JPH06256239A - Production of methanol - Google Patents

Abstract

PURPOSE:To obtain a methanol production apparatus having high energy efficiency and advantageous for scaling-up. CONSTITUTION:Methanol is produced from a hydrocarbon by using a fluidized layer catalytic reactor 19 containing heat-transfer tubes 20 as the methanol synthesis reactor, recovering the high-pressure steam obtained from the reactor and using the steam as a power for compressors 32,51 of the methanol production apparatus or as a power for a gas turbine or an oxygen separator.

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for producing methanol from hydrocarbons, and more particularly to a method for producing methanol from hydrocarbons which synthesizes methanol using a fluidized bed catalytic reactor.

[0002]

2. Description of the Prior Art Methanol is used in large quantities as an inexpensive fuel that is low in pollution and easy to transport.
The development of ultra-large equipment with a capacity of over 000T / D is required. In recent years, a fluidized bed catalytic reactor has been developed as a response to an ultra-large-sized apparatus for producing such fuel methanol. For example, JP-A-60-84142 and JP-A-60-84142
60-122040 and JP-A-60-106534 describe a method for producing a fluidized catalyst for methanol synthesis.
No. 63-211246 describes the catalyst and reaction conditions when carrying out methanol synthesis using a fluidized bed catalyst.

The biggest problem in the development of such a large-sized methanol production apparatus is the increase in the size of a gas reforming apparatus for producing synthesis gas from hydrocarbons. In the conventional steam reforming apparatus, a reforming furnace is used. Since it is a method of externally heating the reaction tube at 1,500 to 2000 T / D is the limit for increasing the size of the methanol production equipment. As a gas reforming apparatus in a large-scale apparatus, a system combining steam reforming and partial oxidation has recently attracted attention. This is because hydrocarbon and steam are mixed to carry out a primary reforming reaction, then oxygen is added to carry out a partial oxidation and a secondary reforming reaction, and the obtained high temperature gas is used as a heating source for the primary reforming reaction. It is a thing. This method does not require the use of a reforming furnace that heats the reaction tube externally without supplying heat from the other side. Therefore, since high-pressure synthesis gas can be obtained, there is no need to raise the pressure using a synthesis gas compressor. There is an advantage that the synthesis reaction can be carried out directly, and since the reforming reaction is carried out under high pressure, it is easy to increase the size of the apparatus. As for the self-heat exchange type reactor for carrying out the primary reforming reaction and the secondary reforming reaction in this way, it is described in JP-A-60-186401, JP-A-1-261201, JP-A-2-18303, etc. The structure is shown.

[0004]

There is a demand for improvement in energy efficiency in the development of a large-scale methanol production apparatus, and in the gas reforming apparatus, the self-heating for performing the primary reforming reaction and the secondary reforming reaction as described above is required. Although an exchange type reactor is being developed, a method for effectively recovering reaction heat in a fixed catalyst reactor and using it in a process has been developed in a methanol synthesizer. However, in the fixed catalyst reactor, the temperature difference between the reaction section and the heat recovery section has a limit, so that there is a limit to the recovery of reaction heat, and it is difficult to increase the reaction rate in the reactor. Therefore, after separating methanol from the reaction gas from the reactor, a large amount of gas must be circulated to the reactor, which requires compression power and enlarges the reactor, which limits the upsizing of the methanol synthesizer. It will be. An object of the present invention is to develop a method for producing methanol that has high energy efficiency and can be made larger.

[0005]

Means for Solving the Problems As a result of diligent studies on the method for producing methanol having the above-mentioned problems, the present inventor has found that by using a fluidized bed catalytic reactor in a methanol synthesizer, the heat of reaction can be improved as high-pressure steam. The present inventors have found that a method for producing methanol which has high energy efficiency and can be made larger can be obtained by efficiently collecting and effectively using this in the process, and arrived at the present invention.

[0006]

Means for Solving the Problems That is, the present invention provides a method for producing methanol from a hydrocarbon, which comprises (1) indirectly heating a mixed gas of a hydrocarbon and steam to carry out a catalytic reaction to produce hydrogen, carbon monoxide and The process of producing a synthesis gas containing carbon dioxide as an active ingredient, and (2) using a fluidized bed catalytic reactor having a heat transfer tube inside, perform a methanol synthesis reaction at 60 to 120 atm and transfer the heat of reaction to the reaction. A method for producing methanol characterized in that it has a step of generating high-pressure steam of 40 to 60 atm by transmitting it to saturated water via a heat pipe, and recovering power from the high-pressure steam obtained in step (2). is there.

