JP2008214565A - Apparatus for supplying mixed gas and method for adjusting variation in composition in the apparatus for supplying mixed gas - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide an apparatus for supplying a mixed gas that is suitable for the stabilization of calorific value of a fuel gas such as a city gas and to provide a method for adjusting the variation in a composition of a mixed gas in the apparatus. <P>SOLUTION: In the apparatus for supplying a mixed gas, each of two packed columns is filled with the same adsorbent material therein. A piping extension S1 of a piping L3a extending from a branch piping L3 downstream of the packed column is formed so as to be longer than a piping extension S2 of a piping L4a. The piping L3a is provided with a plurality of outlets 10 in its passage and is constituted so as to render a piping extension S1 variable by means of the outlets. A value representing the variation in calorific value of a fuel gas to be supplied to a load apparatus 5 is adjusted by properly adjusting the opening degree of each of flow rate control valves V1 and V2 and/or the piping extension S1 of the piping L3a based on a measured value by a calorimeter 7. The control of calorific value is effected firstly by the action of the adsorbent material in each of the filling columns. The additional control of heat value is effected by the phase shift of the variation in calorific value by virtue of the difference in the extension of the branch piping and still further, the variation in calorific value can be kept to the minimum by appropriately setting a flow rate ratio and a piping extension S1. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

The present invention relates to a mixed gas supply device and a composition variation adjusting method thereof, and more particularly to a mixed gas supply device suitable for stabilizing a calorific value of fuel gas such as city gas and a composition variation adjusting method thereof.

  In recent years, LNG (liquefied natural gas) satellite bases have been built with increasing demand for city gas in regions far from metropolitan areas. The LNG satellite base is a facility equipped with LNG storage tanks and vaporizers. After transporting LNG from the coastal LNG receiving terminal by lorry and storing it in the LNG storage tank, the LNG is vaporized to industrial parks and residential areas. It is for supply as city gas.

In such an LNG satellite supply system, there is a case where the heat generation amount fluctuation of the supply gas accompanying the start of operation of the carburetor, load fluctuation, temperature change or the like becomes a problem. Various techniques have been disclosed. As an improvement of the vaporizer itself, a technique for purging LPG from a purge line when the LNG vaporizer is stopped has been proposed (for example, Patent Document 1).
In addition, as a calorific value adjustment device using an adsorbent, a technique for suppressing the calorific value by providing an adsorbent packed tower filled with activated carbon on the downstream side of the vaporizer has been proposed (for example, Patent Document 2). FIG. 16 shows a conventional calorific value adjusting device 100 using such an adsorbent packed tower. A conventional calorific value adjusting device 100 mainly includes an LNG storage tank 101, a vaporizer 102 using outside air as a heat source, and an adsorbent packed tower 103. The adsorbent packed tower 103 is filled with activated carbon having a pore diameter of 2.0 to 3.0 nm. With such a configuration, the LNG supplied via the tank lorry 105 and the line 106 is temporarily stored in the LNG storage tank 101, vaporized by the vaporizer 102 to become natural gas, and further passed through the adsorbent packed tower 103. Thus, when the composition ratio of the high boiling point (heavy hydrocarbon) component is high and the gas calorific value is high on the outlet side of the vaporizer, the high boiling point component is adsorbed by the adsorbent, and the composition ratio of methane which is the low boiling point component is When the gas calorific value is high and the gas calorific value is low, the adsorbed high boiling point component is desorbed to suppress the calorific value.

JP-A-7-109476 JP 2005-273753 A

  However, in the conventional calorific value adjustment method using an adsorbent, the amount of gas adsorbed per unit volume of the packed tower is limited because the adsorbent adsorbed amount is limited. Therefore, when a high degree of heat generation stabilization such as city gas supply is required, it is necessary to increase the amount of adsorbent filling, which increases the capacity of the packed tower and complicates construction work and installation work. There is an inevitable problem.

