JP2017155035A - Olefin production system and olefin production method - Google Patents

Abstract

PROBLEM TO BE SOLVED: To efficiently produce an olefin.SOLUTION: There is provided an olefin production system 100 which comprises: a reformer 110 for reforming methane, carbon dioxide and water steam into carbon monoxide and hydrogen; an FTO reactor 150 for generating a mixed gas containing at least an olefin from the carbon monoxide and hydrogen obtained by the reformer 110; and a separator 200 for separating at least an olefin from the mixed gas obtained by the FTO reactor 150.SELECTED DRAWING: Figure 1

Description

  The present disclosure relates to an olefin production system for producing olefin, and an olefin production method.

  Olefin is a raw material for synthetic rubbers such as styrene / butadiene rubber and nitrile / butadiene rubber, and synthetic resins such as ABS resin (Acrylonitrile Butadiene Styrene copolymer), and therefore demand is high and production is large. Conventionally, olefins have been produced by cracking (catalytic cracking) of petroleum naphtha (for example, Patent Document 1). However, there is a problem that it is necessary to install an oil distillation plant or an LNG distillation plant, which increases the manufacturing cost.

  Therefore, it is conceivable to synthesize olefins using FTO (Fischer-Tropsch to olefins) reaction. For example, iron-based catalysts have been developed as FTO reaction catalysts (Non-patent Documents 1 and 2).

JP 2001-40369 A JP2015-164909A

Hirsa M. Torres Galvis et al. Science 335, 835 (2012).

  As described above, although a catalyst that can be used for the FTO reaction has been developed, a specific olefin production system using the FTO reaction has not been proposed yet.

  This indication aims at providing the olefin manufacturing system and olefin manufacturing method which can manufacture an olefin efficiently in view of such a subject.

  In order to solve the above problems, an olefin production system according to one embodiment of the present disclosure is obtained by a reformer that reforms methane, carbon dioxide, and steam into carbon monoxide and hydrogen, and the reformer. An FTO reactor that generates a mixed gas containing at least an olefin from the carbon monoxide and the hydrogen, and a separator that separates at least the olefin from the mixed gas obtained by the FTO reactor.

  The separator may separate carbon dioxide from the mixed gas, and the carbon dioxide separated by the separator may be introduced into the reformer.

  The separator may separate methane from the mixed gas, and the reformer may be introduced with methane separated by the separator.

  In addition, a steam turbine that converts the energy of water vapor into electric power is provided, the separation device separates one or both of methane and carbon monoxide from the mixed gas, and the steam turbine includes Water vapor obtained by burning one or both of the separated methane and carbon monoxide may be introduced.

  The separation device may separate carbon monoxide from the mixed gas, and the carbon monoxide separated by the separation device may be introduced into the FTO reactor.

  The reformer, the FTO reactor, and the separation device may be maintained within a predetermined pressure range.

  In order to solve the above problems, an olefin production method according to one embodiment of the present disclosure is obtained in a step of reforming methane, carbon dioxide, and water vapor into carbon monoxide and hydrogen, and the step of reforming. And a step of generating a mixed gas containing at least an olefin from the carbon monoxide and the hydrogen, and a step of separating at least the olefin from the mixed gas obtained in the step of generating the mixed gas.

  According to this indication, an olefin can be manufactured efficiently.

It is a figure explaining the olefin manufacturing system concerning a 1st embodiment. It is a figure explaining a separator. It is a figure which shows the temperature distribution of the part enclosed with the broken line of FIG. It is a figure explaining a power generator. It is a flowchart for demonstrating the flow of a process of an olefin manufacturing method. It is a figure explaining the result of the 1st simulation. It is a figure explaining the olefin production system of 2nd Embodiment. It is a figure explaining the relationship between the reaction rate and the selectivity of an olefin in a catalyst. It is a figure explaining the result of the 2nd simulation. It is a figure explaining the result of the 3rd simulation.

  Hereinafter, embodiments of the present disclosure will be described in detail with reference to the accompanying drawings. The dimensions, materials, and other specific numerical values shown in the embodiments are merely examples for facilitating understanding, and do not limit the present disclosure unless otherwise specified. In the present specification and drawings, elements having substantially the same function and configuration are denoted by the same reference numerals, and redundant description is omitted. Also, illustration of elements not directly related to the present disclosure is omitted.

