JP5886443B2 - Syngas production method and apparatus - Google Patents

Description

  The present invention relates to a method and apparatus for producing synthesis gas from hydrocarbons and water.

  An important part of the global economy is based on crude oil as a raw material or energy source. Otto diesel fuel for personal and goods transport, heavy oil as marine and electric plant fuel and light oil for domestic heating are therefore produced from crude oil. Also, many raw materials for the chemical industry are derived directly or indirectly from crude oil. Currently, great efforts are being made to substitute products made from crude oil with other raw materials or other processes. In the energy field, natural gas and renewable energy are used in place of crude oil in the operation of power plants. Although electric engines, natural gas engines and hydrogen fuel cells have been tested for transportation applications, they have not been established commercially.

Attempts have been made to produce fat products from natural gas or coal on an industrial scale. For example, a process for converting natural gas to liquid fuel is known (so-called gas liquefaction process or GTL process). Nevertheless, these processes generally involve a significant amount of CO ₂ emissions and are associated with high costs. In addition, these processes are generally not able to provide independently hydrogen and CO or CO _2. These attempts are therefore limited to some isolated applications for economic and ecological reasons.

Synthesis gas, or syngas for short, is a gaseous mixture of carbon monoxide and hydrogen that can also contain carbon dioxide. For example, the synthesis gas is generated by gasifying a carbon-containing fuel into a gaseous product having a predetermined calorific value, that is, synthesis gas. Syngas is about 50% of the energy density of natural gas. Syngas is combustible and can therefore be used as a fuel source. Syngas can also be used as an intermediate in the production of other chemical products. For example, syngas can be generated by coal or waste gasification. During the production of synthesis gas, carbon can react with water and hydrocarbons can react with oxygen. There are commercially available technologies for treating synthesis gas to produce industrial gases, fertilizers, chemical products and other chemical products. However, the best known techniques for syngas production and conversion (eg, aqueous shift reactions) generate larger amounts of extra CO ₂ by synthesizing the required amount of hydrogen, which CO ₂ There is a problem that it is finally released into the atmosphere as a gas that adversely affects the climate. Partial oxidation of methane by the reaction formula 2CH ₄ + O ₂ → 2CO + 4H ₂ , which is another known technique for producing synthesis gas, can reach a maximum ratio of H ₂ and CO of 2.0. . However, the disadvantage is the use of pure oxygen, a powerful energy.
European Patent Publication No. EP0219163A discloses a method for producing synthesis gas in which hydrocarbons are decomposed in a first reaction chamber to produce carbon and hydrogen, and the carbon is transported to the second reaction chamber and contacted with water.
International Publication No. WO 00/06671 A1 converts a biological material into waste gas such as carbon and water vapor or CO _{2 in} the presence of air in a first reaction chamber, and synthesis gas is converted from the carbon and water vapor in a second reaction chamber. A method for producing the produced synthesis gas is disclosed.

Therefore, the first problem to be solved by the present invention is to convert a hydrocarbon-containing fluid into a synthesis gas having a variable hydrogen content without generating large amounts of CO ₂ .

The above problems are solved by the method according to claims 1, 2 and 13 and the device according to claims 17, 18 and 26 . Embodiments also derive from the dependent claims.

In particular, the synthesis gas production method comprises at least partially decomposing a hydrocarbon-containing fluid into carbon and hydrogen by introduction of energy provided by heat, the carbon and hydrogen having a temperature of at least 200 ° C. after the decomposition step. . A portion of the carbon generated by the cracking process comes into contact with water at a temperature between 800 ° C. and 1700 ° C. When the carbon comes into contact with water after the cracking process, the carbon produced by the cracking process has a temperature of 50 Cool only at a temperature (° C) of less than Here, at least a portion of the water is converted into synthesis gas along with the carbon produced by the cracking process. By this method, it is possible to convert a carbon-containing fluid into a synthesis gas having a variable hydrogen content without generating a significant amount of CO ₂ . In an advantageous manner, at least part of the energy necessary to obtain carbon (by cracking hydrocarbons) is introduced in the form of heat for conversion. In addition, hydrogen and various different forms of carbon can be produced as by-products.

  If the cracking process occurs at a temperature of 1000 ° C. or higher and the carbon is in contact with water at a temperature of at least 1000 ° C., particularly at a temperature of 1000 ° C. to 1200 ° C., the additional heat provided for the conversion It is not necessary or only requires a little additional heat. Preferably, the heat required to reach a temperature of 800 ° C. to 1700 ° C. (especially 1000 ° C. to 1200 ° C.) for conversion is essentially dependent on the heat used for the cracking of the hydrocarbon-containing fluid, and Provided completely. Here, basic and complete means that at least 80%, in particular at least 90%, of the required heat comes from the decomposition process.

  In one embodiment, the carbon obtained from the cracking process and the hydrogen obtained from the cracking process are both in contact with water. Hydrogen does not affect the conversion and can function as an additional heat transfer material. This is particularly advantageous when the carbon and hydrogen have a temperature of 1000 ° C. (preferred conversion temperature) or higher. In this case, the gas after conversion is not pure water gas but syngas having a different mixing ratio.

  Further, the carbon obtained in the decomposition step can be separated from the hydrogen obtained in the decomposition step before the step of bringing the carbon into contact with water.

  To increase the energy efficiency of this method, at least a portion of the carbon and / or at least a portion of the heat obtained from the cracking step heats the water prior to contacting the water with the carbon. And / or can be used to heat a process chamber in which water is in contact with carbon. In this sense, after conversion, the synthesis gas has a temperature of 800 ° C. to 1700 ° C. and at least part of the heat of the synthesis gas is used to preheat the water before the step of contacting the water with carbon. It should be noted that it is possible to do. At least a portion of the heat and / or a portion of the heat of the carbon obtained in the cracking step and / or a portion of the converted synthesis gas may be used as energy for the cracking of the hydrocarbon-containing fluid. It can also be used to generate electricity that can be used as an energy carrier for introduction.

  Preferably, the energy for cracking the hydrocarbons is introduced mainly via plasma. This is a particularly direct and efficient way to introduce energy. Preferably, the cracking step is carried out in a Kburner reactor capable of continuously cracking the hydrocarbon stream.

In the method for generating synthesis gas, additional hydrogen and / or carbon monoxide and / or another synthesis gas can be added to the synthesis gas to obtain the desired composition. When contacting both carbon and hydrogen with water, it is particularly effective to add additional carbon monoxide to the synthesis gas to reduce the CO / H ₂ ratio. During the process for contacting essentially pure carbon with water, it is useful to add additional carbon monoxide to increase the CO / H ₂ ratio. In particular, in order to obtain the desired mixing ratio of CO / H ₂ , the two syngas generated separately by the above-described methods (method of performing pre-separation of carbon and hydrogen, method of not performing pre-separation of carbon and hydrogen) It is possible to mix the streams.

Preferably, additional hydrogen is generated from the step of cracking the hydrocarbon-containing fluid into carbon and hydrogen by introduction of energy at least partly by heat. Therefore, the decomposition process can provide the necessary carbon and the necessary hydrogen for C · H ₂ O conversion in one step. In one embodiment, at least a portion of the hydrogen is generated by the process of decomposing the carbon-containing fluid with a microwave plasma at a temperature of 1000 ° C. or less, particularly 600 ° C. or less.

If additional hydrogen (more hydrogen than is obtained by the production of carbon required for C · H ₂ O conversion) is needed to obtain a specific mixing ratio of the synthesis gas, it can be It is preferable to generate the hydrogen having high energy efficiency. Preferably, the ratio of CO to hydrogen (CO: H ₂ ) in the synthesis gas is adjusted to a value between 1: 1 and 1: 3, in particular a value of 1: 2.1.

