KR20070033031A - Gas reforming equipment - Google Patents

Abstract

Low calorie gas can be reformed as a fuel for stable gas turbines. To prepare a reformed gas containing hydrogen gas by providing a natural gas (NG) supply line (7) and an air supply line (8), by mixing NG gas and air, and chemically reacting the mixed gas to reform. Reforming gas production apparatus 3 having a reaction vessel for mixing, low-calorie gas and the reforming gas supplied from the reforming gas production apparatus 3, the mixing regulator for supplying as a fuel gas to the gas turbine equipment (1) (5), a reformed gas supply passage 4 for supplying a reformed gas from the reformed gas production device 3 to the blending control device 5, and a gas turbine installation 1 from the blending control device 5 And a fuel gas supply passage 2 for supplying fuel gas to the fuel cell), and a control device 10 for controlling the operations of the reformed gas production apparatus 3 and the mixing regulator 5.

Gas, reforming, turbine, fuel, mixing, air, steam, natural gas

Description

Gas Reforming System {GAS REFORMING SYSTEM}

The present invention relates to a gas reforming plant. More specifically, the low calorie gas (for example, blast furnace gas (BFG) and other steelmaking by-product gas) as the fuel of the gas turbine, in order to enable continuous stable combustion, the low calorie The present invention relates to a gas reformer that adjusts a gas component or a gas calorie of a fuel gas by additionally adding a reformed gas to the gas.

Background Art Conventionally, examples of low-calorie gas use have increased the use of by-product gas such as BFG as a fuel for gas turbines in steelmaking, for example, to generate electricity. On the other hand, since the energy efficiency in a furnace is improving, the heat generation amount of BFG as process exhaust gas is decreasing year by year. When such a low calorie furnace gas is used as a fuel, misfire of a gas turbine easily occurs, and when a misfire occurs, the gas turbine is urgently stopped. In addition, in the case of BFG having a low hydrogen content, ignition flame resistance is poor, and thus it is likely to become a fired state. In addition, the low calorie gas may vary in its characteristics, calorific value, generation amount, and the like.

In order to solve this problem, it is proposed to increase the calorific value and the amount of gas itself by burning coke furnace gas (also referred to as COG) or natural gas (also referred to as NG) to BFG, which is a low calorie, and to burn it (patent document). 1 and Patent Document 2).

The reason for using COG is that it is easy to mix because COG is a medium calorie gas and the calorie difference with low calorie gas is small, and to increase the hydrogen content in low calorie gas because the main component of COG is hydrogen. This is because the complex flame retardancy can be improved.

However, COG is not a gas that is readily available everywhere. COG contains ammonia, hydrogen cyanide, and the like, and harmful nitrogen oxides are generated in a large amount by combustion. In addition, unsaturated oxides such as nitrogen oxide and butadiene cyclopentadiene, which are included in COG, are polymerized to produce a polymer gum substance (also called NO-Gum), thereby controlling fuel. An abnormality may occur in a valve, a gas turbine nozzle, or the like. To solve this problem, a large-scale COG pretreatment facility (a device for the removal of ammonia and hydrogen cyanide and hydrogenation) is required. In addition, COG may be required because it includes a lot of hydrogen sulfide (H ₂ S), a desulfurization apparatus for reducing the concentration of sulfur dioxide in the exhaust gas after combustion. As a result, the installation cost greatly increases, and the maintenance load thereof increases.

On the other hand, when NG is mixed, since general NG does not contain hydrogen, compared with the case where COG is mixed, fuel gas must be made high in calories to maintain combustion stability. The result is an increase in so-called 'harmful thermal NO' during combustion. In addition, most of the combustible components contained in NG are methane-based hydrocarbons, and there is a fear that the composition of the low-calorie gas is greatly changed when it is mixed with the low-calorie gas. In addition, natural gas is a high calorie gas (about 40 MJ / m 3 N), and there is a big difference from the calorie (about 12 MJ / m 3 N or less) of low calorie gas. For this reason, since the vaporization effect of NG is clear, the mixing ratio of the low calorie gas and natural gas at the time of vaporization must be made small, and as a result, securing gas mixing property becomes difficult. In the case where the deviation of its 'unsteadyness' is large, the effect appears at the time of combustion in the gas turbine, and a nonuniformity in combustion temperature occurs. If this nonuniformity is severe, it damages the combustor or turbine part of a gas turbine.

Patent Document 1: Japanese Patent Application Laid-Open No. 2002-155762

Patent Document 2: Japanese Patent Application Laid-Open No. 9-317499

In order to stably burn low-calorie gas, such as BFG, as a fuel gas, the present inventors are not a unique method of ensuring stable combustion by mixing high-calorie gas with low-calorie gas and increasing the calorific value of this mixed gas. At the same time, it was noted that it is effective to increase the hydrogen content in the low calorie gas to the level required for stable combustion. This is because hydrogen gas has good complex flame resistance and can effectively use this property.

Further, the inventors of the present invention provide a stable operation including a partial load operation of a gas turbine or a case in which the supply amount of low-calorie gas to the combustion device is reduced and the output of a gas turbine, which is a kind of combustion device, must be lowered. When this difficult state is achieved, the low-calorie gas is vaporized by separately generating heavy calorie gas (gas of about 20 MJ / m 3 N) of heat generated by the reforming gas production facility and mixing it with the low calorie gas. The idea was to continue driving. This is because when the high-calorie gas such as natural gas is used for the low-calorie gas evaporation, since the mixing ratio of the high-calorie gas to the low-calorie gas is small, it is difficult to ensure uniform gas mixing properties. This is because it is possible to increase the size, the difference in the calorie difference between the two kinds of gases to be mixed, so that it is easy to ensure uniform gas mixing properties, and the amount of hydrogen gas having good ignition flame resistance also increases after mixing.

The present invention has been made in this way. When using a low-calorie gas having stable properties as a fuel gas of a gas turbine, by adding a reforming gas to it, the low-calorie gas property is modified to produce a stable fuel gas, and combustion stability is realized. An object of the present invention is to provide a gas reforming facility (gas characteristic improvement facility).

Gas reforming facility of the present invention for the above purpose,

Manufacture of reformed gas provided with a natural gas supply line and an air supply line, and having a reaction vessel for producing a reformed gas containing hydrogen gas by mixing natural gas and air, and chemically reacting and reforming the mixed gas. Device,

A mixing regulator for mixing low-calorie gas and reformed gas supplied from the reforming gas producing apparatus and supplying the reformed gas as a fuel gas to a gas turbine facility;

A reformed gas supply passage for supplying a reformed gas from the reformed gas production apparatus to the mixing regulator;

A fuel gas supply passage for supplying fuel gas from the mixing regulator to a gas turbine facility;

It is provided with the control apparatus for controlling the operation | movement of the said reforming gas manufacturing apparatus and the mixing adjustment apparatus.