(First Embodiment: Olefin Production System 100)
FIG. 1 is a diagram illustrating an olefin production system 100 according to the present embodiment. As shown in FIG. 1, the olefin production system 100 includes a reformer 110, a first water separator 130, an FTO reactor 150, a separation device 200, and a power generation device 300.

As shown in FIG. 1, methane (CH ₄ ), steam, and carbon dioxide (CO ₂ ) are introduced into the reformer 110, and these are subjected to a pressure of about 2 MPa (20 bar) and a temperature of about 1100 ° C. And reforming to carbon monoxide (CO) and hydrogen (H ₂ ). In the present embodiment, the amount of methane, water vapor, and carbon dioxide introduced is set so that the ratio of carbon monoxide obtained by the reformer 110 to hydrogen is 1: 1 to 1: 1.5. .

  Methane is heated to a predetermined temperature by the heater 102 and then introduced into the reformer 110. In this embodiment, natural gas or shale gas is introduced into the reformer 110 as methane. The steam is heated to a predetermined temperature by the heater 104 and then introduced into the reformer 110. Carbon dioxide is boosted by the compressor 106, heated to a predetermined temperature by the heater 108, and then introduced into the reformer 110. In addition, the reformer 110, the FTO reactor 150, and the separation apparatus 200 of this embodiment are maintained within a predetermined pressure range (for example, about 2 MPa). Therefore, it is not necessary to provide a booster other than the compressor 106, and the cost required for boosting the gas can be reduced.

  The reformed gas (carbon monoxide, hydrogen, and water vapor) generated by the reformer 110 is introduced into the first water separator 130 via the valve 122a and the heat exchangers 122 and 124. The heat exchangers 122 and 124 cool the reformed gas to a predetermined temperature. Note that water vapor obtained by cooling the reformed gas in the heat exchanger 122 is introduced into the power generation apparatus 300 described later.

  The first water separator 130 is constituted by a gas-liquid separator, and removes water (condensed water vapor) from the reformed gas. The reformed gas (carbon monoxide and hydrogen) from which water has been removed by the first water separator 130 is heated to a predetermined temperature by the heater 142 and then introduced into the FTO reactor 150.

In the FTO reactor 150, for example, the reaction of the following formulas (1) and (2) proceeds under a pressure of about 2 MPa (20 bar) and a temperature of 340 ° C., and carbon monoxide obtained by the reformer 110 is obtained. And a mixed gas containing at least olefin from hydrogen and hydrogen. In addition, since the catalyst used with the FTO reactor 150 can utilize the existing technique, detailed description is abbreviate | omitted here.
_{nCO + 2nH 2 → - (CH} 2) n- + nH 2 O ... formula (1)
CO + H ₂ O → CO ₂ + H ₂ Formula (2)
In addition, the enthalpy change of Formula (1) is (DELTA) H = -165kJ / mol, and the enthalpy change of Formula (2) is (DELTA) H = -39.8kJ / mol.

  In addition, when the hydrogen introduced into the FTO reactor 150 exceeds 1.5 times that of carbon monoxide, the production amount of paraffin relatively increases. However, in this embodiment, since the ratio of carbon monoxide introduced into the FTO reactor 150 and hydrogen is 1: 1 to 1: 1.5, C2 (carbon number 2) is used in the FTO reactor 150. ˜C4 (carbon number 4) olefin can be efficiently produced (for example, about 62.5%).

  The mixed gas thus generated in the FTO reactor 150 is cooled to a predetermined temperature by the heat exchanger 122 and then introduced into the separation device 200.

  FIG. 2 is a diagram illustrating the separation device 200. As shown in FIG. 2, the mixed gas generated in the FTO reactor 150 is first introduced into a second water separator 210 (gas-liquid separator) that constitutes the separation apparatus 200, and a part of water is separated. The The mixed gas from which a part of the water has been separated is cooled to a predetermined temperature by the heat exchanger 212, and after the water is separated by the third water separator 214 (gas-liquid separator), the desiccant (adsorption) Water is further removed by the fourth water separator 216 filled with the agent.

  Thus, the mixed gas from which water has been removed is introduced into the extractive distillation unit 218, and olefins and paraffins having 5 or more carbon atoms (C5) are separated. Then, the mixed gas from which the C5 or higher olefin and paraffin have been removed is introduced into the carbon dioxide separator 220 to separate the carbon dioxide. The carbon dioxide separator 220 is filled with, for example, Selexol (registered trademark) or an amine absorbing solution, and efficiently separates carbon dioxide from the mixed gas.

