Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/83—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with rare earths or actinides
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
  • C07B61/00—Other general methods
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
  • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
  • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
  • C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C9/00—Aliphatic saturated hydrocarbons
  • C07C9/02—Aliphatic saturated hydrocarbons with one to four carbon atoms
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon

Definitions

• FT synthesis is a reaction in which a mixed gas of carbon monoxide and hydrogen is reacted in the presence of a catalyst to produce a hydrocarbon mixture.
• the FT synthesis reaction is a gas-solid contact reaction in which synthesis gas is reacted using a solid catalyst, and initially a fixed-bed reactor was used as the reaction device.
• Other types of reactors include slurry and circulating fluidized bed reactors.
• Patent Document 1 describes that the use of a catalyst composition containing iron, cobalt, and ruthenium as the main catalyst and a non-zeolitic silico-aluminum phosphate molecular sieve as an auxiliary catalyst/carrier increases the selectivity and conversion rate of liquid hydrocarbons from hydrocarbons having a carbon number of 5 (hereinafter referred to as C5) to gasoline-equivalent fractions up to 420°F (216°C).
• Patent Document 2 describes an example in which a manganese oxide carrier containing an alkali metal (potassium in the example) added to a ruthenium-based catalyst, which was originally intended for use in a fixed-bed reactor, is used to apply the catalyst to a liquid-phase slurry process, thereby increasing the olefin selectivity and conversion rate of the olefin/paraffin ratio in the produced hydrocarbons.
• the present invention aims to provide a manufacturing device that includes an FT reaction catalyst that can efficiently convert carbon dioxide into hydrocarbons in the FT reaction of a raw material gas that contains carbon dioxide.
• the present inventors have found that by using, as a reaction apparatus for carrying out the FT reaction, an FT synthesis reaction apparatus comprising a reaction vessel and a plate-shaped heat exchanger having an uneven surface, it is possible to precisely maintain the reaction temperature within an appropriate range, thereby increasing the conversion rate to hydrocarbons by the FT reaction, and have completed the present invention. That is, the present invention provides an FT synthesis reaction apparatus and an FT synthesis reaction method characterized as follows.
• the FT synthesis reactor of the present invention which has been made to solve the above problems, is characterized by comprising a reaction vessel and a plate-shaped heat exchanger having an uneven surface. According to this feature, it is possible to increase the heat transfer surface area, and by efficiently removing heat generated by the FT reaction in the reaction vessel, it is possible to precisely maintain the reaction temperature within an appropriate range, thereby increasing the conversion rate of the FT reaction to hydrocarbons.
• one embodiment of the FT synthesis reaction apparatus of the present invention is characterized in that the temperature inside the reaction vessel during the FT synthesis reaction is 200 to 270°C. This feature makes it possible to further increase the conversion rate and selectivity to hydrocarbons in the FT reaction.
• one embodiment of the FT synthesis reaction apparatus of the present invention is characterized in that the volume of the reaction vessel is 1000 L or less. This feature allows the entire FT synthesis reactor to be made compact, saving space. This also gives more freedom in the installation location, and considering the possibility of future biomass raw materials, it is possible to provide a compact facility that brings the raw material supply point and the user closer together.
• One embodiment of the FT synthesis reaction apparatus of the present invention is characterized in that the internal pressure during the reaction in the reaction vessel is 1000 kPa or less. According to this feature, since the FT reaction can be carried out at a relatively low pressure, the reaction vessel can be made light and simple, and this also increases the degree of freedom in choosing the installation location of the equipment.
