AT519584A2 - Process for producing dimethyl ether from water, carbon dioxide and lean gases - Google Patents

Abstract

The invention relates to a process for the production of dimethyl ether (DME) (38) from a synthesis gas reactor (8) for lean gas (1), consisting of carbon monoxide (CO) and hydrogen (H2), consisting of non-condensable components residual gas consisting of carbon monoxide (CO), hydrogen (H2), carbon dioxide (C02), methane (CH4) and ethane (C2H4), in a reforming reactor (30) to a synthesis gas (17) consisting of carbon dioxide (C02) and hydrogen (H2) is converted and in a synthesis gas reactor (21) to dimethyl ether (DME), and from a synthesis gas reactor (21) for a gas / vapor mixture of carbon dioxide (C02) and hydrogen (H2) in which the converted residual gas from the syngas reactor (8) for lean gas is recycled. The recovered condensate (26) from the synthesis gas reactors consisting of dimethyl ether (DME), Methanoi (MeOH) and water (H20) is in the subsequent two-stage distillation into the desired product dimethyl ether (DME) (38), Methanoi (MeOH) (45) and water (H 2 O) (49). The amount of methanoi {MeOH) (45) is converted into dimethyl ether (DME) and water (H20) in a dehydration reactor (58). The water (H20) (49) recovered during the distillation is used to produce hydrogen (H2 ) (57) using wet electrolysis (66), the hydrogen (H2) (5,18) that is used to synthesize carbon dioxide (C02) to dimethyl ether (DME) to give the Zero property To ensure emission. The reforming of the residual gases from the synthesis gas reactors (8,21) is reformed by means of water vapor (54) from the process water (49) to a mixture of carbon dioxide (C02) and hydrogen (H2) and admixed with the carbon dioxide (13, 15) (17) ,

Description

Process for the production of dimethyiethger (DME) from carbon dioxide, water and

lean gases

The invention relates to a process for the production of dimethyl ether (DME) (38) from a synthesis gas reactor (8) for lean gas (l), consisting of carbon monoxide (CO) and hydrogen (H2), consisting of non-condensable components residual gas consisting of carbon monoxide (CO), hydrogen (H2), carbon dioxide (C02), methane (CH4) and ethane (C2H4), in a reforming reactor (30) to a synthesis gas (17) consisting of carbon dioxide (C02) and hydrogen (H2) is converted and in a synthesis gas reactor (21) to dimethyl ether (DME), and from a synthesis gas reactor (21) for a gas / vapor mixture of carbon dioxide (C02) and hydrogen (h2) in which the converted residual gas from the syngas reactor (8) for lean gas is recycled. The recovered condensate (26) from the synthesis gas reactors (8,21) consisting of dimethyl ether (DME), methanol (MeOH) and water (H20) is in the subsequent two-stage distillation into the desired product dimethyl ether (DME) (38), methanol ( MeOH) (45) and water (H20) (49). The resulting amount of methanol (MeOH) (45) is converted into dimethyl ether (DME) and water (H20) in a dehydration reactor (58). The water (H20) (49) recovered in the distillation is used to produce hydrogen (H2 ) (57) using wet electrolysis (66), the hydrogen (H2) (5,18) that is used to synthesize carbon dioxide to dimethyl ether (DME) to ensure zero emission , The reforming of the residual gases from the synthesis gas reactors (S, 21) is reformed by means of water vapor (54) from the process water (49) to a mixture of carbon dioxide (C02) and hydrogen (H2) and added to the carbon dioxide (13,15) (17) ,

Dimethyl ether (DME) is the simplest ether, consisting of two methyl groups (CH3) linked by an oxygen atom (O). The chemical name of DME is CH3-0-CH3, whereby the bond of the oxygen atom (O) with the two carbon atoms (C) is given by a simple bond. Dimethyl ether (DME) is typically used in the cosmetics industry, and in China, India, Korea dimethyl ether is used as a diesel substitute fuel. As can be seen from the chemical structure, dimethyl ether (DME) consists of six hydrogen atoms (H), two carbon atoms (C) and one oxygen atom (O).

Dimethyl ether (DME) is usually generated via methanol in two process steps. The first process step produces methanol (MeOH), in the second process step dimethyl ether (DME) is generated from methanol (MeoH) via dehydration. The catalysts used are known and state of the art, for the methanol synthesis from carbon monoxide (CO) and hydrogen (H 2) CuO-ZnO-Al 2 O 3, for the dehydration of the zeolite HSZM-5, for the methanol synthesis from carbon dioxide (CO 2) and hydrogen ( H2) CuO-ZnO-ZrO2.

Carbon dioxide (C02) is a non-reactive substance, which can occur in three phases, vapor, liquid and solid, with the vapor and liquid phases being of importance in the technical field. the thermodynamic properties are given by Tc = 30.98 [° C], pc = 73.77 [bar]. The states of matter essential to this invention are: p = 30 bar Ts = -5 ° C. p = 50 bar TS = 14.2 ° C. p = 70 bar Ts = 28.6 ° C. (p = vapor pressure, Ts = boiling temperature)

All other thermodynamic states in the invention are in the overheated vapor state.

Water (H20) is also a non-reactive substance, a very good solvent and a polar liquid, which can occur in three phases, vapor, liquid, solid, with all three phases being of importance in the technical field. For the invention, the aggregate states liquid and vapor are important.

p = 5 bar TS = 151 ° C

p = 10 bar TS = 179.8 ° C

p = 15 bar TS = 198 ° C

p = 20 bar TS = 212 ° C (p = vapor pressure, Ts = boiling temperature)

Methanol (MeQH) is the simplest alcohol and occurs in the production of dimethyl ether (DME) as an intermediate in direct synthesis. For the invention, the aggregate states liquid and vapor are important. p = 5 bar TS = 111 ° C p = 10 bar Ts = 136 ° C p = 15 bar TS = 153 ° C p = 20 bar Ts = 165 ° C (p = vapor pressure, Ts = boiling temperature)

Residual gases and lean gases are gases whose composition consists of partly oxidizable gas components. Such gases are biogas, landfill gas, wood gases, mine gases, pyrolysis gases. The known property is the low energy content in the form of the calorific value (kWh / Nm3) in the order of magnitude of 0.5 to 6.0 kWh / Nm3.