  The present invention is for solving such a problem, and in a mixed gas supply apparatus using an adsorbent, the composition fluctuation is suppressed to a certain range without increasing the adsorbent filling amount of the packed tower. The present invention provides a mixed gas supply device that enables supply. The gist of the present invention is as follows. That is,

The invention according to claim 1 is provided in a supply line for supplying a mixed gas whose gas composition varies over time, a parallel pipe section having a plurality of branch pipes in the supply line path, and in one or more branch pipe paths And a phase difference adjusting means for changing the phase of the composition fluctuation of the mixed gas passing through a part of the branch pipes with respect to the phase of the composition fluctuation of the other branch pipes. This is a mixed gas supply device.
Originally, the amount of suppression of the gas composition fluctuation range is determined by the amount of adsorbent packed, but the present invention makes it possible to suppress the fluctuation range beyond that limit by creating a phase difference in the gas composition fluctuation at the exit of each packed tower. Become.
In the present invention, “composition variation” is not limited to periodic variation, but also includes non-periodic variation, and includes not only continuous variation but also single variation. The term “phase” is a concept that means the time and timing until a result appears on the downstream side when a periodic or aperiodic composition fluctuation occurs. Furthermore, the “phase difference” is a concept that means a phase shift.
In the present invention, the “mixed gas” is a concept including a raw material gas, a by-product gas, an exhaust gas, a produced gas by biomass, and the like in the chemical industry.
In addition, as the “adsorbent” used in the present invention, activated carbon, zeolite, silica gel, mesoporous silica, activated alumina, organometallic complex, and the like can be used. Examples of the activated carbon include coal raw material activated carbon, coconut husk activated carbon, charcoal, petroleum raw material activated carbon, bamboo charcoal, phenol resin activated carbon, rayon-derived activated carbon, acrylonitrile-derived activated carbon, grass charcoal, sawdust charcoal, and peat.

In the above-mentioned invention, it is also possible to provide an apparatus in which means for adjusting the flow rate ratio of the mixed gas passing through each branch pipe is added to the parallel pipe section (claim 2).
In each of the above inventions, the “phase difference adjusting means” can be a difference in the material of the adsorbent to be packed (Claims 3 and 4) or a difference in the aspect ratio of each packed tower (Claim 5).
By making the aspect ratio (container length / inner diameter) of the filled containers different, a phase difference can be generated. In a filled container having a large aspect ratio, the fluctuation cycle is delayed because the discharge of the inflowing gas is delayed. Conversely, in a filled container having a small aspect ratio, the delay of the fluctuation cycle is small.
Furthermore, the “phase difference adjusting means” may be a difference in the shape of the adsorbent packed in each packed tower (claim 6). For example, if the particle size of the adsorbent decreases, the diffusion of gas in the container is delayed and the phase is delayed, and if the particle size increases, the phase delay decreases.

The “phase difference adjusting means” may be a difference in the pipe extension of the parallel pipe section (Claim 7), and the pipe extension can be arbitrarily adjusted (Claim 8).
For example, the phase of the mixed gas passing through the packed tower can be delayed by extending the length of the downstream piping of the packed tower.
Furthermore, a device in which two or more of the above “phase difference adjusting means” are combined can be provided. By combining two or more, a synergistic effect can be expected in adjusting the phase difference.
In each of the above inventions, a fuel gas can be used as the “mixed gas” (Claim 10), and a city gas mainly composed of methane can be used (Claim 11).