  The carbon dioxide separated by the carbon dioxide separator 220 is introduced into the reformer 110 and reused. As a result, it is possible to avoid a situation where carbon dioxide is exhausted unnecessarily, and the yield can be improved.

  The mixed gas from which carbon dioxide has been removed by the carbon dioxide separator 220 is cooled to a predetermined temperature by the heat exchanger 222 and then introduced into the demethanizer 230. The demethanizer 230 separates the mixed gas into a first mixed gas of carbon monoxide, hydrogen, and methane, a first liquid, and a second liquid. The first mixed gas is cooled to a predetermined temperature by the heat exchanger 232 and then expanded by the expander 234. Thereby, energy can be recovered and the temperature of the first mixed gas can be further cooled by expanding the energy. The first mixed gas expanded by the expander 234 is introduced into the power generation apparatus 300 after a part of the cold heat is recovered by the heat exchanger 236.

  The first liquid is introduced into the deethanizer 240 and separated into methane and a third liquid. The methane separated by the deethanizer 240 is cooled to a predetermined temperature by the heat exchanger 242 and then introduced into the reformer 110 and reused. As a result, it is possible to avoid a situation where methane is exhausted unnecessarily, and it is possible to improve the yield.

The third liquid is heated (refluxed) by the reboiler 244 and then introduced into the C2 distillation column 250. The C2 distillation column 250 separates the third liquid into ethylene (C ₂ H ₄ ) and ethane (C ₂ H ₆ ). The ethylene (olefin) is cooled to a predetermined temperature by the heat exchanger 252 and then sent to a subsequent process. Further, ethane is heated (refluxed) to a predetermined temperature (−8 ° C.) by the reboiler 254, and then sent to a subsequent process.

On the other hand, the second liquid separated by the demethanizer 230 is heated (refluxed) to a predetermined temperature (for example, 62 ° C.) by the reboiler 238 and then introduced into the depropanizer 260. The depropanizer 260 separates the second liquid into the second mixed gas and the fourth liquid. The second mixed gas is cooled to a predetermined temperature by the heat exchanger 262 and then introduced into the C3 distillation column 270. The C3 distillation column 270 separates the second mixed gas into propylene (C ₃ H ₆ ) and propane (C ₃ H ₈ ). The propylene (olefin) is cooled to a predetermined temperature by the heat exchanger 272, and then sent to a subsequent process. Propane is heated (refluxed) to a predetermined temperature by the reboiler 274 and then sent to a subsequent process.

The fourth liquid separated in the depropanizer 260 is heated (refluxed) to a predetermined temperature by the reboiler 264 and then introduced into the C4 distillation column 280. The C4 distillation column 280 separates the fourth liquid into butene (C ₄ H ₈ ) and butane (C ₄ H ₁₀ ). The butene (olefin) is cooled to a predetermined temperature by the heat exchanger 282 and then sent to a subsequent process. The butane is heated (refluxed) to a predetermined temperature by the reboiler 284, and then sent to a subsequent process.

  FIG. 3 is a diagram showing a temperature distribution in a portion surrounded by a broken line in FIG. As shown in FIG. 3, in this embodiment, the heat exchanger 222 includes a first heat exchanger 222a, a second heat exchanger 222b, a third heat exchanger 222c, and a fourth heat exchanger 222d. Consists of. As described above, a mixed gas (for example, 30 ° C.) is introduced into the first heat exchanger 222a, and the first heat exchanger 222a cools the mixed gas to 20 ° C. And the 2nd heat exchanger 222b cools 20 degreeC mixed gas to 17 degreeC. The third heat exchanger 222c cools the 17 ° C. mixed gas to −30 ° C. Further, the fourth heat exchanger 222d cools the −30 ° C. mixed gas to −62 ° C. Thus, the mixed gas cooled to −62 ° C. is introduced into the demethanizer tower 230.