• One embodiment of the FT synthesis reactor of the present invention is characterized in that the raw synthesis gas supplied to the reaction vessel contains carbon dioxide. According to this feature, by making effective use of carbon dioxide, it can contribute to carbon recycling, which has become an issue in recent years, and can also be used for the purpose of addressing environmental issues.
• one embodiment of the FT synthesis reaction apparatus of the present invention is characterized in that it has a reaction catalyst containing at least one selected from yttrium, cerium, lanthanum, praseodymium, neodymium, holmium, sodium, potassium, rubidium, cesium, beryllium, magnesium, calcium, strontium, barium, and copper.
• This feature makes it possible to improve the carbon conversion rate to hydrocarbons compared to conventional catalysts, and to perform an efficient FT reaction. Furthermore, this feature makes it possible to efficiently convert not only carbon monoxide but also carbon dioxide to hydrocarbons.
• the FT synthesis reaction method of the present invention for solving the above problems is characterized in that heat exchange is carried out using a plate-shaped heat exchanger having uneven surfaces. According to this feature, it is possible to increase the heat transfer surface area, and by efficiently removing heat generated by the FT reaction in the reaction vessel, it is possible to precisely maintain the reaction temperature within an appropriate range, thereby increasing the conversion rate of the FT reaction to hydrocarbons.
• the present invention provides a manufacturing device that includes an FT reaction catalyst that can efficiently convert carbon dioxide into hydrocarbons in the FT reaction of a raw material gas that contains carbon dioxide.
• FIG. 1 is a schematic explanatory diagram showing the configuration of an FT synthesis reaction apparatus of the present invention.
• FIG. 2 is a schematic explanatory diagram showing a heat exchange section in the FT synthesis reactor of the present invention.
• FIG. 1 is a schematic diagram showing an existing FT synthesis reaction apparatus.
• the present invention relates to an FT reaction apparatus which efficiently performs an FT reaction by precisely controlling heat generated during the reaction in an apparatus for producing liquid hydrocarbons through an FT synthesis reaction.
• the FT synthesis reaction apparatus and the FT synthesis reaction method according to the present invention will be described in detail below with reference to the drawings.
• the FT synthesis reaction catalyst and the FT synthesis reaction method described in the embodiments are merely exemplified to explain the FT synthesis reaction apparatus, and are not limited thereto. Furthermore, the FT synthesis reaction method is replaced by the explanation of the FT synthesis reaction apparatus.
• the FT reaction apparatus 100 of the first embodiment is an apparatus in which a raw synthesis gas 20 is blown into a medium oil 14 in which a fine powder-like FT reaction catalyst 10 is suspended, to cause a reaction, and the converted hydrocarbon fraction 30 is extracted as a product gas 31 and a product liquid 32, and is generally a bubble column reaction vessel.
• Fig. 1 is a schematic diagram showing the configuration of an FT reactor 100 according to a first embodiment of the present invention. As shown in Fig. 1, the FT reactor according to the first embodiment includes an FT reaction catalyst 10, a raw synthesis gas 20, a reaction vessel 40 forming the outer shell of the FT reactor 100, and a heat exchanger 50 for controlling the reaction temperature in the FT reaction. Each component will be described in detail below.
• the catalyst 10 causes the FT reaction by contacting with the raw synthesis gas 20 .
• the catalyst 10 is a fine powder consisting of a main catalyst 11, an auxiliary catalyst 12, and a carrier 13, and is suspended in a medium oil .
• the main catalyst 11 is a main component of the catalyst 10 that causes the FT reaction by contacting with the raw synthesis gas 20 .
• a metal catalyst selected from cobalt, ruthenium, and iron is used as the main catalyst for the FT reaction. Iron is inexpensive but has relatively low catalytic activity, while ruthenium is a precious metal with high catalytic activity but is extremely expensive.
• the products of the FT reaction using iron-based catalysts are characterized by a high naphtha content and also contain oxygen-containing compounds. For this reason, cobalt is most preferably used to obtain middle distillates such as diesel, jet fuel, and kerosene.