上式において、Ｓｉ、ｆｉはそれぞれ都市ガス中の各可燃性ガスの燃焼速度及び係数、Ａｉは都市ガス中の各可燃性ガスの含有率（体積百分率）、Ｋは減衰係数である。各係数の具体的数値についてはガス事業法に示されているため、ここでは省略する。
従って、本発明による混合ガス供給装置通過後の混合ガスのＷＩ及びＭＣＰを、例えば１３Ａ都市ガスの範囲に制御することにより、供給域内で都市ガス１３Ａ用機器を良好に燃焼させることができる。 The invention of claim 12 is provided with the mixed gas supply device of claim 10 or 11, and further configured such that the calorific value of the fuel gas or city gas after passing through the parallel pipe section can be adjusted within a predetermined range. Is a calorific value adjustment device.
When the composition variation occurs in the fuel gas, the calorific value also varies accordingly. The present invention adjusts the calorific value using the above-mentioned mixed gas supply device in order to suppress the calorific value fluctuation accompanying the composition fluctuation of the fuel gas.
Currently, city gas nationwide is classified into 14 types of gas groups based on the Wobbe index and burning rate index, and city gas companies can supply city gas of the specified gas type to consumers in the supply area. As required by the Gas Business Law. For example, 13A city gas mainly composed of methane is defined as 52.7 ≦ WI ≦ 57.8 and 35 ≦ MCP ≦ 47. Here, the Wobbbe index (WI) is a numerical value obtained by dividing the calorific value H (MJ / m3) of the gas by the square root of the specific gravity s of the gas with respect to air.
WI = H / √s
This is an index of complete combustibility of gas equipment.
The combustion rate index (MCP) is expressed by the following equation.

In the above equation, Si and fi are the burning rate and coefficient of each combustible gas in the city gas, Ai is the content (volume percentage) of each combustible gas in the city gas, and K is the attenuation coefficient. Specific numerical values for each coefficient are shown in the Gas Business Law, and are therefore omitted here.
Therefore, by controlling the WI and MCP of the mixed gas after passing through the mixed gas supply apparatus according to the present invention within the range of, for example, 13A city gas, the city gas 13A equipment can be burned well in the supply area.

A thirteenth aspect of the present invention is the mixed gas supply apparatus according to any one of the first to eleventh aspects, wherein when the cycle of the composition variation cycle of the mixed gas that passes through each branch pipe is the same, the mixture that passes through some branch pipes A composition variation adjustment method in a mixed gas supply apparatus, wherein the phase of a gas composition variation cycle is adjusted to be delayed by π radians with respect to the phase of another branch pipe.
The waveform of the composition variation at the downstream side merging portion of the parallel piping portion is a combination of the composition variation waveforms of the mixed gas passing through each branch piping. In this case, when the composition variation period is the same, the variation width is minimized when the phase difference is π radians. Therefore, the composition fluctuation can be effectively suppressed by making such adjustment.

  According to a fourteenth aspect of the present invention, there is provided the mixed gas supply apparatus according to the tenth or eleventh aspect, wherein the calorific value of the fuel gas or the city gas whose gas composition changes with time is adjusted to be within a predetermined range. It is a calorific value adjustment method in a mixed gas supply device characterized by controlling one or both of a phase difference and a flow rate ratio.

According to the present invention, it is possible to provide a mixed gas supply device that enables gas supply while suppressing composition fluctuation within a certain range without increasing the amount of adsorbent packed in the packed tower.
Further, in the invention using fuel gas as a mixed gas, even if a gas accompanied by a calorific value variation is supplied from a supplier, the calorific value variation is suppressed to a certain range and supplied to the consumer. Is possible.