Table 1: Representation of the weak gases in the composition Vol%

In addition to the oxidizable components in the form of carbon monoxide (CO), hydrogen (H2), methane (CH4), ethane (C2H4), low components of hydrocarbons, non-oxidizable gas components are included, such as nitrogen (N2), carbon dioxide (CO2), water vapor ( H20). In general, the residual gases and lean gases also impurities such as particles, ammonia (NH3), hydrogen sulfide (H2S), carbon monoxide (COS), tars (CxHy) in low concentrations of 1mg / Nm3 to 1000 mg / Nm3. The invention assumes that the pollutants of the lean gases and synthesis gases have the following limits:

CxHy <100 ppm COS <1 ppm H2S <1 ppm NH3 <1 ppm

Particles <1 ppm with a particle diameter dp <1 pm N2 <100 ppm

Achieving the gas purity of synthesis gases and lean gases is state of the art, and involves charcoal cleaning, washing the gas with water, and using ultrafine filters in the form of depth filters.

The patent WO 2016104290 describes the separation of the product mixture from the dimethyl ether (DME) synthesis reactor and the separation of the gas and vapor mixture. The vapor mixture is cooled and then separated into the three components dimethyl ether, methanol (MeOH) and water (H2Q). The disadvantage of this invention is that the invention deals only with the separation of the condensate, without the question of the utilization of the incurred methanol (MeOH) and water (H20). Another disadvantage of the invention is that the composition of the syngas is neither purified nor treated.

The patent WO 9623755 A1 describes the production of dimethyl ether (DME) in a synthesis reactor, and the use of the recovered methanol condensate as a detergent for the off-gas to separate carbon dioxide (C02) from the offgas. In this case, a part of the methanol (MeOH) is dehydrogenated to dimethyl ether (DME). The disadvantage of the invention is that it does not address the composition of the synthesis gas. The use of methanol (MeOH) as a detergent in a gas with the composition of carbon monoxide (CO), carbon dioxide (C02), hydrogen (H2), methane (CH4), and higher hydrocarbons (CxHy) due to the affinity of methanol (MeOH ) to carbon monoxide (CO) and carbon dioxide (C02) that in addition to carbon dioxide (C02) and carbon monoxide (CO) is discharged, but also a residual amount of carbon dioxide (C02) and carbon monoxide (CO) remains in the offgas, the higher hydrocarbons (CxHy) also remain in the residual gas together with hydrogen (H2). The dehydration in the gas scrubber takes place only to a very small extent, and has the disadvantage that the offgas now also includes the desired product gas dimethyl ether (DME).

Patent DE 4222655 A1 describes the production of dimethyl ether (DME) from a gas mixture of carbon monoxide (CO), hydrogen (H 2) and carbon dioxide (CO 2), and the subsequent off-gas scrubber with methanol (MeOH) to reduce the carbon dioxide content in the recycle gas , The disadvantage of this invention is the undefined gas purity prior to dimethyl ether (DME) synthesis, and the recycle of the off-gas into the synthesis reactor, resulting in a consequent concentration of contaminants which reduces the efficiency of synthesis gas production.

The object, which is now asked, comprises the production of dimethyl ether (DME) from a gas mixture of carbon dioxide (C02) and hydrogen (H2), from a gas mixture of carbon monoxide (CO) and hydrogen (H2) in one process step, the regulation of Gas concentrations in relation to carbon dioxide (C02) and hydrogen (H2), the gas concentration with respect to carbon monoxide (CO) and hydrogen (H2), the utilization of residual gases from the reactors for the production of dimethyl ether, the recovery of materials such as water (H20) and methanol (MeOH), so that the zero emission property is ensured. In addition, the process must be scalable in production performance and in the utilization of carbon dioxide (C02) and water (H20).

The invention is based on the production of dimethyl ether (DME) based on carbon monoxide (CO) and hydrogen (H2) based on the following chemical equations:

As can be seen from the chemical sum equation, the molar ratio for carbon monoxide to hydrogen is 1: 1. In order to achieve this molar ratio for the production of dimethyl ether, a regulation of the gas concentrations is carried out according to the invention. For lean gases in Table 1 it can be seen that the proportion of carbon monoxide (CO) is always greater than the molar fraction of hydrogen H 2). In order to achieve the molar ratio, the required hydrogen H2) is supplied according to the invention. CuO-ZnO-Al 2 O 3 catalysts are generally used for the synthesis of methanol from carbon dioxide (CO) and hydrogen (H 2), and for dehydration HSZM-5 zeolites.

Further, the conversion of carbon monoxide (CO) and hydrogen (H2) to dimethyl ether (DME) yields, besides DME, also carbon dioxide (CO 2) as a product. Since the conversion in the synthesis reactor is not complete, but two process steps carried out by means of a mixture of catalysts in a synthesis reactor, in addition to dimethyl ether (DME), also methanol (MeOH) and water (H20) are formed. The incomplete reaction yields unconsumed carbon monoxide (CO), hydrogen (H2), methane (CH4), ethane (C2H4), and carbon dioxide (CO2).

The invention solves the problem of the property of zero emission, by the utilization of the off-gas in a reforming reactor, which operates on the basis of steam reforming. This converts the gaseous non-condensable gases into hydrogen H2) and carbon dioxide (CO2):

The offgas is converted into a gas mixture of carbon dioxide (C02) and hydrogen (H2).

As can be seen from the table of weak gases, the weak gases usually consist not only of carbon monoxide and hydrogen, but also of a proportion of carbon dioxide (C02). The invention solves the problem of controlling the gas concentration in that carbon dioxide is separated after compression by cooling of the compressed synthesis gas and deposited and stored in the liquid phase. This carbon dioxide thus obtained is then processed with the converted offgas consisting of carbon dioxide (C02) and hydrogen (H2) in a second dimethyl ether (DME) synthesis step.

The invention solves the problem of utilization of carbon dioxide (CO 2) to dimethyl ether (DME) by coupling a second synthesis process to produce dimethyl ether (DME) in one process step.

The production of dimethyl ether (DME) based on carbon dioxide (C02) and hydrogen H2) is based on the following chemical equations:

As can be seen from the chemical equations, the molar ratio of carbon dioxide (C02) and hydrogen H2) has a ratio of 1: 3 when a complete conversion of carbon dioxide (CO2) and hydrogen (H2) to dimethyl ether (DME) and water (H2O) should be done. As can be seen from the summation equation, a direct synthesis in a reactor with the combination of two catalysts is possible. As a rule, CuO-ZnO-ZrO 2 catalysts are used for the synthesis of methanol from carbon dioxide (CO 2) and hydrogen (H 2), and for dehydration HSZM-5 zeolites.

