10 to 50 atm. Will be

FIG. 2 shows the arc plasma reactor A of FIG.
The specific structure of PR is shown. In FIG. 2, an arc plasma reactor APR includes an arc plasma reactor 14 connected to a carbon raw material charging device 12, a plasma power supply 16,
And a cooler H1. The raw material input device 12 includes a hopper 20 for storing a solid carbon raw material such as powdered, pelletized or massive graphite, granular activated carbon, spherical carbon or carbon powder, a screw feeder 22, and a rotary valve 24. 14 is charged with a carbon raw material. The plasma reactor 14 includes a cylindrical outer insulating casing 26 made of a heat-resistant ceramic, and an inner insulating casing 32 having an arc plasma reaction chamber 34, and has an insulating electrode holder 28 attached to a top end thereof with a bolt 30. Prepare. When the granular carbon material is supplied into the arc plasma reaction chamber 34, a large number of minute arc passages 3
5 are formed in the plasma arc reaction chamber 34, and a large amount of small plasma arcs due to sparks are uniformly generated in the plasma arc reaction chamber 35 in the small arc passage. At this time, the raw water turns into steam due to the high temperature on the upstream side of the plasma arc reaction chamber 34, and a small flow of the water vapor contacts and reacts with the carbon of the carbon material while passing through the small arc passage, thereby synthesizing as shown in the above-mentioned reaction formula. Gas is generated.

The insulating holder 28 is a rod-shaped multi-phase AC electrode 3
6, 38 and 40 are supported. Below the insulating casing 32, a disc-shaped ground electrode 42 for emitting thermoelectrons for arc generation is arranged. A cylindrical arc plasma reaction chamber 34 is formed inside the inner insulating casing 32. The ground electrode 42 is supported by an electrode holder 78 formed at the lower end of the insulating casing 26, and is fixed by bolts 80. The electrode holder 28 has a carbon material supply port 50 connected to the carbon material charging device 12. A raw water supply port 52 for introducing raw water or water vapor is disposed adjacent to and above the arc electrodes 36, 38, and 40 above the insulating cane 26. The reason is that the arc electrode is effectively cooled by the raw water or steam to prevent an abnormal temperature rise of the arc electrode. A cooling portion 63 composed of a spiral cooling passage 54 is formed on the outer periphery of the inner casing 32, and these cooling passages communicate with each other through a communication passage 64. The insulating casing 26 has an inlet 74 and an outlet 76. The inlet 74 is connected to the raw water supply pump P <b> 1 and the recycle line R, and the outlet 76 communicates with the raw water supply port 52. An end plate 82 is fixed to a flange portion 78 constituting a lower end portion of the insulating casing 26 via a bolt 80, and a sealing material 83 is disposed between them. At the lower end of the arc plasma reaction chamber 34, a filter 84 is supported by an end plate 82. The end plate 82 has a synthesis gas outlet 86. Reference numeral 88 indicates a seal member.

The three-phase AC electrodes 36, 38, and 40 are connected to the three-phase AC power supply 16, and a ground electrode 42 is connected to the neutral point. From the three-phase AC power supply 16 to the three-phase AC electrodes 36, 3
8, 40 and the neutral electrode 42, the output frequency 50-6
0Hz, output voltage 30-240V, output current 50-20
0 A three-phase AC power is supplied. At this time, of the three-phase AC electrodes 36, 38, and 40, current flows alternately from the two electrodes and the three electrodes to the neutral electrode 42, and arc plasma is generated in the gap between the carbon raw materials by sparks. The generation position of the plasma arc continuously changes in accordance with the phase of the three-phase alternating current, a large amount of ionized ions are always present in the gap between the carbon materials, and thermoelectrons are constantly emitted from the ground electrode 42. , A plasma arc is always generated stably.

Referring to FIGS. 1 and 2, a method for producing butane and propane according to a preferred embodiment of the present invention will be described as follows.

Step 1 (hereinafter abbreviated as ST): an insulating casing 32 having a raw water supply port 52 and a synthesis gas outlet 86, an arc plasma reaction chamber 34 formed in the insulating casing, and an arc plasma reaction chamber The arc plasma reactor 14 including the multi-phase AC electrodes 36, 38, 40 and the ground electrode 42 arranged at 34 is prepared.