Hereinafter, embodiments of the present invention will be described in more detail with reference to FIGS. In addition, in order to avoid duplication description, in each figure, the same structure is shown using the same code | symbol. Needless to say, the scope of the present invention is described in the claims and is not limited to the following embodiments.
(First embodiment)
This embodiment uses a fuel gas (LNG raw material) whose composition changes over time as a “mixed gas”, and uses a difference in pipe extension as a “phase difference adjusting means”, thereby changing the composition (heating value fluctuation). It is intended to suppress this.
FIG. 1 is a diagram illustrating an overall configuration of a fuel gas supply apparatus 1 according to the present embodiment. The fuel gas supply apparatus 1 includes an LNG storage tank 4, a vaporizer 3, two adsorbent packed towers 2a and 2b provided in parallel in the path of the branch pipes L3 and L4, and a load apparatus at the end of the supply line. 5 (for example, a gas engine). The LNG storage tank 4 stores LNG carried by a tank truck (not shown). These devices are connected by pipes L1 to L5. The same adsorbent (for example, coal raw material activated carbon, coconut shell raw material activated carbon, etc.) is packed in the two packed towers. On the upstream side of the packed towers of the branch pipes L3 and L4, flow control valves V1 and V2 are arranged, respectively. A calorimeter 7 is disposed in the pipe L5 path. The pipe extension S1 of the downstream pipe L3a of the packed tower downstream of the branch pipe L3 is formed longer than the pipe extension S2 of the pipe L4a. Further, a plurality of outlets 10 are provided in the middle of the pipe L3a, so that the pipe extension S1 is variable.
The fuel gas supply device 1 includes a control unit 8 and appropriately adjusts the opening of the flow rate adjusting valves V1 and V2 and / or the piping L3a piping extension S1 based on the measurement value of the calorimeter 7 to the load device 5. It is configured such that the calorific value fluctuation value of the supplied fuel gas can be adjusted.

With the above configuration, the fuel gas supply device 1 vaporizes the LNG in the LNG storage tank 4 with the vaporizer 3 into natural gas, passes through the adsorbent packed towers 2a and 2b, and then passes through the supply line L5 to load the load device. 5 is supplied. In this case, first, the calorific value is suppressed by the action of the adsorbent in each packed tower. Further, the heat generation amount is further suppressed by the shift of the heat generation amount fluctuation phase due to the difference in the branch pipe extension. However, by appropriately setting the flow rate ratio and the pipe extension S1 as described above, the heat generation amount fluctuation should be minimized. Can do. The relationship between the length of the pipe and the phase shift can be expressed by the following equation.

In this embodiment, the pipe extension and the flow rate ratio of the branch pipe L3a are appropriately selected. However, the pipe extension and the flow rate ratio that minimize the variation in the heat generation amount are known in advance and fixed to those values. It can also be in the form.
Moreover, although it was set as the form which arrange | positions an adsorbent packed tower in both branch piping path | routes, the form which arrange | positions a packed tower only to one branch pipe, and does not arrange a packed tower in the other branch pipe, lengthens the pipe extension It is good. Further, the length of the pipe extension may be variable.
Moreover, although the form which arrange | positions two adsorbent packed towers in parallel was shown, it is good also as a form which arrange | positions three or more packed towers in parallel, and makes each piping extension and flow rate ratio variable.
Moreover, although it was set as the form filled with the same adsorbent in two packed towers, it is good also as a form filled with a different adsorbent. Moreover, it can also be set as the form which uses the thing of a different shape with the same adsorbent.

(Second embodiment)
Next, another embodiment of the present invention will be described. FIG. 2 is a diagram illustrating an overall configuration of the fuel gas supply device 20 according to the present embodiment. The fuel gas supply device 20 is different from the fuel gas supply device 1 described above in that the aspect ratios (container length / inner diameter) of the two packed towers 21a and 21b are different. That is, the aspect ratio AR1 of the packed tower 21a is X1 / D1, whereas the aspect ratio AR2 of the packed tower 21b is X2 / D2, and AR1> AR2. Moreover, the point which is not provided with the extension piping part and the flow control valves V1 and V2 differs. Since the other configuration is the same as that of the fuel gas supply device 1, a duplicate description is omitted.
In the fuel gas supply device 20, since the discharge of the gas flowing into the packed tower 21a side having a large aspect ratio is delayed, the phase of fluctuation of the calorific value is delayed as compared with the packed tower 21b side. This makes it possible to reduce the fluctuation range of the calorific value as compared with the same type of fuel supply device having a packed tower with the same aspect ratio.
In the present embodiment as well, it is possible to further adjust the fluctuation range of the calorific value as a form including the extension pipe portion and the flow rate adjusting valves V1, V2.

