JP4801939B2 - Dimethyl ether reforming system and operating method thereof - Google Patents

Description

  The present invention relates to, for example, a dimethyl ether reforming system including a reformer that converts dimethyl ether into hydrogen-rich gas using exhaust heat from a prime mover, and an operation method thereof.

In recent years, dimethyl ether (DEM; CH ₃ OCH ₃ ) has attracted attention as a light oil alternative fuel, but this dimethyl ether can generate a steam reforming reaction and generate hydrogen by using an appropriate catalyst. This reaction is an endothermic reaction, and a highly efficient power generation system can be constructed in combination with exhaust heat recovery of a gas turbine (see, for example, Patent Document 1).

In this power generation system, a reformer filled with a copper / zinc-based catalyst having a heat-resistant temperature of about 350 ° C. is used. Therefore, a superheater or an evaporator for adjusting the temperature of the exhaust gas from a gas turbine of about 550 ° C. Had to be installed in front of the reformer. And the temperature of the exhaust_gas | exhaustion from a gas turbine was adjusted with the superheater, the evaporator, etc., and the temperature in a reformer was controlled to 250-400 degreeC. In this power generation system, the supply molar flow rate ratio of water vapor to dimethyl ether is set in the range of 3 to 15 in consideration of the thermal efficiency of the gas turbine alone.
JP 2004-144018 A

  In the power generation system equipped with the conventional steam reforming mechanism of dimethyl ether, the temperature of the exhaust from the gas turbine at about 550 ° C. is reduced to about 250 to 400 ° C. because a copper / zinc-based catalyst is used in the reformer. The temperature adjusting device to be used has to be an indispensable configuration, and the configuration and control of the system are complicated. It is also conceivable to perform steam reforming of dimethyl ether using a noble metal catalyst having a higher heat resistance temperature than that of a copper / zinc catalyst. For example, the temperature of the reformed gas and the mixing ratio of dimethyl ether and steam are optimal. Operating conditions were not clear.

  Accordingly, in order to solve the above problems, the present invention uses a noble metal catalyst as a catalyst, and includes a reformer capable of directly exchanging heat with the exhaust from the prime mover, and is capable of operating the system under optimum conditions. An object of the present invention is to provide a reforming system and an operation method thereof.

To achieve the above object, dimethyl ether reforming system of the present invention, the prime mover and, as 3-9 molar feed flow rate of steam to feed molar flow rate of dimethyl ether, it is formed by combined mixed and the said dimethyl ether vapor and the mixed gas, via a catalytic noble metal-based e Bei a reformer for conversion to reformed gas by the exhaust heat from the prime mover, the temperature of the reformed gas is four hundred thirty to four hundred and seventy ° C., and the modified The LHV heat increase rate indicating the ratio of the lower calorific value of the gas to the lower calorific value of the dimethyl ether before reforming is 6% or more.

The method of operating dimethylether reforming system of the present invention, as 3-9 molar feed flow rate of steam to feed molar flow rate of dimethyl ether, the combined mixed and the said dimethyl ether vapor, a mixed gas forming a gas mixture , the mixed gas and a reforming step for converting the reformed gas at a temperature of 430-470 ° C. the waste heat from the prime mover through the catalyst noble metal, the lower heating value of the reformed gas before modification The LHV heat increase rate which shows the ratio increased with respect to the low calorific value of the dimethyl ether is 6% or more.

According to the dimethyl ether reforming system and the operation method of the dimethyl ether reforming system, chemical exhaust heat recovery is achieved by using a noble metal catalyst and setting the operating conditions within a reformed gas temperature range of 430 to 470 ° C. The amount can be maximized and the thermal efficiency in the system can be greatly improved.

According to the method of operating these dimethyl ether reforming system and dimethyl ether reforming system, by setting the operating conditions in the range of 3 to 9 molar feed flow rate of steam to the feed molar flow of di-methyl ether, chemical The amount of exhaust heat recovery can be maximized and the thermal efficiency of the system can be greatly improved.