  As described above, the demethanizer 230 separates the mixed gas into the first mixed gas, the first liquid, and the second liquid. Then, the first mixed gas is cooled by the heat exchanger 232. If it demonstrates concretely, in this embodiment, the heat exchanger 232 is comprised including the 4th heat exchanger 232a, the 5th heat exchanger 232b, and the 6th heat exchanger 232c. The fourth heat exchanger 232a cools the first mixed gas at −62 ° C. to −119 ° C. The fifth heat exchanger 232b raises the temperature of the first mixed gas at −119 ° C. to −111 ° C. The sixth heat exchanger 232c raises the temperature of the first mixed gas at −111 ° C. to −29 ° C.

  The first mixed gas at −29 ° C. is expanded by the expander 234, cooled to −133 ° C., and further cooled by the heat exchanger 236. In the present embodiment, the heat exchanger 236 includes a seventh heat exchanger 236a, an eighth heat exchanger 236b, a ninth heat exchanger 236c, and a tenth heat exchanger 236d. The seventh heat exchanger 236a raises the temperature of the first mixed gas cooled to −133 ° C. by the expander 234 to −120 ° C. The eighth heat exchanger 236b raises the temperature of the first mixed gas at −120 ° C. to −38 ° C. The ninth heat exchanger 236c raises the temperature of the first mixed gas at −38 ° C. to 16 ° C. The tenth heat exchanger 236d raises the temperature of the first mixed gas at 16 ° C. to 27 ° C. Thus, the first mixed gas heated to 27 ° C. is introduced into the power generation apparatus 300.

  On the other hand, the first liquid separated in the demethanizer 230 is introduced into the deethanizer 240, cooled to −68 ° C., and separated into methane and a third liquid. Methane (−68 ° C.) separated by the deethanizer 240 is cooled by the heat exchanger 242. More specifically, the heat exchanger 242 includes an eleventh heat exchanger 242a and a twelfth heat exchanger 242b. The eleventh heat exchanger 242a cools −68 ° C. methane to −96 ° C. The twelfth heat exchanger 242b raises the temperature of −96 ° C. methane to −30 ° C. Thus, methane heated to −30 ° C. is introduced into the reformer 110.

  The third liquid (−68 ° C.) separated by the deethanizer 240 is heated to −22 ° C. by the reboiler 244 and then introduced into the C2 distillation column 250. Then, the C2 distillation column 250 separates the third liquid into ethylene and ethane, and the ethylene is cooled to −29 ° C. by the heat exchanger 252.

  Here, heat exchange is performed between the first heat exchanger 222a and the tenth heat exchanger 236d, and the heat of the mixed gas introduced into the first heat exchanger 222a is converted into the tenth heat exchanger 236d. (The heat exchange amount is 16 kW), the mixed gas introduced into the first heat exchanger 222a is cooled and introduced into the tenth heat exchanger 236d. It becomes possible to raise the temperature of the first mixed gas.

  In addition, heat exchange is performed between the second heat exchanger 222b and the ninth heat exchanger 236c, and the heat of the mixed gas introduced into the second heat exchanger 222b is transferred to the ninth heat exchanger 236c. The first mixed gas to be introduced can be moved (the amount of heat exchange is 35 kW), the mixed gas introduced into the second heat exchanger 222b is cooled, and the first mixed gas introduced into the ninth heat exchanger 236c is cooled. It becomes possible to raise the temperature of one mixed gas.

  Furthermore, heat exchange is performed between the fourth heat exchanger 222d and the sixth heat exchanger 232c, and the heat of the mixed gas introduced into the fourth heat exchanger 222d is transferred to the sixth heat exchanger 232c. The first mixed gas to be introduced can be moved (a heat exchange amount is 691 kW), and the mixed gas introduced into the fourth heat exchanger 222d is cooled and the first heat exchanger 232c introduced into the sixth heat exchanger 232c is cooled. It becomes possible to raise the temperature of one mixed gas.

  Further, heat exchange is performed between the fourth heat exchanger 232a and the seventh heat exchanger 236a, and the heat of the first mixed gas introduced into the fourth heat exchanger 232a is converted into the seventh heat exchanger. 236a can be moved to the first mixed gas (heat exchange amount is 101 kW), the first mixed gas introduced into the fourth heat exchanger 232a is cooled, and the seventh heat exchanger 236a is It is possible to raise the temperature of the introduced first mixed gas.

  Further, heat exchange is performed between the eleventh heat exchanger 242a and the fifth heat exchanger 232b, and the heat of methane introduced into the eleventh heat exchanger 242a is introduced into the fifth heat exchanger 232b. The first mixed gas introduced into the fifth heat exchanger 232b can be cooled while the methane introduced into the eleventh heat exchanger 242a is cooled. It is possible to raise the temperature of the gas.