ST2: Arc Plasma Reaction Chamber 34
Is filled with a solid carbon material to form a minute arc passage 35 in a gap between the carbon materials.

ST3: Arc electrodes 36, 38, 40
To generate micro arc plasma in the micro arc passage 35, and raise the temperature in the reaction chamber to 800.
The input voltage is controlled so as to be within the range of １０００1000 ° C. In this temperature range, the ratio of hydrogen generation to Co is 2 to 2.
This is 5, and the molar ratio of Co / H in the synthesis gas can be adjusted to an appropriate range.

ST4: Raw water or water vapor H ₂ O is passed through the raw water supply port 52 into the minute arc passage 35, and the water vapor and the carbon of the carbon material are contact-reacted in the presence of arc plasma. A synthesis gas containing hydrogen and carbon monoxide as in (1) and (2) is generated.

ST5: The synthesis gas is taken out from the synthesis gas outlet 86, the synthesis gas is cooled by the heat exchanger H and the cooler C1, the steam is separated by the separator S1, and the compressor CM
To about 50 atm.

ST6: The synthesis gas is introduced into the methanation catalyst of the methanation reaction tank MR, and methane gas is synthesized from the synthesis gas by the above reaction formula.

ST7: The methane gas is cooled by the cooler C2, and the methane gas is separated by the pressure reducing valve V from the steam-water separator S.
After cooling under reduced pressure in step 2, the produced water is separated and condensed from the methane gas.

ST8: The methane gas is converted to acetylene by a microwave plasma reaction in the acetylene synthesis tower AS.

ST9: Acetylene and methane are mixed at a ratio of 0.05 to 5 mol with respect to 100 of acetylene, and the mixture is brought into contact with solid superacid catalyst pellets to be converted into n-butane.

ST10: n-Butane is brought into contact with a zeolite catalyst and converted into propane by a polymerization reaction.

Next, the operation of the butane / propane production apparatus 10 shown in FIG. 1 will be described. In FIG. 1, first, the screw feeder 22 and the rotary valve 24 are driven to fill the arc plasma reactor APR with a carbon material such as granular activated carbon to a predetermined level. At that time, the rotary valve 24 and the screw feeder 22 are stopped.
Next, the raw water supply pump P1 is driven, and three-phase AC power is supplied to the arc electrode of the plasma arc reactor APR. At this time, the raw water supplied to the arc plasma reaction chamber from the raw water supply port 52 is converted into steam at a high temperature near the upstream thereof, is divided into a large number of minute flows, flows into a large number of minute arc passages, and flows into the minute arc passage. Flows from the upstream to the downstream of the arc plasma reaction chamber. In this state, synthesis gas is generated as described above. The synthesis gas is converted to 60 in the heat exchanger H and the first cooler C1.
The temperature is cooled to 90 ° C. to 90 ° C., and water is separated as condensed water from the synthesis gas in the separator S1. The condensed water undergoes heat conversion in the heat exchanger H via the recycle line R, and then joins with the raw water. On the other hand, the synthesis gas is 10 to 5
After being pressurized to 0 atm, it is introduced into the methanation reaction tower MR. The reactor MR is maintained at 250 to 600 ° C., and the methanation catalyst is a known nickel catalyst or USP.
4,238,371, USP 4,368,142, US
The methanation catalyst disclosed in P4,774,261 or JP-A-5-184925 is used. The methane gas is cooled by the second cooler C2 and sent to the steam separator S2 via the pressure reducing valve V, where water is separated and recovered from the methane gas. The condensed water collected at this time is combined with the raw water by the recycling line R and the circulation pump P2, and is reused in the above-described cycle. Methane gas is converted to acetylene in the acetylene synthesis tower AS, and the flow control valve CV1
Is mixed at a predetermined ratio with the methane gas whose flow rate is controlled in the above, and is converted to n-butane by the solid superacid catalyst SC, and then converted to propane by a polymerization reaction in the polymerization catalyst tower PC.