  According to the dimethyl ether reforming system and the operation method thereof of the present invention, a noble metal catalyst is used as a catalyst, a reformer capable of directly exchanging heat with the exhaust from the prime mover is provided, and the system can be operated under optimum conditions. .

  Hereinafter, a dimethyl ether reforming power generation system 10 according to an embodiment of the dimethyl ether reforming system of the present invention will be described with reference to the drawings.

  FIG. 1 is a diagram showing an outline of a dimethyl ether reforming power generation system 10.

  As shown in FIG. 1, the dimethyl ether reforming power generation system 10 mainly includes a prime mover 100, a reformer 200, an evaporator 300, and a dimethyl ether vaporizer 400.

  Connected to the dimethyl ether vaporizer 400 are a dimethyl ether supply pipe 402 for supplying liquid dimethyl ether 401 and a dimethyl ether outlet pipe 404 for guiding the dimethyl ether 403 vaporized by the dimethyl ether vaporizer 400 to the reformer 200. A water supply pipe 302 that supplies water 301 and a steam outlet pipe 304 that guides the steam 303 generated in the evaporator 300 to the dimethyl ether outlet pipe 404 are joined to the evaporator 300. The reformer 200 is joined with a reformed gas outlet pipe 202 that guides the reformed gas 201 to the combustor 102 of the prime mover 100.

  The prime mover 100 is mainly composed of a compressor 101, a combustor 102, and a turbine 103. The compressor 101 compresses the atmosphere 104 and supplies the compressed air to the combustor 102. In the combustor 102, combustion is performed by the compressed air supplied from the compressor 101 and the hydrogen-rich (hydrogen-rich) reformed gas 201 reformed by the reformer 200 to generate combustion gas. The high-temperature and high-pressure combustion gas generated in the combustor 102 is supplied to the turbine 103, and the turbine 103 is rotationally driven to be exhausted.

The reformer 200 uses the exhaust heat exhausted from the turbine 103 to convert the mixed gas of the dimethyl ether 403 vaporized by the dimethyl ether vaporizer 400 and the steam 303 generated by the evaporator 300 into a hydrogen-rich reformed gas 201. It is to be modified. The exhaust heat from the turbine 103 is transmitted to the reforming reaction section through, for example, a heat exchanger. In addition, for example, an alumina-supported noble metal catalyst that is a noble metal catalyst is mounted in the reforming reaction section, and a reforming reaction is caused through this catalyst. Examples of the alumina-supported noble metal catalyst include a catalyst in which platinum (Pt) or palladium (Pd) is supported on a γ-alumina (γ-Al ₂ O ₃ ) support. Note that the precious metal catalyst is not limited to these, and even when the exhaust heat from the turbine 103 is directly used, the catalyst is sufficiently thermally resistant and promotes the steam reforming reaction of dimethyl ether. Anything can be used.

  The evaporator 300 applies the exhaust heat from the turbine 103 from which part of the heat amount has been recovered by the reformer 200 to, for example, water 301 supplied to the evaporator 300 via a heat exchanger, and evaporates the water 301. It is something to be made.

  The dimethyl ether vaporizer 400 gives the exhaust heat from the turbine 103 from which a part of the amount of heat has been recovered by the evaporator 300 to, for example, the liquid dimethyl ether 401 supplied to the dimethyl ether vaporizer 400 via a heat exchanger. It is something to be made.

  Next, the operation of the dimethyl ether reforming power generation system 10 will be described.

  As shown in FIG. 1, the exhaust from the turbine 103 is subjected to heat exchange in the order of the reformer 200, the evaporator 300, and the dimethyl ether vaporizer 400. At that time, the temperature of the exhaust gas from the turbine 103 is, for example, about 550 to 400 ° C. at the stage of the reformer 200, about 400 to 200 ° C. at the stage of the evaporator 300, and 200 to 150 ° C. at the stage of the dimethyl ether vaporizer 400. For example, it is exhausted to the atmosphere at a temperature of about 150 to 100 ° C. or higher. In addition, these temperature ranges are illustrations and are not limited to these ranges.