  Further, heat exchange is performed between the heat exchanger 252 and the eighth heat exchanger 236b, and the first mixing in which the heat of ethylene introduced into the heat exchanger 252 is introduced into the eighth heat exchanger 236b. It can be moved to gas (the amount of heat exchange is 640 kW), and the ethylene introduced into the heat exchanger 252 can be cooled and the temperature of the first mixed gas introduced into the eighth heat exchanger 236b can be raised. It becomes possible.

  Further, heat exchange is performed between the heat exchanger 252 and the twelfth heat exchanger 242b, and the heat of ethylene introduced into the heat exchanger 252 is transferred to methane introduced into the twelfth heat exchanger 242b. (The amount of heat exchange is 14 kW), and the ethylene introduced into the heat exchanger 252 can be cooled and the temperature of the methane introduced into the twelfth heat exchanger 242b can be raised.

  Therefore, the first refrigerator (−40 ° C.) recovers 635 kW of thermal energy from the third heat exchanger 222c, and the second refrigerator (−120 ° C.) generates heat of the fourth heat exchanger 232a to 1403 kW. It will be enough if energy is recovered. By configuring the heat exchangers 222, 232, 236, 242, and 252 as described above, heat energy can be used efficiently, and energy (cost) for heating and cooling the gas can be reduced. It becomes possible to reduce.

  FIG. 4 is a diagram illustrating the power generation device 300. As illustrated in FIG. 4, the power generation device 300 includes a boiler 310. In the boiler 310, pure water, air, and fuel gas are introduced, and the fuel is burned with air to boil the pure water to generate water vapor. The pure water is heated to a predetermined temperature by the heater 302 and then introduced into the boiler 310. In addition, the air is pressurized by the compressor 304, heated to a predetermined temperature by the heater 306, and then introduced into the boiler 310.

  The fuel gas is heated to a predetermined temperature by the heater 308 and then introduced into the boiler 310. In the present embodiment, the first mixed gas separated in the demethanizer 230 is introduced into the boiler 310 as a fuel gas. Thereby, it is possible to generate electric power with the first mixed gas, and it is possible to recover energy.

  The steam turbine 314 converts the energy of the steam generated by the boiler 310 and the steam (high-pressure steam) generated by the heat exchanger 122 into electric power. Energy can be recovered by the configuration in which the steam generated in the heat exchanger 122 is introduced into the steam turbine 314.

  Thus, the electric power generated by the steam turbine 314 is used for driving the compressors 106 and 304 and cooling the separation device 200. For example, the power consumption of the compressor 106 is about 3700 kW, the power consumption of the compressor 304 is about 900 kW, the power consumption of the separation device 200 is about 2300 kW, and the power generation of the steam turbine 314 is about 10300 kW. It is. Therefore, power consumption of the entire olefin production system 100 can be reduced.

  In the boiler 310, excess steam is cooled by the heat exchanger 312 and then discharged to the outside, and the steam that has passed through the steam turbine 314 is cooled by the heat exchanger 316 and then discharged to the outside. The Rukoto.

(Olefin production method)
Then, the olefin manufacturing method using the said olefin manufacturing system 100 is demonstrated. FIG. 5 is a flowchart for explaining the process flow of the olefin production method. As shown in FIG. 5, the olefin production method includes a step of reforming methane, carbon dioxide, and steam into carbon monoxide and hydrogen in the reformer 110 (step S110), and in the FTO reactor 150. A step of generating a mixed gas containing at least an olefin from carbon monoxide and hydrogen (step S120), and a step of separating at least the olefin from the obtained mixed gas in the separation device 200 (step S130) are included.

  As described above, according to the olefin production system 100 of the present embodiment and the olefin production method using the olefin production system 100, olefins can be produced efficiently.

(First simulation)
In the olefin production system 100, the production amount when the carbon dioxide separated by the carbon dioxide separator 220 is not reused by the reformer 110 (Example 1), and the production amount when the carbon dioxide is reused (Example 2) Was estimated by simulation.

