WO2021220930A1

WO2021220930A1 - Vaporization-utilizing hydrocarbon production system with power generation facility

Info

Publication number: WO2021220930A1
Application number: PCT/JP2021/016273
Authority: WO
Inventors: 信三伊藤
Original assignee: 株式会社ユーリカエンジニアリング
Priority date: 2020-04-30
Filing date: 2021-04-22
Publication date: 2021-11-04
Also published as: JPWO2021220455A1; JP6964920B1; WO2021220455A1; JPWO2021220930A1

Abstract

A vaporization-utilizing hydrocarbon production system with a power generation facility is configured such that at least one of hydrogen and carbon dioxide is fed in a liquid form and is vaporized with a vaporizer. A mixed gas composed of a hydrogen gas and a carbon dioxide gas flows through a reaction tube in a hydrogeneration reactor under a specified pressure at a specified temperature and a specified mass flow rate, and undergoes a hydrogeneration reaction in the presence of a hydrogeneration reaction catalyst and is thereby chemically converted to a synthetic hydrocarbon gas. High-temperature water that has cooled the reaction tube and has been heated with reaction heat generated as the result of the hydrogeneration reaction and the synthetic hydrocarbon gas that has been generated in the reaction tube are fed to a boiler, and the high-temperature water is vaporized with combustion heat of the synthetic hydrocarbon gas to generate high-pressure steam. The high-pressure steam drives a condensing turbine power generator to generate electric power. The vaporization-utilizing hydrocarbon production system with a power generation facility can be driven with low-carbon-derived electric power generated with the high-pressure steam in the condensing turbine power generator, and can generate the synthetic hydrocarbon gas with a low energy and at low cost.

Description

Hydrocarbon production system using vaporization with power generation equipment

The present invention relates to a system in which a condensate turbine power generation facility is added to a hydrocarbon production system for producing synthetic hydrocarbon gas by hydrogenating hydrogen gas and carbon dioxide gas.

The problem of global warming is becoming more serious, and there are moves to limit thermal power generation that uses fossil fuels that emit large amounts of carbon dioxide. However, equipment that uses fossil fuels such as thermal power generation has low operating costs, and if the amount of carbon dioxide emitted to the atmosphere can be reduced to the extent that it does not adversely affect the environment, it can become a powerful power supply equipment. .. Therefore, it is desired to develop a hydrocarbon production device that recovers carbon dioxide emitted by combustion of fossil fuel _{and reacts it with CO 2-} free hydrogen to produce synthetic hydrocarbon gas such as synthetic methane gas at low cost and with low energy. ing.
Patent Document 1 describes a methane synthesizer that synthesizes methane by supplying hydrogen gas and carbon dioxide gas, which are raw material gases, to a reactor filled with a catalyst by a compressor and causing a methanation reaction.
In Patent Document 2, steam is generated by the heat stored in the heat storage device, the steam is used to drive a condensing turbine generator to generate electricity, and the generated power is used to electrolyze water to produce hydrogen, which is fossilized. Described is an apparatus for producing a synthetic hydrocarbon gas by steam reforming a fuel with steam extracted from the condensate turbine to generate a reaction gas and adding the hydrogen to the reaction gas.

Japanese Unexamined Patent Publication No. 2011-241182 Japanese Unexamined Patent Publication No. 55-54394

The methane synthesizer described in Patent Document 1 has a problem that a large amount of energy is consumed for pressurizing the raw material gas because hydrogen gas and carbon dioxide gas as raw material gases must be pressurized by a compressor.
Patent Document 2 describes a synthetic hydrocarbon production apparatus equipped with a condensate turbine power generation apparatus. However, hydrogen gas and carbon dioxide gas are hydrolyzed to produce synthetic hydrocarbon gas, and hydrogen is produced. The technique of generating high-pressure steam by the reaction heat generated by the chemical reaction and the combustion heat of the synthetic hydrocarbon gas and driving the condensate turbine generator with the high-pressure steam to generate power is not disclosed. Further, since hydrogen gas is supplied to the component adjusting furnace by a blower, the pressurizing power of hydrogen gas becomes large.

In the present invention, at least one of hydrogen and carbon dioxide is supplied to the reaction tube of the hydrogenation reactor by utilizing the phase conversion from the liquid phase to the gas phase, and hydrogen gas and carbon dioxide gas are hydrogenated in the reaction tube. To generate synthetic hydrocarbon gas, the reaction tube is cooled and high-temperature water heated by the heat of hydrogenation reaction drives the condensate turbine generator with high-pressure steam generated by heating the synthetic hydrocarbon gas in the boiler. It is an object of the present invention to provide a vaporization-utilized hydrogen production system with a power generation facility, which can operate with low carbon-derived electric power and can produce synthetic hydrogen gas at low energy and low cost.