  The liquid dimethyl ether 401 supplied to the dimethyl ether vaporizer 400 by a pressurizer 500 such as a pump is heated and vaporized to become gaseous dimethyl ether 403. The gaseous dimethyl ether 403 flows through the dimethyl ether outlet pipe 404 toward the reformer 200.

  Water 301 supplied to the evaporator 300 by a pressurizing machine 501 such as a pump is heated and evaporated to become a vapor 303. The steam 303 flows through the steam outlet pipe 304 and flows into the dimethyl ether outlet pipe 404 in the vicinity of the reformer 200. The steam 303 that has flowed out into the dimethyl ether outlet pipe 404 is mixed with the dimethyl ether 403 flowing through it, and flows into the reformer 200 as a mixed gas. Here, in order to promote mixing of the dimethyl ether 403 and the steam 303 on the downstream side of the portion of the dimethyl ether outlet pipe 404 into which the steam 303 is introduced, for example, it is preferable to include a mixing promoting member such as a mixer.

  In addition, although the structure which introduce | transduces the vapor | steam 303 into the dimethyl ether extraction piping 404 near the reformer 200 was employ | adopted here, it is not restricted to this structure. For example, dimethyl ether 403 and steam 303 may be separately supplied to the reformer 200 and mixed in the reformer 200. In this case, in order to mix dimethyl ether 403 and steam 303 uniformly, it is preferable to provide a mixing promoting member such as a mixer in the reformer 200.

Subsequently, the mixed gas flowing into the reformer 200 undergoes a dimethyl ether steam reforming reaction represented by the following formula (1) by exhaust heat from the turbine 103 via a noble metal catalyst, and a hydrogen-rich reforming It is converted to gas 201. The reformed gas 201 converted to the hydrogen-rich reformed gas 201 is supplied to the combustor 102.
_{C 2 H 6 O + 3H 2} O ⇔ 6H 2 + 2CO 2 -122kJ / mol ... formula (1)

Note that the reaction of the above formula (1) does not directly occur, but sequentially proceeds through methanol by dimethyl ether hydrolysis of the following formula (2), and further causes the methanol decomposition reaction of the following formula (3). It is a reaction.
_{C 2 H 6 O + H 2} O ⇔ 2CH 3 OH-23.6kJ / mol ... formula (2)
CH ₃ OH⇔CO + 2H ₂ −90.76 kJ / mol (3)

  Here, the reactions of the above formulas (2) and (3) are both endothermic reactions, and exhaust heat is chemically recovered, so that power generation efficiency can be improved.

On the other hand, carbon monoxide (CO) undergoes a shift reaction of the following formula (4), and is in a chemical equilibrium state with hydrogen (H ₂ ) and carbon dioxide (CO ₂ ).
CO + H ₂ O⇔H ₂ + CO ₂ +41 kJ / mol (4)

Furthermore, the methane formation reaction of the following formula (5) is also likely to occur.
CO + 3H ₂ ＣＨCH ₄ + H ₂ O + 206 kJ / mol (5)

  Here, since the reactions of the above-described formulas (4) and (5) are both exothermic reactions, exhaust heat cannot be recovered, and improvement in power generation efficiency cannot be expected. Therefore, it is necessary to obtain a reformed gas composition that suppresses the reactions of formulas (4) and (5) as much as possible and maximizes the amount of chemical heat recovery. For this purpose, it is necessary to set the reaction conditions such as the reformed gas temperature and the value of the supply molar flow rate of the steam 303 relative to the supply molar flow rate of the dimethyl ether 403 in the mixed gas (hereinafter referred to as S / DME) within the optimum range. It becomes.

  Therefore, in the present invention, the reformed gas temperature is set to 370 to 530 ° C. The reason why the reformed gas temperature is within this range is that a preferable LHV heat increase rate cannot be obtained at temperatures outside this range, that is, below 370 ° C. and above 530 ° C. The reformed gas temperature at the catalyst outlet is more preferably 400 to 500 ° C., and the reformed gas temperature at the catalyst outlet is more preferably 430 to 470 ° C. Here, the reformed gas temperature refers to the temperature of the reformed gas at the catalyst outlet, but it is sufficient to have a device configuration in which the reforming reaction is performed in the reformer 200 substantially in these temperature ranges. is there. The LHV heat increase rate, which will be described in detail later, indicates the ratio of the lower heating value of the reformed gas to the lower heating value of the dimethyl ether before the reforming. Here, from the viewpoint of improving the power generation efficiency by 1 point or more, the preferable LHV heat increase rate is set to 6% or more.