  FIG. 6 is a diagram for explaining the result of the first simulation. In FIG. 6, Example 1 is shown in black and Example 2 is shown in white. As shown in FIG. 6, in Example 1, it turned out that an olefin (C2-C4) can be produced more than paraffin (C2-C4). Moreover, also in Example 2, it was confirmed that olefin (C2-C4) can be produced more than paraffin (C2-C4), and also compared with Example 1, the production amount of olefin (C2-C4) is 65. It was found that it improved by about%.

(Second Embodiment: Olefin Production System 400)
In the first embodiment, the configuration in which the first mixed gas separated by the demethanizer 230 is introduced into the power generation apparatus 300 has been described. The olefin production rate can be further improved by reusing the first mixed gas. In this embodiment, an olefin production system 400 in which the first mixed gas is reused to improve the olefin production rate will be described.

  FIG. 7 is a diagram illustrating an olefin production system 400 according to the second embodiment. As shown in FIG. 7, the olefin production system 400 includes a reformer 110, a first water separator 130, an FTO reactor 150, a separation device 200, and a power generation device 300. In addition, about the component substantially equivalent to the said olefin manufacturing system 100, the same code | symbol is attached | subjected and description is abbreviate | omitted.

  The catalyst used in the FTO reactor 150 of the olefin production system 400 is a catalyst having a relatively low olefin selectivity, although the reaction rate is relatively low. FIG. 8 is a diagram for explaining the relationship between the reaction rate and the olefin selectivity in the catalyst. As shown in FIG. 8, the reaction rate of the catalyst and the selectivity of the olefin that can be used in the FTO reactor 150 vary depending on the type, but the reaction rate is in the range of 5% to 90%, and the selectivity of the olefin. Is in the range of 25% to 90%. In this embodiment, the FTO reactor 150 uses a catalyst (shown by hatching in FIG. 8) that has a relatively low reaction rate but a relatively high olefin selectivity. Thereby, although the production rate is low, high-purity olefin can be produced (impurities are reduced).

  In the olefin production system 400, at least a part of the first mixed gas (carbon monoxide, hydrogen, methane) separated by the demethanizer tower 230 (see FIG. 2) constituting the separation device 200 is passed through the heater 142. And introduced into the FTO reactor 150. Thereby, carbon monoxide contained in the first mixed gas can be reused. Therefore, although the reaction rate of the catalyst is relatively low, it is possible to efficiently produce a high-purity olefin. That is, the production rate of olefin can be improved.

(Second simulation)
The catalyst used in the FTO reactor 150 is a catalyst having a reaction rate and an olefin selectivity shown by black circles in FIG. 8 and a carbon monoxide recovery ratio of 0.5. The selectivity was simulated. The carbon monoxide recovery ratio is defined as “the amount of carbon monoxide returned from the demethanizer 230 to the FTO reactor 150 / the amount of carbon monoxide separated by the demethanizer 230”.

FIG. 9 is a diagram for explaining the result of the second simulation. When the carbon monoxide recovery ratio was 0.5, the selectivity for carbon dioxide (CO ₂ ) (C mol% (mole percentage of carbon)) was 25 C mol%. The selectivity of methane (C1) was 9 Cmol%. The selectivity for ethylene was 10.22 Cmol%. Ethane selectivity was 3.78 Cmol%. The selectivity for propylene was 15.12 Cmol%. Propane selectivity was 1.82 Cmol%. The selectivity of butylene was 10.22 Cmol%. Butane selectivity was 4.48 Cmol%. The selectivity of the compound having 5 or more carbon atoms (C5 +) was 20.36 Cmol%.

  From the above results, it was confirmed that the selectivity for olefins (ethylene, propylene, butylene) was relatively high when the carbon monoxide recovery ratio was 0.5.

(Third simulation)
The higher the carbon monoxide recovery ratio (closer to 1), the better the olefin production rate. In contrast, as the carbon monoxide recovery ratio increases, the amount of gas to be processed in the FTO reactor 150 and the separation device 200 (demethanizer 230) increases. For this reason, the larger the carbon monoxide recovery ratio, the larger the device and the higher the cost of the device.

  Therefore, the catalyst used in the FTO reactor 150 is a catalyst with a reaction rate and an olefin selectivity shown by black circles in FIG. 8, and a carbon monoxide recovery ratio and an internal rate of return (IRR). And the relationship was simulated.