The synthesis of carbon dioxide (C02) and hydrogen H2) into dimethyl ether (DME) has the advantage that the carbon dioxide (C02) usually present in lean gases (see Table 1) can be separated off and recycled. This is not the case with all known processes; on the contrary, the classical direct synthesis of carbon monoxide (CO) and hydrogen (H2) always produces carbon dioxide (CO 2), see the summation equation for lean gas. The carbon dioxide (C02) inhibits the presence of carbon monoxide (CO) synthesis on the catalyst and degrades the yield of dimethyl ether in the product gas. The approach of using a mixture as multi-hybrid catalysts has not gone beyond the laboratory scale, and is unstable in the industrial scale solution.

The scalability of the reactors (8,21) is an essential feature. The low gas volume flows are usually limited, bearing in mind that lean gases such as biogas, wood gases, mine gases, coal gas are only by-products of actual main processes such as fermentation, gasification, pyrolysis or Verkockung. These plants are decentralized small plants, so that the volume flows are usually limited to 1000 Nm3 / h lean gas.

Scalable is the synthesis gas reactor (21) on the basis of carbon dioxide (C02) and hydrogen (H2), since not only the resulting carbon dioxide from the lean gas (l) deposited via the heat exchanger (3), as liquid carbon dioxide (C02) the carbon dioxide ( 13) added. Thus, the lean gas is reduced to the components hydrogen (H2) and carbon monoxide (CO) and in the lean gas synthesis reactor (8) carbon dioxide (CO2) is formed again, which together with the unused gas components carbon monoxide (CO) and hydrogen (H2 ) and the minor proportions of methane (CH4) and ethane (C2H4) which are contained as interfering products in the product gas. The gaseous fractions are converted to carbon dioxide (C02) and hydrogen (H2) either with methane via the dry partial oxidation reforming process, or are converted with steam via the steam reforming process. The resulting mixture of hydrogen (H2) and carbon dioxide (CO2) is converted in the synthesis gas reactor (21) to dimethyl ether (DME).

Dry reforming (partial oxidation):

The oxygen necessary for the dry reforming can be obtained from the electroylation (66) of water (49) to hydrogen (5,18) and oxygen (02) (69). The advantage of this method is the partial use of the resulting oxygen (69) from the electrolysis (66).

Steam reforming:

The steam reforming has the advantage that the resulting process water (H20) (49) in the reforming reactor (30) is utilized as water vapor (H20) (55).

The control of the gas concentrations of the input gases for the synthesis reactor for the production of dimethyl ether, as well as the gaseous residual gases from the synthesis reactor (21) and the lean gas reactor (8) is an advantage of this invention.

In general, the concentrations of lean gas vary due to the different raw materials used in the production of lean gases. Therefore, one can never assume a stable existing gas concentration in the components carbon monoxide (CO), hydrogen (H 2) and carbon dioxide (CO 2). This property is known. The advantage of this invention is now to control the concentration in the molar ratio of carbon monoxide (CO) to hydrogen (H2) by hydrogen (H2) (5) is supplied. The hydrogen (H2) (5) is recovered from the process water (49) obtained in the process.

Due to the fact that carbon dioxide (CO 2) is also present in the lean gas (1), it has been separated by liquefaction via the heat exchanger (3). The liquid carbon dioxide (CO 2) is combined with the carbon dioxide (13) from the tank (13) in the mixer (15). It is still carbon dioxide. This gas stream is mixed in the mixer (17), the reformed gas mixture of carbon dioxide (C02) and hydrogen (H2) and determined in the sequence, the gas concentration of carbon dioxide (CO2) and hydrogen H2). In the Miseher (19) the hydrogen H2) is mixed in order to achieve a controlled molar ratio of carbon dioxide (C02) and hydrogen H2) of 1: 3. The hydrogen 18) is recovered from the process water (49) obtained in the process.

The gaseous residual gas from the product gas from the lean gas reactor (8), which remains after depositing the liquid components such as dimethyl ether (DME), methanot (MeOH) and water (H20) stored in the tank (26), the gaseous residual gas from the product gas from the Synthesis gas reactor (21), which remains stored in the tank (26) after deposition of the liquid components such as dimethyl ether (DME), methanol (MeOH) and water (H20), is fed to the reforming reactor (30). The proportion of gas components such as carbon monoxide (CO), methane (CH4), ethane (C2H4) is determined and thus the required oxygen (51) from the electrolysis (66) regulates supplied, or the required water vapor (H20) (55) regulated supplied so as to achieve a complete conversion of the oxidizable gas components to carbon dioxide (C02) and hydrogen H2) regulated.

The separation of the obtained after the synthesis step by cooling condensate consisting of dimethyl ether (DME), methanol (MeOH), water (H 2 O), via the known methods of two-stage distillation. The products are stored in tanks, dimethyl ether (DME) in the tank (38), methanol (MeOH) in the tank (45) and process water (H20) in the tank (49).

The required electrical energy includes the energy for the compression of the lean gas from ambient pressure to the synthesis pressure, as well as the electrical energy for generating hydrogen H2) by means of electrolysis to hydrogen (H2) and oxygen 02) from the process water (H20) is supplied externally. It can also be used on renewable energy sources, we wind energy, or solar energy from photovoltaic.

The invention solves the problem of scalability by the utilization of carbon dioxide (CO 2) by conversion of carbon dioxide (CO 2) and hydrogen (H 2) to dimethyl ether (DME). This plant part, this reactor part as a synthesis reactor (21) is scalable and not limited in size. This means that with more carbon dioxide (C02) in the tank (13) you have to provide more water for the electrolysis in order to generate the proportion of hydrogen (H2), as well as the corresponding amount of electrical energy.