  In the present invention, S / DME is set to 3-9. The S / DME is set within this range. When the ratio is below 3, steam becomes insufficient, black carbon is deposited on the surface of the catalyst, and the activity of the catalyst is remarkably reduced. Because you can't. As described above, the preferred LHV heat increase rate is 6% or more. Further, since S / DME is preferably 3 or more and close to 3, it is more preferable to set S / DME to 3-6, and even more preferable to set S / DME to 3-4.

  As described above, in the dimethyl ether reforming power generation system 10, the noble metal catalyst is used, the reforming gas temperature is set in the range of 370 to 530 ° C., and the S / DME is set in the range of 3 to 9. The amount of exhaust heat recovery can be maximized and the power generation efficiency can be greatly improved. Furthermore, since the exhaust heat of the turbine is used in the reformer 200, the evaporator 300, and the dimethyl ether vaporizer 400, the power generation efficiency can be improved. In the reformer 200 using a noble metal catalyst as the catalyst, the exhaust from the turbine 103 can be directly heat-exchanged, so that the system configuration and control can be simplified.

  In the following examples, it will be described that the set reformed gas temperature range and S / DME range are suitable.

  First, in Example 1, it will be described with reference to the drawings that the reformed gas temperature is preferably set in the range of 370 to 530 ° C. In the second embodiment, the fact that it is preferable to set S / DME in the range of 3 to 9 will be described with reference to the drawings.

Example 1
Table 1 shows noble metal species, noble metal loadings, and carrier species for the four types of catalysts (catalyst A to catalyst D) tested in Example 1.

  In the test in Example 1, about 3.6 g of catalyst pellets in the quartz tube and the quartz packing before and after the catalyst pellet are mixed, and a mixed gas mixed so that S / DME becomes 3 is supplied to the quartz tube. did. The pressure condition was 0.4 MPa (gauge pressure). For each catalyst, measurement of the heat increase rate (LHV heat increase rate) of the lower heating value (LHV) when the temperature at a predetermined point inside the catalyst packed bed is 350 ° C., 400 ° C., 450 ° C., 500 ° C., 550 ° C. Went. The temperature at a predetermined point inside the catalyst packed bed was measured with a thermocouple and controlled with a PID controller so that the temperature would be the set temperature described above. Here, since the amount of the catalyst is very small and the heater heat supply has a sufficient margin for the reaction heat, the temperature at a predetermined point in the catalyst packed bed can be the same as the catalyst outlet temperature.

Here, the LHV heat increase rate (%) is calculated using the following equation (6).
LHV heat increase rate = {(reformed gas LHV × reformed gas outlet flow rate) / (dimethyl ether LHV × dimethyl ether supply flow rate) −1} × 100 (6)

  FIG. 2 shows the relationship between the temperature inside the catalyst packed bed and the LHV heat increase rate when the catalysts A to D are used.

  From the measurement results shown in FIG. 2, it was found that the LHV heat increase rate changes with a peak with respect to the temperature inside the catalyst packed bed. In addition, as described above, from the viewpoint that the power generation efficiency is improved by 1 point or more, the LHV heat increase rate is preferably 6% or more, and the temperature inside the catalyst packed bed that satisfies it, that is, reforming of the catalyst outlet The gas temperature was found to be 370-530 ° C. Furthermore, it turned out that a higher LHV heat increase rate can be obtained in the temperature range of 400-500 degreeC. Moreover, it turned out that the temperature range in which the LHV heat increase rate in each catalyst shows a peak is 430-470 degreeC.