Low-calorie gas is, for example, blast furnace gas (BFG), by-product gas generated by the direct reduction iron or molten reduction iron method, coke furnace gas (COG), converter gas (LDG), and coal bed. By-products generated by the oil refining process from coal gas (Coal Mine Gas, denoted as CMG), tail gas generated from gas-to-liquid (GTL) process, and oil sand Thermal chemical reaction of raw materials by gas, landfill gas, landfill gas, and other similar high heat generated from the process of fermentation and decomposition of wastes, including gas generated by waste incineration using plasma, and municipal waste. Low-calorie gases, such as by-product gas, generated in conjunction with these. That is, the present invention can be applied even when the above gas is used alone or in combination of two or more kinds of gases so as to be used as a mixed gas of BFG and COG. Natural gas also contains liquefied natural gas.

Further, the reformed gas production apparatus further includes a steam (hereinafter simply referred to as steam) supply line, and is reformed by reforming by further adding and chemically reacting steam to a mixed gas of natural gas and air. It is preferable that it is comprised so that gas can be supplied to the said mixing regulator. This is because the hydrogen concentration of the reformed gas is further increased by the mixing of the steam.

A fuel gas hydrogen concentration detector is further provided in at least a fuel gas supply passage of the reformed gas supply passage and the fuel gas supply passage,

It is preferable that the control device is configured to adjust the amount of the reformed gas supplied from the reformed gas production device to the mixing regulator based on the detection information of the hydrogen concentration detector.

A fuel gas hydrogen concentration detector is further provided in at least a fuel gas supply passage of the reformed gas supply passage and the fuel gas supply passage,

It is preferable that the control device is configured to change the hydrogen concentration of the reformed gas by changing the mixing ratio of natural gas and air in the reformed gas production apparatus based on the detection information of the hydrogen concentration detector.

The reformed gas production apparatus includes a steam supply line, further comprising a fuel gas hydrogen concentration detector provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage,

It is preferable that the control device is configured to change the hydrogen concentration of the reformed gas by changing the mixing ratio of natural gas, air and steam in the reformed gas production apparatus based on the detection information of the hydrogen concentration detector. . This is because the adjustment range of the hydrogen concentration of the reformed gas is expanded by mixing the steam.

A fuel gas hydrogen concentration detector provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage;

And a dilution gas supply device for diluting the fuel gas with the dilution gas, which is installed in the mixing regulator,

It is preferable that the control device is configured to mix the dilution gas from the dilution gas supply device with respect to the fuel gas based on the detection information of the hydrogen concentration detector.

And a fuel gas hydrogen concentration detector provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage,

It is preferable that the control device is configured to change the calorific value of the reformed gas by changing the mixing ratio of natural gas and air in the reformed gas production apparatus based on the detection information of the hydrogen concentration detector.

The reformed gas production apparatus includes a steam supply line, further comprising a fuel gas hydrogen concentration detector provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage,

It is preferable that the control device is configured to change the calorific value of the reformed gas by changing the mixing ratio of natural gas, air and steam in the reformed gas production apparatus based on the detection information of the hydrogen concentration detector.

And further comprising fuel gas calorific value measuring means provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage,

It is preferable that the control device is configured to adjust the amount of the reformed gas supplied from the reformed gas production device to the mixing control device based on the detection information of the calorific value measuring means.

And further comprising fuel gas calorific value measuring means provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage,

It is preferable to configure so that the said control apparatus may change the calorific value of a reformed gas by changing the mixing ratio of natural gas and air in a reformed gas manufacturing apparatus based on the detection information of the said calorific value measuring means.

The reformed gas production apparatus includes a steam supply line, further comprising fuel gas calorific value measuring means provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage,

It is preferable that the control device is configured to change the calorific value of the reformed gas by changing the mixing ratio of natural gas, air and steam in the reformed gas production apparatus based on the detection information of the calorific value measuring means.

And a pressure measuring means for measuring the internal pressure of the passage provided in the fuel gas supply passage,

It is preferable to comprise so that the said control apparatus may adjust the quantity of the reformed gas supplied from the reformed gas manufacturing apparatus to the mixing regulator based on the measurement information of the said pressure measuring means.

Fuel gas calorific value measuring means provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage;

And a dilution gas supply device for diluting the fuel gas with the dilution gas, which is installed in the mixing regulator,

It is preferable that the control device is configured to mix the dilution gas from the dilution gas supply device with respect to the fuel gas based on the detection information of the calorific value measuring means.

It is preferable that the said reformed gas manufacturing apparatus further includes the heating steam supply line for supplying the steam for heating from a gas turbine installation, in order to promote the chemical reaction in the reaction container.

In addition to the heating steam supply line, the reformed gas production apparatus is used for heating for promoting a chemical reaction in the reaction vessel, and extracting high-temperature compressed air from a gas turbine facility and supplying it to the reaction vessel. Iii) preferably further provided with a line and configured to selectively supply steam and hot bleed. This is because a heat source necessary for accelerating the reaction can be obtained because at the time when the chemical reaction in the reaction vessel is started, it is a transient state in which no steam is generated in the equipment.

The reformed gas production apparatus includes a heat exchange means in its reformed gas supply passage, and the heat exchange means includes a mixed gas of natural gas and air supplied to the reaction vessel, and a reformed gas supplied to the mixing regulator; It is preferable to be comprised so that heat exchange of may be carried out. This is because the reformed gas that has been heated can be cooled to an appropriate temperature and the mixed gas can be preheated prior to the reaction.

It is preferable that the said reformed gas supply passage is equipped with the cooling means for cooling the reformed gas supplied to the said mixing regulator.

It is preferable that the said cooling means is provided downstream of the said heat exchange means in a reformed gas supply passage, and is comprised so that the liquid in reformed gas may be condensed and removed.

A buffer tank is provided in the reformed gas supply passage, and the buffer tank is preferably configured to stabilize the pressure of the reformed gas supplied to the mixing regulator by absorbing the variation in the reformed gas flow rate. . This is because the reforming gas can be uniformly mixed with the low calorie gas in the mixing regulator.