Figures Figure 1

Figure 1 shows the coupling of dimethyl ether synthesis reactors, the synthesis reactor (8) for weak gases consisting of carbon monoxide and hydrogen. The lean gas (l) usually consists of carbon monoxide (CO), hydrogen (H2) and carbon dioxide (C02) and accumulates at ambient pressure. The lean gas (l) is brought to the pressure with the compressor (2) and the carbon dioxide (C02) in the condenser (3) deposited as a liquid phase, the reduced lean gas is now heated again via the heat exchanger (4). In the mixer (6) hydrogen is supplied) and the lean gas via the volume flow regulator (7) fed to the synthesis reactor (8). Since the reaction is exothermic, this reactor (8) is cooled with the heat exchanger (11). The product gas is brought to a lower pressure via the throttle controller (9) and separated via the condenser (10) into a condensate portion of water, methanol and dimethyl ether and into a non-condensable fraction. The noncondensable portion is fed to the reformer (3Q). Liquid carbon dioxide (13) is throttled to a low pressure ^ 4) and mixed with the liquid carbon dioxide from the condenser (3) (15) and heated via the heat exchanger (16). In addition, the product gas from the reformer (30) is added (17). The gas mixture of hydrogen and carbon dioxide is supplemented by hydrogen 18) in the mixer (19). The gas mixture is fed via the volume flow regulator (20) to the synthesis gas reactor (21), which is cooled by the heat exchanger (22). The product gas is brought to a low pressure via the throttle controller (23) and fed to the condenser (24). The condensate is collected in the tank (26). The non-condensable gases and vapors are fed to the reformer (30). In the reformer, these residual gases from the reactors (8, 21) are first compressed via a compressor (34) to the pressure in the reformer (30) and regulated in the volume flow and pressure (29). The compressed residual gases from the synthesis reactors (8,21) along with external via the regulator (51) supplied oxygen (02) (51) reformed via the process of dry reforming to a gas mixture of carbon dioxide and hydrogen. The reformer (30) is supplied with heat via (31) regulated in pressure and volume flow (32) and supplied to a heat exchanger (33) to cool the product gas and fed to the mixing chamber (17).

The condensate in the tank (26) is fed via a pump (27) and the associated pressure and volume flow regulator (28) of the first distillation stage (35). In the distillation stage dimethyl ether (DME) is separated from condensate, the dimethyl ether vapor (DME) is controlled in the pressure and volume flow (36) and fed to the condenser (37) and the dimethyl ether (DME) is stored liquefied in the tank (38). The heat is supplied to the distillation via the heat exchanger (40), the condensate is fed via the pump (39) and the regulator (41) to the second distillation stage (42), in which the separation of methanol from water takes place. In the second distillation stage (42) dimethyl ether (DME) is separated from condensate, the methanol vapor (MeoH) is controlled in the pressure and volume flow (43) and fed to the condenser (44) and the dimethyl ether (MeOH) is liquefied in the tank (45). stored. The distillation is supplied via the heat exchanger (47), the heat, the water as condensate via the pump (46) and the controller (48) fed to the tank (49). From the tank the water with the pump (SO) is provided for further utilization.

Figure 2

Figure 2 shows the coupling of dimethyl ether synthesis reactors, the synthesis reactor (8) for weak gases consisting of carbon monoxide and hydrogen. The lean gas (l) usually consists of carbon monoxide (CO), hydrogen (H 2) and carbon dioxide (CO 2) and accumulates at ambient pressure. The lean gas (l) is brought to the pressure with the compressor (2) and the carbon dioxide (C02) in the condenser (3) deposited as a liquid phase, the reduced lean gas is now heated again via the heat exchanger (4). In the mixer (6) hydrogen is supplied) and the lean gas via the volume flow regulator (7) fed to the synthesis reactor (8). Since the reaction is exothermic, this reactor (8) is cooled with the heat exchanger (11). The product gas is brought to a low pressure via the throttle controller (9) and into a condensate portion of water via the condenser (IO).

Methanol and dimethyl ether and separated into a non-condensable fraction. The non-condensable portion is fed to the reformer (30). Liquid carbon dioxide (t3) is throttled to a low pressure 14) and mixed with the liquid carbon dioxide from the condenser (3) (15) and heated via the heat exchanger (16). In addition, the product gas from the reformer (30) is added (17). The gas mixture of hydrogen and carbon dioxide is supplemented by hydrogen (18) in the mixer (19). The gas mixture is fed via the volume flow regulator (20) to the synthesis gas reactor (21), which is cooled by the heat exchanger (22). The product gas is brought to a low pressure via the throttle controller (23) and fed to the condenser (24). The condensate is collected in the tank (26). The non-condensable gases and vapors are fed to the reformer (30). In the reformer, these residual gases are first compressed via a compressor (34) to the pressure in the reformer (30) and regulated in volume flow and pressure (29). The compressed residual gases from the synthesis reactors (8,21) together with water vapor (55) from the

Process water (49), which is converted into water vapor (54) in the evaporator consisting of pump (52) and evaporator (53), is reformed via the process of steam reforming to a gas-vapor mixture of carbon dioxide and hydrogen. The reformer (30) is supplied with heat via (31) regulated in pressure and volume flow (32) and supplied to a heat exchanger (33) to cool the product gas and fed to the mixing chamber (17).

The condensate in the tank (26) via a pump (27) and the associated pressure and

Volume flow controller (28) of the first distillation stage (35) supplied. In the distillation stage dimethyl ether (DME) is separated from condensate, the dimethyl ether vapor (DME) is controlled in the pressure and volume flow (36) and fed to the condenser (37) and the dimethyl ether (DME) is stored liquefied in the tank (38). The heat is supplied to the distillation via the heat exchanger (40), the condensate is fed via the pump (39) and the regulator (41) to the second distillation stage (42), in which the separation of methanol from water takes place. In the second distillation stage (42) dimethyl ether (DME) is separated from condensate, the methanol vapor (MeoH) is controlled in the pressure and volume flow (43) and fed to the condenser (44) and the dimethyl ether (MeOH) is liquefied in the tank (45). stored. The distillation is supplied via the heat exchanger (47), the heat, the water as condensate via the pump (46) and the controller (48) fed to the tank (49). From the tank, the water, which is not used for steam reforming, is made available for further use via the pump (50).

Figure 3

Figure 3 shows the coupling of dimethyl ether synthesis reactors, the synthesis reactor (8) for weak gases consisting of carbon monoxide and hydrogen. The lean gas (l) usually consists of carbon monoxide (CO), hydrogen (H2) and carbon dioxide (C02) and accumulates at ambient pressure. The lean gas (l) is pressurized by the compressor (2) and the carbon dioxide (C02 ) deposited in the condenser (3) as a liquid phase, the reduced lean gas is now heated again via the heat exchanger (4). Hydrogen (5) is fed into the mixer (6) and the weak gas is fed via the volume flow regulator (7) to the synthesis reactor (8). Since the reaction is exothermic, this reactor (8) is cooled with the heat exchanger (11). The product gas is brought to a low pressure via the throttle regulator (9) and separated via the condenser (1Q) into a condensate fraction of water, methanol and dimethyl ether and into a non-condensable fraction. The non-condensable portion is fed to the reformer (30). Liquid carbon dioxide (13) is throttled to a low pressure 14) and mixed with the liquid carbon dioxide from the condenser (3) (15) and heated via the heat exchanger (16). In addition, the product gas from the reformer (30) is added (17). The gas mixture of hydrogen and carbon dioxide is supplemented by hydrogen 18) in the mixer (19). The gas mixture is fed via the volume flow regulator (20) to the synthesis gas reactor (21), which is cooled by the heat exchanger (22). The product gas is brought to a low pressure via the throttle controller (23) and fed to the condenser (24). The condensate is collected in the tank (26). The non-condensable gases and vapors are fed to the reformer (30). In the reformer, these residual gases are first compressed via a compressor (34) to the pressure in the reformer (30) and regulated in volume flow and pressure (29). The compressed residual gases from the synthesis reactors (8,21) together with water vapor (55) from the process water (49), which is converted in the evaporator consisting of pump (52) and evaporator (53) to steam (54), through the process steam reforming to a gas