In the above embodiment, a temperature sensor is attached to a three-phase AC electrode or an insulating casing to generate a temperature signal, and the temperature signal is compared with an optimal reference temperature signal stored in a computer to output an output of a three-phase AC power source composed of an inverter. The operating temperature in the arc plasma reaction chamber may be constantly maintained at a stable level by controlling the frequency to a predetermined level. In addition, the feed water supply pump P1 is periodically stopped to preferentially use the condensed water of the first and second steam separators, thereby replenishing the shortage and reducing the feed amount of the feed water. It is possible to

The butane and propane production method and apparatus of the present invention have the following advantages. (1) Since the starting materials of butane and propane use extremely inexpensive water and inexpensive solid carbon material, the cost of the raw materials can be greatly reduced, and the cost of butane and propane can be greatly reduced. (2) Using a small, high-performance arc plasma reactor,
Since a large amount of synthesis gas is generated, the production efficiency of butane and propane is high. (3) Since all carbon materials are used only for syngas generation and are not used as fuel for combustion in the reformer, the utilization efficiency of raw materials is extremely high. (4) In the arc plasma reactor, the Co / H2 ratio in the synthesis gas can be changed depending on the operating temperature in the reactor reaction chamber, so that the operation control of the butane / propane production plant can be easily optimized. (5) In the synthesis gas production, usually, a complicated process of periodically interrupting the synthesis gas generation process and supplying air to the reformer to burn the hydrocarbon fuel is required. Since these complicated processes are not required, the operation control of the butane / propane production plant is extremely simplified, and the operation cost can be greatly reduced. (6) In the present invention, methane is synthesized from water and a carbon material, and then acetylene is synthesized from methane to form an intermediate component, and n-butane is obtained at a high conversion rate from the intermediate component. Very low-cost butane and propane can be produced in high yield. (7) By-product water is collected as a by-product at the time of syngas generation and methane synthesis, and if this is discarded outside, the cost for environmental measures will increase the cost. In the present invention, since the by-produced water is recycled as a raw material, the environmental load is extremely low. (8) According to the method of the present invention, it is possible to instantaneously start up and shut down the production plant only by shutting off the supply of power to the arc electrode and turning on / off the power of the pump. Sometimes it is extremely safe, and it is advantageous for safety measures to the local residents. (9) Since the manufacturing apparatus of the present invention is small, compact, and high-performance, and the manufacturing process is simplified,
Return on investment in a short time. (10) Since the butane / propane production plant of the present invention is small, high-performance and safe, it is possible to set up a production plant adjacent to the consuming area, thereby greatly reducing transportation costs and environmental damage caused by truck transportation. Prevention becomes feasible.

In the above embodiment, the arc plasma reactor is described as supplying the raw water from the upstream and taking out the synthesis gas from the synthesis gas outlet provided downstream. However, when the amount of slag generated is large depending on the type of carbon material, Alternatively, a raw water supply port may be provided downstream of the reactor, and a synthesis gas outlet may be provided upstream of the reactor to separate slag and synthesis gas by a cyclone. Although the plasma arc reactor has been described as using a rod-shaped three-phase AC electrode, the three-phase AC electrode is cylindrically arranged at intervals in the axial direction, and a rod-shaped ground electrode is disposed at the center thereof. May be used.

[0034]

As is apparent from the above, according to the method and apparatus for producing butane and propane of the present invention,
It is possible to mass-produce butane and propane at very low cost near the consuming area, and has a very high practical contribution. Moreover, according to the present invention, there is no emission of harmful substances such as wastewater, so that the environmental load is extremely small. Furthermore, since water and carbon materials, which are the starting materials for butane and propane, can be procured for an extremely long period of time, stable supply at low cost is possible without being affected by the rise in international oil prices.

[Brief description of the drawings]

FIG. 1 is a schematic view of a butane / propane production apparatus according to a preferred embodiment of the present invention.

FIG. 2 shows a cross-sectional view of the arc plasma reactor of FIG.