According to the present invention, NG with almost no impurities can be reformed to show hydrogen gas, and the clean reformed gas containing the hydrogen gas can be used as a gas for reforming characteristics of low-calorie gas such as BFG. As a result, low-calorie gas can be made into a stable fuel, such as stabilizing the hydrogen gas content rate of low-calorie gas.

In addition, even when the supply amount of low-calorie gas is reduced, operation of a facility is performed by steaming low-calorie gas by the reformed gas containing the hydrogen gas which is good in mixing property with good low-calorie, and has a complex ignition flame resistance. You can continue reliably.

1 is a block diagram showing an outline of a gas reforming plant of an embodiment of the present invention.

FIG. 2 is a block diagram showing an example of a reformed gas production apparatus in the facility of FIG. 1.

FIG. 3 is a block diagram illustrating an example of a fuel gas supply line supplied to a gas turbine power generation facility in the facility of FIG. 1.

4 is a block diagram illustrating an example of a gas turbine power generation facility in the facility of FIG. 1.

5 is a graph showing the calorific value of the mixed gas with respect to the mixing ratio of air to NG assuming that the component is only CH ₄ .

FIG. 6 is a graph showing the volume ratio of the main combustion component of the gas after the reforming process to the mixing ratio of air to NG assuming that the component is only CH ₄ .

FIG. 7 is a block diagram showing another example of the portion 'A' in the reformed gas production apparatus of FIG. 2.

8 is a block diagram illustrating still another example of a portion 'A' in the reformed gas production apparatus of FIG. 2.

FIG. 9 is a block diagram showing another embodiment of a gas turbine power generation facility and a supply line of fuel gas supplied to the power generation facility in the facility of FIG. 1.

<Explanation of symbols for the main parts of the drawings>

1: gas turbine power generation equipment 2: fuel gas supply piping

3: reforming gas manufacturing apparatus 4: reforming gas supply piping

5: mixing adjusting device 6: accessories

7: NG supply piping 8: air supply piping

9: steam supply piping for heating 10: control unit

11: first mixer 12: catalytic reaction vessel

13: heat exchanger

14: mist separator

15: Filter 16: Boosting fan

16a: bypass piping 17: mixed gas supply piping

18: second mixer 19: cooler

20: buffer tank 21: H ₂ densitometer

22: O ₂ densitometer 23: CO densitometer

24: CH ₄ concentration meter 25: bypass piping

26: BFG supply piping 27: buffer tank

28: CO densitometer 29: H ₂ densitometer

30: dilution unit 31: dilution gas supply piping

32: damper 33: H ₂ densitometer

34: calorimeter (gas analyzer) 35: fuel compressor

36 gas turbine 37 combustor

38: generator 39: bypass piping

40: cooler 41: heat recovery boiler

42: steam turbine 43: chimney

44: generator 45: steam supply pipe

51 to 58: flow rate regulating valve 61 to 66: pressure gauge

71 to 76: flowmeters 81 to 89: thermometers

91: steam piping 92: extraction piping

93: flow control valve 94: third mixer

95: booster compressor 96: bypass piping

97: air cooler 98: flow control valve

99: air compressor 100: bypass piping

101: air cooler 102, 103: flow control valve

104: fourth mixer 111: CH ₄ densitometer

112: CO densitometer 113: CH ₄ densitometer

AIR: Air BFG: Furnace Gas

NG: Natural Gas U: Where Used

EMBODIMENT OF THE INVENTION The Example of the gas reformer of this invention is described, referring an accompanying drawing.

FIG. 1 is a block diagram showing an outline of a gas reforming facility (hereinafter, simply referred to as “equipment”) as an embodiment of the present invention. This equipment comprises a fuel gas supply pipe 2 for supplying fuel gas mainly composed of low-calorie gas (hereinafter referred to as BFG in the present embodiment) to the gas turbine power generation equipment 1, and reformed gas for producing reformed gas. The reforming gas supply piping 4 which joins the reformed gas to the fuel gas supply piping 2 from the manufacturing facility 3, the reformed gas manufacturing facility 3, the fuel gas supply piping 2, and the reformed gas supply piping ( It is provided at the joining point of 4), and is equipped with the mixing regulator 5 which mixes BFG and reforming gas, and adjusts fuel gas. The gas turbine power generation equipment 1 is provided with auxiliary equipment 6 that effectively uses the arrangement. The reformed gas production facility 3 is connected to an NG supply pipe 7, an air supply pipe 8, and a steam pipe 91 that supply NG as a raw material of the reformed gas, air, and steam. In addition, the reforming gas manufacturing facility 3 is referred to as a heating steam supply pipe 9 and a gas turbine bleed air pipe (hereinafter, simply referred to as an `` extraction pipe '') that are heated therein to partially oxidize NG. 92 is connected. In addition, the facility is provided with a control device 10 for controlling the production of the reformed gas, the supply of the reformed gas, and the mixing adjustment of the BFG and the reformed gas.

In the reforming gas production plant 3, NG is mixed with air to partially oxidize, and methane gas (CH ₄ ) in NG is decomposed to decompose hydrogen gas (H ₂ ), carbon monoxide (CO), carbon dioxide (CO ₂ ), and water ( H ₂ O) is presentized. The liquefied water is discharged as a drain, but all are mixed with BFG as a reforming gas. As described above, since only NG is decomposed but pure hydrogen is not taken out, pretreatment facilities such as desulfurization, tar removal, and naphthalene removal are unnecessary. In addition, the CH _4, H _2, CO is obtained as a combustible minutes. By changing the mixing ratio of NG and air, it is possible to adjust the ratio of these combustible components. Therefore, it is possible to make it suitable for the component of the low calorie gas selected as fuel gas.

Although piping facilities differ slightly when the NG used is low pressure and high pressure, both are described together in FIG. For example, the reformed gas supply pipe 4 differs depending on whether NG is low pressure or high pressure. However, in FIG. 1, the low pressure reformed gas supply pipe 4a and the high pressure reformed gas supply pipe 4b are shown together. The low pressure NG refers to a case where the NG supplied to the reformed gas production facility 3 is lower than the pressure required for the feed fuel to the gas turbine. The high-pressure NG refers to NG having a pressure higher than the pressure required for the feed fuel to the gas turbine, for example, in a state in which liquefied natural gas is vaporized in a sealed place.