• the main catalyst used is a catalyst containing one selected from cobalt, ruthenium and iron, and preferably a catalyst containing cobalt.
• the amount of the main catalyst (cobalt, etc.) is preferably 5% by weight or more and 25% by weight or less, based on the weight of the main catalyst metal in the catalyst. More preferably, it is 7.5% by weight or more and 17% by weight or less, and even more preferably, it is 8% by weight or more and 15% by weight or less.
• the reaction proceeds easily, but if the upper limit of this range is exceeded, the activity of the FT reaction with respect to the increase in the amount of support tends to saturate, and the technical significance in terms of cost becomes weak. On the other hand, if it is less than the lower limit of this range, the activity per amount of catalyst decreases, which is not preferable.
• the auxiliary catalyst 12 is added to the main catalyst 11 to enhance the catalytic activity of the FT reaction.
• the present invention is characterized in that, in addition to the main catalyst, the auxiliary catalyst contains at least one rare earth element selected from the group consisting of yttrium, cerium, lanthanum, praseodymium, neodymium, and holmium, at least one alkali metal selected from the group consisting of sodium, potassium, rubidium, and cesium, at least one alkaline earth metal selected from the group consisting of beryllium, magnesium, calcium, strontium, and barium, and copper.
• the auxiliary catalyst contains at least one rare earth element selected from the group consisting of yttrium, cerium, lanthanum, praseodymium, neodymium, and holmium, at least one alkali metal selected from the group consisting of sodium, potassium, rubidium, and cesium, at least one alkaline earth metal selected from the group consisting of beryll
• yttrium, cerium, lanthanum, praseodymium, neodymium, holmium, and copper are preferred, yttrium, cerium, lanthanum, praseodymium, neodymium, and holmium are more preferred, and yttrium is the most preferred. It is believed that the addition of the auxiliary catalyst increases the amount of carbon monoxide and carbon dioxide adsorbed on the catalyst surface, and also increases the number of reaction active sites.
• auxiliary catalyst is preferably 1/30 to 1/3 of the weight of the main catalyst (such as cobalt), and more preferably 1/20 to 1/5.
• the support 13 supports the main catalyst 11 and the auxiliary catalyst 12 .
• a carrier containing at least one of silica (SiO 2 ), alumina (Al 2 O 3 ), and zeolite (aluminosilicate) is used.
• silica is chemically stable and therefore does not affect the main catalyst or auxiliary catalyst. This allows the chemical properties of the main catalyst and auxiliary catalyst to be fully exhibited.
• the specific surface area is large, the contact efficiency with the raw material gas (substrate) is high, and the FT reaction can be efficiently carried out.
• the medium oil 14 is a liquid medium for suspending the catalyst and filling the reaction vessel for the gas-liquid contact reaction.
• liquid hydrocarbons are used as the medium oil 14, and it is preferable to use paraffin-based liquid hydrocarbons having 10 to 20 carbon atoms. A fine powder catalyst, which will be described later, is suspended in this.
• the liquid hydrocarbons filled at the beginning of the reaction are replaced by liquid hydrocarbons, which are the product, as the reaction progresses.
• the raw synthesis gas 40 serves as a raw material for producing hydrocarbons by the FT reaction.
• the feed gas for a normal FT reaction consists of hydrogen (H 2 ) and carbon monoxide (CO), but in the present invention, carbon dioxide (CO 2 ) is contained in the feed gas 4. Since the rate of the FT reaction depends on the hydrogen partial pressure, a certain degree of H2 partial pressure is necessary, and the partial pressure ratio (molar ratio) of hydrogen to the total of (carbon monoxide + carbon dioxide) in the feed gas of the present invention is appropriately 0.6 to 2.7, preferably 0.8 to 2.5, and more preferably 1 to 2.3.
• the ratio of carbon monoxide to carbon dioxide can be varied depending on the purpose, and the ratio of carbon dioxide is increased for the purpose of carbon recycling, and the ratio of carbon monoxide is increased to increase the conversion rate to hydrocarbons.
• the ratio of carbon dioxide to carbon monoxide is not particularly limited, but the proportion of carbon dioxide to the total amount of carbon monoxide and carbon dioxide must be 1 volume % or more. It is preferably 10% or more, more preferably 30% or more, and even more preferably 40% or more.