Next, when the catalyst B was used, the reformed gas at the quartz tube outlet at each temperature described above was sampled at 200 ° C., and the component composition was quantified by gas chromatography based on calibration with an external standard gas. The analyzed components are seven components of hydrogen (H ₂ ), methane (CH ₄ ), carbon monoxide (CO), carbon dioxide (CO ₂ ), methanol (CH ₃ OH), dimethyl ether (DME) and water vapor. In addition, the supply gas was mixed with a small amount of pure nitrogen whose flow rate is known as an internal standard, and the flow rate of each component was determined by simultaneously quantifying with the same gas chromatograph.

FIG. 3 shows the relationship between the temperature inside the catalyst packed bed and the component composition of the reformed gas.
From the measurement results shown in FIG. 3, as the temperature increased, the residual amount of dimethyl ether decreased, and dimethyl ether was not detected when the temperature was 500 ° C. or higher. As in the case of dimethyl ether, the residual amount of methanol decreased with increasing temperature, and it was found that the reactions of the above formulas (2) and (3) proceeded.

  However, it has been found that with increasing temperature, the mole fraction of methane that decreases the amount of chemical heat recovery increases. This is presumed to be due to the fact that methane, which should decrease at high temperatures in equilibrium, increased as a result of an increase in reaction rate according to the Arrhenius law. In hydrogen, carbon monoxide and carbon dioxide, the equilibrium law was dominant with respect to the temperature change, and the concentration of hydrogen and carbon monoxide showed a peak when the temperature was around 450 ° C.

  Considering that the reactions of the above-mentioned formulas (2) and (3), which are endothermic reactions, have already been completed, and that the amount of recovered chemical exhaust heat decreases with an increase in the exothermic reaction, the catalyst B is used. It was found that the amount of chemical heat recovery increased most when the temperature inside the catalyst packed bed, that is, the temperature of the reformed gas at the catalyst outlet was around 450 ° C. Further, the temperature at which the amount of chemical heat recovery is most increased (around 450 ° C.) is the same as the temperature indicating the peak value of the LHV heat increase rate calculated by the equation (6) when using the catalyst B described above. . In practice, it is difficult to always set the set temperature to a constant value. Therefore, taking into account some temperature fluctuations, for example, 430 ° C. to 470 ° C. centering on the temperature of 450 ° C. showing this peak value. It is preferable that the range of the degree is an optimum range.

  In addition, although the LHV heat increase rate and the component composition based on the experiment conducted under the pressure condition of 0.4 MPa (gauge pressure) were shown here, the pressure was changed from normal pressure to 2.0 MPa, and the other Even in tests conducted under pressure conditions, the optimum temperature range did not deviate significantly.

  As described above, a dimethyl ether reforming power generation system that uses a noble metal catalyst and has a reformed gas temperature of 370 to 530 ° C. to maximize the amount of chemical exhaust heat recovery and greatly improve power generation efficiency. It became clear that

(Example 2)
In Example 2, the catalyst B shown in Table 1 was used to increase the LHV in the same manner as in Example 1 for three mixed gases having S / DME of 3.0, 5.7, and 8.4. The heat rate was calculated and the component composition of the reformed gas was measured. The pressure condition was 0.4 MPa (gauge pressure), and the temperature at a predetermined point inside the catalyst packed bed of the catalyst B was 450 ° C.

  FIG. 4 shows the relationship between S / DME and LHV heat increase rate. FIG. 5 shows the relationship between S / DME and the component composition of the reformed gas. In addition, the component composition shown by FIG. 5 is a dry component except water vapor | steam.

  As S / DME increased, the methane formation reaction of the above formula (5) was suppressed and methane formation was expected to decrease. However, as shown in FIG. 5, methane did not decrease, and its molar fraction changed little. I did not. In addition, carbon monoxide is decreased and carbon dioxide is increased. This is considered to be because the equilibrium is shifted so that hydrogen and carbon dioxide are generated according to the above-described equation (4). In the formula (4), when the reaction for generating hydrogen and carbon dioxide, that is, the reaction to the right side of the formula (4) proceeds, the reaction is an exothermic reaction, so the LHV heat increase rate decreases. Furthermore, the LHV heat increase rate also decreases due to a decrease in carbon monoxide and an increase in unreacted dimethyl ether.