The fluidized bed catalytic reactor has a higher heat transfer efficiency of the reaction gas as compared with the conventional fixed catalytic bed reactor, so that more high-pressure steam can be recovered and the temperature distribution in the catalytic bed is uniform. The present invention has characteristics such that a high reaction rate can be obtained and a circulation amount of a reaction gas can be reduced, a side reaction product amount can be reduced, distillation purification can be easily performed, and a pressure loss in a catalyst layer can be small. The method of (1) above enhances the energy efficiency of the entire methanol production apparatus by utilizing the fact that the heat recovery is enhanced and the energy consumption of the process is reduced by using a fluidized bed catalytic reactor. In the synthesis gas generator of the present invention, a large-scale methanol production apparatus having higher energy efficiency can be obtained by using the self-heat exchange type reactor that performs the above-mentioned primary reforming reaction and secondary reforming reaction. You can Less than,
The method of the present invention will be described in detail.

Although natural gas containing methane as a main component is usually used as the raw material hydrocarbon in the step (1), LPG, naphtha, etc. are also used depending on the site conditions. Further, in order to improve the basic unit of the raw material, a purge gas from the synthesis system is mixed with the hydrocarbon. Although a nickel-based catalyst is usually used as the steam reforming catalyst, it is necessary to desulfurize the hydrocarbon as a raw material in advance in order to avoid a decrease in the activity of the reforming catalyst. Steam of mixed gas of hydrocarbon and steam /
Steam is used so that the carbon ratio is usually about 2.0 to 3.5, preheated to 400 to 550 ° C and supplied to the reactor.

In the steam reforming reaction, a mixed gas of hydrocarbon and steam is indirectly heated to carry out a contact reaction to obtain a reformed gas at 700 to 900 ° C. This high-temperature reformed gas is subjected to various heat recovery and then cooled to be a synthesis gas containing hydrogen, carbon monoxide, and carbon dioxide as effective components. As will be described later, after indirect heating to carry out a contact reaction, oxygen is added to carry out a partial oxidation, and a secondary reforming reaction is further carried out using a reforming catalyst. The reformed gas temperature in the case of only the primary reforming reaction is 850 to 900 ℃, and the pressure is limited to about 10 to 25 atm in order to obtain the desired reaction rate, but partial oxidation and secondary reforming reaction In this case, since the secondary reformed gas of 930 to 1000 ° C is obtained, the temperature of the primary reformed gas can be set to 750 to 800 ° C and the pressure can be increased to about 30 to 45 atm. When the secondary reformed gas is used as the heat source for the primary reforming reaction as described above, the temperature of the primary reformed gas can be increased by increasing the oxygen content to obtain the secondary reformed gas at 980 to 1080 ° C. 700 to 800
The process can be carried out at a temperature of 60 ° C. and a pressure of 60 to 120 atm without using a syngas compressor.

That is, when the secondary reforming reaction is carried out after the primary reformed gas is partially oxidized, the pressure of the gas reforming apparatus can be increased and the power of the syngas compressor is reduced. The energy efficiency can be increased, and the gas reforming apparatus can be downsized by increasing the pressure, which is advantageous for a large-sized methanol apparatus, but an oxygen gas is required, so an oxygen separation apparatus is additionally required. Also, if the secondary reformed gas is used as the heat source for the primary reforming reaction, the pressure difference between the inside of the primary reforming reaction tube and the heating gas becomes small, so a heat exchange type reactor can be used, and an external heat type reactor can be used. Since the reforming furnace of No. 1 is not required, the gas reforming apparatus can be operated at a higher pressure and it is easy to cope with an increase in size. If the pressure of the gas reformer is made equal to the pressure of the methanol synthesizer, the syngas compressor can be eliminated.