  In the method for producing a synthetic hydrocarbon having a functional group and / or having no functional group, in the first step, as described above, a synthesis gas is produced, and the synthesis gas has a functional group and / or a functional group. The synthesis gas is contacted with a suitable catalyst for conversion to a synthetic hydrocarbon free of benzene. Here, the temperature of the catalyst and / or the synthesis gas is set or adjusted within a predetermined temperature range. In this way, it is possible to generate synthesis gas by mixing CO with hydrogen before or when contacting the synthesis gas with the catalyst.

  In one embodiment, the synthesis gas conversion is performed by a Fischer-Tropsch process, in particular an SMDS process. Also, the synthesis gas can be converted by a Bergius-Pier process, a peer process, or a combination of a peer process and an MtL process. It is the process choice that largely determines the nature of the synthetic hydrocarbons with and / or without functional groups.

  Preferably, the hydrocarbon-containing fluid to be cracked is natural gas, methane, wet gas, heavy oil or a gas mixture thereof.

  The syngas generator comprises a hydrocarbon converter that decomposes the hydrocarbon-containing fluid into carbon and hydrogen, the hydrocarbon converter having at least one inlet for the hydrocarbon-containing fluid and at least one outlet for carbon and / or hydrogen. At least one process chamber and at least one unit for introducing at least partly heat energy into the process chamber. The apparatus also comprises a C converter for water and carbon conversion, the C converter having at least one additional process having at least one inlet for water, at least one inlet for at least carbon and at least one outlet. And at least a carbon inlet is directly connected to at least one outlet of the hydrocarbon converter. Here, the term “directly connected” means that the carbon discharged from the hydrocarbon converter on the way to the C converter without using any additional energy to heat the carbon, It means that 50% or more of (° C.) is not cooled, and the temperature is preferably lowered by a temperature (° C.) of 20% or less. A separation unit for separating carbon from hydrogen can be provided between the location of the cracking step and at least one outlet of the hydrocarbon converter. This unit can form part of the hydrocarbon converter or it can be located outside the hydrocarbon converter as a separation unit. The separation unit between the outlet of the hydrocarbon converter and the inlet of the C converter does not interfere with the direct connection as long as the above conditions are met.

  Preferably, at least one unit for introducing energy into the process chamber is configured such that the unit can at least locally generate a temperature of 1000 ° C. or higher, in particular 1500 ° C. or higher. Yes. In one embodiment, at least one unit for introducing energy into the process chamber is a plasma unit. In particular, when the decomposition temperature is maintained at 1000 ° C. or lower, at least one unit for introducing energy into the process chamber comprises a microwave plasma unit.

  For a particularly simple embodiment of the device, the C converter process chamber is formed by a hydrocarbon converter outlet pipe connected to a water supply pipe.

  In one embodiment of the invention, a separation unit for separating carbon and hydrogen generated by cracking is provided near the hydrocarbon converter, and a separate outlet from the separation unit is for the separated material. The outlet for carbon is connected to the C converter.

  Preferably, the hydrocarbon converter is a Kuberner reactor that can provide the temperature necessary to continuously decompose the carbon-containing fluid over a long period of operation.

  The apparatus provides at least one for supplying hydrogen and / or carbon and / or separated synthesis gas to the C converter or downstream mixing chamber for simple and efficient production of synthesis gas having a variable mixing ratio. It is possible to provide two separate supply pipes.

  In one embodiment, the apparatus for syngas production comprises at least one additional hydrocarbon converter that decomposes the hydrocarbon-containing fluid into carbon and hydrogen. The at least one additional hydrocarbon converter also includes at least one process chamber having at least one inlet for the hydrocarbon-containing fluid and at least one for introducing energy comprising at least partially heat into the process chamber. One unit and a separation unit that separates carbon and hydrogen obtained by cracking, the separation unit has separate outlets for carbon and hydrogen, and the outlet for hydrogen is connected to a separation supply pipe for hydrogen Has been. For energy efficiency reasons, the at least one additional hydrocarbon converter is preferably of the type that decomposes at a temperature of 1000 ° C. or less, in particular 600 ° C. or less, by microwave plasma.

  An apparatus for converting a synthesis gas into a hydrocarbon having a functional group and / or having no functional group includes an apparatus for generating the specific type of synthesis gas and a CO converter. The CO converter includes a process chamber equipped with a catalyst, means for bringing synthesis gas into contact with the catalyst, and a control unit for controlling or adjusting the temperature of the catalyst and / or synthesis gas to a predetermined temperature. Thus, the part of the apparatus for generating synthesis gas can be incorporated into a CO converter, for example a mixing chamber for CO and additional hydrogen, carbon and / or another synthesis gas. In one embodiment, the CO converter comprises a Fischer-Tropsch converter, in particular an SMDS converter. The CO converter includes a Bergius-Peer converter, a peer converter, or a combination of a peer converter and an MtL converter. It is also possible that several CO converters of the same type or of different types are included in the device.

  Preferably, the apparatus comprises a control unit that controls or regulates the pressure of the synthesis gas in the CO converter.

  Hereinafter, the present invention will be described in detail with reference to embodiments and drawings.

FIG. 1 is a schematic view of a plant for syngas production. FIG. 2 is a schematic diagram of another plant for syngas production. FIG. 3 is a schematic view of a plant for the production of hydrocarbons with and / or without functional groups. FIG. 4 is a schematic diagram of another plant for the production of hydrocarbons with and / or without functional groups according to another embodiment. FIG. 5 is a schematic view of a plant for producing hydrocarbons with and / or without functional groups according to another embodiment. FIG. 6 is a schematic view of a plant for producing hydrocarbons with and / or without functional groups according to another embodiment. FIG. 7 is a schematic view of a plant for syngas production according to another embodiment. FIG. 8 is a schematic view of a plant for producing hydrocarbons with and / or without functional groups according to another embodiment.

  In the following description, terms such as top, bottom, right and left, and similar terms, relate to the direction and arrangement shown in the drawings, and are meant only for the description of the embodiments. It should be noted. These terms indicate preferred correspondence, but are not limiting. In the different drawings, the same reference numerals are used to describe the same or similar parts.

  In the following specification, methods and apparatus for handling “hot” materials or performing “hot” processes are described. In this detailed description, the phrase “hot” means a temperature of 200 ° C. or higher, preferably 300 ° C. or higher.

  The synthesis gas may be any gas mainly composed of carbon monoxide and hydrogen. A gas (synthetic gas) consisting of carbon monoxide and hydrogen in an approximately equal amount (1: 1) is called water gas. As used herein, the phrase “syngas” includes water gas as a particular mixture of syngas.

  FIG. 1 shows a plant 1 that produces synthesis gas. FIG. 1 also demonstrates the basic production process for synthesis gas production according to this detailed description.

  The plant 1 for producing synthesis gas comprises a hydrocarbon converter 3 having a hydrocarbon inlet 4 and a first carbon outlet 5, an optional hydrogen outlet 6 and an optional second carbon outlet 7. The plant 1 for generating synthesis gas includes a C converter 9 having a water inlet 10, a carbon outlet 11 (also referred to as a C inlet), and a synthesis gas outlet 12. The hydrocarbon converter 3 and the C converter 9 are arranged so that the carbon outlet 5 of the hydrocarbon converter 3 is connected to the carbon inlet 11 of the C converter 9 via the direct connection portion 8, and the outlet 5 is connected to the C converter 9. The carbon inlet 11 is directly formed. In this way, it is possible to transport carbon directly from the hydrocarbon converter 3 to the C converter 9.