A condensate turbine power generation facility is installed in a vaporization-utilized hydrocarbon production system that supplies hydrogen and carbon dioxide to a hydrogenation reactor using phase conversion from a liquid phase to a gas phase and causes a hydrogenation reaction to produce synthetic hydrocarbon gas. It is a vaporization utilization hydrocarbon production system attached to an annexed power generation facility, and the vaporization utilization hydrocarbon production system supplies a liquefied hydrogen supply device that supplies liquefied hydrogen at a first mass flow rate and a liquefied carbon dioxide at a second mass flow rate. The ratio of the number of moles of hydrogen molecules contained in the first mass flow rate to the number of moles of carbon dioxide molecules contained in the second mass flow rate is the ratio of the number of moles of carbon dioxide molecules contained in the first mass flow rate of the hydrogen to be hydrolyzed. A liquefied carbon dioxide supply device that supplies the liquefied carbon so as to have a ratio of the number of moles to the number of moles of the carbon dioxide, and a first vaporization that vaporizes the liquefied hydrogen supplied from the liquefied hydrogen supply device into hydrogen gas. The device, the second vaporizer that vaporizes the liquefied carbon dioxide supplied from the liquefied carbon dioxide supply device into carbon dioxide gas, and the hydrogen gas and the dioxide that are communicated with the first vaporizer and the second vaporizer. The carbon gas is flowed as a mixed gas having a predetermined mass flow rate at a predetermined pressure and a predetermined temperature suitable for the hydrogenation reaction, and the hydrogenation reaction is carried out under a hydrogenation reaction catalyst filled therein to cause the synthetic hydrocarbon gas and water vapor. Condensed water is supplied from the reaction tube configured to flow out as a reaction gas containing the above, and the reaction heat generated in the hydrogenation reaction is transferred to the condensed water and inside the reaction tube. A hydrogenation reactor provided with a cooling unit that maintains the temperature at the predetermined temperature at which the hydrogenation catalyst is active and sends out the condensed water as high-temperature water, and one of the high-temperature cooling water flowing out from the condensate turbine power generation facility. A heat exchanger that transfers heat from the high temperature side where the part flows to the low temperature side where the antifreeze heat medium flows, and vaporizes the liquefied hydrogen of the first mass flow rate into the hydrogen gas of the first temperature at the predetermined pressure. The amount of heat per unit time required to cause the heat and the amount of heat required to vaporize the liquefied carbon dioxide of the second mass flow rate into the carbon dioxide gas at the second temperature at the predetermined pressure. The heat exchanger that transfers the added amount of heat per unit time for vaporization from a part of the high-temperature cooling water to the antifreeze heat medium, and the heat exchanger between the low temperature side of the heat exchanger and the first vaporizer. The first heat quantity supply circulation circuit that circulates the freezing heat medium and supplies the heat quantity per unit time to the first vaporizer, and the antifreeze between the low temperature side of the heat exchanger and the second vaporizer. Circulate the heat medium A heat transfer device for vaporization including a second heat quantity supply circulation circuit for supplying the heat quantity per second unit time to the second vaporizer, and the reaction gas supplied from the reaction tube to the synthetic hydrocarbon gas and water. The condensate turbine power generation facility includes a gas-water separation device for separation, and the condensate turbine power generation facility burns a generator driven by a steam turbine and at least a part of the synthetic hydrocarbon gas supplied from the gas-water separation device. The boiler that heats the high-temperature water supplied from the cooling unit of the hydrogenation reactor to convert it into high-pressure steam and supplies it to the steam turbine, and the low-pressure steam discharged from the steam turbine is supplied from the cooling water supply device. It is a vaporization utilization hydrocarbon production system with a power generation facility, which comprises a condenser which condenses the cooling water into the condensed water by the cooling water and heats the cooling water into high-temperature cooling water to flow out.

When only one of hydrogen and carbon dioxide is supplied in the liquid phase, the vaporization utilization hydrocarbon production system is a liquefied raw material supply device that supplies one of the hydrogen and the carbon dioxide in the liquid phase at a third mass flow rate. , The other raw material gas supply device that supplies the other of the hydrogen and the carbon dioxide in a gas phase at a predetermined pressure and a fourth mass flow rate, and is a liquefied raw material of the third mass flow rate and the other raw material of the fourth mass flow rate. The other that supplies the other raw material gas so that the ratio of the number of moles of hydrogen contained in the gas to the number of moles of carbon dioxide is the ratio of the number of moles of the hydrogen that undergoes the hydrogenation reaction to the number of moles of the carbon dioxide. The raw material gas supply device, the third vaporizer that vaporizes the liquefied raw material supplied from the liquefied raw material supply device into one raw material gas, and the one raw material gas that is communicated with the third vaporizer and the other raw material gas supply device. And the other raw material gas are flown as a mixed gas having a predetermined mass flow rate at the predetermined pressure and the predetermined temperature suitable for the hydrogenation reaction, and the hydrogenation reaction is carried out under the hydrogenation catalyst filled therein to carry out the synthetic hydrocarbon. Condensed water is supplied from a reaction tube configured to flow out as a reaction gas containing gas and water vapor, and the reaction heat generated in the hydrogenation reaction is transferred to the condensed water to transfer the heat to the condensed water. A hydrogenation reactor having a cooling unit that maintains the inside of the reaction tube at the predetermined temperature at which the hydrogenation catalyst is active and sends out the condensed water as high-temperature water, and high-temperature cooling that flows out from the condensate turbine power generation facility. A heat exchanger that transfers heat from the high temperature side where a part of water flows to the low temperature side where the antifreeze heat medium flows. A heat exchanger that transfers heat from a part of the high-temperature cooling water to the antifreeze heat medium, a low-temperature side of the heat exchanger, and the third vaporization of the amount of heat required for vaporizing the raw material gas per third unit time. A heat transfer device for vaporization that circulates the antifreeze heat medium between the vessel and supplies the amount of heat per unit time to the third vaporizer, and the reaction gas supplied from the reaction tube is synthetically carbonized. It is equipped with a gas-water separator that separates hydrogen gas and water.

In the vaporization-utilization hydrocarbon production system attached to the power generation facility according to the present invention, the vaporization-utilization hydrocarbon production system supplies at least one of hydrogen and carbon dioxide as a liquefaction raw material to the vaporizer at a set mass flow rate. The vaporizer supplies a set amount of heat to the liquefied raw material, vaporizes it into one raw material gas at a predetermined pressure, and supplies it to a reaction tube filled with a hydrogenation catalyst of the hydrogenation reactor. The reaction tube contains one raw material gas and the other raw material gas as components, and the ratio of the number of moles of hydrogen to the number of moles of carbon dioxide is the number of moles of hydrogen and the number of moles of carbon dioxide that undergo a hydrogenation reaction. As a mixed gas having a ratio of At this time, in the reaction tube, the reaction heat generated in the hydrogenation reaction is transferred from the reaction gas to the condensed water in the cooling unit, and the inside is maintained at a predetermined temperature at which the hydrogenation catalyst is active.