In step (2), a fluidized bed catalytic reactor is used to carry out a methanol synthesis reaction from hydrogen, carbon monoxide and carbon dioxide according to the following reaction formula. CO + 2H ₂ → CH ₃ OH + 21.6 kcal / mol CO ₂ + H ₂ → CO + H ₂ O − 9.8 kcal /
mol CO ₂ + 3H ₂ → CH ₃ OH + H ₂ O + 11.
A copper-based catalyst is usually used in the 8 kcal / mol methanol synthesis reaction, and the reaction is carried out at a temperature of 200 to 300 ° C and a pressure of 60 to 120 atm.
As a fluidized catalyst for the methanol synthesis reaction, a catalyst in which a catalyst component is supported on a strong carrier such as silica, alumina or zirconium is usually used, and the particle size of the catalyst is 1 to 250 μm.
m.

For the methanol synthesis reaction, a fluidized bed catalytic reactor having a heat transfer tube inside is used, and the reaction heat is transferred to saturated water through the heat transfer tube to a high pressure of 40 to 60 atm, preferably 45 to 55 atm. Steam is recovered. The obtained high-pressure steam is processed in step (1)
In some cases, the steam is used as the raw material steam, but by using this steam as a power source for the synthesis gas compressor, the synthesis gas circulator, the raw hydrocarbon gas compressor, etc., the energy efficiency of the methanol production apparatus can be increased. Power is also recovered by the gas turbine using the purge gas of the methanol synthesizer.By introducing high-pressure steam with fuel into the combustion chamber of this gas turbine, power is recovered from the steam and NOx in the exhaust gas is removed. descend.

When performing partial oxidation, a cryogenic separation method or a PSA method is generally used as an oxygen separator, and the oxygen gas used for partial oxidation is usually 98% or more in purity. The high-pressure steam recovered from the fluidized bed catalytic reactor is also used as a power source for an air compressor for oxygen separation and a refrigerator for deep-chill separation,
A gas turbine as described above can be used. Further, when performing partial oxidation, it is possible to mix a part of the raw material hydrocarbon with the oxygen gas to carry out the partial oxidation, and it is also possible to mix a part of the raw material steam. By mixing a part of the raw material hydrocarbon and the part of the raw material steam during the partial oxidation, the load on the primary reforming reaction tube is reduced.

Next, an embodiment of the present invention will be described with reference to the drawings. As described above, the gas reforming apparatus of the step (1) in the present invention is (a) in the case of only the primary reforming, (b) in the case of performing the secondary reforming by partially oxidizing the primary reformed gas, (c) A high-temperature secondary reformed gas may be used as a heat source for the primary reforming reaction to further raise the reforming pressure. Each case will be described.

FIG. 1 (a) is a system diagram of an example in which the gas reformer of FIG. 1 (a) is a primary reformer only, in which a general steam reformer, a synthesis gas compressor and a fluidized bed catalytic reactor are combined. It is a methanol production device. After the desulfurization treatment, the raw material hydrocarbons are introduced from the flow channel 1 and mixed with the raw material steam from the flow channel 2. The mixed gas passes through the flow path 3 and the mixed gas heater 4
Is heated to 400 to 550 ° C. and introduced into the primary reforming reaction tube 6 through the flow path 5. The primary reforming reaction tube is filled with a Ni-based catalyst, and the primary reforming reaction tube 6 is heated in the primary reforming furnace 7 by combustion of the fuel from the flow path 8 to perform the steam reforming reaction. In the combustion waste gas convection section 9 of the reforming furnace 7, a high pressure steam heater I10, etc. is installed in addition to the mixed gas heater 4 to recover heat, and the combustion waste gas finally reaches 150 to 170 ° C. Released into the atmosphere.

The gas leaving the primary reforming reaction tube 6 has a pressure of 10 to 10
25 atm, temperature 850-900 ℃, about 90% of raw hydrocarbons
% Is reformed, and H ₂ , CO, and
CO ₂ and unreacted water vapor are contained, and some heat recovery and cooling of the high pressure steam heater II 13 etc. is performed between the flow path 11 and the suction 12 of the syngas compressor, and condensed water is separated. Been 30
Introduced into the syngas compressor 14 at ~ 40 ° C. This synthesis gas compressor 14 compresses the synthesis gas to 60 to 120 atm, and
Sent to the synthetic system via. This syngas merges with the circulating gas from the flow path 16 and passes through the flow path 17, and then in the syngas heater 18.
It is heated to 180 to 230 ° C. and introduced into the methanol synthesis reactor 19. The reactor 19 is filled with a fluid catalyst,
The methanol synthesis reaction is carried out at 240 to 280 ° C.