Steam mixture of carbon dioxide and hydrogen reformed. The reformer (30) is supplied with heat via (31) regulated in pressure and volume flow (32) and supplied to a heat exchanger (33) to cool the product gas and fed to the mixing chamber (17).

The condensate in the tank (26) is fed via a pump (27) and the associated pressure and volume flow regulator (28) of the first distillation stage (35). In the distillation stage dimethyl ether (DME) is separated from condensate, the dimethyl ether vapor (DME) is controlled in the pressure and volume flow (36) and fed to the condenser (37) and the dimethyl ether (DME) is stored liquefied in the tank (38). The heat is supplied to the distillation via the heat exchanger (40), the condensate is fed via the pump (39) and the regulator (41) to the second distillation stage (42), in which the separation of methanol from water takes place. In the second distillation stage (42) dimethyl ether (DME) is separated from condensate, the methanol vapor (MeoH) is controlled in the pressure and volume flow (43) and fed to the condenser (44) and the dimethyl ether (MeOH) is liquefied in the tank (45). stored. The distillation is supplied via the heat exchanger (47), the heat, the water as condensate via the pump (46) and the controller (48) fed to the tank (49). From the tank, the water, which is not used for steam reforming, is made available for further use via the pump (50).

The residual methanol recovered in the tank (45) is fed via the pump (56) and associated control (57) to the dehydration reactor (56) which is externally heated by the heat exchanger (59), the product gas of dimethyl ether (DME) and water is reduced in pressure via the throttle controller (60), and fed to the condenser (61). The condensate of dimethyl ether (DME), water (H 2 O) and methanol (MeOH) is stored in the tank (26).

Figure 4

Figure 4 shows the coupling of dimethyl ether synthesis reactors, the synthesis reactor (8) for weak gases consisting of carbon monoxide and hydrogen. The lean gas (l) usually consists of carbon monoxide (CO), hydrogen (H2) and carbon dioxide (C02) and accumulates at ambient pressure. The lean gas (l) is brought to the pressure with the compressor (2) and the carbon dioxide (C02) in the condenser (3) deposited as a liquid phase, the reduced lean gas is now heated again via the heat exchanger (4). Hydrogen (5) is fed into the mixer (6) and the weak gas is fed via the volume flow regulator (7) to the synthesis reactor (8). Since the reaction is exothermic, this reactor (8) is cooled with the heat exchanger (11). The product gas is brought to a lower pressure via the throttle regulator (9) and separated via the condenser (IO) into a condensate fraction of water, methanol and dimethyl ether and into a non-condensable fraction. The non-condensable portion is fed to the reformer (30). Liquid carbon dioxide (13) is throttled to a low pressure (14) and mixed with the liquid carbon dioxide from the condenser (3) (15) and heated via the heat exchanger (16). In addition, the product gas from the reformer (30) is added (17). The gas mixture of hydrogen and carbon dioxide is supplemented by hydrogen 18) in the mixer (19). The gas mixture is fed via the volume flow regulator (20) to the synthesis gas reactor (21), which is cooled by the heat exchanger (22). The product gas is brought to a low pressure via the throttle controller (23) and fed to the condenser (24). The condensate is collected in the tank (26). The non-condensable gases and vapors are fed to the reformer (30). In the reformer, these residual gases are first compressed via a compressor (34) to the pressure in the reformer (30) and regulated in volume flow and pressure (29). The compressed residual gases from the synthesis reactors (8,21) together with water vapor (55) from the process water (49), which is converted in the evaporator consisting of pump (52) and evaporator (53) to steam (54), via the method the steam reforming to a gas-vapor mixture of carbon dioxide and hydrogen reformed. The reformer (30) is supplied with heat via (31) regulated in pressure and volume flow (32) and supplied to a heat exchanger (33) to cool the product gas and fed to the mixing chamber (17).

The condensate in the tank (26) is fed via a pump (27) and the associated pressure and volume flow regulator (28) of the first distillation stage (35). In the distillation stage dimethyl ether (DME) is separated from condensate, the dimethyl ether vapor (DME) is controlled in the pressure and volume flow (36) and fed to the condenser (37) and the dimethyl ether (DME) is liquefied in the tank (38) stored. The heat is supplied to the distillation via the heat exchanger (40), the condensate is fed via the pump (39) and the regulator (41) to the second distillation stage (42), in which the separation of methanol from water takes place. In the second distillation stage (42) dimethyl ether (DME) is separated from condensate, the methanol vapor (MeoH) is controlled in pressure and Voiumenstrom (43) and fed to the condenser (44) and the dimethyl ether (MeOH) is liquefied in the tank (45) stored. The distillation is supplied via the heat exchanger (47), the heat, the water as condensate via the pump (46) and the controller (48) fed to the tank (49). From the tank, the water, which is not used for steam reforming, is made available for further use via the pump (50).

The hydrogen (5, 18) supplied to the mixers (6, 19) is generated from the process water (49) via the wet electrolysis. The process water is supplied with the pump (50) to the heat exchanger (64), regulated in the pressure (65) and the electrolysis (66) to hydrogen (67) and oxygen (68) converted.