  As shown in FIG. 4 and FIG. 5, when S / DME is increased, the above-described LHV heat increase rate is decreased, the reaction of generating hydrogen and carbon dioxide of formula (4) is promoted, and carbon monoxide is decreased. As a result, the LHV heat increase rate decreased from 10.2% to 6.5% with increasing S / DME. In addition, although the LHV heat increase rate of 6% or more which is a preferable range of the above-mentioned LHV heat increase rate is not illustrated, S / DME was satisfied up to about 9. In addition, the dimethyl ether reforming power generation system 10 is provided with a control system that keeps the amount of steam constant. However, in actual operation, it is predicted that the flow rate will be temporarily unstable. It is preferable to have a margin of about 9. Moreover, under the condition of steam shortage where the value of S / DME is less than 3 which is the stoichiometric ratio of the formula (1), black carbon is deposited on the catalyst surface, and the activity of the catalyst is remarkably deteriorated.

  From the above results, it was found that a smaller water vapor amount, that is, a smaller S / DME value is desirable for increasing the chemical heat recovery amount, and a S / DME range of 3 to 9 is preferred. Further, it was found that the S / DME of 3 is preferable in the range. However, since it is conceivable that fluctuations occur when S / DME is controlled in an actual machine, S / DME is more preferably 3 to 6, and even more preferably S / DME is in the range of 3 to 4. Good.

  Although the results are not shown, the same tendency as the above results was obtained in the test when the pressure was 2 MPa.

  As described above, by using a noble metal catalyst and setting S / DME to 3 to 9, a dimethyl ether reforming power generation system capable of maximizing chemical exhaust heat recovery and greatly improving power generation efficiency is obtained. It became clear that

(Other embodiments)
Here, a dimethyl ether reformed power generation system 20 of another embodiment different from the configuration of the dimethyl ether reformed power generation system 10 will be described with reference to the drawings. In addition, the same code | symbol is attached | subjected to the part same as the structure of the dimethyl ether reforming electric power generation system 10, and the overlapping description is simplified or abbreviate | omitted.

  In the dimethyl ether reforming power generation system, the exhaust temperature from the turbine 103 may be higher than the temperature required in the reformer 200 by, for example, 100 ° C. or more. In such a case, it is preferable to provide a superheater between the turbine 103 and the reformer 200 so that the temperature of the reformer 200 becomes appropriate. Here, the dimethyl ether reforming power generation system 20 configured to include the superheater 600 so as to cope with such a case will be described.

FIG. 6 is a diagram showing an outline of the dimethyl ether reforming power generation system 20.
As shown in FIG. 6, the dimethyl ether reforming power generation system 20 mainly includes a prime mover 100, a reformer 200, an evaporator 300, a dimethyl ether vaporizer 400 and a superheater 600.

  In the dimethyl ether reforming power generation system 20, the steam outlet pipe 304 that leads the steam 303 generated in the evaporator 300 to the dimethyl ether outlet pipe 404 is branched, and the other end of the branched steam outlet pipe 304 a is joined to the superheater 600. Yes. The superheater 600 is joined with a superheated steam outlet pipe 602 that guides the superheated steam 601 heated by the superheater 600 to the combustor 102 of the prime mover 100.

  The superheater 600 uses the exhaust heat from the turbine 103 to heat the steam 303 supplied to the superheater 600 to form superheated steam 601.

  The dimethyl ether reforming power generation system 20 can be operated to control the amount of steam to the reformer 200 so that S / DME becomes 3 to 9, and to send the remaining steam to the superheater 600. The superheated steam 601 superheated by the superheater 600 is supplied to the combustor 102 through the superheated steam outlet piping 602. In addition, in the evaporator 300, it is possible to generate the vapor | steam equivalent to about 15 by S / DME.

  Thus, by providing the superheater 600, it is possible to supply exhaust heat at an appropriate temperature to the reformer 200, and to use the superheated steam 601 superheated by the superheater 600 in the combustor 102. it can.