A large number of heat transfer tubes are provided in the methanol synthesis reactor.
20 is installed, the boiler water from the flow path 21 is heated and boils, and the high-pressure steam and the boiler water are separated in the steam separator 23 through the flow path 22. In addition, the water / water separator 23 has a flow path 24.
The boiler supply water is supplied from the boiler in proportion to the amount of high-pressure steam generated.
Since the reactor 19 is filled with a fluidized catalyst to obtain high heat transfer efficiency, high pressure steam of about 40 to 60 atm is recovered.

The reaction gas from the methanol synthesis reactor 19 undergoes some heat recovery and cooling of the synthesis gas heater 18 and the like between the flow paths 26 and 27, and the methanol separator 28 separates crude methanol. Then, it is sent from the flow path 29 to the distillation step. The unreacted gas from the methanol separator 28 is used as a circulating gas in the flow path 30.
And is introduced into the synthetic circulating gas compressor 32 via the flow path 31. It should be noted that a part of the unreacted gas is extracted as a purge gas from the flow path 33 and is mainly mixed with the flow path 8 as a fuel for the reforming furnace. In the synthetic circulating gas compressor 32, the pressure is increased by about 4 to 6 atm and the synthetic gas is merged through the flow path 16.

The high-pressure vapor recovered from the methanol synthesis reactor is split from the flow path 34 at point A, and a part of it is flow path 35.
After that, it is used for the raw material steam (the dotted line shows the flow path of the recovered high-pressure steam). In addition, other recovered high-pressure steam is in the flow path.
It is sent to the high-pressure steam heater I10 and the high-pressure steam heater II13 via 36 and the flow path 37 to become superheated steam, and the flow path 38 and the flow path
The synthetic gas compressor turbine 41 is driven from the flow path 40 via the point B where 39 is gathered, and the synthetic circulating gas compressor turbine 43 is driven from the flow path 42. The exhaust gas from each turbine is sent to the cooling / condensing system via the flow paths 44 and 45.

FIG. 2 (b) is a system diagram showing an example of the case where the primary reformed gas is partially oxidized for further secondary reforming, and the flow until it exits the primary reforming reaction tube 6 is as shown in FIG. It is the same.
However, in the case of (b), since partial oxidation and secondary reforming reaction are performed after the primary reforming reaction, gas reforming is performed at high pressure, and the reaction gas from the primary reforming reaction tube 6 becomes pressure
The temperature is 30 to 45 atm and the temperature is 750 to 800 ℃. Therefore, the reforming rate of the reaction gas from the primary reforming reaction tube 6 becomes 30 to 50% and is introduced into the secondary reforming furnace 47 through the flow path 46.

The oxygen gas used for the partial oxidation is produced in the oxygen separator 48. This oxygen gas is introduced into the secondary reforming reactor 47 from the flow path 49, and after partial oxidation is performed,
The secondary reforming reaction is performed by the reforming catalyst. The flow after the secondary reforming is the same as the flow after the flow path 11 in FIG. However
In the case of (b), the reforming pressure becomes high, so the syngas compressor
The required power of 14 is reduced and the gas reformer is downsized, which is advantageous for large-scale equipment. The high-pressure steam recovered from the methanol synthesis reactor is also used as a power source for the air compressor and the refrigerator in the air separation device 48 from the flow path 50.

FIG. 3 (c) is a system diagram showing an example of the case where a high-temperature secondary reformed gas is used as a heat source for the primary reforming reaction and the reforming pressure is further increased. In this case, since the reforming pressure is increased to 60 to 120 atm, the raw material hydrocarbons are first introduced into the raw material hydrocarbon compressor 51 from the flow passage 1 and boosted in pressure, and then the flow passage 52 is passed through the flow passage 52. The raw material from is mixed with steam. The mixed gas is heated to 400 to 550 ° C. by the mixed gas heater 4 via the flow path 3 and introduced into the primary reforming reactor 53 via the flow path 5. The primary reforming reactor has a large number of reaction tubes and is filled with a Ni-based catalyst equivalent to that shown in FIGS. This reaction tube is heated from the outside by a high temperature secondary reformed gas, and the temperature is 700 to 800 ℃.
And about 25-35% of the hydrocarbons are reformed.