  FIG. 10 is a diagram for explaining the result of the third simulation. As shown in FIG. 10, the IRR increases as the recovery ratio increases until the carbon monoxide recovery ratio reaches 0.9. However, if the carbon monoxide recovery ratio exceeds 0.9, the IRR decreases as the recovery ratio increases. Therefore, the IRR can be set to 0.2 or more by setting the carbon monoxide recovery ratio to 0.75 or more and 0.95 or less. Further, by setting the carbon monoxide recovery ratio to 0.9, the IRR can be improved to 0.36.

  From the above results, it is confirmed that the olefin production rate can be improved while suppressing the cost of the olefin production system 400 itself and the running cost by setting the carbon monoxide recovery ratio to 0.75 or more and 0.95 or less. It was done.

  As mentioned above, although embodiment of this indication was described referring an accompanying drawing, it cannot be overemphasized that this indication is not limited to the above-mentioned embodiment. It will be apparent to those skilled in the art that various changes and modifications can be made in the scope described in the claims, and these are naturally within the technical scope of the present disclosure. Is done.

  For example, in the above embodiment, the configuration in which carbon dioxide separated by the carbon dioxide separator 220 is introduced into the reformer 110 has been described as an example. However, the carbon dioxide separated by the carbon dioxide separator 220 may not be introduced into the reformer 110 and may be used in other processes.

  In the above-described embodiment, the configuration in which the methane separated in the deethanizer 240 is introduced into the reformer 110 has been described as an example. However, the methane separated in the deethanizer 240 may not be introduced into the reformer 110, and may be used in other processes, for example, the boiler 310 of the power generation apparatus 300.

  Moreover, in the said embodiment, the structure which utilizes the 1st mixed gas as fuel gas with the electric power generating apparatus 300 was mentioned as an example, and was demonstrated. However, the first mixed gas may be introduced into the reformer 110 and reused. Further, the pressure swing adsorption (PSA) method may be used to separate hydrogen from the first mixed gas, introduce hydrogen into the reformer 110, and use methane and carbon monoxide in the power generator 300. . Further, hydrogen may be used in the power generation apparatus 300 and methane and carbon monoxide may be introduced into the reformer 110. Further, although the olefin production system 100 has been described by taking the configuration including the power generation device 300 as an example, the power generation device 300 is not an essential configuration.

  Moreover, in the said embodiment, the reformer 110, the FTO reactor 150, and the separation apparatus 200 were mentioned as an example, and demonstrated the structure maintained within the predetermined pressure range. However, the reformer 110, the FTO reactor 150, and the separation device 200 may have different pressures.

  In addition, each process of the olefin manufacturing method of this specification does not necessarily need to process in time series along the order described as a flowchart, and may include a parallel process.

  The present disclosure can be used for an olefin production system and an olefin production method for producing olefin.

100 Olefin Production System 110 Reformer 130 First Water Separator 150 FTO Reactor 200 Separator 314 Steam Turbine 400 Olefin Production System

Claims (7)

A reformer that reforms methane, carbon dioxide, and steam into carbon monoxide and hydrogen;
An FTO reactor for producing a mixed gas containing at least an olefin from the carbon monoxide and the hydrogen obtained by the reformer;
A separation device for separating at least olefin from the mixed gas obtained by the FTO reactor;
An olefin production system comprising: The separation device separates carbon dioxide from the mixed gas;
The olefin production system according to claim 1, wherein carbon dioxide separated by the separation device is introduced into the reformer. The separation device separates methane from the mixed gas,
The olefin production system according to claim 1 or 2, wherein methane separated by the separation device is introduced into the reformer. A steam turbine that converts the energy of water vapor into electricity;
The separation device separates one or both of methane and carbon monoxide from the mixed gas,
4. The steam according to claim 1, wherein water vapor obtained by burning one or both of methane and carbon monoxide separated by the separation device is introduced into the steam turbine. 5. Olefin production system. The separation device separates carbon monoxide from the mixed gas;
The olefin production system according to any one of claims 1 to 4, wherein carbon monoxide separated by the separation device is introduced into the FTO reactor.   The olefin production system according to any one of claims 1 to 4, wherein the reformer, the FTO reactor, and the separation device are maintained within a predetermined pressure range. Reforming methane, carbon dioxide and water vapor to carbon monoxide and hydrogen;
Generating a mixed gas containing at least an olefin from the carbon monoxide and the hydrogen obtained in the reforming step;
Separating at least olefin from the mixed gas obtained in the step of generating the mixed gas;
An olefin production method comprising:

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