(Third embodiment)
Furthermore, another embodiment of the present invention will be described. FIG. 3 is a diagram showing an overall configuration of the fuel gas supply device 30 according to the present embodiment. The fuel gas supply device 30 differs from the fuel gas supply device 10 described above in that there is no packed tower in any of the branch pipes L9 and L10, and the pipe extension of the branch pipe L9 is used as a phase difference adjusting means. Is to make it longer. Other configurations are the same as those of the fuel gas supply apparatus 1.
With the above configuration, the flow rate fluctuation range can be reduced by adjusting the flow rate ratio based on the measurement value of the calorimeter 7 and delaying the phase of the fluctuation cycle on the branch pipe L9 side at the junction P1 by π radians. It becomes possible.
In the present embodiment, the pipe extension and the flow rate ratio of the branch pipe L9 may be fixed to values such that the phase is delayed by π radians.

In order to confirm the calorific value suppression effect according to the present invention, the following tests were conducted.
(Test adsorption material)
Two types of adsorbents, ie, coal raw material activated carbon and coconut shell raw material activated carbon were used (hereinafter, the coal raw material activated carbon may be abbreviated as activated carbon A and the coconut shell raw material activated carbon may be referred to as activated carbon B). The physical properties of the activated carbons A and B are shown in Table 1, and the pore size distribution (by nitrogen adsorption DFT method) is shown in FIG. Moreover, the pressure-adsorption amount characteristic with respect to the methane and propane of activated carbon A and B is shown in FIG.4 (b).

（試験ガス）
２分間、ＬＮＧ気化ガス（組成：CH4：90.8%、C2H6：5.0%、C3H8：3.0%、i-C4H10：0.6%、n-C4H10：0.6%）を流し、その後１分間、このガスに添加用ガス（プロパン：ブタン＝１：１）を添加するサイクルを繰り返すことにより、周期的に組成（発熱量）が変動するガスを調製した。試験ガスの発熱量変動は、最小４４．８ＭＪ/ｍ３、最大５０．８ＭＪ/ｍ３であり、ΔＨ＝２．８５ＭＪ/ｍ３であった。ここにΔＨは、ΔＨ＝（Ｈｍax−Ｈmin）／２、すなわち発熱量最大値Ｈｍaxと最小値Ｈminの差の１/２であり、発熱量変動幅比較の指標となる数値である。

(Test gas)
Flow LNG vapor (composition: CH4: 90.8%, C2H6: 5.0%, C3H8: 3.0%, i-C4H10: 0.6%, n-C4H10: 0.6%) for 2 minutes, then add to this gas for 1 minute By repeating the cycle of adding gas (propane: butane = 1: 1), a gas whose composition (calorific value) fluctuates periodically was prepared. The calorific value variation of the test gas was a minimum of 44.8 MJ / m3, a maximum of 50.8 MJ / m3, and ΔH = 2.85 MJ / m3. Here, ΔH is ΔH = (Hmax−Hmin) / 2, that is, 1/2 of the difference between the maximum calorific value Hmax and the minimum value Hmin, and is a numerical value serving as an index for comparing the calorific value fluctuation range.

(Test equipment)
A test device in which two adsorbing materials were filled in two filling containers (total volume of 30 cc) arranged in parallel was used. In this case, in accordance with the first embodiment, the pipe extension on the downstream side of one filling container (container 1) is made longer than that of the other filling container (container 2), so that the predetermined amount of time in the calorific value fluctuation cycle is reached. A phase difference was created. The calorific value fluctuation period at the container outlet was the same for both the container 1 and the container 2 at 1 period (2π radians) = 180 sec. For reference, Table 2 shows the correspondence between the radian display of the phase difference and the time display.