In the condensate turbine power generation facility, the condensate turbine is rotated by high-pressure steam to drive a generator to generate electricity. The low-pressure steam discharged from the condensate turbine exchanges heat with the cooling water in the condenser to become condensed water, and the cooling water becomes high-temperature cooling water. The condensed water is sent to the hydrogenation reactor, the heat of reaction is transferred by the cooling unit, and it becomes high temperature water and is sent to the boiler. The boiler burns at least a part of the synthetic hydrocarbon gas generated by the hydrogenation reactor to convert high-temperature water into high-pressure steam and supplies it to the condensate turbine. The vaporizer is supplied with the set amount of heat from a part of the high-temperature cooling water.

Using the synthetic hydrocarbon gas generated by the hydrogenation reactor of the vaporization-utilized hydrocarbon production system and the recovered reaction heat, high-pressure steam that rotates the condensate turbine of the condensate turbine power generation facility is generated and condensate. The high-temperature cooling water sent from the turbine power generation facility is used to vaporize the liquefied raw material into one raw material gas and supply it to the hydrogenation reactor, so heat energy is efficiently used and the pressurizing power of the raw material gas is reduced. Therefore, synthetic hydrogen gas and electric power can be produced at low cost. Furthermore, low-carbon-derived electric power can be used to cover the electric power used in the vaporization-utilized hydrocarbon production system attached to the power generation facility.

It is a block diagram which shows the whole structure of the vaporization utilization hydrocarbon production system with the power generation facility which concerns on 1st Embodiment. It is a block diagram which shows the whole structure of the vaporization utilization hydrocarbon production system attached to the power generation facility which concerns on 2nd Embodiment. It is a block diagram which shows the whole structure of the vaporization utilization hydrocarbon production system attached to the power generation facility which concerns on 3rd Embodiment.

1. 1. Configuration of 1st Embodiment As shown in FIG. 1, the vaporization utilization hydrocarbon production system 1a provided with a power generation facility according to the 1st embodiment is a vaporization utilization for producing synthetic hydrocarbon gas by hydrogenating hydrogen and carbon dioxide. It is equipped with a hydrocarbon production system 2 and a condensate turbine power generation facility 3.

The vaporization utilization hydrocarbon production system 2 includes a liquefied hydrogen supply device 10 for supplying liquefied hydrogen, a liquefied carbon dioxide supply device 15 for supplying liquefied carbon dioxide, a first vaporizer 20 for vaporizing liquefied hydrogen into hydrogen gas, and the like. A second vaporizer 25 that vaporizes liquefied carbon dioxide into carbon dioxide gas and a mixed gas that is a mixture of hydrogen gas and carbon dioxide gas are chemically reacted under a hydrogenation catalyst to form a reaction gas containing synthetic hydrocarbon gas and water vapor. A hydrogenation reactor 30 including a reaction tube 31 that flows out and a cooling unit 32 that cools the reaction gas, and the amount of heat and the second mass per unit time required for vaporizing the liquefied hydrogen of the first mass flow rate Q1. A part of the high-temperature cooling water flowing out from the condensate turbine power generation facility 3 flows through the heat quantity Q per unit time for vaporization, which is the sum of the heat quantity per second unit time required for vaporizing the liquefied carbon dioxide in the flow rate Q2. A heat exchanger 45 that transfers heat from the high temperature side to the low temperature side where the antifreeze heat medium flows, and a heat quantity C1 per unit time is supplied to the first vaporizer 20 from the low temperature side of the heat exchanger 45, and the second unit. It includes a heat transfer device 46 for vaporization that supplies the amount of heat C2 per hour to the second vaporizer 25, and a gas-water separation device 40 that separates the reaction gas supplied from the reaction tube 31 into synthetic hydrocarbon gas and water.
The condensate turbine power generation facility 3 includes a generator 51 driven by a steam turbine 50, a boiler 52 that supplies high-pressure steam to the steam turbine 50, a condenser 55 of the steam turbine 50, and a cooling pipe of the condenser 55. A cooling water supply device 57 for supplying cooling water to the 56 is provided.

The liquefied hydrogen supply device 10 is composed of a first tank 11 for storing liquefied hydrogen and a first pump 12 for sucking and discharging liquefied hydrogen from the first tank 11. The liquefied carbon dioxide supply device 15 includes a second tank 16 for storing liquefied carbon dioxide and a second pump 17 for sucking and discharging liquefied carbon dioxide from the second tank 16.

The first pump 12 of the liquefied hydrogen supply device 10 is connected to the first vaporizer 20, and supplies liquefied hydrogen having a first mass flow rate Q1 to the first vaporizer 20 at a predetermined pressure P. The first vaporizer 20 has a heat quantity C1 per unit time, which is a heat quantity per unit time required to vaporize the liquefied hydrogen of the first mass flow rate Q1 into a hydrogen gas having a first temperature T1 at a predetermined pressure P. , It is supplied from the low temperature side of the heat exchanger 45 via the antifreeze heat medium circulating in the first heat quantity supply circulation circuit 47.

The second pump 17 of the liquefied carbon dioxide supply device 15 is connected to the second vaporizer 25, and at a predetermined pressure P, the liquefied carbon dioxide of the second mass flow rate Q2 at a predetermined ratio to the first mass flow rate Q1 is discharged to the second vaporizer. Supply to 25. In the second vaporizer 25, the amount of heat per unit time, which is the amount of heat required to vaporize the liquefied carbon dioxide of the second mass flow rate Q2 into the carbon dioxide gas of the second temperature T2 at a predetermined pressure P, is the amount of heat per unit time. C2 is supplied from the low temperature side of the heat exchanger 45 via the antifreeze heat medium circulating in the second heat quantity supply circulation circuit 48. The heat transfer device 46 for vaporization is configured by the first heat supply circulation circuit 47 and the second heat supply circulation circuit 48.

The hydrogenation reactor 30 includes a reaction tube 31 filled with a known hydrogenation catalyst, and a cooling unit 32 that maintains the inside of the reaction tube 31 at a predetermined temperature T at which the hydrogenation catalyst exhibits activity. The first vaporizer 20 is connected to the first inflow port 33 of the reaction tube 31 by a conduit 21, and the second vaporizer 25 is connected to the second inflow port 34 by a conduit 26. The hydrogen gas and the carbon dioxide gas having the second mass flow rate Q2 are supplied to the inlet side of the reaction tube 31 as a mixed gas having a predetermined pressure P and a temperature lower than the predetermined temperature T at a predetermined mass flow rate Q (= Q1 + Q2).
A preheating section for transmitting the reaction heat was provided on the inlet side of the reaction tube 31, and the temperature of the mixed gas was raised to a predetermined temperature T by the reaction heat in the preheating section, and then the hydrogenation catalyst was filled. It may be allowed to flow in the reaction part.