The obtained primary reformed gas is introduced into the secondary reforming reactor 47 through the flow path 54. Oxygen gas used for partial oxidation is produced in the oxygen separation device 48, introduced into the secondary reforming reactor 47 from the flow path 49, and after partial oxidation is performed, the secondary reforming reaction is performed by the reforming catalyst. Be seen. The temperature of the reaction gas from the secondary reforming catalyst layer is 980 to 1080 ° C, and about 90% or more of hydrocarbons are reformed. The obtained high temperature secondary reformed gas is introduced into the primary reforming reactor 53 from the flow path 55 to heat the internal reaction tube. As described above, if a part of the raw material hydrocarbon is mixed into the oxygen gas used for the partial oxidation, the load on the primary reforming reactor can be reduced. In addition, the primary reforming reactor 53 and the secondary reforming reactor
47 can be integrated, and various structures have been proposed. After the secondary reformed gas heats the reaction tube in the primary reforming reactor, heat recovery and cooling are performed between the channel 56 and the channel 57 in the same manner as in FIG. 1, and the condensed water is separated. Introduced into the synthesis circulation gas compressor 32 without using the synthesis gas compressor. The flow of the methanol synthesizer after the flow path 17 is the same as that in FIG.

In FIG. 3, the purge gas of the methanol synthesizer is extracted from the flow path 58 and is introduced into the gas turbine engine 60 via the flow path 59 to recover the power. The gas turbine engine 60 is supplied with other fuel together with the purge gas from the flow path 61, and further from the flow path 62 is also supplied with the high-pressure steam recovered by the methanol synthesizer. By thus introducing high-pressure steam together with fuel into the gas turbine engine 60, power is recovered from the steam and
The effect of reducing NOx is obtained. This gas turbine is directly connected to the air compressor 62, and the air from the flow passage 63 is compressed and introduced into the oxygen separation device 48 via the flow passage 64.
In addition to the heating of high-pressure steam shown in FIGS. 1 and 2,
High-pressure steam heater installed in the exhaust duct 65 of the gas turbine
This is also performed in III 66, and high-pressure steam from the methanol reactor is supplied from the flow path 67. In addition, the superheated high-pressure steam is
It is also sent to the raw material hydrocarbon compressor turbine 69 from 68, and power recovery is performed.

[0025]

EXAMPLES Next, the present invention will be described more specifically by way of examples. As described above, the schematic flow of the present invention is shown in FIGS.
However, in terms of process thermal efficiency and upsizing, Fig. 3
Since the above flow is considered to be the most advantageous, an example of the process calculation result in the flow of FIG. 3 is shown in the embodiment.

As shown in FIG.
It was supplied at an atmospheric pressure of 26 ° C. and the raw material hydrocarbon compressor 51 boosted the pressure to 87 atmospheric pressure. Although not shown in the flow, a part of the purge gas of the methanol synthesizer was mixed with the raw material hydrocarbon for desulfurization. This raw material hydrocarbon is split into two, and the split stream is combined with the raw material steam from the flow path 2 in the primary reforming reactor 53.
Then, the split stream was introduced into the secondary reforming reactor 47 together with the oxygen gas from the flow path 49. Raw water vapor from channel 2 is 85 atm 400
The temperature was 0 ° C., and the mixed gas of the split-flow raw material hydrocarbon was heated to 500 ° C. by the mixed gas heater 4 and introduced into the primary reforming reactor 53. Oxygen gas was introduced into the secondary reforming reactor 47 together with the raw material hydrocarbons which were split at 86 at 250 ° C. The flow rate and composition of each flow are as follows. In addition, CH in the table below
₃ OH is a numerical value including by-products such as dimethyl ether.