  The hydrocarbon converter 3 may be any converter as long as it can convert or decompose the introduced hydrocarbon into carbon and hydrogen. The hydrocarbon converter 3 comprises a process chamber with an inlet for a hydrocarbon-containing fluid, at least one unit for introducing cracking energy into the fluid, and at least one outlet. The decomposition energy is provided at least in part by heat provided by, for example, plasma. Nevertheless, the decomposition energy can also be provided by other means, and if the decomposition is mainly caused by heat, the fluid should be heated above 1000 ° C, especially at temperatures above 1500 ° C. Should be heated.

  In the described embodiment, a Kuburner reactor is used, which provides the required heat by a plasma arc. However, other reactors are known which operate at lower temperatures, in particular below 1000 ° C., and introduce additional energy into the hydrocarbon in addition to heat, for example by microwave plasma. As described further below, the present invention contemplates both types of reactors (including reactors that operate without plasma), and particularly contemplates the combined use of both types of reactors. Hydrocarbon converters that operate at temperatures above 1000 ° C. are referred to as high temperature reactors, whereas converters that operate at temperatures below 1000 ° C., particularly temperatures from 200 ° C. to 1000 ° C., are referred to as low temperature reactors.

Within the hydrocarbon converter, hydrocarbons (C _n H _m ) are broken down into hydrogen and carbon by heat and / or plasma. The hydrocarbon is preferably introduced into the reactor as a gas. In standard conditions, liquid hydrocarbons can be vaporized prior to introduction into the reactor, or the hydrocarbons can be introduced as microdroplets. Both forms are designated as fluids below.

  Hydrocarbon decomposition should be done in the absence of oxygen if possible to suppress the formation of carbon oxides or water. Nevertheless, the small amount of oxygen that can be introduced with the hydrocarbons does not harm the process.

  The above-described Kuburner reactor decomposes a hydrocarbon-containing fluid at high temperatures into pure carbon (eg, activated carbon, carbon black, graphite, industrial soot) and hydrogen, and possibly impurities, in a plasma combustor. The hydrocarbon-containing fluid used as starting material for the hydrocarbon converter 3 is, for example, methane, natural gas, biogas, wet gas or heavy oil. However, hydrocarbons with synthetic functional groups and / or no functional groups can also be used as starting materials for the hydrocarbon converter 3. After the initial decomposition step, the elements are usually present as a mixture, in particular in the form of an aerosol. This mixture can be introduced into another process in this manner, as described below, or the mixture can be separated into individual elements in a separation unit (not shown). Although the separation unit is configured as a separate unit, in the present patent application such a separation unit is considered as part of the hydrocarbon converter 3. If no separation unit is provided, the carbon outlet 5 is the only outlet of the hydrocarbon converter 3 and directs the carbon and hydrogen mixture (aerosol) directly to the C converter 9. In the case of providing a separation unit, it is possible to introduce carbon that is at least partially separated from hydrogen into the C converter 9 using the carbon outlet 5. The separated hydrogen, and optionally additional carbon, can be discharged through optional outlets 6 and 7.

The C converter 9 may be any C converter as long as it can generate synthesis gas from carbon (C) and water (H ₂ O). In the embodiment of FIG. 1, within the C converter 9 H ₂ O passes over carbon or water vapor is introduced into the carbon and hydrogen stream and mixed with the stream, thereby the chemical formula C + H It is converted as ₂ O → CO + H ₂ .
Within the C converter 9 the following reaction takes place:
C + H ₂ O → CO + H ₂ + 131.38 kJ / mol endothermic reaction CO + H ₂ O → CO ₂ + H ₂ −41.19 kJ / mol The following reaction takes place in an exothermic reaction Budoir equilibrium:
2C + O ₂ → 2CO + 172.58 kJ / mol endothermic reaction

Since all three reactions are in equilibrium with each other, the process in C converter 9 preferably occurs at a high temperature of 800 ° C. to 1700 ° C., more preferably at a high temperature of 1000 ° C. to 1200 ° C. This is because the second reaction is dominant at low temperatures. The heat required to reach the temperature is mainly provided by the material originating from the hydrocarbon converter 3. This point will be described in detail below. Under these conditions, water (H ₂ O) in the C converter 9 is steam, and water can already be introduced as steam. The water supply during operation is controlled to avoid multiples of excess water to avoid strong cooling. When excessive cooling is performed in the C converter 9, the reaction 2 is dominant.

C-converter 9 operates at a high temperature of 1000 ° C. to 1200 ° C. to suppress the exothermic water shift reaction CO + H ₂ O → CO ₂ + H ₂ and optimize the proportion of carbon monoxide in the synthesis gas Is the best. The reaction in the C converter 9 is known to those skilled in the art and is therefore not further described here.

The operation of the plant 1 for generating synthesis gas is described below with reference to FIG. In the following, it is assumed that the hydrocarbon converter 3 is a Kuburner type high temperature reactor. A hydrocarbon-containing fluid (particularly gaseous) is introduced into the hydrocarbon converter 3 via a hydrocarbon inlet 4. When the hydrocarbon is, for example, methane (CH ₄ ), 1 mol of carbon and 2 mol of hydrogen are generated from 1 mol of methane. The hydrocarbons are converted in the plasma torch of the hydrocarbon converter 3 at about 1600 ° C. according to the following reaction formula: Here, the introduced energy is heat generated in the plasma by electric energy.
C _n H _m + energy → nC + m / 2H ₂

  With proper process control, the Kuburner reactor can convert nearly 100% of hydrocarbons to their constituents in continuous operation.

  In the following, it is considered that carbon and hydrogen are separated in the hydrocarbon converter 3 and most are discharged in a separated state. However, carbon and hydrogen can be discharged as a mixture and introduced into the C converter 9 without being separated. Hydrogen does not interfere with the conversion process within the C converter 9 and functions as an additional heat transfer material. The carbon is at least partially introduced directly from the carbon outlet 5 to the carbon inlet 11 of the C converter 9. Leading directly from the outlet 5 of the hydrocarbon converter 3 to the carbon inlet 11 of the C converter 9 means that all the deformations in which the temperature of the introduced material is not subject to cooling of more than 50% (preferably more than 20%). Is included. Since the carbon discharged from the hydrocarbon converter 3 is at a high temperature, preferably 1000 ° C. or higher, the heat energy possessed by the carbon is, for example, the temperature required for the conversion process in the C converter 9 operating at a temperature of about 1000 ° C. Can be used to maintain

  The connection 8 connecting the hydrocarbon converter 3 and the C converter 9 is designed so that the carbon is not cooled very much during the passage from the hydrocarbon converter 3 to the C converter 9 (50% or less, preferably 20% or less with respect to temperature). Has been. For example, the connection 8 is specially insulated and / or actively heated, and the device is preferably not supplied with additional heat, i.e. additional heat is added in addition to heat introduction in the hydrocarbon converter 3. It is never supplied. Due to the operating temperature in the hydrocarbon converter 3, the hydrogen generated in the hydrocarbon converter 3 also has thermal energy. Therefore, one possibility to heat the connection 8 is to use a hydrogen to directly or indirectly heat the connection 8 between the hydrocarbon converter 3 and the C converter 9 via the heat exchanger unit. The heat energy of hydrogen discharged from the outlet 6 is used.