• Other components such as sulfur, organic nitrogen, and phosphorus are obviously harmful, but as long as they do not interfere with the reaction, there is no problem if substances other than the main components mentioned above are mixed in.
• the hydrocarbon fraction 30 is a hydrocarbon fraction having a wide range of distribution produced by the FT synthesis reaction, and contains not only paraffins but also olefins and the like.
• the product gas 31 is a hydrocarbon fraction 30 that has a relatively low boiling point and a low carbon number, for example, C1 to C4 hydrocarbons, specifically, methane, ethane, ethylene, propane, propylene, butane, butene, etc.
• the product liquid 32 is a hydrocarbon fraction 30 that has a relatively high boiling point and a high carbon number, and is, for example, a middle fraction such as a heavy naphtha fraction (crude gasoline), kerosene, or diesel.
• a middle fraction such as a heavy naphtha fraction (crude gasoline), kerosene, or diesel.
• the reaction vessel 40 is a pressure-resistant vessel for use in a gas-liquid contact reaction, and is intended to be filled with an oil medium 14 in which a catalyst 10 is suspended, and to cause the reaction to proceed at the gas-liquid interface by blowing in a raw synthesis gas 20 from the bottom.
• a liquid hydrocarbon oil medium 14 in which a fine powder catalyst 10 is suspended is used as the liquid, and the raw synthesis gas 20 is blown in the form of fine bubbles from the bottom of the reactor to aerate the reaction.
• the reaction vessel 40 also includes a heat exchanger 50 that controls the reaction temperature in the FT reaction within the reaction vessel 40, a raw synthesis gas supply pipe L1 that introduces the raw synthesis gas 20, a product gas extraction pipe L2 that removes the gas produced by the FT reaction from the reaction vessel 40, and a product liquid extraction pipe L3 that removes the liquid produced by the FT reaction from the reaction vessel 40.
• the reaction vessel 40 There are no particular limitations on the shape, capacity, and material of the reaction vessel 40. Chain growth in the FT reaction is pressure dependent. In the present invention, the reaction is carried out under conditions of normal pressure to 1000 kPa, preferably 100 kPa to 900 kPa, more preferably 200 kPa to 800 kPa, and even more preferably 400 kPa to 800 kPa. Moreover, the capacity of the reaction vessel 40 is preferably 1000 L or less. By making the capacity of the reaction vessel 40 1000 L or less, the entire FT synthesis reaction apparatus 100 can be made compact, and space can be saved.
• a gas disperser 41 for dispersing the raw synthesis gas 20 into fine bubbles may be installed at the bottom of the reaction vessel 40. This makes it possible to increase the contact area between the catalyst 10 and the raw synthesis gas 20, thereby enabling the FT reaction to be carried out more efficiently.
• the raw synthesis gas supply pipe L1 is a line that supplies the raw synthesis gas 20 into the reaction vessel 40.
• the raw synthesis gas supply pipe L1 may be any type as long as it can supply the raw synthesis gas 20 into the reaction vessel 40.
• the raw synthesis gas supply pipe L1 is provided at the bottom of the reaction vessel 40 so as to communicate with the reaction vessel 40. This allows the raw synthesis gas 20, which has a lighter specific gravity than the medium oil 14 in which the catalyst 10 is suspended, to rise in the reaction vessel 40 as raw synthesis gas bubbles 21. Therefore, the raw synthesis gas 20 can be brought into contact with the medium oil 14 in which the catalyst 10 is suspended over a wide area, making it possible to perform an efficient FT reaction.
• the product gas extraction pipe L2 is a line for extracting the product gas generated by the FT reaction described later from inside the reaction vessel 40.
• the product gas extraction pipe L2 is in communication with the inside of the reaction vessel 40, and is used to extract gaseous components such as light gas or volatile oil fractions from the products generated by the FT reaction and the hydrocarbons generated by the FT reaction from inside the reaction vessel 40.
• the product gas extraction pipe L2 may be of any type as long as it can extract the product gas. It is preferable that the product gas extraction pipe L2 is provided in the upper part of the reaction vessel 40 so as to be in communication with the reaction vessel 40 as shown in FIG. 1. This makes it possible to efficiently extract the product gas having a relatively low boiling point outside the reaction vessel 40. The extracted product gas is separated and purified as appropriate.