(Test method)
Each packing container is filled with the adsorbent in the combination of No. 1 to No. 3 in Table 3, and the test gas is allowed to flow in the inflow conditions of a superficial velocity of 2000 h ⁻¹ and a temperature of 25 ° C. The calorific value of the gas was measured with a calorimeter (manufactured by Advantica, product name: GasPT). In the measurement, the relationship between the flow rate ratio change and the calorific value fluctuation was examined using the phase difference as a parameter.

（測定結果）
図５に、No.１条件における各位相差での発熱量変動の流量比依存性結果を示す。同図において縦軸ΔＨは、ΔＨ＝（Ｈｍax−Ｈmin）／２、すなわち発熱量最大値Ｈｍaxと最小値Ｈminの差の１/２であり、発熱量変動幅比較の指標である。ここに、横軸においてＦ１、Ｆ２はそれぞれ容器１、容器２の流量であり、Ｆ１／（Ｆ１＋Ｆ２）は全体流量に対する容器１の比率である。なお、従来技術の容器１個を用いる場合（図１６参照）は、Ｆ１＝１、Ｆ２＝０であるから、ΔＨは図５において横軸Ｆ１／（Ｆ１＋Ｆ２）＝１における値となる。

(Measurement result)
FIG. 5 shows the result of the flow rate dependency of the variation in heat generation at each phase difference under No. 1 condition. In the figure, the vertical axis ΔH is ΔH = (Hmax−Hmin) / 2, that is, 1/2 of the difference between the maximum calorific value Hmax and the minimum value Hmin, and is an index for comparing the calorific value fluctuation range. Here, on the horizontal axis, F1 and F2 are the flow rates of the containers 1 and 2, respectively, and F1 / (F1 + F2) is the ratio of the container 1 to the total flow rate. When one conventional container is used (see FIG. 16), F1 = 1 and F2 = 0, so ΔH is the value on the horizontal axis F1 / (F1 + F2) = 1 in FIG.

From this figure, this material has the maximum effect of suppressing the fluctuation when the flow ratio is 50:50 and the phase difference π (90 seconds), but no container or one container is also obtained under other flow ratio and phase difference conditions. It can be seen that the suppression effect is high compared to the above conditions.
FIG. 6 is a diagram showing a change in heat generation amount variation time when the flow ratio is 50:50 and the phase difference is π (90 seconds).
7 and 8 show the same measurement results as in No. 2 condition. 9 and 10 show the same measurement results as in No. 3 conditions.

(Test equipment)
As shown in FIG. 15, a test apparatus was used in which the adsorbent-filled container 3 (internal volume 30 cc) was arranged only in one branch pipe of the parallel pipe section, and only the bypass pipe was not arranged in the other. And the piping extension part by the side of a filling container was made longer than the bypass piping side, and it was made for the predetermined | prescribed phase difference to arise in the emitted-heat amount fluctuation | variation. For example, the phase delay is π / 5 radians (18 seconds long) when the pipe inner diameter is 4.35 mm and the pipe extension is 20.1 m.
(Test method)
Under the conditions of Nos. 4 and 5 in Table 3, the container 3 was filled with an adsorbent, and the same measurement as in Example 1 was performed.
(Measurement result)
FIG. 11 is a diagram showing the flow ratio dependency measurement result of the calorific value fluctuation at each phase difference under No. 4 (activated carbon A) condition. Further, FIG. 12 shows heat amount fluctuation time transition data when (1) flow rate ratio = 81: 19, phase difference 0, and (2) flow rate ratio = 81: 19, phase difference π / 5 (18 seconds). FIG.
ΔH = 0.58 (MJ / m3) in (1), ΔH = 0.42 in (2), value when one pipe is not extended, ΔH = 0.73 (see Example 1) It can be seen that the effect of suppressing the variation in heat generation is higher than

FIG. 13 is a diagram showing a flow ratio dependency measurement result of a heat generation amount variation at each phase difference under No. 5 (activated carbon B) condition. Moreover, FIG. 14 shows calorific value fluctuation time transition data when (1) flow rate ratio = 93: 7, phase difference 0, and (2) flow rate ratio = 83: 17, phase difference π / 4 (22 seconds). FIG. In the case of activated carbon B (coconut shell raw material activated carbon), it can be seen that the same calorific value fluctuation suppressing characteristics as activated carbon A (coal raw material activated carbon) are exhibited.
As described above, the heating value fluctuation suppressing effect according to the present invention has been demonstrated under any of No. 1 to No. 5.