In the C converter, water introduced through the water inlet 10 of the C converter 9, in particular water introduced in the form of steam, is led onto and / or mixed with hot carbon. C converters are best operated at high temperatures. This is because the reaction in the C converter 9 is an endothermic reaction, whereas the aqueous shift reaction is an exothermic reaction. It is known to those skilled in the art that the reaction depends on pressure and temperature, and therefore will not be described in detail. The amount of water or carbon introduced into the C-converter 9 can both be controlled (open loop) and / or adjustable (closed loop) by suitable means.
_{C + H 2 O → CO +} H 2; ΔH = + 131.38kJ / mol

  Also here, the boudoir equilibrium is a limited factor. This is because the mixture is substantially composed of carbon monoxide and hydrogen at a temperature of 1000 ° C. or higher and no excess water is present. Since the C converter 9 preferably operates at a temperature> 1000 ° C., it is advantageous to preheat water introduced into the water inlet 10 of the C converter 9. For example, water preheating can be performed directly or indirectly using heat energy contained in hot hydrogen via a heat exchanger unit. Preferably, the heat contained in the carbon is sufficient to heat the water to the desired temperature. Optional additional heating to heat the C converter 9 or elements contained within the C converter only if the heat generated in the hydrocarbon converter 3 is not sufficient to reach the desired conversion temperature of about 1000 ° C. Units can be provided. Such a unit can also be provided as a preheating unit near the supply line for water or carbon. Such a unit can only be provided for the start-up phase of the plant in order to bring the C converter 9 or the part containing the plant medium to the starting temperature so that the device can reach the desired temperature state sooner. It is. It may initially take a long time to exclusively heat the part containing all the media via the heat generated in the hydrocarbon converter 3.

Hot synthesis gas (CO + H ₂ ) is discharged from the C converter 9 at a temperature higher than 1000 ° C. (depending on the operating temperature of the C converter 9). The synthesis gas discharged from the C converter 9 can be used to preheat water introduced into the water inlet 10 directly or indirectly via a heat exchanger unit (not shown in FIG. 1). Has some thermal energy. With suitable operating parameters, ie temperatures between 1000 ° C. and 1200 ° C. (and the separation of hydrogen and carbon in the hydrocarbon converter 3), synthesis gas is produced and CO and H ₂ in the synthesis gas have a 1: 1 ratio. This synthesis gas is called water gas. If the hydrocarbon converter 3 does not separate hydrogen and carbon and does not have appropriate operating parameters in the C converter 9 respectively, i.e. not adjusted to a temperature of 1000 ° C. to 1200 ° C., the CO / A synthesis gas having an H ₂ ratio is produced.

As described above, the hydrocarbon converter 3 can include a second carbon outlet 7 for discharging carbon. The carbon produced by the hydrocarbon converter 3 is discharged at different rates via the first carbon outlet 5 and the second carbon outlet 7 after the separation of each of C and H ₂ (or as a C—H ₂ mixture). Is possible. The second carbon outlet 7 is used to discharge a part of the generated carbon that is not used by the C converter 9 to generate synthesis gas. The amount of carbon that is not used depends on the desired composition of the synthesis gas that will be exhausted from the C converter 9. The carbon discharged through the second carbon outlet 7 can be discharged as another form such as activated carbon, graphite, carbon black, carbon cone, or carbon disk. Depending on the form and quality of the discharged carbon, the discharged carbon can be used as a raw material for the chemical industry or the electronics industry. For example, it can be used in the manufacture of semiconductors, tires, inks, toners or similar products. The carbon produced by the hydrocarbon converter 3 is a high purity raw material that can be processed very well.

  With the above-described method for generating synthesis gas, hot carbon or hot water from the hydrocarbon converter 3 in the C converter 9 with no external energy supply or at least a substantial amount of external energy supply with hot water or hot water. It can be converted to synthesis gas. Preferably at least 80%, in particular at least 90% of the heat required to reach the conversion temperature can be attributed to the heat generated from the hydrocarbon converter 3.

FIG. 2 shows a plant 20 for producing synthesis gas, which comprises the aforementioned elements of the plant 1 and a mixing chamber 21 for producing synthesis gas. The mixing chamber 21 includes a synthesis gas inlet 22 for introducing synthesis gas, an H ₂ inlet 23 for introducing hydrogen, and a synthesis gas outlet 24 for discharging synthesis gas. The synthesis gas inlet 22 is connected to the synthesis gas outlet 12 of the C converter 9. The H ₂ inlet 23 of the mixing chamber 21 is connected to the H ₂ outlet 6 of the hydrocarbon converter 3. As will be apparent to those skilled in the art, in the embodiment in which the C—H ₂ mixture is introduced into the C converter 9 via the carbon outlet 5, the synthesis gas having a C—H ₂ mixing ratio of about 1: 3 is automatically generated. Generated. In such cases, the mixing chamber 21 may be omitted or the mixing chamber 21 may be used to produce different mixing ratios, or mixed with CO to reduce the H ₂ content of the synthesis gas. It may be introduced into the room.

The mixing chamber 21 may be any device suitable for mixing gases, and in a simple case, the mixing chamber 21 may be in the form of a pipe with appropriate inlets and outlets. good. It is introduced by the mixing chamber 21 and in particular via the H ₂ inlet 23 of the mixing unit 21 and / or the inlet (not shown) connected to the CO source (not shown) and / or the second synthesis gas source. By controlling / adjusting (open / closed loop) the amount of hydrogen (additional), the mixture of syngas at the syngas outlet 24 can be affected to obtain a composition that is compatible with subsequent processes. In particular, the second synthesis gas source may be the second C converter 9 operated in parallel with the first C converter. Both C converters 9 are supplied with carbon and / or hydrogen from the commonly used hydrocarbon converter 3 or another converter unit. In particular, substantially pure carbon (after hydrogen separation) can be supplied to the first converter, and carbon and hydrogen can be supplied to the second converter. Here, the first C converter produces a substantially water gas having a CO: H ₂ mixing ratio of about 1: 1, and the second C converter has a synthesis gas having a CO: H ₂ mixing ratio of about 1: 3. Is generated. Combining these two syngases results in a CO: H ₂ mixing ratio of about 1: 2, and excess hydrogen (from the separation step prior to introduction into the first C converter) further increases the mixing ratio. Used for

For many processes, for example for Fischer-Tropsch synthesis, the ratio of hydrogen to CO should be high. By means of the mixing chamber 21, the desired ratio of hydrogen to CO, for example a 1: 1 ratio corresponding to water gas, can be achieved at the synthesis gas outlet 24. It is conceivable that only a part of the synthesis gas and / or a part of hydrogen is supplied to the mixing chamber 21, and a part of the synthesis gas and hydrogen that are not introduced into the mixing chamber are discharged from the process as pure gases.
Thus, for example, a) exhausting only synthesis gas, b) exhausting only hydrogen, c) exhausting a CO and hydrogen synthesis gas mixture, or d) water gas stream, hydrogen stream, And synthesis gas mixtures (any ratio between CO and hydrogen) or various synthesis gas streams with different ratios of carbon monoxide and hydrogen can be discharged.

In FIG. 2, the plant 20 that generates synthesis gas includes a C heat exchanger unit 25, a synthesis gas heat exchanger unit 26, and an H ₂ heat exchanger unit 27. The C heat exchanger unit 25 is in thermal contact with and in contact with the connection 8 between the hydrocarbon converter 3 and the C converter 9 and reaches the conversion temperature in the C converter 9 when necessary. Excess heat that is not needed for this purpose is drawn from the connection or, if necessary, heat is introduced from other areas of the plant.

  The synthesis gas heat exchanger unit 26 is in thermal conduction and contact with the connection portion between the C converter 9 and the mixing chamber 21, draws excess heat from the connection portion, and is included in the hot synthesis gas. To draw out a lot of heat. The extracted heat can be used, for example, to preheat water introduced into the C converter 9. For this heat transfer, so-called countercurrent heat exchanger units are particularly suitable, as is known in the art.