Figure 5

Figure 5 shows the control of the gas concentration for the individual synthesis gas reactors (8,21). Regulation (70) ensures that the optimum gas composition for the synthesis gas reactors is input. The following sensors are used for control (70): - lean gas (t): concentration (71), volume flow (72), temperature (73), pressure (74) - lean gas (l) without carbon dioxide: concentration (75), volumetric flow (76), temperature (77), pressure (78) - hydrogen (S): concentration (79), volume flow (80), temperature (81), pressure (82) - hydrogen 18): concentration (83), volume flow ( 84), temperature (85), pressure (86) - residual gas from synthesis reactor (8):

Concentration (87), volume flow (88), temperature (89), pressure (90) - reforming gas from reforming reactor (30):

Concentration (91), volumetric flow (92), temperature (93), pressure (94) - Synthesis gas for synthesis reactor (21): concentration (95), volumetric flow rate (96), temperature (97), pressure (98) - residual gas synthesis reactor (21):

Concentration (99), volume flow (100), temperature (101), pressure (102) - water vapor (55): concentration (103), volume flow (104), temperature (105), pressure (106)

Figure 6

Figure 6 shows the formation of a synthesis gas reactor as slurry reactors in a vertical construction, wherein as a carrier liquid paraffin oil is used, in which the catalysts are registered. The gas enters the bottom of the reactor, the Produktgasastritt at the top of the reactor, the oil catalyst mixture is circulated by a pump and the heat extracted from the oil through a heat exchanger.

Figure 7

Figure 7 shows the formation of a synthesis gas reactor as a membrane reactor in a horizontal design. The catalysts are applied in a Trägermembam, which is porous and thus allow contact between the catalyst and the incoming gas, the product gas is passed through a separator with demister to separate condensate.

Symbols and symbols 1 Low carbon monoxide (CO), carbon dioxide (C02), hydrogen (H2) 2 gas compressor 3 condenser for carbon dioxide (C02) 4 low carbon heat exchanger consisting of carbon monoxide (CO) and hydrogen (H2) 5 hydrogen ( H2) 6 Mixing chamber lean gas (l) and hydrogen (H2) (5) 7 Pressure and volumetric flow controller 8 Synthesis gas reactor 9 Pressure and volumetric flow controller 10 Capacitor for Dimethy! Ether (DME), Water (H20), Methanol (MeOH) 11 Cooling of the Synthetic reactor (l) 12 Liquid condensate pressure and volumetric flow controller 13 Liquid carbon dioxide (C02) - Tank 14 Pressure and volumetric flow controller 15 Mixing chamber 16 Heat exchanger 17 Mixing chamber for synthesis gas from reformer (30) 18 Hydrogen 19 Mixing chamber 20 Pressure and volumetric flow controller 21 Synthesis gas reactor 22 Heat exchanger 23 for dimethyl ether (DME), water (H20), methanol (MeOH) Pressure and volumetric flow controller 24 Condenser for dimethyl ether (DME), water (H20), methanol (MeOH) 25 Pressure and volumetric flow controller 2 6 Condensate tank for dimethyl ether (DME), water (H20), methanol (MeOH) 27 Pump 28 Pressure and volumetric flow controller 29 Pressure and volumetric flow controller 30 Reformer reactor 31 Heat supply Reformer - Reactor 32 Pressure and volumetric flow controller 33 Heat exchanger 34 Gas compressor 35 Distillation for dimethyl ether (DME) 36 Pressure and volumetric flow controller 37 Condenser 38 Dimethyl ether tank 39 Pump 40 Heat exchanger 41 Pressure and volumetric flow controller 42 Distillations for methanol (MeoH) 43 Pressure and volumetric flow controller 44 Condenser 45 Methanol tank 46 Pump 47 Heat exchanger 48 Pressure and flow control Volume flow controller 49 Water tank (process water) 50 Pump 51 Oxygen (02) 52 Pump 53 Evaporator 54 Water vapor 55 Pressure and volume controller 56 Pump Methanol (MeOH) 57 Pressure and volume controller 58 Dehydration reactor 59 Heat supply Dehydration reactor 60 Pressure and volume controller 61 Condenser 62 Inert gases 63 Pressure and volumetric flow controllers 64 Heat exchangers 65 Pressure and volumetric flow controllers 66 Wet electrolyzer 67 Pressure and volume flow controller 68 Oxygen 69 Electrical energy for the wet Electrolyser 70 Regulator 71 Concentration (C0, C02, H2) 72 Flow 73 Temperature 74 Pressure 75 Concentration (CO, C02, H2) 76 Flow 77 Temperature 78 Pressure 79 Concentration (C0, C02> H2) 80 Volume flow 81 Temperature 82 Pressure 83 Concentration (C0, C02> H2) 84 Volume flow 85 Temperature 86 Pressure 87 Concentration (C0, C02, H2> CH4, C2H4) 88 Volume flow 89 Temperature 90 Pressure 91 Concentration (C0, C02> H2) 92 Volume flow 93 Temperature 94 Pressure 95 Concentration (C0, C02, H2) 96 Volume flow 97 Temperature 98 Pressure 99 Concentration (C0, C02, H2> CH4, C2H4) 100 Volume flow 101 Temperature 102 Pressure 103 Concentration ( H20) 104 Volume flow 105 Temperature 106 Pressure 107 Concentration (02) 108 Volume flow 109 Temperature 110 Pressure

Claims (8)