The pressure of the reformed gas obtained using the low pressure NG is also low. In this case, the low-pressure reformed gas is sent to the mixing regulator 5 through the low-pressure reformed gas supply pipe 4a, where it is mixed with the BFG. In the mixing regulator 5, the amount of the reformed gas supplied to the BFG from the reformed gas supply pipe 4a is adjusted while supplying the diluent gas as necessary so that the hydrogen gas content rate in the fuel gas is within a predetermined range. . In the gas turbine power generation facility 1, a gas turbine is operated and generated using this modified mixed BFG as a fuel. As described later, the auxiliary facilities 6 are provided with a heat recovery boiler 41 and a steam turbine 42 using an array from the gas turbine 36.

When using high pressure NG, since it uses a high pressure thing also in the air supply piping 8 as mentioned later, it differs from the case of using low pressure NG. In addition, the pressure of the reformed gas obtained using the high pressure NG becomes high. The high pressure reformed gas is not sent to the mixing regulator 5, but is sent directly to the fuel gas supply piping 2 in the gas turbine power generation facility 1 via the high pressure reformed gas supply piping 4b, where BFG and Are mixed.

With reference to Figs. 2 to 3, each of the facilities 2, 3, 5, and 6 will be described. First, a case of using low pressure NG will be described, and a difference related to the case of using high pressure NG thereafter will be described. Explain.

(Configuration of Low Pressure Reforming Gas Production Facility 3)

2, the conceptual diagram of the equipment piping which comprises the reformed gas manufacturing facility 3 is shown. In an actual machine, the quantity, piping order, etc. of each apparatus may change. In addition, not only a spare device, a preliminary system, a repairing device, a monitoring device, a high functionalization, high precision, stabilization, and a simplification, but also according to the intention of a facility designer or a user, each detail part is changed within the scope of the present invention. There is a case.

The reforming gas production plant 3 includes a first mixer 11 for mixing NG and air, a reaction vessel 12 for partially oxidizing by heating the mixed gas, and a mixed gas sent to the reaction vessel 12. And a heat exchanger 13 for performing heat exchange with the gas heated to high temperature by the reaction heat. In order to heat the reaction vessel 12 to a temperature necessary for chemical reaction of the mixed gas, steam is supplied from the heating steam supply pipe 9 connected to the reaction vessel 12, or the gas turbine air compressor 38a. The extracted hot compressed air is supplied through the flow control valve 103 from the bleeding pipe 92 connected to the reaction vessel 12 (see FIG. 4). The thermometer 89 is provided in the bleeding pipe 92. When the high temperature compressed air from the gas turbine air compressor 38a cannot be used, the steam from the heating steam supply pipe 9 is used. In addition, steam and hot compressed air are supplied only at the start of the reaction vessel 12, and after the start of the reaction, the reaction is continued by the heat of reaction of the mixed gas itself.

Each piping of the reformed gas production facility 3 is provided with various measuring instruments and flow rate regulating valves (hereinafter referred to as "flow rate regulating valves"). These are explained according to the flow of the fluid.

First, after passing through the flow control valve 51, NG supplied through the NG supply pipe 7 reaches the mist separator 14 and the liquid portion is removed. The pressure gauge 61 and the flowmeter 71 are provided in the pipe 7 leading to the first mixer 11 of the reformed gas production facility 3. The pressure gauge 63 is also provided in the first mixer 11.

The air supplied through the air supply pipe 8 is damped by the filter 15, and then, by the boosting fan 16, the first mixer 11 through the flow control valves 52a and 52b. Is sent to. In the first mixer 11, air is mixed with NG. A pressure gauge 62 and a flow meter 72 are provided downstream of the flow control valve 52a in the air supply pipe 8. In addition, the air supply pipe 8 is provided with a bypass pipe 16a for bypassing the boosting fan 16. The bypass pipe 16a is provided with a flow rate control valve 53. This bypass pipe 16a is for ensuring the minimum flow rate which the continuous operation of the boosting fan 16 is possible.

On the other hand, the steam supplied through the steam pipe 91 passes through the flow control valve 93 and is supplied to the third mixer 94 to be mixed with the mixed gas of NG and air. Reference numeral 76 denotes a 'flow meter'.

In the reformed gas production facility 3, the mixed gas obtained by mixing air and NG by the first mixer 11 is heated by the heat exchanger 13, and then sent to the reaction vessel 12. The thermometers 81 and 82 are provided in the mixed gas supply piping 17 of the upstream and downstream of the heat exchanger 13, respectively. Thermometers 83 and 84 are provided in the reaction vessel 12 and the steam supply pipe 9 for heating, respectively. In the reaction vessel 12, NG is partially oxidized and its containing CH ₄ is decomposed into H ₂ , CO, CO ₂ , and H ₂ O. These are sent to the reformed gas supply pipe 4 as reformed gas without being separated. The reformed gas in the reformed gas supply pipe 4 is cooled by the mixed gas of NG and air by passing through the heat exchanger 13 described above. The pressure gauge 64 and the thermometer 85 are provided in the part of the reformed gas supply pipe 4 between the reaction vessel 12 and the heat exchanger 13.

The reformed gas supply pipe 4 is continuously provided from the reformed gas production facility 3 to the second mixer 18 of the mixing regulator 5. The reformer gas supply piping 4 after exiting the reformed gas production facility 3 is provided with a cooler 19 and a buffer tank 20. The buffer tank 20 is for absorbing fluctuations in the reformed gas flow rate. The reformed gas is cooled by the cooler 19, and the condensed liquid portion is discharged as a drain. Thereafter, the reformed gas is sent to the second mixer 18 while adjusting the flow rate by the flow control valve 54 in a state in which the buffer tank 20 is filled in a predetermined amount. The flow rate of the reformed gas adjusted by the flow control valve 54 is detected by the flow meter 73 provided downstream of the flow control valve.

In the reformed gas supply pipe 4 portion between the cooler 19 and the buffer tank 20, the thermometer 86, the H ₂ densitometer 21, the O ₂ densitometer 22, CO are directed downstream of the reformed gas flow. The densitometer 23 and the CH ₄ densitometer 24 are provided. The pressure gauge 64 is provided in the buffer tank 20. The reformed gas supply pipe 4 is provided with a bypass pipe 25 for bypassing the buffer tank 20.

(Configuration of the Mixing Adjusting Device 5)

Next, the mixing adjustment apparatus 5 is demonstrated, referring FIG. The BFG supply piping 26 is connected to the mixing regulator 5. The BFG supply pipe 26 is provided with a thermometer 87, a buffer tank 27, and a pressure gauge 65. When the flow volume of BFG fluctuates, the buffer tank 27 is for alleviating the fluctuation | variation of the pressure resulting from it.