• the product liquid extraction pipe L3 is a line for extracting the product liquid generated by the FT reaction described later from inside the reaction vessel 40.
• the product liquid extraction pipe L3 is in communication with the inside of the reaction vessel 40, and is used to extract liquid components such as light kerosene or wax components having a large number of chain carbon atoms generated by the FT reaction from inside the reaction vessel 40 among the products generated by the FT reaction.
• the product liquid extraction pipe L3 may be of any type as long as it can extract the product liquid. It is preferable that the product liquid extraction pipe L3 is provided in the middle of the reaction vessel 40 so as to communicate with the reaction vessel 40 as shown in FIG. 1. This makes it possible to efficiently extract the product liquid having a relatively high boiling point outside the reaction vessel 40.
• the product liquid is also appropriately fractionated and refined.
• the heat exchange section 50 is intended to maintain the temperature inside the reaction vessel 40 within a predetermined range.
• the heat exchange unit 50 is configured by closely stacking a number of heat exchange plates 51 each having an uneven shape with recesses 52.
• the heat exchange unit 50 also includes a cooling medium inlet pipe L4 for introducing a cooling medium into the heat exchange unit 50, and a heating steam outlet pipe L5 for guiding heating steam from the heat exchange unit 50.
• the existing FT reactor 200 uses a tubular or coiled cooling tube as the heat exchanger 60.
• the heat exchange medium introduced from the bottom of the reactor passes through the cooling tube of the heat exchanger 60 and is turned into heated steam from the top and discharged from the system.
• the heat exchanger 60 uses a plurality of cooling tubes that converge, there is a problem that sludge adheres between the tubes and the desired performance cannot be achieved. In addition, a lot of effort is required for maintenance such as scaling.
• the heat exchange section 50 is a plate-shaped heat exchange plate 51, so that sludge is less likely to adhere to the heat exchange section 50 than in the existing FT reaction apparatus 200, which uses a heat exchange section in which multiple cooling pipes are converged.
• the structure of the heat exchange section is simple, maintenance such as cleaning is also easy.
• the heat exchange unit 50 of the present invention is characterized by having a plurality of heat exchange plates 51 having recesses 52 on the surface, resulting in an uneven shape. This makes it possible to increase the heat transfer surface area, and the reaction temperature using the catalyst 10 in the reaction vessel 40 can be maintained within a predetermined range.
• reaction temperature The FT reaction is generally carried out at a temperature ranging from about 150°C to 300°C.
• the reaction temperature of the catalyst 10 is less than 200°C, the conversion rate of CO and CO2 in the FT reaction tends to decrease, and if it is 270°C or higher, the product distribution becomes lighter, and the yield of middle distillates may decrease. Therefore, by setting the reaction temperature of the catalyst 10 of the present invention to the range of 200° C. to 270° C., carbon dioxide can be efficiently converted into liquid hydrocarbons. More preferably, the reaction temperature of the catalyst 10 is set in the range of 220° C. to 250° C.
• reaction temperature By keeping the reaction temperature in this range, it is possible to maximize the capacity of the catalyst 10, and carbon dioxide can be converted into liquid hydrocarbons more efficiently.
• the reaction temperature if the reaction temperature is below this range, the wax content in the product increases, and a step for removing the wax (de-waxing) becomes necessary, which is not preferable because the process configuration becomes complicated.
• the reaction temperature exceeds this range, it is considered that the gas fraction such as LPG and methane tends to increase. Therefore, if gas such as LPG and methane increases in the unreacted raw material gas (synthesis gas and carbon dioxide), the partial pressure of the unreacted raw material gas may decrease significantly, which is not preferable.
• the heat exchange medium introduction pipe L4 introduces a heat exchange medium into the heat exchange section 50.