The H ₂ heat exchanger unit 27 is in thermal contact with the connection between the hydrocarbon converter 3 and the mixing chamber 21 and draws excess heat from the contact, and thus is hot in the contact. It comes to draw from hydrogen. The heat extracted in one of the heat exchanger units 25, 26 or 27 is used to heat other areas of the plant, in particular to keep the C converter warm or to preheat water introduced into the C converter. Can be used to Some of the heat extracted by the heat exchanger unit can be converted to electricity, for example, by a steam generator and steam turbine or other suitable device.

The operation of generating synthesis gas by the plant 20 is similar to the operation of the plant 1 according to FIG. 1 with respect to the operation of the hydrocarbon converter 3 and the C converter 9. In the plant 20 that generates the synthesis gas, the desired mixing ratio of hydrogen and CO is set in the mixing chamber according to the desired composition of the synthesis gas, and is discharged through the synthesis gas outlet 24 of the mixing chamber 21. Preferably, but not necessarily, hydrogen is provided by the hydrocarbon converter 3 as described above. Other hydrogen sources are also conceivable, in particular the second hydrocarbon converter 3, in particular a low temperature hydrocarbon converter. If the entire amount of synthesis gas and / or the entire amount of H ₂ is not used, a gas that is not mixed in the mixing chamber, for example, a portion of the synthesis gas and / or H ₂ can be treated separately. is there.

FIG. 3 shows a plant 30 for the production of synthetic hydrocarbons with and / or without functional groups, the plant 30 comprising a water gas production plant and a CO converter 31 (as shown in FIG. 1). I have. The plant components corresponding to FIG. 1 will not be described in order to avoid redundant description. The CO converter 31 is located downstream of the C converter 9, and the CO converter 31 has a synthesis gas inlet 32 for introducing synthesis gas, an H ₂ inlet 33 for introducing hydrogen, and / or functional groups. A hydrocarbon outlet 34 is provided for discharging synthetic hydrocarbons having no functional group. The synthesis gas inlet 32 of the CO converter 31 is connected to the synthesis gas outlet 12 of the C converter 9 by a synthesis gas connection portion 35. The H ₂ inlet 33 of the CO converter 31 is connected to the H ₂ outlet 6 of the hydrocarbon converter 3 by an H ₂ connection 36.

It should be noted that the H ₂ inlet 33 and the H ₂ connection 36 of the CO converter 31 are optional components. Depending on the composition of the synthesis gas exhausted from the C converter 9 and by the synthetic hydrocarbons with and / or without functional groups produced by the CO converter 31, the synthesis gas is fed into the synthesis gas outlet 12 of the C converter 9. When exhausted from the synthesis gas, the synthesis gas already has the proper composition for further processing by the CO converter 31. In this case, it is not necessary to introduce hydrogen via the H ₂ connection 36. Optionally, the H ₂ connection 36 can also serve to introduce another material, such as an alkene for synthesis of CO or aldehyde (hydroformylation) to reduce the H ₂ content of the synthesis gas. .

The plant 30 for optionally producing hydrocarbons also comprises the heat exchanger units 25, 26, 27 described in connection with the plant 20 (FIG. 2), i.e. the plant 30 is also a C heat exchanger. 25, the synthesis gas heat exchanger 26 and the H ₂ heat exchanger 27 are provided, and all operations are as described above (see the description of FIG. 2).

  The CO converter 31 may be any CO converter as long as it is a CO converter for producing a synthetic hydrocarbon having a functional group and / or not having a functional group. In the embodiment shown in FIG. 3, the CO converter with suitable catalyst and temperature and / or pressure control unit is preferably a Fischer-Tropsch converter, a Bergius peer converter or a peer converter.

In one embodiment, the CO converter 31 comprises a Fischer-Tropsch converter. Fischer-Tropsch converters catalytically convert synthesis gas into hydrocarbons and water. Some embodiments of the Fischer-Tropsch reactor and the Fischer-Tropsch process are well known to those skilled in the art and will not be described. The main reaction equation is as follows:
nCO + (2n + 1) H ₂ → C _n H _{2n + 2} + nH ₂ O nCO for alkane + (2n) H ₂ → C _n H _2n + nH ₂ O nCO for alkene + (2n) H ₂ → C _n H _{2n + 1} OH + (N-1) For H ₂ O alcohol

  The Fischer-Tropsch process can be performed as a high temperature process or a low temperature process, and the process temperature is typically in the range of 200 ° C to 400 ° C. Known variants of the Fischer-Tropsch process are high-load synthesis, Sintole synthesis and Shell's SMDS process (SMDS = Shell Middle Distillate Synthesis). Fischer-Tropsch converters typically produce wet gases (propane, butane), gasoline, kerosene, soft paraffin, solid paraffin, methane, diesel fuel, or a mixture of these hydrocarbons. It is known to those skilled in the art that Fischer-Tropsch synthesis is an exothermic reaction. The reaction heat from the Fischer-Tropsch process can be used, for example, to preheat water by a heat exchanger unit (not shown). For example, a process of preheating water introduced into the C converter 9 is conceivable, in which case the first preheating step is realized by preheating the CO converter 31 (in the embodiment of the Fischer-Tropsch converter) and the heat exchanger There is a next step of heating the water with heat from one or more of the units 25, 26, 27.

  In another embodiment, the CO converter 31 comprises a combination of a Bergius-Peer converter or MtL converter (MtL = Methanol-to-Liquid) and a peer converter.

  In the Bergius-Pier converter, the Bergius-Pier process, well known to those skilled in the art, is performed, where hydrocarbons are generated in an exothermic chemical reaction by hydrogenating carbon with hydrogen. The range of products from the Bergius Pier process depends on the reaction conditions and control of the reaction process. A predominantly liquid product is obtained, which can be used as fuel, for example heavy oil and medium oil (medium viscosity oil). Known variants of the Bergius Pier process include, for example, a console process and an H-coal process.

  In the above combination of peer converter and MtL converter, first the synthesis gas is converted to methanol by a peer process. The MtL converter is a converter that converts methanol into gasoline. A widespread process is the MtL process of ExxonMobil or Esso. The starting material for the MtL converter is typically methanol, for example methanol from a peer converter. The exit product produced by the MtL converter is gasoline, which is suitable for Otto engine operation.

In summary, regardless of the operating principle described above, the CO converter 31 produces, as an output or final product, a synthetic hydrocarbon with and / or without functional groups from CO and H _2. Can do. By the heat exchanger unit, the process heat generated during the exothermic conversion reaction in the CO converter 31 can be used to heat different parts of the plant or increase the efficiency of the plant described above. It can be used to generate electricity for

  As long as a mixture of hydrocarbons is obtained as the outlet product of the CO converter 31 that cannot be further processed directly as a final product after separation and purification or cannot be sold profitably, these hydrocarbons such as methane Alternatively, short chain alkanes can be reused in the process described above. For this purpose, the plant 30 is provided with a recycle connection 39 that allows a part of the synthetically produced hydrocarbons to be returned to the hydrocarbon inlet 4 of the hydrocarbon converter 3. Inappropriate hydrocarbon treatment or separation steps are carried out so that the composition of the synthetically produced hydrocarbon to be recycled does not introduce inappropriate hydrocarbons into the hydrocarbon inlet 4.