The reaction tube 31 hydrogenates hydrogen gas and carbon dioxide gas, which are components of the supplied mixed gas, under a hydrogenation catalyst to generate a reaction gas containing synthetic hydrocarbon gas and water vapor, and sends it out from the outlet 35. .. The mixed gas having a temperature lower than the predetermined temperature T is raised by the internal temperature when flowing into the reaction tube 31, and is raised by the reaction heat of the hydrogenation reaction as the hydrogenation reaction progresses. It is configured to maintain the mixed gas cooled by 32 and flowing in the reaction tube 31 at a predetermined temperature T. That is, the condensed water sent from the condenser 55 of the condensate turbine power generation facility 3 flows into the cooling unit 32 surrounding the outer periphery of the reaction tube 31 from the inlet 36, and comes into contact with the outer periphery of the reaction tube 31 to be hydrogenated. By absorbing the reaction heat generated in the reaction, turning it into high-temperature water and sending it from the outlet 37 to the boiler 52 of the condensate turbine power generation facility 3, the reaction heat is transferred from the reaction gas to the condensed water, and the reaction tube 31 The inside of the temperature is maintained at a predetermined temperature T. The inlet 36 is arranged on the outlet 35 side of the reaction tube 31, and the outlet 37 is arranged on the

inlets

33 and 34.

In this way, the reaction tube 31 is communicated with the first vaporizer 20 and the second vaporizer 25, and the predetermined pressure P suitable for the hydrogenation reaction is prepared by using hydrogen gas and carbon dioxide gas as a mixed gas having a predetermined mass flow rate Q. A flow provided with a throttle resistance that flows at a predetermined temperature T and undergoes a hydrogenation reaction under a hydrogenation reaction catalyst filled therein to form a reaction gas containing synthetic hydrocarbon gas and water vapor, and maintains an internal pressure at a predetermined pressure P. It is configured to flow out through the outlet 35. In the cooling unit 32, condensed water is supplied from the condensate turbine power generation facility 3, and the reaction heat generated in the hydrogenation reaction is transferred from the reaction gas to the condensed water, and the inside of the reaction tube 31 is inside the reaction tube 31 at a predetermined temperature T at which the hydrogenation catalyst is active. And send the condensed water to high temperature water. The predetermined pressure P is a pressure suitable for the hydrogenation reaction, and the predetermined temperature T is a temperature at which the hydrogenation catalyst exhibits activity.

For example, in the case of producing synthetic methane gas, a catalyst in which Ni, Rh, Ru, Pd, Pt or the like is supported on a carrier is used as a methaneation catalyst, and a hydrogenation reaction is carried out according to the chemical formula (1). The predetermined pressure P is 1 to 5 MPa, and the predetermined temperature T is 250 to 500 ° C.
CO ₂ + 4H ₂ = CH ₄ + 2H ₂ O (exothermic reaction 164 kJ / mol-CO ₂ ) (1)
Synthetic ethylene gas is produced by the hydrogenation reaction represented by the chemical formula (2).
_{_{_{_{2CO 2 + 6H 2 = C 2}}}} H 4 + 4H 2 O ( exothermic reaction _{152kJ / mol-CO 2) (} 2)

A predetermined ratio R (= Q1: Q2) of the first mass flow rate Q1 of the liquefied hydrogen discharged from the first pump 12 and the second mass flow rate Q2 of the liquefied carbon dioxide discharged from the second pump 17 is a hydrogenation reaction. Assuming that the ratio of the number of moles of hydrogen to the number of moles of carbon dioxide is M1: M2, the number of moles of hydrogen molecules contained in the first mass flow rate Q1 and the number of moles of carbon dioxide molecules contained in the second mass flow rate Q2 The ratio of is set to be M1: M2. It is preferable to set a predetermined ratio R based on the ratio of the number of moles of hydrogen gas that actually undergoes a hydrogenation reaction efficiently in the reaction tube 31 to the number of moles of carbon dioxide gas. For example, in the case of synthetic methane gas production, the ratio of the number of moles of hydrogen to be hydrolyzed to the number of moles of carbon dioxide is 4: 1, the molecular weight of hydrogen is 2, and the molecular weight of carbon dioxide is 44, so Q1: Q2 = 4 × 2: 1 × 44 = 2: 11.

The vaporization heat transfer device 46 having the first heat quantity supply circulation circuit 47 and the second heat quantity supply circulation circuit 48 is antifreeze between the low temperature side of the heat exchanger 45 and the first vaporizer 20 and the second vaporizer 25. The heat medium is circulated to vaporize liquefied hydrogen and liquefied carbon dioxide. The first heat quantity supply circulation circuit 47 circulates an antifreeze heat medium between the low temperature side of the heat exchanger 45 and the first vaporizer 20, and supplies the heat quantity C1 per unit time to the first vaporizer 20. The liquefied hydrogen at the predetermined pressure P and the first mass flow rate Q1 is vaporized into the hydrogen gas at the predetermined pressure P and the first temperature T1. The second heat supply circulation circuit 48 circulates the antifreeze heat medium between the low temperature side of the heat exchanger 45 and the first vaporizer 25, and supplies the heat quantity C2 per second unit time to the first vaporizer 25. The liquefied carbon dioxide at the predetermined pressure P and the second mass flow rate Q2 is vaporized into the carbon dioxide gas at the predetermined pressure P and the second temperature T2.

For start-up, when the vaporization utilization hydrocarbon production system 2 is started, a heat medium is circulated between the heat exchanger 45 and the high temperature side, and the amount of heat required for the start is supplied to the first vaporizer 20 and the second vaporizer 25. The heat supply device 70 is connected to the high temperature side of the heat exchanger 45 by

conduits

71 and 72.