• the heat exchange medium is a gas or liquid medium introduced for the purpose of keeping the temperature inside the reaction vessel 40 within a predetermined range in order to perform an efficient FT reaction.
• the temperature inside the reaction vessel 40 needs to be raised to a temperature required for the FT reaction to occur.
• a high-temperature medium such as heated steam is introduced as a heat exchange medium through the heat exchange medium introduction pipe L4, and the temperature inside the reaction vessel 40 is raised to a temperature required for the FT reaction.
• the heat exchange medium discharge pipe L5 discharges the heat exchange medium introduced from inside the reaction vessel 40 to the heat exchange section 50 to the outside of the heat exchange section 50.
• the discharged heat exchange medium may be cooled or heated again and introduced again into the heat exchange section 50 through the heat exchange medium introduction pipe L4.
• the reaction vessel 40 is filled with the medium oil 14 in which the catalyst 10 is suspended.
• the raw synthesis gas 20 is introduced into the reaction vessel 40 from the raw synthesis gas inlet pipe L1.
• the raw synthesis gas 20 is dispersed into minute bubbles by the gas disperser 41, and the raw synthesis gas bubbles 21 spread evenly throughout the medium oil 14 in which the catalyst 10 is suspended, which has been filled into the reaction vessel 40, and rise within the reaction vessel 40.
• a high-temperature heat exchange medium such as heated steam is introduced from the heat exchange medium introduction pipe L4 into the heat exchange section 50.
• the heat exchange plates 51 which have an uneven shape due to the recesses 52 and thus have an increased heat transfer surface area, can efficiently heat the medium oil 14 in which the catalyst 10 is suspended, and the temperature inside the reaction vessel 40 can be increased to a temperature required for the FT reaction.
• product gas and product liquid are produced.
• the product gas is constantly removed from the top of the reaction vessel 40 to the outside of the reaction vessel 40 through the product gas removal pipe L2
• the product liquid is constantly removed from the middle of the reaction vessel 40 to the outside of the reaction vessel 40 through the product liquid removal pipe L3.
• a low-temperature heat exchange medium such as cooling water is introduced into the heat exchange section 50 through the heat exchange medium inlet pipe L4.
• the multiple heat exchange plates 51 which have an uneven shape due to the recesses 52 and therefore an increased heat transfer surface area, can efficiently cool the medium oil 14 in which the catalyst 10 is suspended, and lower the temperature inside the reaction vessel 40 to the temperature required for the FT reaction.
• the heat exchange medium such as cooling water heated inside the heat exchange section 50 is then led out of the reaction vessel 40 through the heat exchange medium outlet pipe L5.
• the above-mentioned embodiment shows an example of an FT reaction apparatus and an FT reaction method.
• the FT reaction apparatus and the FT reaction method according to the present invention are not limited to the above-mentioned embodiment, and the FT reaction apparatus and the FT reaction method according to the above-mentioned embodiment may be modified within the scope of the gist of the claims.
• a heat exchange medium such as heated or cooled cooling water led out from the heat exchange medium lead-out pipe L5 may be used for heating or cooling another FT reactor 100. This makes it possible to operate a plurality of FT reaction devices 100 in an energy-saving manner.
• the FT synthesis reaction apparatus and FT synthesis reaction method of the present invention can be used to produce a hydrocarbon mixture from a raw material gas that includes carbon dioxide.

Landscapes

• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Engineering & Computer Science (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Chemical Kinetics & Catalysis (AREA)
• General Chemical & Material Sciences (AREA)
• Materials Engineering (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Priority Applications (1)

Applications Claiming Priority (2)

Publications (1)

Family

ID=91195678

Family Applications (1)

Country Status (2)

Citations (4)

• 2023
  • 2023-11-20 JP JP2024560150A patent/JPWO2024111562A1/ja active Pending
  • 2023-11-20 WO PCT/JP2023/041691 patent/WO2024111562A1/ja not_active Ceased

Patent Citations (4)

Also Published As

Similar Documents

Legal Events