  FIG. 4 shows another embodiment of a plant 40 for producing synthetic hydrocarbons with and / or without functional groups. The plant 40 includes the above-described plant 20 for generating synthesis gas and the CO converter 31 described in the embodiment of FIG. The synthesis gas outlet 24 of the mixing chamber 21 is connected to the synthesis gas inlet 32 of the CO converter 31. The mixing chamber 21 is set up to provide a synthesis gas at the synthesis gas outlet 24 that meets the needs of the CO converter 31 in use. The other components of the plant 40 are similar to those described above, and the operation of the individual components is similar to the method described above.

  Depending on the size of the plant, it is conceivable to operate a plurality of hydrocarbon converters in parallel to obtain the desired conversion capacity. As described above, the hydrocarbon converter can be configured as a high temperature hydrocarbon converter and / or a low temperature hydrocarbon converter. High temperature hydrocarbon converters operate at temperatures above 1000 ° C., and low temperature hydrocarbon converters operate at temperatures from 200 ° to 1000 ° C. Here, an additional energy source, for example a microwave unit, can be provided to input energy directly into the hydrocarbon in order to decompose the hydrocarbon into carbon and hydrogen.

  As an example of a plant having a plurality of hydrocarbon converters operating in parallel, FIG. 5 shows another embodiment of a plant 30 for producing synthetic hydrocarbons with and / or without functional groups. Show. FIG. 5 uses the same reference numerals as in the previous embodiment as long as the same or similar components are described. In the embodiment shown in FIG. 5, a combination of high temperature hydrocarbon converter 3 a and low temperature hydrocarbon converter 3 b is shown instead of a single hydrocarbon converter 3.

The high temperature hydrocarbon converter 3a includes a hydrocarbon inlet 4a, a first outlet 5a for discharging carbon, and a second outlet 6a for discharging hydrogen. Also, a single outlet 5a can be provided for a mixture of carbon and hydrogen (especially aerosol). The first outlet 5 a is connected to the C inlet 11 of the C converter 9 by the connecting portion 8. An optional second outlet 6 a of the high temperature hydrocarbon converter 3 a is connected to the H ₂ inlet 33 of the CO converter 31. The high temperature hydrocarbon converter 3a can optionally be provided with another outlet for carbon (not shown in FIG. 5).

The low temperature hydrocarbon converter 3b includes a process chamber having a hydrocarbon inlet 4b, a first outlet 5b for discharging carbon, a second outlet 6b for discharging hydrogen, and an optional third outlet 7b for discharging carbon. . Preferably, the low-temperature hydrocarbon converter 3b includes a separation unit for separating hydrogen and carbon after decomposition, and for introducing hydrogen and carbon to respective outlets. The first outlet 5b is optionally connected to the C inlet 11 of the C converter 9 via the connecting portion 8, but is also connected to the carbon integrated unit. The second outlet 6 b of the low temperature hydrocarbon converter 3 b is connected to the H ₂ inlet 33 of the CO converter 31. The optional third outlet 7b is connected to a carbon accumulation unit, and the carbon accumulated from this carbon accumulation unit can be extracted, for example, in carbon black, activated carbon or another form.

As described above, when it is not necessary to introduce hydrogen through the H ₂ connection portions 36a and 36b, the H ₂ inlet 33 and the H ₂ connection portions 36a and 36b of the CO converter 31 are optional components. Become.

  The hydrocarbon introduced into the hydrocarbon inlet 4a and the hydrocarbon introduced into the hydrocarbon inlet 4b may be the same hydrocarbon or different hydrocarbons. Hydrocarbons from the first hydrocarbon source may be introduced into the hydrocarbon inlet 4a, for example, natural gas from a natural gas source may be introduced into the hydrocarbon inlet 4a. However, for example, synthetically produced and / or non-functional hydrocarbons may be introduced into the hydrocarbon inlet of the low temperature hydrocarbon converter 3b, for example via the optional recycle connection 39 described above. It is possible to introduce into 4b. In order to utilize several parallel operated hydrocarbon converters 3, 3a, 3b, the plant 30 can be easily increased or decreased in size, easier to control, and different types. Of carbon can be produced.

Also, the high temperature hydrocarbon converter 3a can be advantageously used for producing hot carbon for the conversion process in the C converter 9, preferably at a temperature of 1000 ° C. or higher. In particular, since the C—H ₂ mixture obtained by decomposition can be directly introduced into the C converter, the high-temperature hydrocarbon converter 3a can operate without a separation unit. In this case, the C converter 9 produces syngas at the outlet, for example, having a C—H ₂ mixing ratio of about 1: 1.

However, low temperature hydrocarbon converter 3b is a synthesis gas produced in the CO converter 31, or 1: mainly used to provide additional hydrogen C-H ₂ mixture for generating with large C-H ₂ mixture ratio than 3 Is done. Since heat transfer from the low temperature hydrocarbon converter 3b to the next process is not necessary, the low temperature hydrocarbon converter 3b can be advantageously operated at temperatures below 1000 ° C., preferably at the lowest possible temperature.

Thus, some of the carbon produced in the hydrocarbon converters 3a, 3b (preferably the high temperature hydrocarbon converter 3a) can be introduced into the C converter 9 during operation of the plant 30, whereas another part. Of carbon (preferably part from the low temperature hydrocarbon converter 3b) can also be diverted from the process as a feedstock to produce further products. Such products are, for example, carbon black or special carbon obtained as a black powdered solid such as industrial soot, activated carbon, carbon disc or carbon corn.
This carbon is used as a colored soot for fillers, color printing, inks, paints in the rubber industry or as a starting material for the production of, for example, zinc-carbon batteries and electrical components for the production of cathodes or anodes. It is an industrially important product that can be used. Excess hydrogen can be diverted for the chemical industry and can be used to generate electricity (either by combustion or by fuel cells). Here, the low temperature hydrocarbon converter 3b is preferably operated so that the low temperature hydrocarbon converter 3b only provides the additional hydrogen needed.

  FIG. 6 shows another embodiment of the plant 40 for producing synthetic hydrocarbons with and / or without functional groups, in this alternative embodiment a plurality of parallel operated high temperatures. And / or a low temperature hydrocarbon converter is likewise provided. The plant 40 for producing hydrocarbons shown in FIG. 6 is different from the plant 30 shown in FIG. 5 in that the mixing chamber 21 is located upstream of the CO converter 31. The mixing chamber 21 mixes a synthesis gas particularly suitable for the CO converter 31 and sends the synthesis gas to the CO converter 31. The components shown in FIG. 6 have already been described and operate according to the principles described above. Therefore, detailed description is omitted to avoid redundant description.

7 and 8 show embodiments of plants 20 and 30, which include a C heat exchanger unit 25, a synthesis gas heat exchanger unit 26 and an H ₂ heat exchanger unit 27, and each heat exchange. The generator unit is connected to the engine / generator device 45. The engine / generator device 45 is suitable for generating electricity at least partly from surplus heat from different parts of the plant, which can be supplied to the high-voltage wiring network or 20, in particular can be used to operate a hydrocarbon converter. The engine / generator device 45 can also be connected to a heat exchanger unit (not shown in FIG. 8), which dissipates heat generated by the exothermic conversion process that occurs in the CO converter 31. . It is therefore possible on the one hand to cool the CO converter in a controlled and regulated manner, which is advantageous for the operation of the process and on the other hand it is possible to generate electricity. The engine / generator device 45 may be any device that is suitable for converting thermal energy into electricity, such as a combination of a steam turbine and a generator or a combination of a piston engine and a generator. .

  During operation, the engine / generator device 45 converts excess plant heat into electricity, i.e., converts heat not needed for carbon-water conversion into electricity.