[0027]

[Chemical formula 1] Raw hydrocarbon split stream (flow path 1) Split composition CH ₄ 3380.6 kg-mol / h 2253.5 kg-mol / h 78.67 mol% C ₂ H ₆ 277.4 184.9 6.45 C ₃ H ₈ 107.4 71.9 2.51 C ₄ H ₁₀ 49.3 32.9 1.15 C ₅ H ₁₂ 16.8 11.2 0.39 C ₆ H ₁₄ 5.9 3.9 0.14 CO 26.9 18.0 0.63 CO ₂ 66.6 44.5 1.55 H ₂ 343.6 229.0 8.00 N ₂ 18.4 12.2 0.43 H ₂ O 0.1 0.1 0.00 CH ₃ OH 3.6 2.4 0.08 Total 4297.0 2864.5 100.00 Raw water vapor (flow path 2) 13726.1 kg-mol / h Oxygen gas (flow path 49) O ₂ 3068.4 kg-mol / h 99.50 mol% N ₂ 15.4 0.50 Total 3083.8 100.00

The temperature of the secondary reforming outlet (flow passage 55) is about 1030 ° C.
After the heat exchange in the primary reforming reactor (flow path 56), the temperature was about 570 ° C. The flow rate and composition are as follows.

After the heat of the synthesis gas is recovered and cooled, the condensed water is separated, and then the purge gas of the methanol synthesis apparatus is changed to PS.
A hydrogen gas obtained by separation 458.1 kg-mol / h and flow path 31
The synthetic recycle gas from was mixed and introduced into the synthetic recycle gas compressor 32 at 75.5 atm. The gas pressurized by the compressor was introduced into the methanol synthesis reactor 19 at 198 ° C. and 80 atm via the synthesis gas heater 18. In the methanol synthesis reactor, a methanol synthesis reaction with a fluidized catalyst was performed, and 185.2 T / H of saturated steam (260 ° C) at 47 atm was generated. The reaction gas at the outlet of the methanol synthesis reactor has a pressure of 78 atm and a temperature of 264 ° C. The amount of gas at the inlet and the outlet of the methanol synthesis reactor and the composition thereof are as follows.

[0030]

Chemical formula 3 Inlet gas (flow path 17) Outlet gas (flow path 26) kg-mol / h mol% kg-mol / h mol% CH ₄ 29325.1 25.93 29325.1 29.37 CO ₂ 8760.3 7.74 7115.5 7.12 CO 8806.3 7.79 3831.0 3.84 H ₂ 63774.6 56.39 48889.1 48.96 N ₂ 1888.0 1.67 1888.0 1.89 H ₂ O 41.7 0.04 1699.9 1.70 CH ₃ OH 497.0 0.44 7103.9 7.12 Total 113093.0 100.00 99852.5 100.00

The reaction gas at the outlet of the methanol synthesis reactor was subjected to heat recovery and cooling, and crude methanol condensed at 40 ° C. in the methanol separator 28 was separated. The amounts and compositions of the separated gas and crude methanol are as follows.

Separation gas (flow path 30) Crude methanol (flow path 29) kg-mol / h mol% kg-mol / h mol% CH ₄ 29243.4 32.03 81.7 0.96 CO ₂ 6980.2 7.64 135.2 1.58 CO 3825.9 4.19 5.1 0.06 H ₂ 48848.5 53.49 40.7 0.48 N ₂ 1886.5 2.07 1.8 0.02 H ₂ O 20.3 0.02 1679.4 19.67 CH ₃ OH 509.0 0.56 6585.3 77.23 Total 91313.8 100.00 8539.2 100.00

A part (2140.8 kg-mol / h) of this separated gas was withdrawn from the channel 58 as a purge gas and used for desulfurization of the raw material hydrocarbons, the PSA unit and the power recovery gas turbine. Of the 185.2 T / H high-pressure steam recovered from the methanol synthesis reactor, 19.2 T / H was introduced into the combustion chamber of a gas turbine engine with an output of 21000 KW / H using the above-mentioned purge gas and other fuels, and NOx Lowered and recovered power. Remain
High-pressure steam of 166 T / H was heated to 350 ° C in the high-pressure steam heater I10, high-pressure steam heater II13 and high-pressure steam heater III66.
The hydrocarbon feedstock compressor turbine 69 is heated to 43.
5 T / H (output 8370 KW / H), synthetic circulating gas compressor turbine
It used 43.6 T / H (output 8390 KW / H) at 43 and 78.9 T / H at the oxygen separator 48. The back pressure of each turbine was 0.135 atm absolute.