  As described above, in the dimethyl ether reforming power generation system 20, the noble metal catalyst is used, the reforming gas temperature is set in the range of 370 to 530 ° C., and the S / DME is set in the range of 3 to 9. The amount of exhaust heat recovery can be maximized and the power generation efficiency can be greatly improved. Furthermore, since the exhaust heat of the turbine is used in the superheater 600, the reformer 200, the evaporator 300, and the dimethyl ether vaporizer 400, the power generation efficiency can be improved.

  The dimethyl ether reforming power generation system 20 described above has a configuration in which the superheated steam 601 is supplied to the combustor 102 via the superheater 600. For example, when it is not necessary to pass the superheater 600, that is, When the exhaust heat from the turbine 103 can be directly supplied to the reformer 200, steam that is not used for the mixed gas generated in the evaporator 300 may be supplied directly to the combustor 102. Further, when the exhaust heat from the turbine 103 can be directly supplied to the reformer 200, the evaporator 300 evaporates the water 301 necessary for forming the mixed gas, and does not introduce steam into the superheater 600. Also good. In these cases, the exhaust heat from the turbine 103 may be supplied to the reformer 200 without passing through the superheater 600 in order to prevent the superheater 600 from deteriorating.

  Here, in the above-described embodiment, the dimethyl ether reforming power generation system 10 including a gas turbine as a prime mover has been described. However, the application of the dimethyl ether reforming system of the present invention is not limited to this. For example, the dimethyl ether reforming system of the present invention can be applied to power for driving a ship.

The figure which shows the outline | summary of the dimethyl ether reforming electric power generation system of one embodiment of this invention. The figure which shows the relationship between the temperature inside a catalyst packed bed, and a LHV heat increase rate. The figure which shows the relationship between the temperature inside a catalyst packed bed, and the component composition of reformed gas. The figure which shows the relationship between S / DME and a LHV heat increase rate. The figure which shows the relationship between S / DME and the component composition of reformed gas. The figure which shows the outline | summary of the dimethyl ether reforming electric power generation system of other embodiment of this invention.

Explanation of symbols

  DESCRIPTION OF SYMBOLS 10 ... Dimethyl ether reforming power generation system, 100 ... Prime mover, 101 ... Compressor, 102 ... Combustor, 103 ... Turbine, 104 ... Atmosphere, 200 ... Reformer, 201 ... Reformed gas, 202 ... Reformed gas outlet piping, 300 DESCRIPTION OF SYMBOLS ... Evaporator 301 ... Water, 302 ... Water supply piping, 303 ... Steam, 304 ... Steam outlet piping, 400 ... Dimethyl ether vaporizer, 401 ... Liquid dimethyl ether, 402 ... Dimethyl ether supply piping, 403 ... Evaporated dimethyl ether, 404 ... Dimethyl ether outlet pipe, 500, 501, pressurizer.

Claims (2)

Prime mover,
Kai as 3-9 molar feed flow rate of steam to feed molar flow rate of dimethyl ether, a mixed gas formed by the said and the dimethyl ether steam combined mixed by exhaust heat from the prime mover through the catalyst noble metal for example Bei a reformer to convert to quality gas,
The temperature of the reformed gas is 430 to 470 ° C., and the LHV heating rate indicating the ratio of the lower heating value of the reformed gas increasing with respect to the lower heating value of the dimethyl ether before reforming is 6% or more A dimethyl ether reforming system characterized by As 3-9 molar feed flow rate of steam to feed molar flow rate of dimethyl ether, and the said dimethyl ether steam combined mixed, a mixed gas forming a gas mixture,
A reforming step of converting the mixed gas into a reformed gas having a temperature of 430 to 470 ° C. by exhaust heat from a prime mover through a noble metal catalyst,
A method for operating a dimethyl ether reforming system, characterized in that an LHV heat increase rate indicating a ratio of an increase in the lower calorific value of the reformed gas with respect to the lower calorific value of the dimethyl ether before reforming is 6% or more.

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