In the BFG supply pipe 26 in the mixing regulator 5, the CH ₄ concentration meter 111, the CO concentration meter 28, the H ₂ concentration meter 29, the second mixer 18, and the dilution device 30 are provided. In turn, downstream of the fluid stream. However, the arrangement of such devices is shown as an example and is not limited thereto. The BFG and the reformed gas (H ₂ , CO, CO ₂ , H ₂ O, etc.) are mixed by the second mixer 18 to become a mixed gas (fuel gas), and through the fuel gas supply pipe 2, the gas turbine It is sent to the fuel compressor 35 (refer FIG. 4) of the power generation installation 1. As shown in FIG.

The dilution device 30 is for lowering the H ₂ concentration by mixing nitrogen gas (N ₂ ) or the like when the H ₂ concentration in the fuel gas exceeds a predetermined range. The dilution device 30 is connected to a supply pipe 31 for supplying N ₂ gas or the like as a dilution gas from a supply source such as nitrogen gas N ₂ (not shown). The flow control valve 55 and the flowmeter 74 are provided in the dilution gas supply piping 31.

In the fuel gas supply pipe 2 from the mixing regulator 5 to the gas turbine power generation facility 1, the vibration suppressor 32, the CO concentration meter 112, and H _{2 are} directed downstream. The densitometer 33, the CH ₄ densitometer 113, the pressure gauge 66, the thermometer 88, and the calorimeter (for example, gas analyzer) 34 are provided.

(Configuration of Gas Turbine Power Generation Facility 1)

Referring to FIG. 4, the fuel gas supply pipe 2 in the gas turbine power generation facility 1 is provided with the fuel compressor 35 driven by the motor M, and fuel gas is supplied to the fuel compressor 35. As a result, it is pumped to the combustor 37 of the gas turbine 36 through the fuel gas supply pipe 2. The flowmeter 75 and the flow control valve 56 are provided in the fuel gas supply pipe 2 part between the fuel compressor 35 and the combustor 37. The generator 38 is connected to the gas turbine 36. Reference numeral '38a' is an 'air compressor' of a gas turbine. The fuel compressor 35 is provided with a bypass pipe 39. This bypass pipe 39 is for controlling the fuel gas pressure at the outlet of the compressor 38a to a predetermined pressure, and includes a flow rate control valve 57 and a cooler 40.

The auxiliary equipment 6 installed in the gas turbine power generation facility 1 includes a heat recovery boiler 41, a steam turbine 42 for generating power by steam of the heat recovery boiler 41, And a chimney 43 for dissipating the exhaust gas. The generator 44 is connected to the steam turbine 42. In addition, a steam supply pipe 45 for supplying steam from the heat recovery boiler 41 to a predetermined use point UP is provided, and the steam supply pipe 45 has a flow control valve 58. Is installed. The steam for piping may be supplied to the reaction vessel 12 described above by the steam supply pipe 45.

The operation of the above gas reforming facility is controlled by the control device 10. The control apparatus 10 mixes the required amount of reforming gas and dilution gas with BFG in a required amount, and controls the mixing regulator 5 for improving the characteristics of the BFG, and NG according to the request instruction from the mixing regulator 5. And control of the reformed gas production apparatus 3 for producing a reformed gas for a predetermined use from a mixed gas of air and air. It is as follows.

(Control of reforming gas manufacturing apparatus 3)

The reformed gas obtained by chemically reacting NG has a much higher hydrogen content and calorific value than BFG. Therefore, the control of the reformed gas production apparatus 3 is intended to adjust the production amount of the reformed gas and the supply amount to the mixing regulator 5, the hydrogen content of the reformed gas, and the calorific value of the reformed gas so as to match the required numerical values. I am doing it as one. Therefore, the supply amount of NG, air, and steam to the reforming gas manufacturing apparatus 3, and these mixing ratios are adjusted. The mixing ratio of NG and air is required hydrogen concentration in the fuel gas determined according to the gas turbine used, hydrogen concentration in the previously measured BFG, reforming gas production capacity of the reforming gas production apparatus 3, and full load operation of the gas turbine. It is predetermined based on the fuel consumption of the city and the like. This predetermined mixing ratio (reference mixing ratio) is changed as necessary.

Adjustment of the supply amount of NG and air, and these mixing ratios is performed by adjusting the opening degree of the flow control valves 51, 52a, 52b of each supply piping 7,8. The mixing ratio of NG and air is feedback-controlled based on the measurement information by the flowmeters 71 and 72 of each supply piping 7 and 8 so that it may become the above-mentioned reference mixing ratio. The adjustment of the production amount of the reformed gas and the supply amount to the mixing regulator 5 is performed so that the internal pressure of the first mixer 11 or the internal pressure of the buffer tank 20 on the reformed gas supply pipe 4 is within a predetermined range. This is achieved by controlling the NG flow rate by the flow rate control valve 51. Since the mixing ratio is determined in advance, when the NG flow rate (measured by the flowmeter 71) is determined by the flow regulating valve 51, the degree of opening of the flow regulating valve 52a of the air supply pipe 8 is automatically determined. Is determined, and the air flow rate (measured by the flow meter 72) is adjusted by the flow rate control valve 52b. One flow control valve 52a is a fixed opening valve that automatically determines the opening degree according to the mixing ratio of NG and air. The other flow control valve 52b operates as an automatic control valve for surely adjusting the mixing ratio. The flow rate ratio of these flow regulating valves 52a and 52b can be set arbitrarily.

As shown in FIG. 5, the calorific value of the reformed gas is maximum when the volume ratio of air to be mixed with NG (assuming CH ₄ is 100) is '0', and is lowered as the ratio increases. On the other hand, the hydrogen concentration in the reformed gas is '0' when the volume ratio of air is '0', increases around 20 to 35 (%), and then decreases as the air ratio increases. 5 is a graph showing the calorific value of the mixed gas with respect to the mixing ratio of air to NG assuming that the component is only CH ₄ . 6, the component is CH ₄ It is a graph which shows the volume ratio of the main combustion component of the reformed gas after manufacture with respect to the mixing ratio of air with respect to NG assumed only.

When the mixing ratio of NG and air is the same, steam has the effect of increasing the concentration of hydrogen in the reforming gas. Therefore, when a reforming gas having a higher hydrogen concentration is required than that obtained by adjusting the mixing ratio of the same NG and air. Supplied to. Since the calorific value also changes in accordance with the change in the hydrogen concentration, the vapor concentration may be adjusted for the purpose of adjusting the calorific value.