  The engine / generator device 45 and the heat exchanger units 25, 26 and 27 are optional components that can be used in all the plants mentioned above. Depending on the operating temperature of each hydrocarbon converter 3, 3a, 3b, the carbon discharged from each second carbon outlet 7, 7a, 7b contains a substantial amount of thermal energy. Depending on the desired temperature of the exhausted carbon, a large amount of heat energy can be dissipated by a heat exchanger unit (not shown), and this heat can be reused in the process described herein. Yes and / or can be converted to electricity using the engine / generator device 45.

  Cooling of hydrogen from hydrocarbon converters 3, 3a, 3b and / or synthesis gas from C converter 9 in plants 30 and 40 for producing synthetic hydrocarbons with and / or without functional groups The cooling is performed in a range in which the temperature of the hydrocarbon and hydrogen does not fall below the operating temperature of the CO converter 31. The operating temperature of the CO converter 31 is usually between 200 ° C. and 400 ° C., depending on the process selected.

  In all the plants mentioned above, the hydrocarbon converter 3 is a high temperature reactor operating at a temperature of 1000 ° C. or higher (eg, a Kuburner high temperature reactor) or a low temperature reactor operating at a temperature between 200 ° C. and 1000 ° C. (eg, Kuburner low-temperature reactor). Currently tested low temperature reactors operate at temperatures from 400 ° C to 900 ° C. In the case of a low temperature reactor operating at a temperature of 200 ° C. to 900 ° C., since the C converter 9 operates at a temperature between 800 ° C. and 1700 ° C., preferably between 1000 ° C. and 1200 ° C., the carbon introduced Is preheated at the connection 8 between the hydrocarbon converter 3 and the C converter 9. It will be clear from FIGS. 7 and 8 that a combination of a high temperature converter and / or a low temperature converter can be used in all the plants 1, 20, 30 and 40 described above.

  In all the plants 1, 20, 30 and 40 described above, unless a portion of the carbon produced by the hydrocarbon converters 3, 3a and 3b is converted in the C converter 9 of the plants 1, 20, 30 and 40, the carbon Some can be diverted as carbon black, activated carbon or other raw materials. It is further noted that multiple C converters are provided in all of the plants described above. Here, when water is added, each of these C converters can convert a portion of the carbon to synthesis gas. Also, by supplying undesired hydrocarbons to the hydrocarbon inlets 4, 4 a, 4 b of the hydrocarbon converter 3, a synthetic carbon having an undesirable functional group and / or having no functional group generated by the CO converter 31. The optional recycling of hydrogen can be carried out in all the plants 30 and 40 described above.

  Surplus hydrogen can be produced in the plants 1, 20, 30 and 40 and in the process for producing synthesis gas and / or synthetic hydrocarbons with and / or without functional groups. Excess hydrogen remains with, for example, synthesis gas having a low hydrogen content, and depending on the synthesized hydrocarbons produced by the CO converter 31, it is not necessary to introduce hydrogen into the mixing chamber 21 or the CO converter 31. . In these cases, excess hydrogen can be converted to electricity directly by combustion or by a fuel cell. Therefore, these methods can be practically performed without external electrical input. This is particularly advantageous for plants operating at remote locations where a powerful and common high voltage distribution network is not available. It should be noted that some of the hydrogen produced by the hydrocarbon converter 3 can be taken directly from the process and can be provided to the market as a product.

  In all plants, the flow of carbon, synthesis gas, hydrogen and external CO between the converters 3, 9, 31 and the mixing chamber 21 can be controlled by valves, shutters, sliders and the like. In particular, the inflow of synthesis gas and hydrogen or CO into the CO converter 31 is considered to be controllable by a valve. The mixing of synthesis gas and hydrogen or CO at the desired ratio occurs directly in the CO converter 31.

  In all the above-mentioned plants, the CO converter 31 may be composed of a plurality of CO converters (not shown), and the hydrogen generated and separated by the hydrocarbon converters 3, 3 a, 3 b and the synthesis generated by the C converter 9. The total amount of gas can be arbitrarily distributed to a plurality of CO converters. Each CO converter has one of the above designs and an operating mode. The CO converters may be the same design or have different designs or modes of operation. In embodiments with different CO converters, the individual CO converters are each operated with differently configured syngas to produce different end products.

To further illustrate the method, some examples are given below:
Example 1
When 1 part of methane is cracked with a hydrocarbon converter, 1 part of carbon and 2 parts of hydrogen are obtained. In the C converter, the carbon reacts with 1 part water to form 1 part carbon monoxide and 1 part hydrogen. After adding 1.1 parts of hydrogen, the synthesis gas reacts in a CO converter and is converted to paraffin (hydrocarbon compound). Thereafter, still enough hydrogen is utilized to break down the paraffin into diesel, otto fuel or kerosene in a further step.

Example 2
When 1 part of propane (butane) is cracked with a hydrocarbon converter, 3 (4) parts of carbon and 4 (5) parts of hydrogen are obtained. In the C converter, the carbon reacts with 3 (4) parts of water to form 3 (4) parts of carbon monoxide and 3 (4) parts of hydrogen. After adding 3.3 (4.4) parts of hydrogen, the synthesis gas reacts in a CO converter and is converted to paraffin. In any case, the amount of hydrogen remaining is just enough to break down the paraffin into diesel, otto fuel or kerosene in a further step.

Example 3
When cracking 1 part heavy oil (eg C ₂₀ H ₄₂ ) with a hydrocarbon converter, 20 parts carbon and 21 parts hydrogen are obtained. In the C converter, the carbon reacts with 20 parts of water to form 20 parts of carbon monoxide and 20 parts of hydrogen. After adding 21 parts of hydrogen, the synthesis gas reacts in another CO converter and is converted to 20 parts of methanol.

  In the method described here, the hydrogen produced by cracking the hydrocarbons in the hydrocarbon converter 3 is separated from the carbon formed in the cracking process, and then separated to form a synthesis gas with a low hydrogen content. Hydrogen can be added to the low hydrogen content synthesis gas in the desired ratio. Therefore, a range of the ratio of hydrogen to CO is obtained between 1.0 and 3.0. By partially oxidizing the surplus carbon, the ratio <1.0, and by not using surplus carbon, the ratio> 3.0 can be achieved.

  Although the invention has been described in detail with reference to preferred embodiments, the individual features of the described embodiments can be freely combined as long as they are compatible. Also, individual features of the above-described embodiments can be omitted as long as those features are not absolutely necessary. Many variations will be apparent to those skilled in the art without departing from the scope of the invention. In a particular simple embodiment of a plant that generates synthetic hydrocarbons with and / or without functional groups, the C converter is a simple pipe (for example, without a separation unit, a high temperature hydrocarbon converter As the outlet pipe), and the water inlet leads to said pipe. The water inlet should join the pipe so that the two media streams mix well. In particular, in order to heat the pipe to the operating temperature at the beginning of the operation, the pipe is preferably insulated at the inlet portion and may be connected to a heating unit. Also downstream, the pipe can be connected to a heat exchanger that uses this heat to draw excess heat and heat other parts of the plant and / or generate electricity. preferable. In addition, the pipe may be an inlet pipe for hydrogen (e.g., so that the same pipe functions not only as a C converter but also as a mixing chamber for producing synthesis gas having a specific mixing ratio). Or downstream of the heat exchanger. The inlet pipe for hydrogen may start from the outlet for hydrogen of the low temperature hydrocarbon converter (comprising a separation unit). In this case, the output end of the pipe from which the synthesis gas having a predetermined mixing ratio is discharged may end in the CO converter.