At the outlet 35 of the reaction tube 31 of the hydrogenation reactor 30, the reaction gas generated by the hydrogenation reaction of hydrogen gas and carbon dioxide gas in the hydrogenation reactor 30 is separated into synthetic hydrocarbon gas and water. A known gas-water separator 40 is connected. At least a part of the separated synthetic hydrocarbon gas is supplied to the boiler 52, and the rest is sent to the synthetic hydrocarbon gas utilization unit 41. Water is discharged into the discharge groove 42. The separated synthetic hydrocarbon gas is supplied to the boiler 52 at a mass flow rate corresponding to the amount of power generated by the condensate turbine power generation facility 3.

In the condensate turbine power generation facility 3, the steam turbine 50 is rotated by the high-pressure steam supplied from the boiler 52, and the generator 51 is driven by the steam turbine 50 to generate electricity. The generated electric power is used as electric power for the vaporization-utilizing hydrocarbon production system 1a attached to the power generation facility, and the surplus electric power is sold. The steam whose pressure has dropped by rotating the steam turbine 50 is cooled by the condenser 55 to become condensed water, which is supplied to the cooling unit 32 of the hydrogenation reactor 30. The condensed water absorbs the reaction heat of the hydrogenation reaction from the reaction tube 31 while flowing through the cooling unit 32, raises the temperature to high temperature water (for example, 15 MPa, 250 ° C.) and supplies it to the heat exchange unit 53 of the boiler 52. Will be done. In the boiler 52, synthetic hydrocarbon gas is supplied from the gas water separator 40 to the combustion chamber 54 and burned, and the high temperature water supplied to the heat exchange unit 53 is heated to generate high-pressure steam (for example, 12 MPa, 540 ° C.). do.

The condenser 55 is provided with a cooling pipe 56 through which cooling water circulates, and the low-pressure steam discharged from the steam turbine 50 and flowing into the condenser 55 transfers heat of condensation to the cooling water to become condensed water. A cooling water supply device 57 is connected to the cooling pipe 56, and the cooling water is circulated. The cooling water supply device 57 uses, for example, a pump 58 that pumps seawater as cooling water, a pipeline 59 to which the pump 58 is connected to send seawater from the sea to the cooling pipe 56, and seawater that has been circulated through the cooling pipe 56 and heated to a high temperature. A pipeline 60 for returning to the sea as high-temperature cooling water is provided. The pipeline 60 is branched at a branch point 61 and connected to the pipeline 71, a part of the high temperature cooling water is circulated on the high temperature side of the heat exchanger 45, and the return point 62 on the upstream side of the pump 58 is circulated in the pipeline 59. It is configured to return a part of the high-temperature cooling water circulated on the high-temperature side of the heat exchanger 45 to the upstream side of the pump 58. The heat exchanger 45 added the heat quantity C1 per first unit time and the heat quantity C2 per pipeline to the antifreeze heat medium circulating in the heat transfer device 46 for vaporization from a part of the high temperature cooling water. The amount of heat C per unit time for vaporization is thermally transferred.
The cooling water supply device 57 may pump river water / lake water with a pump 58 and circulate the cooling pipe 56 as cooling water. Further, a cooling tower may be provided to circulate the cooling water between the cooling tower and the cooling pipe.

2. Operation and Effect of First Embodiment The liquefied hydrogen supply device 10 sucks liquefied hydrogen from the first tank 11 by the first pump 12 and discharges it at a first mass flow rate Q1 and a predetermined pressure P. The liquefied carbon dioxide supply device 15 sucks liquefied carbon dioxide from the second tank 21 by the second pump 17, and discharges it at a second mass flow rate Q2 and a predetermined pressure P.

The amount of heat C1 per hour required to vaporize the liquefied hydrogen of the first mass flow rate Q1 into the hydrogen gas having the predetermined pressure P1 and the first temperature T1 and the liquefied carbon dioxide of the second mass flow rate Q2 are set to the predetermined pressure P and the second. The amount of heat C per hour for vaporization, which is the sum of the amount of heat C2 per second hour required for vaporizing into carbon dioxide gas at two temperatures T2, is sent from the cooling pipe 56 of the condenser 55 to the high temperature side of the heat exchanger 45. Heat is transferred from a part of the high-temperature cooling water that circulates to the antifreeze heat medium that circulates on the low-temperature side of the condenser 55.
The first vaporizer 20 is supplied with the amount of heat C1 per unit time by the antifreeze heat medium circulating in the first heat quantity supply circulation circuit 47 from the low temperature side of the heat exchanger 45, and determines the liquefied hydrogen of the first mass flow rate Q1. It is vaporized into hydrogen gas having a pressure P and a first temperature T1. The second vaporizer 25 is supplied with heat C2 per second unit time by an antifreeze heat medium circulating in the second heat supply circulation circuit 48 from the low temperature side of the heat exchanger 45, and liquefied carbon dioxide of the second mass flow rate Q2. It is vaporized into carbon dioxide gas having a predetermined pressure P and a second temperature T2.

The vaporized hydrogen gas and carbon dioxide gas are mixed and flow into the reaction tube 31 as a mixed gas lower than a predetermined pressure P and a predetermined temperature T, but the temperature is raised by the internal heat generation of the reaction tube 31 and the reaction tube 31 is mass-produced. While flowing at the flow rate Q, it undergoes a hydrogenation reaction under a hydrogenation catalyst and chemically changes into a reaction gas containing synthetic hydrocarbon gas and water vapor to release reaction heat. At this time, in the cooling unit 32, condensed water is supplied from the condenser 55 of the condensate turbine 50, and the reaction heat generated in the hydrogenation reaction is transferred from the reaction gas to the condensed water, and the hydrogenation catalyst moves inside the reaction tube 31. The temperature is maintained at a predetermined temperature T indicating activity, and the condensed water is converted into high-temperature water and sent out.