In the production of the reformed gas, for safety reasons, the oxygen concentration in the reformed gas is controlled to be equal to or less than a predetermined value (for example, 1% by volume). For this purpose, on the basis of the detection result of the O ₂ concentration meter 22, and carries out a feedback control by the direction of reducing the mixing ratio of air flow rate control valve (52b). Further, to adjust the heating value of the fuel gas, H ₂ concentration meter (21), CO concentration meter (23), CH ₄ concentration meter 24, the control device 10 from the information detected by the pressure gauge 64 and thermometer 86 Calculates the calorific value of the reformed gas. This is because the combustible components of the reformed gas using NG are mainly H ₂ gas, CO gas, and CH ₄ gas. Based on this calculated calorific value, it adjusts by changing an air mixing ratio using the flow control valve 52b so that it may become a predetermined | prescribed calorific value. In addition, the use of the detected temperature and the detected pressure for calculating the calorific value is because steam partial pressure correction is performed.

(Control of the Mixing Adjuster 5)

The control of the mixing regulator 5 controls the amount of the reforming gas to be mixed with the BFG to be supplied to the gas turbine 36, and further, issues a hydrogen concentration change command to the reforming gas producing apparatus 3. By further mixing the gas for dilution with BFG, it aims at making hydrogen density | concentration of a mixed gas (fuel gas) suitable for a request value. In addition, it is also possible to adjust the calorific value of the fuel gas by issuing an instruction for changing the calorific value of the reformed gas to the reformed gas production apparatus 3. Since the amount of fuel gas consumed by the gas turbine 36 varies with the load of the gas turbine, the amount and mixing ratio of the BFG, the reformed gas, and the dilution gas are adjusted in conjunction with the operation control of the gas turbine 36.

First, the hydrogen content control in fuel gas is demonstrated. Since hydrogen gas has a high combustion speed and good ignition flame resistance, it contributes to maintaining stable combustion of low-calorie BFG. Therefore, with respect to the low-calorie gas with low hydrogen content rate, the control apparatus 10 controls so that the hydrogen concentration in fuel gas may be maintained at a predetermined value (for example, 4 volume%). This is because, in the case of a gas turbine, when the hydrogen content of BFG is 2% by volume or less, it is likely to be misfired. In addition, the planned mixing ratio and maximum mixing ratio of BFG and the reforming gas in hydrogen concentration control can be arbitrarily set by manual input. The planned mixing ratio and the maximum mixing ratio will be described later.

If the hydrogen concentration falls below a predetermined value even by adjusting (increasing) the supply amount of the reformed gas, the control device 10 issues a low-alarm and provides hydrogen to the reformed gas production device 3. Issue a concentration increase command. In the reformed gas manufacturing apparatus 3 which received this command, the air mixing ratio to NG is changed, and the hydrogen concentration in reformed gas is raised. Since the hydrogen concentration in the reformed gas is the maximum at the mixing ratio of NG and air at about 30% by volume, when it is necessary to further increase the hydrogen concentration in the reforming gas even at this mixing ratio, the mixing ratio of NG and air is fixed and steam Mix. Since the calorific value also increases with the increase in the hydrogen concentration, the calorific value control can also be performed by changing the mixing ratio of steam. The maximum value of the mixing amount of steam is below the saturation pressure under the concentration condition of the third mixer 94.

When the hydrogen concentration falls below a predetermined value even by raising the hydrogen concentration of the reformed gas to the maximum, the control device 10 issues a low-low alarm and switches from hydrogen concentration control to calorific value control. That is, the command to increase the calorific value of the reformed gas is issued to the reformed gas production apparatus 3. In the reformed gas production apparatus 3 that has received this command, the amount of heat generated by the reformed gas is increased by changing the air mixing ratio to NG. Specifically, the calorific value of the reformed gas is increased by lowering the air mixing ratio to NG.

On the other hand, if the hydrogen concentration exceeds a predetermined value even by adjusting (decreasing) the supply amount of the reformed gas, the control device 10 issues a high-alarm and at the same time the reformed gas production device 3. A command to lower the hydrogen concentration is issued. In the reformed gas manufacturing apparatus 3 which received this command, the air mixing ratio to NG is changed, and the hydrogen concentration in reformed gas is reduced.

Further, when the hydrogen concentration exceeds a predetermined value even by lowering the hydrogen concentration of the reformed gas to a minimum, the control device 10 issues a high-high-alarm and at the same time the hydrogen concentration reaches a predetermined value. The required flow rate (detected by the flowmeter 74) of the dilution gas supplied to the dilution apparatus 30 is adjusted by adjusting the flow control valve 55 of the dilution gas supply piping 31. N ₂ is usually used as the diluent gas, but is not limited thereto.

The above control is a control for maintaining the hydrogen concentration in the BFG used as the fuel gas at a predetermined value, but there is also a low calorie by-product gas having a sufficient original hydrogen concentration and stable (at least 5% by volume). However, even such a low calorific by-product gas may change the calorific value (gas calorie) under the influence of the change in the operating conditions in the main operation process. In order to cope with the calorie fluctuation in such a case, it is also possible to perform control (heat generation amount control) to maintain operation by stabilizing the calorific value of fuel gas.

That is, the reformed gas supply pipe 4 and the fuel gas supply H ₂ concentration meter 29 is installed in the pipe (2) flow meters (73, 74, 75) installed in the fuel gas supply pipe (2), CO concentration meter 28, , The calorific value of the BFG is calculated on the basis of the detection results by the CH ₄ concentration meter 111, the pressure gauge 65, and the thermometer 87, and the flow meter 73 and the H ₂ concentration meter provided in the reformed gas supply pipe 4. 21) The calorific value of the reformed gas is calculated based on the detection results by the CO densitometer 23, the CH ₄ densitometer 24, the pressure gauge 64, and the thermometer 86. When the total calorific value is less than the calorific value required for the operation of the gas turbine 36, the reformed gas supply pipe 4 supplies the reformed gas having a higher calorie value to the required calorific value of the fuel gas. The supply amount of the reformed gas is controlled by the flow control valve 54. In addition, the use of the detected temperature and the detected pressure for calculating the calorific value is because steam partial pressure correction is performed.

The use of the concentration meters 21, 23, 24, 28, 29, and 111 of each component gas for the concentration detection for calorific value calculation is because the detection speed is fast and suitable for process control. On the other hand, the above-described calorimeter 34 capable of accurately measuring gas components although the detection speed is slow is used to monitor the change in the properties of the fuel gas. Therefore, the flammable component of the fuel gas after mixing BFG and reforming gas can be measured by the said calorimeter 34, and can be fed back to the control apparatus 10 for adjustment.