Claims (22)

The introduction of energy breaks down the hydrocarbon containing fluid into carbon and hydrogen, at least a portion of the energy is provided by heat, the carbon and hydrogen having a temperature of at least 200 ° C. after the cracking step;
When water is brought into contact with at least a part of the carbon produced in the decomposition step at a temperature of 800 ° C. to 1700 ° C. and carbon is brought into contact with water, the carbon obtained in the decomposition step is The temperature is cooled by 50% or less of the temperature (° C.),
A synthesis gas generation method for converting at least a part of carbon and water obtained in the decomposition step into synthesis gas,
A method for producing synthesis gas, comprising bringing carbon obtained in the decomposition step and hydrogen obtained in the decomposition step into contact with water. The introduction of energy breaks down the hydrocarbon containing fluid into carbon and hydrogen, at least a portion of the energy is provided by heat, the carbon and hydrogen having a temperature of at least 200 ° C. after the cracking step;
When water is brought into contact with at least a part of the carbon produced in the decomposition step at a temperature of 800 ° C. to 1700 ° C. and carbon is brought into contact with water, the carbon obtained in the decomposition step is The temperature is cooled by 50% or less of the temperature (° C.),
A synthesis gas generation method for converting at least a part of carbon and water obtained in the decomposition step into synthesis gas,
Prior to the step of contacting the carbon with water, at least a portion of the carbon obtained in the cracking step is separated from the hydrogen obtained in the cracking step;
A method for producing synthesis gas, wherein at least a part of the separated hydrogen is added to the synthesis gas produced in the conversion step.   The method for generating synthesis gas according to claim 1 or 2, wherein the decomposition step occurs at a temperature of 1000 ° C or higher, and the carbon contacts with water at a temperature of at least 1000 ° C.   The heat required to reach a temperature of 800 ° C. to 1700 ° C. for conversion is essentially and completely derived from the heat provided to decompose the fluid containing the hydrocarbon. The synthesis gas generation method according to any one of claims 1 to 3.   At least a portion of the carbon obtained from the cracking step and / or a portion of the hydrogen obtained from the cracking step and / or at least a portion of the heat of the synthesis gas may be used before Used to heat and / or used to heat process chambers in which water is in contact with carbon and / or used for power generation, electricity in particular for decomposing fluids containing hydrocarbons The synthesis gas generation method according to any one of claims 1 to 4, wherein the synthesis gas generation method is provided as an energy carrier for introducing energy.   6. The synthesis gas generation method according to claim 1, wherein energy for decomposing the hydrocarbon-containing fluid is introduced by plasma.   7. The method for producing synthesis gas according to claim 6, wherein carbon obtained in the decomposition step and hydrogen obtained in the decomposition step are brought into contact with water in the form of an aerosol.   The method for generating synthesis gas according to claim 2, wherein at least a part of the additional hydrogen is generated by decomposing a hydrocarbon-containing fluid by microwave plasma at a temperature of 1000 ° C or lower. The method for producing synthesis gas according to any one of claims 1 to 8 , wherein the hydrocarbon-containing fluid to be decomposed is natural gas, methane, wet gas, heavy oil, or a mixture thereof. A method for producing a synthetic hydrocarbon having a functional group and / or having no functional group,
A synthesis gas for first generating a synthesis gas by the method according to any one of claims 1 to 9 and converting the synthesis gas into a synthetic hydrocarbon with and / or without functional groups. A synthetic carbon with and / or without functional groups, characterized in that the catalyst and / or the synthesis gas temperature is open-loop controlled or closed-loop controlled to a temperature in a predetermined range. Hydrogen generation method. The functional group according to claim 10 , wherein the conversion of the synthesis gas is performed by any one of a Fischer-Tropsch process, an SMDS process, a Bergius peer process, a peer process, and a combination of a peer process and an MtL process. And / or synthetic hydrocarbon production method having no functional group. A syngas generator,
Equipped with a hydrocarbon converter that breaks hydrocarbon-containing fluids into carbon and hydrogen,
The hydrocarbon converter comprises at least one inlet for a hydrocarbon-containing fluid, at least one outlet for carbon and / or hydrogen, and at least one unit for introducing at least partly heat energy into the process chamber. Having at least one process chamber with
It has a C converter for water and carbon conversion,
The C-converter comprises at least one separate process chamber having at least one inlet for water, at least one inlet for at least carbon, and at least one outlet;
At least the inlet for carbon is directly connected to at least one outlet of the hydrocarbon converter;
The hydrocarbon converter, at least one outlet of the hydrocarbon converter, the C converter, and at least one inlet of the C converter are configured to direct both carbon and hydrogen generated in the hydrocarbon converter to the C converter. A synthesis gas generator characterized by the above. A syngas generator,
Equipped with a hydrocarbon converter that breaks hydrocarbon-containing fluids into carbon and hydrogen,
The hydrocarbon converter comprises at least one inlet for a hydrocarbon-containing fluid, at least one outlet for carbon and / or hydrogen, and at least one unit for introducing at least partly heat energy into the process chamber. Having at least one process chamber with
It has a C converter for water and carbon conversion,
The C-converter comprises at least one separate process chamber having at least one inlet for water, at least one inlet for at least carbon, and at least one outlet;
At least the inlet for carbon is directly connected to at least one outlet of the hydrocarbon converter;
A separation unit for separating carbon obtained by cracking from hydrogen obtained by cracking, the separation unit having individual outlets for substances separated by the separation unit, and the outlet for carbon is connected to a C converter; A synthesis gas generator comprising a separate inlet pipe for hydrogen separated by a separation unit, wherein the inlet pipe for hydrogen guides hydrogen to a C converter or a mixing chamber located downstream of the C converter.   13. The at least one unit for introducing energy into the process chamber is designed such that the unit is capable of generating a temperature of at least 1000 ° C. locally. Syngas generator.   15. The syngas generator according to claim 12, wherein at least one unit for introducing energy into the process chamber comprises a plasma unit.   16. The syngas generator according to claim 12, wherein the process chamber of the C converter is formed by an outlet pipe of a hydrocarbon converter, and the outlet pipe is connected to an inlet for water. .   The synthesis gas generator according to any one of claims 12 to 16, wherein the hydrocarbon converter comprises a Kuburner reactor. The synthesis gas generator according to any one of claims 15 to 17, wherein the hydrocarbon converter is further configured to form an aerosol composed of carbon and hydrogen. Having at least one additional hydrocarbon converter to decompose the hydrocarbon-containing fluid into carbon and hydrogen, the hydrocarbon converter comprising:
At least one process chamber having at least one inlet for the hydrocarbon-containing fluid;
At least one unit for introducing at least partly heat energy into the process chamber,
A separation unit for separating carbon obtained by decomposition and hydrogen obtained by decomposition;
The synthesis according to any one of claims 12 to 18, characterized in that the separation unit has separate outlets for carbon and hydrogen, the outlet for hydrogen being connected to another inlet for hydrogen. Gas generator.   20. The syngas generator according to claim 19, wherein the at least one additional hydrocarbon converter is of a type that performs decomposition by microwave plasma at a temperature of 1000 ° C. or less. An apparatus for converting synthesis gas into a synthetic hydrocarbon having a functional group and / or no functional group,
21. A device according to any one of claims 12 to 20,
A CO converter having a process chamber in which the catalyst is located, means for bringing the synthesis gas into contact with the catalyst, and a control unit for performing open-loop control or closed-loop control of the catalyst temperature and / or the synthesis gas temperature to a predetermined temperature. An apparatus for converting a synthesis gas into a hydrocarbon, comprising:   The CO gas to the hydrocarbon of claim 21, wherein the CO converter comprises any one of a Fischer-Tropsch converter, an SMDS converter, a Bergius peer converter, a peer converter, and a combination of a peer converter and an MtL converter. Conversion device.

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