The reaction gas loses pressure while passing through the outlet 35 provided with the flow path resistance, and is sent to the gas-water separation device 40 in a state where the pressure inside the reaction tube 31 is maintained at a predetermined pressure P. The gas water separation device 40 condenses water vapor to separate the synthetic hydrocarbon gas and water, sends the synthetic hydrocarbon gas to the synthetic hydrocarbon gas utilization unit 41, and discharges the water to the discharge groove 42.

When the vaporization utilization hydrocarbon production system 1a is started, the cooling water supply device 57 stops the circulation of the cooling water between the cooling pipe 56 of the condenser 55 and the heat exchanger 45, and the start-up heat supply device 70 is turned on. It starts and circulates a heat medium with the high temperature side of the heat exchanger 45, and supplies the first vaporizer 20 and the second vaporizer 25 with the amount of heat required for starting. As a result, the liquefied hydrogen and the liquefied carbon dioxide supplied at the starting mass flow rate are vaporized in the first vaporizer 20 and the second vaporizer 25, and the hydrogen gas and the carbon dioxide gas undergo a hydrogenation reaction in the hydrogenation reactor 30. Chemically changes to synthetic hydrocarbon gas and water vapor. When the inside of the reaction tube 31 is heated to a temperature at which the hydrogenation catalyst exhibits activity by the heat of reaction, the start-up heat supply device 70 is stopped, and the cooling tube 56 of the condenser 55 and the high temperature side of the heat exchanger 45 are connected. Start the circulation of cooling water between.

According to the vaporization utilization hydrocarbon production system 1a according to the first embodiment, at least a part of the synthetic hydrocarbon gas generated by the hydrogenation reactor 30 of the vaporization utilization hydrocarbon production system 2 and the hydrogenation reaction heat are utilized. The high-pressure steam that rotates the condensate turbine 50 of the condensate turbine power generation facility 3 is generated, and heat is transferred from the high-temperature cooling water sent from the condensate turbine power generation facility 3 to the first vaporizer 20 and the second vaporizer 25. Then, liquefied hydrogen and liquefied carbon dioxide are vaporized into hydrogen gas and carbon dioxide gas and supplied to the hydrogenation reactor 30. As a result, it is possible to efficiently utilize thermal energy, reduce the pressurizing power of hydrogen gas and carbon dioxide gas, and produce synthetic hydrocarbon gas and electric power at low cost. Further, the electric power used in the vaporization-utilizing hydrocarbon production system 1a attached to the power generation facility can be covered by the low-carbon-derived electric power.

3. 3. Configuration of the 2nd Embodiment As shown in FIG. 2, the vaporization utilization hydrocarbon production system 1b attached to the power generation facility of the 2nd embodiment is attached to the liquefied carbon dioxide supply device 15 and the 2nd calorific value supply circulation circuit 48 in the 1st embodiment. Instead, the carbon dioxide gas supplied from the carbon dioxide gas supply device 18 is pressurized by the compressor 19 and supplied to the reaction tube 31 of the hydrocarbon reactor 30 from the inflow port 34, which is different from the first embodiment. ..

The carbon dioxide gas supply device 18 is connected to the suction port of the compressor 19, and the discharge port of the compressor 19 is connected to the second inflow port 34 of the reaction tube 31 of the hydrogenation reactor 30 via the pipeline 27. The carbon dioxide gas supply device 18 supplies the carbon dioxide gas having the second mass flow rate Q2 to the compressor 19.

4. Operation and Effect of Second Embodiment The amount of heat Q1 per hour required to vaporize the liquefied hydrogen of the first mass flow rate Q1 into hydrogen gas at a predetermined pressure P and the first temperature T1 is the cooling pipe of the condenser 55. Heat is transferred from a part of the high-temperature cooling water that is sent out from 56 and circulates on the high-temperature side of the heat exchanger 45 to the antifreeze heat medium that circulates on the low-temperature side of the condenser 55. The first vaporizer 20 is supplied with the amount of heat C1 per unit time by the antifreeze heat medium circulating in the first heat quantity supply circulation circuit 47 from the low temperature side of the heat exchanger 45, and determines the liquefied hydrogen of the first mass flow rate Q1. It is vaporized into hydrogen gas having a pressure P and a first temperature T1.

The carbon dioxide gas supplied from the carbon dioxide gas supply device 18 at the second mass flow rate Q2 is compressed to a predetermined pressure P by the compressor 19 and the temperature rises. The hydrogen gas vaporized by liquefied hydrogen and the carbon dioxide gas pressurized by the compressor 26 are mixed and flowed into the reaction tube 31 of the hydrocarbon reactor 30 as a mixed gas having a predetermined pressure P and a temperature lower than the predetermined temperature T for reaction. The temperature is raised by the internal heat generation of the tube 31, and while the reaction tube 31 is flowing at the mass flow rate Q, it undergoes a hydrogenation reaction under a hydrogenation catalyst and chemically changes into a reaction gas containing synthetic hydrocarbon gas and water vapor to release the reaction heat. do. The temperature inside the reaction tube 31 is maintained at a predetermined temperature T at which the hydrogenation catalyst exhibits activity by releasing the heat of hydrogenation reaction and cooling by the cooling unit 32.

The second embodiment has almost the same effect as the first embodiment. Further, since the carbon dioxide gas is pressurized by the compressor 26, the system 1b can be easily controlled to a stable operating state.

5. Configuration of Third Embodiment As shown in FIG. 3, the vaporization-utilized hydrocarbon production system 1c attached to the power generation facility of the third embodiment is replaced with the liquefied hydrogen supply device 10 and the first calorific value supply circulation circuit 47 in the first embodiment. The hydrogen gas supplied from the hydrogen gas supply device 13 is pressurized by the compressor 14 and supplied to the reaction tube 31 of the hydrogenation reactor 30 from the inflow port 33, which is different from the first embodiment.

The hydrogen gas supply device 13 is connected to the suction port of the compressor 14, and the discharge port of the compressor 14 is connected to the first inflow port 33 of the reaction tube 31 of the hydrogenation reactor 30 via the pipeline 28. The hydrogen gas supply device 13 supplies the hydrogen gas having the first mass flow rate Q1 to the compressor 14.