In addition, rapid detection rate of the caloric value (the concentration of combustible components) in the fuel gas jeukeung property to have the (卽應性), CO concentration meter 112 and the H ₂ concentration meter which is installed on the fuel gas supply pipe (2) may be calculated by correcting the moisture from 33 CH ₄ and measurement of pressure and temperature measurement by the concentration meter 113 detects the concentration of combustible components, and using the pressure gauge 66 and a thermometer 88. When the calorific value of the fuel gas after mixing exceeds the upper limit of the allowable calorie fluctuation range of the gas turbine, the calorific value is lowered by supplying diluent gas such as N ₂ gas by the diluent gas supply pipe 31.

The planned mixing ratio, minimum mixing ratio and maximum mixing ratio of the BFG and the reforming gas in such calorific value control can be arbitrarily set by manual input. This is because the composition of BFG generated for each furnace and operating conditions is different, and the composition of the reformed gas to be linked to this is inevitably different. In addition, the low-calorie by-product gas may contain a high concentration of hydrogen of 5% by volume or more as described above, but there may be a low concentration such as BFG. In such a gas, it is preferable to maintain the above-mentioned predetermined hydrogen concentration even at the time of heat generation control. This is because hydrogen gas has good ignition flame resistance and is a gas component necessary to secure stable combustion.

The above-described planned mixing ratio is a mixing ratio of the reformed gas having a predetermined hydrogen concentration with respect to BFG of a certain hydrogen concentration, and is a ratio obtained by calculation at the design stage in advance. If this planned mixing ratio is obtained in advance, the control response is good with respect to the hydrogen concentration change of BFG. And fine adjustment is made by a feedback control based on the detection result of the H ₂ concentration meter 33 of the fuel gas supply pipe 2. The maximum mixing ratio is an upper limit of the mixing ratio set in order to prevent excessive mixing of the reformed gas due to a false signal of the meter. Similarly, the minimum mixing ratio is a lower limit of the mixing ratio that is set in order to prevent the mixing gas (lack of calorific value) of the reformed gas due to an incorrect signal of the meter.

Hereinafter, specific calorific value control will be described. If the calorific value of the fuel gas is lower than the predetermined range during normal operation, the control device 10 adjusts the opening degree of the flow rate control valve 54 of the reformed gas supply pipe 4 so that the calorific value of the fuel gas becomes a predetermined value. The flow rate (detected by the flowmeter 73) of the reformed gas supplied to the second mixer 18 is increased to increase.

If the calorific value of the fuel gas is still lower than the set value even when the flow rate of the reformed gas is increased, the control device 10 issues a low-alarm and issues a command to increase the calorific value to the reformed gas production apparatus 3. . In the reformed gas manufacturing apparatus 3 which received this command, the air mixing ratio to NG is changed and the calorific value of reformed gas is raised. The adjustment amount of the air mixing ratio to NG is determined according to the trend of the graph of FIG. If necessary, the amount of heat generated by the reformed gas is increased by changing the mixing ratio of steam.

If the calorific value of the fuel gas is still below the predetermined value even by raising the calorific value of the reformed gas to the maximum, the control device 10 generates a low-low alarm. In response to this, the operator performs appropriate treatment.

On the other hand, if the calorific value exceeds a predetermined upper limit value even by adjusting (reducing) the supply amount of the reformed gas, the control device 10 issues a high-alarm and simultaneously supplies the reformed gas production apparatus 3 to the reformed gas production apparatus 3. Give a command to lower the calorific value. In the reformed gas manufacturing apparatus 3 which received this command, the air mixing ratio to NG is changed and the calorific value of reformed gas is reduced.

In addition, even when the calorific value of the reformed gas is still lowered to a minimum, when the calorific value of the fuel gas still exceeds a predetermined high upper limit value, the control device 10 issues a high-high-alarm and at the same time. The required flow rate of the dilution gas to be supplied to the dilution device 30 by adjusting the flow rate control valve 55 of the dilution gas supply pipe 31 so that the calorific value becomes a predetermined low upper limit (flowmeter 74). Detection).

In addition, when changing the mixing ratio of NG and air at the time of hydrogen concentration control and calorific value control, it is preferable to consider in consideration of the time delay required for mixing.

The calorific value control of the fuel gas described above is control to directly increase or decrease the calorific value by supplying the reformed gas or the dilution gas while detecting the calorific value of the fuel gas.

Next, with reference to FIGS. 7-9, it demonstrates centering on the difference in facilities in the case of using the high pressure NG instead of the low pressure NG mentioned above.

In the case of using the high pressure NG, the air to be supplied accordingly needs to be high pressure. However, the air supply pipe 8 having two types of high pressure specifications will be described below with reference to FIGS. 7 and 8. The piping of the range shown by the dashed-dotted line in FIG. 7 is for high pressure, and is employ | adopted instead of the "A" part enclosed by the 2-dot dashed line in the low pressure air supply piping 8 in FIG.

In the air supply pipe 8 shown in FIG. 7, the high temperature and high pressure air which is extracted through the bleeding pipe 92 connected to the air compressor 38a in the gas turbine described later is flowed by the flow rate control valve 103. Guided in adjustment. A booster compressor 95 is provided downstream of the above-described flow control valves 52a and 52b in the air supply pipe 8. An air supply pipe 8 is connected with a bypass pipe 96 for bypassing the booster compressor 95, and a bypass of the air cooler 97 and the booster compressor 95 is connected to the bypass pipe 96. A flow regulating valve 98 is provided to prevent surging. In this manner, the high temperature and high pressure air from the air compressor 38a in the gas turbine can be used.

The air of low pressure is supplied to the air supply piping 8 shown in FIG. 8 similarly to the low pressure air supply piping 8 in FIG. However, the high pressure air compressor 99 is provided in the high pressure air supply pipe 8 instead of the boosting fan 16 in the low pressure air supply pipe 8 in FIG. 2. In addition, a bypass pipe 100 for bypassing the air compressor 99 is connected to the air supply pipe 8, and an air cooler 101 and an air compressor 99 are connected to the bypass pipe 100. Flow control valve 102 is provided to prevent the surging of water.