[Explanation of symbols]

12 carbon material input device, 13, 15, 19 recycling line, 24 rotary valve, APR arc plasma reactor, H heat exchanger, C1 cooler, S1, S2
Steam-water separator, CM compressor, MR methanation reactor, C2 cooler, V pressure reducing valve, AS acetylene synthesis tower, SC solid superacid catalyst tower, PC polymerization catalyst tower,

──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. ⁷ Identification symbol FI Theme coat ゛ (Reference) C07C 1/04 C07C 1/04 4/10 4/10 9/08 9/08 9/10 9/10 / / C07B 61/00 300 C07B 61/00 300

Claims (8)

[Claims] An arc plasma including an insulating casing having a raw water supply port and a synthesis gas outlet, an arc plasma reaction chamber formed in the insulation casing, and an arc electrode disposed in the arc plasma reaction chamber. A step of preparing a reactor; a step of filling a solid carbon material in an arc plasma reaction chamber to form a small arc passage in a gap between the solid carbon materials; Generating a fine arc plasma in the raw material water or water vapor through a raw water supply port into the micro arc passage to cause a contact reaction between the water vapor and the carbon of the solid carbon material in the presence of the arc plasma to produce hydrogen and Generating a synthesis gas containing carbon monoxide; removing the synthesis gas from the synthesis gas outlet and cooling the synthesis gas;
A step of introducing methane into a methanation reactor to synthesize methane; a step of irradiating methane with microwaves to produce acetylene; and a step of contacting methane and acetylene with a solid superacid catalyst to synthesize butane. And b. Contacting butane with a polymerization reaction catalyst to convert it into propane. 2. A process for producing butane and propane, comprising: 2. The method according to claim 1, further comprising the steps of: cooling the syngas to separate and recover water in the syngas as condensed water; circulating the condensed water to an arc plasma reactor; Butane and propane. 3. The three-phase AC electrode according to claim 1, further comprising: a three-phase AC electrode in which the arc electrode is supported by the insulating casing; and a ground electrode spaced from the three-phase AC electrode. A method for producing butane and propane, wherein a plurality of arc plasmas are generated at the same time. 4. An arc plasma having an insulating casing having a raw water supply port and a synthesis gas outlet, an arc plasma reaction chamber formed in the insulation casing, and an arc electrode disposed in the arc plasma reaction chamber. A step of preparing a reactor; a step of filling a solid carbon material into an arc plasma reaction chamber to form a minute arc passage in a gap between the solid carbon materials; Generating a small arc plasma;
Raw water or water vapor is passed from the raw water supply port into the minute arc passage, and the water vapor and the solid carbon material carbon are contact-reacted in the presence of arc plasma to produce a synthesis gas containing hydrogen and carbon monoxide. Removing synthesis gas from the synthesis gas outlet to cool the synthesis gas; introducing syngas into the methanation reactor to synthesize methane; and irradiating methane with microwaves to produce acetylene. And a step of contacting methane and acetylene with a solid superacid catalyst to synthesize butane. 5. The method according to claim 4, further comprising: cooling the syngas to separate and recover water in the syngas as condensed water; circulating the condensed water to an arc plasma reactor; And supplying the mixture to a methanation reactor. 6. The three-phase electrode and the ground electrode according to claim 4, further comprising a three-phase AC electrode in which the arc electrode is supported by the insulating casing, and a ground electrode spaced from the three-phase AC electrode. Wherein a plurality of arc plasmas are simultaneously generated between the two. 7. A carbon material feed port, a feed water supply port,
An insulating casing having an outlet for syngas;
Arc plasma having an arc plasma reaction chamber formed in an insulating casing, an arc electrode arranged in the arc plasma reactor, and a minute arc passage formed in a gap between carbon materials filled in the arc plasma reactor. A reactor; a raw water supply pump for supplying raw water to a raw water input port; a carbon material supply device for supplying solid carbon material to a carbon material raw input port; and a minute arc by supplying arc generating power to an arc electrode A plasma power source for generating an arc plasma in the passage and causing a reaction between water vapor and a carbon material in a minute arc passage to generate a synthesis gas; and a methanation connected to an arc plasma reactor to synthesize methane from the synthesis gas. An acetylene synthesis tower that generates acetylene by irradiating methane with microwaves; and reacts methane with acetylene in a contact reaction. Solid strong acid catalyst tower for synthesizing butane and; butane polymerization reaction catalyst in contact with converted to propane polymerization catalyst column and; manufacturing apparatus butane and propane, characterized in that more made. 8. A cooling device connected to a methanation reaction tank, a steam-water separator for separating water as condensed water from methane, and a recycling line for circulating the condensed water to an arc plasma reactor according to claim 7. Further equipped butane and propane production equipment.