6. Operation and Effect of Third Embodiment The amount of heat Q2 per second hour required to vaporize the liquefied carbon dioxide of the second mass flow rate Q2 into the carbon dioxide gas of the predetermined pressure P and the second temperature T2 is the condenser 55. Heat is transferred from a part of the high-temperature cooling water that is sent out from the cooling pipe 56 and circulates on the high-temperature side of the heat exchanger 45 to the antifreeze heat medium that circulates on the low-temperature side of the condenser 55. The second vaporizer 25 is supplied with the amount of heat C2 per second unit time by the antifreeze heat medium circulating in the second heat quantity supply circulation circuit 48 from the low temperature side of the heat exchanger 45, and determines the liquefied hydrogen of the second mass flow rate Q2. It is vaporized into carbon dioxide gas having a pressure P and a second temperature T2.

The hydrogen gas supplied from the hydrogen gas supply device 13 at the first mass flow rate Q1 is compressed to a predetermined pressure P by the compressor 14 and the temperature rises. The carbon dioxide gas in which the liquefied carbon dioxide is vaporized and the hydrogen gas pressurized by the compressor 14 are mixed and flow into the reaction tube 31 of the hydrocarbon reactor 30 as a mixed gas having a temperature lower than a predetermined pressure P and a predetermined temperature T. The temperature is raised by the internal heat generation of the reaction tube 31, and while the reaction tube 31 is flowing at the mass flow rate Q, it undergoes a hydrogenation reaction under a hydrogenation catalyst and chemically changes into a reaction gas containing synthetic hydrocarbon gas and water vapor to generate reaction heat. discharge. The temperature inside the reaction tube 31 is maintained at a predetermined temperature T at which the hydrogenation catalyst exhibits activity by releasing the heat of hydrogenation reaction and cooling by the cooling unit 32.

The third embodiment has almost the same effect as the first embodiment. Further, since the hydrogen gas is pressurized by the compressor 14, the system 1c can be easily controlled to a stable operating state.

Hydrogen gas and carbon dioxide gas are introduced into the reaction tube 31 of the hydrogenation reactor 30 separately from the

inflow ports

33 and 34, and mixed in the reaction tube 31 to form a mixed gas. After mixing with a mixer, the mixed gas may be supplied to the reaction tube 31 of the hydrogenation reactor 30 from one inflow port.
In this case, hydrogen gas having a predetermined pressure P is supplied to the first inflow port of the mixer, carbon dioxide gas having a predetermined pressure P is supplied to the second inflow port, and hydrogen gas and carbon dioxide gas are mixed in the mixer to be predetermined. After becoming a mixed gas of pressure P, it is supplied to the reaction tube 31 of the hydrogenation reactor 30 from the inflow port. Since the hydrogen gas and the carbon dioxide gas are mixed and supplied to the reaction tube 31 in this way, the hydrogenation reaction in the reaction tube 31 can be smoothly performed.
Further, a heating coil may be arranged in the mixer to heat the mixed gas to the vicinity of a predetermined temperature T before flowing into the reaction tube 31.

The vaporization utilization hydrocarbon production system attached to the power generation facility according to the above-described embodiment is composed of a hydrogenation reactor 30 having one stage of a reaction tube 31 filled with a hydrogenation catalyst, but is filled with a hydrogenation catalyst. The reactor tubes are arranged in series in multiple stages, a heat exchanger is connected between the adjacent reactor tubes, and the high-temperature reaction gas and unreacted mixed gas sent from the reaction tubes in the previous stage are cooled by the heat exchanger. Even if the present invention is applied to a multi-stage reactor type hydrogenation reactor configured to be supplied to a subsequent reaction tube and to maintain the internal temperature of each reaction tube within an allowable range of a predetermined temperature T. good. In this case, the condensed water condensed by the condenser 55 is circulated through a heat exchanger connected between the adjacent reaction tubes to heat the hot water and supplied to the boiler 52.

1a to 1c: vaporization utilization hydrocarbon production system with power generation equipment 2: vaporization utilization hydrocarbon production system 3: condensate turbine power generation equipment, 10: liquefied hydrogen supply equipment, 12: first pump, 13: hydrogen gas supply equipment , 14, 19: Compressor, 15: Liquefied carbon dioxide supply device, 17: Second pump, 18: Carbon dioxide gas supply device, 20: First vaporizer, 25: Second vaporizer, 30: Hydrogenation reactor, 31: Condenser, 32: Cooling unit, 40: Gas water separator, 45: Heat exchanger, 46: Heat transfer device for vaporization, 47: 1st heat supply circulation circuit, 48: 2nd heat supply circulation circuit, 50 : Condenser, 51: Generator, 52: Boiler, 53: Heat exchanger, 54: Combustion chamber, 55: Condenser, 56: Cooling pipe, 57: Cooling water supply device, 70: Start-up heat supply device