In FIG. 9, the piping installation of the gas turbine power generation equipment 1 which uses the high pressure reforming gas made from high pressure NG is shown, and this corresponds to the piping using the low pressure reforming gas shown in FIG. Here, the mixing adjustment apparatus 5 which mixes and adjusts BFG and reforming gas as shown in FIG. 3 is not provided in the form which gathered together. Specifically, as shown, the pressure gauge 65, the CO concentration meter 28 and the H ₂ concentration meter 29 in the above-described mixing regulator 5 are provided upstream of the fuel compressor 35, The fourth mixer 104 for mixing the reformed gas and the BFG, and the dilution gas supply pipe 31 provided with the flow control valve 55, the flow meter 74, and the dilution device 30 are downstream of the fuel compressor 35. Installed in In this way, the components of the mixing regulator 5 are divided and provided upstream and downstream of the fuel compressor 35. This is because the reformed gas supply pipe 4 is connected to the downstream side of the fuel compressor 35 because the reformed gas to be mixed in the BFG is a high pressure and does not require boosting by the fuel compressor 35. Moreover, the bleed piping 92 is connected to the air compressor 38a in the gas turbine 36. Hot air and high pressure air are sent from the air compressor 38a through the bleeding pipe 92 to the air supply pipe 8 to the above-described reformed gas production apparatus 3. The above point differs from the piping using the low pressure reforming gas shown in FIG. 3 and FIG.

According to the present invention, a conventional large-scale gaseous fuel pretreatment facility or the like is obtained by decomposing NG which hardly contains impurities and generating a clean reformed gas containing hydrogen gas at a necessary concentration, and carefully mixing it with a low-calorie gas having unstable characteristics. It is possible to realize the continuous stable combustion of the gas turbine without the need for this.

Claims (19)

Manufacture of reformed gas provided with a natural gas supply line and an air supply line, and having a reaction vessel for producing a reformed gas containing hydrogen gas by mixing natural gas and air, and chemically reacting and reforming the mixed gas. Device, A mixing regulator for mixing low-calorie gas and reformed gas supplied from the reforming gas producing apparatus and supplying the reformed gas as a fuel gas to a gas turbine facility; A reformed gas supply passage for supplying a reformed gas from the reformed gas production apparatus to the mixing regulator; A fuel gas supply passage for supplying fuel gas from the mixing regulator to a gas turbine facility; And a control device for controlling the operation of the reformed gas production device and the mixing control device. The method of claim 1, The reformed gas production apparatus further includes a steam supply line, and is configured to supply the reformed gas obtained by reforming by further adding a vapor to a mixed gas of natural gas and air and chemically reacting the mixture adjusting device. Gas reforming plant. The method of claim 1, And a hydrogen concentration detector of the fuel gas provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage, And the control device is configured to adjust an amount of the reformed gas supplied from the reformed gas production device to the mixing control device based on the detection information of the hydrogen concentration detector. The method of claim 1, And a hydrogen concentration detector of the fuel gas provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage, The control device is configured to change the hydrogen concentration of the reformed gas by changing a mixing ratio of natural gas and air in the reformed gas production apparatus based on the detection information of the hydrogen concentration detector. equipment. The method of claim 2, And a hydrogen concentration detector of the fuel gas provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage, The control device is configured to change the hydrogen concentration of the reformed gas by changing a mixing ratio of natural gas, air and steam in the reformed gas production apparatus based on the detection information of the hydrogen concentration detector. Gas reforming equipment. The method of claim 1, A hydrogen concentration detector of a fuel gas provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage; And a dilution gas supply device for diluting the fuel gas with the dilution gas, which is installed in the mixing adjusting device, And the control device is configured to mix the dilution gas from the dilution gas supply device with respect to the fuel gas based on the detection information of the hydrogen concentration detector. The method of claim 1, And a hydrogen concentration detector of the fuel gas provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage, The gas reformer is configured to change the calorific value of the reformed gas by changing the mixing ratio of natural gas and air in the reformed gas production apparatus based on the detection information of the hydrogen concentration detector. . The method of claim 2, And a hydrogen concentration detector of the fuel gas provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage, The control device is configured to change the calorific value of the reformed gas by changing the mixing ratio of natural gas, air and steam in the reformed gas production apparatus based on the detection information of the hydrogen concentration detector. Reforming equipment. The method of claim 1, And a calorific value measuring means for fuel gas provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage, And the control device is configured to adjust an amount of the reformed gas supplied from the reformed gas production device to the mixing control device based on the detection information of the calorific value measuring means. The method of claim 1, And a calorific value measuring means for fuel gas provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage, The control device is configured to change the calorific value of the reformed gas by changing the mixing ratio of natural gas and air in the reformed gas production apparatus based on the detection information of the calorific value measuring means. equipment. The method of claim 2, And a calorific value measuring means for fuel gas provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage, The control device is configured to change the calorific value of the reformed gas by changing the mixing ratio of natural gas, air and steam in the reformed gas production apparatus based on the detection information of the calorific value measuring means. Reforming equipment. The method of claim 1, And a pressure measuring means for measuring the internal pressure of the passage provided in the fuel gas supply passage, And the control device is configured to adjust the amount of the reformed gas supplied from the reformed gas production device to the mixing control device based on the measurement information of the pressure measuring means. The method according to claim 1 or 2, Calorific value measuring means for fuel gas provided in at least a fuel gas supply passage among the reformed gas supply passage and the fuel gas supply passage; A dilution gas supply device for diluting the fuel gas with the dilution gas, which is installed in the mixing adjusting device, And the control device is configured to mix the dilution gas from the dilution gas supply device with respect to the fuel gas based on the detection information of the calorific value measuring means. The method of claim 1, The reforming gas production apparatus further comprises a heating steam supply line for supplying heating steam from a gas turbine installation to promote a chemical reaction in the reaction vessel thereof. The method of claim 14, The reforming gas production apparatus further includes a bleed line for extracting hot compressed air from the gas turbine facility and supplying it to the reaction vessel for heating for promoting the chemical reaction in the reaction vessel. A gas reforming plant configured to be able to supply. The method of claim 1, The reformed gas production apparatus includes a heat exchange means in its reformed gas supply passage, and the heat exchange means includes a mixed gas of natural gas and air supplied to the reaction vessel with a reformed gas supplied to the mixing regulator. A gas reforming plant, configured to perform heat exchange. The method of claim 1, The reforming gas supply passage includes cooling means for cooling the reformed gas supplied to the mixing regulator. The method of claim 17, And the cooling means is provided downstream of the heat exchange means in the reformed gas supply passage and configured to condense and remove the liquid in the reformed gas. The method of claim 1, A buffer tank is provided in the reformed gas supply passage, and the buffer tank absorbs the variation in the reformed gas flow rate so that the pressure of the reformed gas supplied to the mixing regulator is stabilized. .

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