claims 1. The process for the production of dimethyl ether (DME) comprising a synthesis reactor for lean gas (8), the compressor (2), the carbon dioxide separator (3), the preheater (4), the mixer (6), controller (7) a synthesis reactor for synthesis gas (21), the throttle controller (9), the heat exchanger (IO), carbon dioxide tank (13), the regulator (14), the mixer (15), the heat exchanger (16) the mixer (17), the mixer (19 ), the regulator (20), the synthesis gas reactor (21), the controller (23), the heat exchanger (24), the compressor (34), the reforming reactor (3Q), the throttle controller (32), the heat exchanger (33), tank (26) Characterized in that - The lean gas (l) consists of a gas mixture of carbon dioxide (C02), carbon monoxide (CO), hydrogen (H2) - The lean gas (l) a concentration of carbon dioxide (C02), minimum 0% vol , maximum 20Vol%, preferably 12Vol% - The lean gas (1) accumulates with a pressure, minimum 0.01 barü, maximum 1 barü, preferably 0.25 barü, - The lean gas (l) has a temperature, minimum 10 C, maximum 40 ° C, preferably 25 ° C - The lean gas (1) via a compressor (2) is compressed to a minimum pressure of 30 barü, maximum 70 barü, preferably 50 barü - The compressor (2) designed as a hydraulic linear piston compressor - The compressed lean gas (l) is cooled to a temperature via the heat exchanger (3), minimum T = -10 ° C, T = 15 ° C, preferably T = 5 ° C - The carbon dioxide from the lean gas (l) at The reduced lean gas (l) after the heat exchanger (3) has a carbon dioxide concentration, minimum 0% by volume, at most 1% by volume, preferably 0.1% by volume, - The reduced lean gas ( l) is heated to a temperature via the preheater (4), minimum 25 ° C, maximum 150 ° C, preferably T = 100 ° C, - The reduced lean gas (l) hydrogen is added via the mixing chamber (6) to a to achieve a molar ratio of carbon monoxide (CO) to hydrogen (H2), minimum 1: 0.8, maximum 1: 1.25, preferably 1: 1 - The concentration moderately improved lean gas is passed to the mixing chamber via a volume flow regulator (7) to control the flow rate, minimum V = 1 Nm3 / h, maximum V = 1000 Nm3 / h, preferably V = 600 Nm3 / h - In the synthesis gas reactor ( 8) from the improved weak gas dimethyiether via direct synthesis by a mixture of catalysts is generated, the synthesis gas reactor (8) at a pressure of minimally p = 30barü, maximum p = 70 barü, preferably p = 50 barü is operated - The synthesis gas reactor (8 ) at a temperature of at least T = 200 ° C, a maximum of T = 300 ° C, preferably T = 250 ° C is operated, - The synthesis gas includes a mixture of catalysts, for the synthesis of methanol from CuO.ZnO and Al203, and for the Dehydration the zeolite HSMZ-5 - The product gas from the synthesis gas reactor (8) is throttled to a pressure with the throttle controller (9), minimum p = 10 barü, maximum p = 25barü, preferably p = 15barü - The product gas from the synthesis gas reactor (p ) cooled to a temperature is minimum T = 25 ° C, maximum T = 50 ° C, preferably T = 25 ° C - The product gas from the synthesis gas reactor (8) via the heat exchanger (10) is separated into a gas phase and liquid phase, - The liquid phase of the product gas from the synthesis gas reactor (8) consists of a mixture of Dimethyiether, methanol and water - The liquid phase of the product gas from the synthesis gas reactor (8) in the tank (26) is stored - the gaseous phase of the product gas from the synthesis gas reactor (8) the compressor (8 The gaseous phase of the product gas from the synthesis gas reactor (21) consists of the following components: carbon monoxide (CO), carbon dioxide (CO 2), hydrogen (H 2), methane (CH 4), ethane (C 2 H 4) - liquid carbon dioxide (CO 2) Tank (13) via the throttle controller (14) is expanded to a pressure, minimum p = 30 barü, maximum P = 60 barü, preferably p = 50barü - Liquid carbon dioxide (C02) from the lean gas (l) deposited in the heat exchanger (3) the carbon dioxide (13) in the mixer (15) zugefüh rt is, - the liquid carbon dioxide (C02) after the mixer (15) in the heat exchanger (16) is evaporated and has a minimum temperature T = 25 ° C, maximum 150 ° C, preferably T = 100 ° C - in the mixer (t7 ) the gaseous mixture from the Refomierungsreaktor (3Q) is supplied to the gaseous carbon dioxide (C02) from the heat exchanger (16) - fed to the gas mixture of carbon dioxide and hydrogen (H2) after the mixer (17) hydrogen (H2) in the mixing chamber (19) is to obtain a molar ratio of carbon dioxide (C02) to hydrogen (H2), minimum 1: 2.5, maximum 1: 3.5, preferably 1: 3 - The treated gas mixture of carbon dioxide and hydrogen via the volume flow controller (20 ) The volume flow controller regulates a volume flow of the treated gas mixture, minimum V = 1 Nm3 / h, maximum V = 2000 Nm3 / h, preferably V = 1000Nm3 / h - In the synthesis gas reactor (21) from the treated gas mixture from the mixer (19) dimethyl ether via direct synthesis by a mixture h is produced on catalysts, - The synthesis gas reactor (21) at a pressure of at least p = 30barü, maximum p = 7Q barü, preferably p = 50 barü is operated - The synthesis gas reactor (21) at a temperature of at least T = 200 ° C. , maximum T = 300 ° C, preferably T = 250 ° C is operated, - The synthesis gas includes a mixture of catalysts, for the synthesis of methanol from CuO.ZnO and ZrO2, and for dehydration the zeolite HSZM-5 - The product gas from the Synthesis gas reactor (21) is throttled to a pressure with the throttle controller (23), minimum p = 10 barü, maximum p = 25barü, preferably p = 15barü - The product gas from the synthesis gas reactor (21) is cooled to a minimum T = 25 ° C, maximum T = 50 ° C, preferably T = 25 ° C - The product gas from the synthesis gas reactor (21) via the heat exchanger (24) is separated into a gas phase and liquid phase, - The liquid phase of the product gas from the synthesis gas reactor (21) consists of a mixture of dimethyl ether, methanol and water - Di e liquid phase of the product gas from the synthesis gas reactor (21) in the tank (26) is stored - the gaseous phase of the product gas from the synthesis gas reactor (21) is supplied to the compressor (34) - The gaseous phase of the product gas from the synthesis gas reactor (21) consists of the following components: carbon dioxide, hydrogen, methane, ethane - The compressor (34) is designed as a hydraulically driven linear piston compressor - The reforming reactor (30) works on the basis of dry reforming with external oxygen (02) (51) Reformierungsreaktor (30) is operated with a pressure, minimum p = 30barü, maximum p = 50barü, preferably p = 50barü - The reforming reactor (30) is operated at a temperature, minimum T = 400 ° C, maximum T = 800 ° C, preferably T = 700 ° C - The reforming reactor (30) is operated with a Ni-based catalyst - The product gas from the reforming reactor (30) from carbon dioxide (C02) and hydrogen (H2 The product gas from the reforming reactor (30) is cooled to a temperature minimum T = 25 ° C, maximum T = 150 ° C, preferably T = 100 ° C ) is supplied 2. The method of claim 1 comprising the pump (52), the evaporator (53), the volume flow and pressure regulator (56), characterized in that - in the reforming reactor (30) the residual gas from the synthesis reactors (8,21) after the heat exchangers (10,24) is reformed by steam reforming to carbon dioxide (C02) and hydrogen (H2), - The steam for the reforming reactor (30) from the process water (49) obtained from the separation of the liquid phase from the synthesis reactors (8,21) stored in the tank (26) which is produced - the process water (49) is brought to an evaporation pressure with the pump, minimum p = 30 barü, maximum p = 70 barü, preferably p = 5Gbarü - in the heat exchanger (53) the process water (49) is evaporated, minimum T = ° C, maximum T = ° C, preferably T = ° C, - the process steam via the volumetric flow controller (55) is fed to the reforming reactor (30) - in the reforming reactor, the mixture of water vapor (H 2 O) and gas phases the synthesis gas reactors (8,21) to a Mixture of carbon dioxide and hydrogen is converted with a Ni-based catalyst 3. The method of claim 1 comprising the pump (56), the dehydration reactor (58), the throttle controller (60), the condenser (61), the volumetric flow controller (63), characterized in that - The methanol (45), the at the separation of the liquid phase from the heat exchanger (10,24) stored in the tank (45), in the streams dimethyl ether (38), methanol (45) and process water (49) - the methanol (45) with the pump (56 ) to a pressure, minimum p = 10 barü, maximum p = 70 barü, preferably p = 50 barü - The methanol (45) is supplied via the pressure and volume flow regulator (57) the dehydration reactor (58), with a minimum V flow rate = 0.1 Nm3 / h, maximum V = 50 Nm3 / h, preferably V = 1 Nm3 / h - In the dehydration reactor (58) the methanol (45) is converted into a gas mixture of dimethyl ether (DME), water vapor (H20) and methanol ( MeOH) converted by means of a catalyst, - The dehydration reactor (58) is operated at a temperature of at least T = 200 ° C, maximum T = 500 ° C, preferably T = 250 ° C - De Hydrogenation reactor (58) the catalyst HSZM-5 is used - The gas mixture is fed via the throttle controller (60) to the heat exchanger (61) - The gas mixture is throttled with the throttle controller (60) to a minimum pressure p = 10barü, maximum p = 30barü , preferably p = 15barü - The gas mixture is cooled in the heat exchanger (61) to a temperature, minimum T = 10 ° C, maximum T = 50 ° C, preferably T = 25 ° C and fed as liquid phase to the tank (26) 4. The method of claim 1 comprising the pump (5Q), the heat exchanger (64), the pressure regulator (65), the electrolyzer (66), the volumetric flow controller (67), characterized in that - The hydrogen (5,18) from The process water (49) is brought to a pressure via the pump (50), minimum p = 30 barü, maximum p = 70 barü, preferably p = 5Q barü, - Das Process water (49) is then heated with a heat exchanger (64) and has a minimum temperature T = 25 ° C, maximum T = 95 ° C, preferably T = 85 ° C - The electrolyzer (66) is based on the wet process operated with the liquor KOH to improve the conductivity - The electrical energy (69) is supplied externally and is for the generation of hydrogen (H2) minimal P = 3,1kWh / Nm3 H2, maximum P = 5 kWh / Nm3 H2, preferably P = 4.1 kWh / Nm3 H2 - The product gas hydrogen (H2) from the electrolyzer (66) is led through a volume flow controller (67), minimum V = 1Nm3 / h, maxima l V = 1000 Nm3 / h, preferably V = 250 Nm3 / h - The product gas hydrogen (H2) from the electrolyzer (66) is the volumetric flow regulator (5.18) the lean gas (l) in the mixer (6) and the synthesis gas (13) supplied in the mixer (19) - The resulting in the electrolysis (66) oxygen (68) is supplied in the process of dry reforming of the reforming reactor (30). 5. The method of claim 1 comprising the controller (70) and the encoder (71), (75), the encoder (79) characterized in that the concentration measurement (71) of the components carbon monoxide (CO), hydrogen (H2) and carbon dioxide The concentration measurement (75) of the substance components carbon monoxide (CO), hydrogen (H2) and carbon dioxide (C02) of the lean gas (l) are recorded after the deposition of carbon dioxide (C02) Measuring data of the sensors (71,75) is the proportion of hydrogen (H2) measuring sensor (79) supplied in the mixer (6) is controlled so that the molar ratio of carbon monoxide (CO) and hydrogen (H2) after the mixer the value minimum 1 : 0.8, at most 1: 1.2 and preferably 1: 1 6. The method of claim 1 comprising the controller (70) and the encoder (91), the encoder (95) and the encoder (83) characterized in that the concentration measurement (91) of the substance components carbon dioxide (C02), hydrogen (H2) The concentration measurement (95) of the substance components carbon dioxide (C02), hydrogen (H2) of the synthesis gas from the mixer (17) are detected based on the measurement data of the encoder (91 , 95) the proportion of hydrogen (H2) measuring sensor (83) which is supplied in the mixer (19) is controlled so that the molar ratio of carbon dioxide (C02) and hydrogen (H2) after the mixer (19) the value minimum 1: 2 , 5, at most 1: 3.5 and preferably 1: 3 7. The method of claim 1 comprising the controller (70) and the encoder (99), encoder (87) and the encoder (103) characterized in that the concentration measurement (99) of the substance components carbon dioxide (CO), methane (CH4) and Ethan (C2H4) of the gaseous components from the product gas of Synthegasreaktors (21) from the heat exchanger (24) are detected, the concentration measurement (87) of the components carbon dioxide (CQ), methane (CH4) and ethane (C2H4) of the gaseous fractions of the Product gas of the lean gas reactor (8) can be detected from the heat exchanger (10), Based on the measured data of the encoder (99,87) the proportion of water vapor (H20) encoder (103) of the refining reactor (30) is supplied, is regulated so that the oxyidizable substances carbon monoxide (CO), methane (CH4) and ethane (C2H4) are completely converted to carbon dioxide (C02) and hydrogen (H2) and residual concentrations of methane (CH4), ethane (C2H4) and carbon monoxide (CO) remain minimal V = 0%, maximum V = 0.1 vol%, be preferably V = 0% 8. The method of claim 1 comprising the controller (70) and the encoder (99), encoder (87) and the encoder (107) characterized in that the concentration measurement (99) of the substance components carbon dioxide (CO), methane (CH4) and Ethan (C2H4) of the gaseous components from the product gas of the Synthegasreaktors (21) from the heat exchanger (24) are detected, the concentration measurement (87) of the components carbon dioxide (CO), methane (CH4) and ethane (C2H4) of the gaseous fractions from the Product gas of the lean gas reactor (8) can be detected from the heat exchanger (IO), Based on the measured data of the encoder (99,87) the proportion of oxygen (02) (68) encoder (107) of the refom reactor (30) is supplied, so regulated that the carbon monoxide (CO), methane (CH4) and ethane (C2H4) are completely converted to carbon dioxide (C02) and hydrogen (H2) and residual concentrations of methane (CH4), ethane (C2H4) and carbon monoxide (CO ) remain minimal V = 0%, maximum V = 0.1Vol%, preferably V = 0%