Claims

A condensate turbine power generation facility is installed in a vaporization-utilizing hydrocarbon production system that supplies hydrogen and carbon dioxide to a hydrogenation reactor using phase conversion from a liquid phase to a gas phase and causes a hydrogenation reaction to produce synthetic hydrocarbon gas. It is a hydrocarbon production system that uses vaporization with an attached power generation facility.
The vaporization-utilizing hydrocarbon production system includes a liquefied hydrogen supply device that supplies liquefied hydrogen at a first mass flow rate, and a liquefied hydrogen supply device.
A liquefied carbon dioxide supply device that supplies liquefied carbon dioxide at a second mass flow rate, the number of moles of hydrogen molecules contained in the first mass flow rate and the number of moles of carbon dioxide molecules contained in the second mass flow rate. A liquefied carbon dioxide supply device that supplies the liquefied carbon so that the ratio is the ratio of the number of moles of the hydrogen that undergoes the hydrogenation reaction to the number of moles of the carbon dioxide.
A first vaporizer that vaporizes the liquefied hydrogen supplied from the liquefied hydrogen supply device into hydrogen gas, and
A second vaporizer that vaporizes the liquefied carbon dioxide supplied from the liquefied carbon dioxide supply device into carbon dioxide gas, and
The hydrogen gas and the carbon dioxide gas are communicated with the first vaporizer and the second vaporizer and flowed as a mixed gas having a predetermined mass flow rate at a predetermined pressure and a predetermined temperature suitable for the hydrogenation reaction, and filled therein. Condensed water is supplied from the reaction tube configured to undergo a hydrogenation reaction under the hydrogenated reaction catalyst to form a reaction gas containing the synthetic hydrocarbon gas and water vapor and flow out, and the condensate turbine power generation facility. The reaction heat generated in the hydrogenation reaction is transferred to the condensed water, the inside of the reaction tube is maintained at the predetermined temperature at which the hydrogenation catalyst is active, and the condensed water is converted into high temperature water and sent out. Hydrogenation reactor and
A heat exchanger that transfers heat from the high temperature side where a part of the high temperature cooling water flowing out of the condensate turbine power generation facility flows to the low temperature side where the antifreeze heat medium flows, and the liquefied hydrogen having the first mass flow rate. The amount of heat per unit time required to vaporize the hydrogen gas at the first temperature at the predetermined pressure and the liquefied carbon dioxide at the second mass flow rate into the carbon dioxide gas at the second temperature at the predetermined pressure. A heat exchanger that transfers heat from a part of the high-temperature cooling water to the antifreeze heat medium by adding the amount of heat per unit time required for vaporization to the amount of heat per unit time for vaporization.
A first heat quantity supply circulation circuit that circulates the antifreeze heat medium between the low temperature side of the heat exchanger and the first vaporizer and supplies heat per unit time to the first vaporizer, and the said For vaporization including a second heat quantity supply circulation circuit that circulates the antifreeze heat medium between the low temperature side of the heat exchanger and the second vaporizer and supplies the heat quantity per second unit time to the second vaporizer. Heat transfer device and
A gas-water separator that separates the reaction gas supplied from the reaction tube into the synthetic hydrocarbon gas and water is provided.
The condensate turbine power generation facility includes a generator driven by a steam turbine and
At least a part of the synthetic hydrocarbon gas supplied from the gas-water separator is burned, and the high-temperature water supplied from the cooling unit of the hydrogenation reactor is heated to be converted into high-pressure steam and supplied to the steam turbine. With a boiler to do
A condenser that condenses the low-pressure steam discharged from the steam turbine into the condensed water by the cooling water supplied from the cooling water supply device and heats the cooling water into the high-temperature cooling water to flow out.
Hydrocarbon production system using vaporization with power generation equipment.
One of hydrogen and carbon dioxide is supplied to the hydrocarbon reactor by utilizing the phase conversion from the liquid phase to the gas phase, and the other is supplied to the hydrocarbon reactor by the compressor in the gas phase and synthesized by hydrogenation reaction. It is a vaporization-utilization hydrocarbon production system with a power generation facility with a condensate turbine power generation facility attached to the vaporization-utilization hydrocarbon production system that produces hydrocarbon gas.
The vaporization-utilizing hydrocarbon production system includes a liquefaction raw material supply device that supplies one of the hydrogen and the carbon dioxide in a liquid phase at a third mass flow rate.
The other raw material gas supply device that supplies the other of the hydrogen and the carbon dioxide in a gas phase at a predetermined pressure and a fourth mass flow rate, and is a liquefied raw material having the third mass flow rate and the other raw material gas having the fourth mass flow rate. The other raw material that supplies the other raw material gas so that the ratio of the number of moles of hydrogen contained in the above to the number of moles of carbon dioxide is the ratio of the number of moles of hydrogen that undergoes the hydrogenation reaction to the number of moles of carbon dioxide. Gas supply device and
A third vaporizer that vaporizes the liquefied raw material supplied from the liquefied raw material supply device into a raw material gas.
It is communicated with the third vaporizer and the other raw material gas supply device, and the one raw material gas and the other raw material gas are flown as a mixed gas having a predetermined mass flow rate at the predetermined pressure and the predetermined temperature suitable for the hydrogenation reaction. Condensed water is supplied from a reaction tube configured to undergo a hydrogenation reaction under a hydrogenation catalyst filled inside to form a reaction gas containing the synthetic hydrocarbon gas and water vapor and to flow out, and the condensate turbine power generation facility. The reaction heat generated in the hydrogenation reaction is transferred to the condensed water, the inside of the reaction tube is maintained at the predetermined temperature at which the hydrogenation catalyst is active, and the condensed water is turned into high-temperature water and sent out. With a hydrogenation reactor and
A heat exchanger that transfers heat from the high temperature side where a part of the high temperature cooling water flowing out of the condensate turbine power generation facility flows to the low temperature side where the antifreeze heat medium flows, and is the liquefaction raw material having the third mass flow rate. A heat exchanger that transfers heat from a part of the high-temperature cooling water to the antifreeze heat medium, which is required to vaporize the heat into the one-sided raw material gas at a third temperature at the predetermined pressure.
A vaporization heat transfer device that circulates the antifreeze heat medium between the low temperature side of the heat exchanger and the third vaporizer and supplies the amount of heat per unit time to the third vaporizer.
A gas-water separator that separates the reaction gas supplied from the reaction tube into the synthetic hydrocarbon gas and water is provided.
The condensate turbine power generation facility includes a generator driven by a steam turbine and
At least a part of the synthetic hydrocarbon gas supplied from the gas-water separator is burned, and the high-temperature water supplied from the cooling unit of the hydrogenation reactor is heated to be converted into high-pressure steam and supplied to the steam turbine. With a boiler to do
A condenser that condenses the low-pressure steam discharged from the steam turbine into the condensed water by the cooling water supplied from the cooling water supply device and heats the cooling water into the high-temperature cooling water to flow out.
Hydrocarbon production system using vaporization with power generation equipment.
The vaporization-utilization hydrocarbon production system according to claim 1 or 2, further comprising a start-up heat supply device for supplying the amount of heat required for starting the vaporization-utilization hydrocarbon production system to the high-temperature side of the heat exchanger. ..