[0033]

EFFECT OF THE INVENTION In the fluidized bed catalytic reactor, not only the contact of gas with the heat transfer tube in the reactor but also the contact of catalyst particles themselves contributes to high heat transfer efficiency and good heat diffusion in the catalyst layer. Since the reaction temperature is uniform and there is no local temperature rise, the reaction rate can be increased and the active ingredient
Since the concentration of (CO, CO ₂ ) can be increased, the amount of circulating gas can be reduced, the pressure of high-pressure steam recovered from uniform temperature distribution and high heat transfer efficiency can be increased, and the pressure loss in the reactor is fixed. Compared with the multi-tube reactor with a catalyst layer, the reaction temperature is uniform, and there is no local temperature rise part, so the amount of side reaction products is reduced and the thermal efficiency in the distillation purification process can be improved. There are advantages such as what can be done.

Therefore, by using the fluidized bed catalytic reactor according to the method of the present invention, higher pressure steam can be obtained and the efficiency of the steam turbine in the compressor or the like can be increased, and the power of the synthetic circulating gas compressor can be increased. There are reductions and improvements in thermal efficiency in the purification distillation step, etc., and energy efficiency in the methanol production device can be further increased. In addition, it is also advantageous for increasing the size of the methanol production device. The method of the present invention is particularly carried out by partially oxidizing the primary reformed gas for further secondary reforming, and combining this high-temperature secondary reformed gas with a gas reformer used as a heat source for the primary reforming reaction. Therefore, a large-sized methanol production apparatus can be obtained with higher energy efficiency.

[Brief description of drawings]

FIG. 1 is a system diagram showing an example of a case where a gas reforming apparatus according to the present invention is a primary reformer only.

FIG. 2 is a system diagram showing an example of a case where the primary reformed gas is partially oxidized and further secondary reforming is performed in the present invention.

FIG. 3 is a system diagram showing a case where the primary reformed gas is partially oxidized and further secondary reformed in the present invention, and the obtained high temperature secondary reformed gas is used as a heat source for the primary reforming reaction. An example is shown.

[Explanation of symbols]

 1 Raw material hydrocarbon flow path 2 Raw material steam flow path 6 Primary reforming reaction tube 14 Syngas compressor 19 Methanol synthesis reactor (fluidized bed catalytic reactor) 23 Steam separator 28 Methanol separator 32 Synthetic circulation gas compressor 47 Secondary reforming reactor 48 Oxygen separator 51 Raw hydrocarbon compressor 53 Primary reforming reactor 60 Gas turbine engine

Claims (7)

[Claims] 1. A method for producing methanol from a hydrocarbon, comprising: (1) performing a catalytic reaction by indirectly heating a mixed gas of hydrocarbon and steam to produce a synthetic gas containing hydrogen, carbon monoxide and carbon dioxide as active ingredients. The manufacturing process and (2) using a fluidized bed catalytic reactor with a heat transfer tube inside, 60 ~ 12
It has a step of performing a methanol synthesis reaction at 0 atm and transferring reaction heat to saturated water through the heat transfer tube to generate high pressure steam at 40 to 60 atm, and the high pressure steam obtained in step (2). A method for producing methanol, characterized in that power is recovered from the fuel. 2. The process for producing methanol according to claim 1, wherein in the step (1), a synthesis gas having a pressure of 10 to 25 atmospheres and a temperature of 850 to 900 ° C. is obtained by a catalytic reaction by indirect heating. 3. In step (1), after a primary reformed gas of 30 to 45 atm 750 to 800 ° C. is obtained by a catalytic reaction by indirect heating, oxygen gas is added to carry out a partial oxidation reaction, and further by an adiabatic catalytic reaction. The method for producing methanol according to claim 1, wherein a secondary reformed gas of 930 to 1000 ° C. is obtained. 4. In the step (1), after a primary reformed gas of 60 to 120 atm 700 to 800 ° C. is obtained by a catalytic reaction by indirect heating, oxygen gas is added to carry out a partial oxidation reaction, and further by an adiabatic catalytic reaction. The method for producing methanol according to claim 1, wherein a secondary reformed gas of 980 to 1080 ° C. is obtained, and the secondary reformed gas is used as a heat source for a catalytic reaction by indirect heating. 5. The method for producing methanol according to claim 1, wherein the power recovered from the high-pressure steam is used in a syngas compressor, a syngas circulator or a raw hydrocarbon gas compressor. 6. The method for producing methanol according to claim 1, wherein high-pressure steam is introduced into a gas turbine engine to recover power. 7. The method for producing methanol according to claim 2, wherein the power recovered from the high-pressure steam is used for oxygen production.