  The present invention is widely used not only for suppressing the calorific value of fuel gas but also for suppressing the composition of a mixed gas composed of a plurality of gas components whose composition varies, such as raw material gas, by-product gas, exhaust gas, and produced gas by biomass in the chemical industry. Is possible.

It is a figure which shows the structure of the fuel gas supply apparatus 1 which concerns on 1st embodiment. It is a figure which shows the structure of the fuel gas supply apparatus 20 which concerns on 2nd embodiment. It is a figure which shows the structure of the fuel gas supply apparatus 30 which concerns on 3rd embodiment. It is a figure which shows the pore size distribution of activated carbon A and B which are test adsorption materials. It is a figure which shows the pressure-adsorption amount characteristic with respect to methane and propane of activated carbon A and B. The result of the flow rate dependency of the calorific value fluctuation in No. 1 condition is shown. It is a figure which shows the calorific value fluctuation | variation time transition at the flow rate ratio of 50:50 in No. 1 conditions, and phase difference (pi) (90 second). It is a figure which shows the flow rate dependence result of the emitted-heat amount fluctuation | variation in No. 2 conditions. It is a figure which shows the calorific value fluctuation | variation time transition at the flow rate ratio of 50:50 and phase difference (pi) (90 second) in No. 2 conditions. It is a figure which shows the flow rate dependence result of the emitted-heat amount fluctuation | variation in No.3 conditions. It is a figure which shows the calorific value fluctuation | variation time transition at the time of flow rate ratio 50:50 and phase difference (pi) (90 second) in No. 3 conditions. It is a figure which shows the flow rate dependence result of the emitted-heat amount fluctuation | variation in No.4 conditions. The figure which shows the calorific value fluctuation | variation time transition in the case of (1) flow rate ratio = 81: 19, phase difference 0, and (2) flow rate ratio = 81: 19, phase difference (pi) / 5 (18 second) in No. 4 conditions. It is. It is a figure which shows the flow-dependency result of the emitted-heat amount fluctuation | variation in No. 5 conditions. The figure which shows the calorific value fluctuation | variation time transition in the case of (1) flow rate ratio = 93: 7, phase difference 0, and (2) flow rate ratio = 83: 17, phase difference π / 4 (22 seconds) in No. 5 condition. It is. FIG. 3 is a diagram showing a test apparatus of Example 2. It is a figure which shows the structure of the conventional calorific value adjustment apparatus.

Explanation of symbols

1, 20, 30 ... Fuel gas supply devices 2a, 2b, 21a, 21b ... Adsorbent packed tower 3 ... Vaporizer 4 ... LNG storage tank 5 ... Load device 7 .... Calorimeters L1 to L10 ... Supply lines V1, V2 ... Flow control valve

Claims (14)

A supply line for supplying a mixed gas whose gas composition varies over time;
A parallel pipe section having a plurality of branch pipes in the supply line path;
An adsorbent packed tower provided in one or more branch piping paths;
A phase difference adjusting means for changing the phase of the composition fluctuation of the mixed gas passing through some branch pipes with respect to the phase of the composition fluctuation of other branch pipes;
A mixed gas supply apparatus comprising: The mixed gas supply apparatus according to claim 1, wherein the parallel pipe section further includes means for adjusting a flow rate ratio of the mixed gas passing through each branch pipe. 3. The mixed gas supply apparatus according to claim 1, wherein the phase difference adjusting unit includes a difference in the material of the adsorbent packed in the packed tower. 4. The mixed gas supply device according to claim 3, wherein the adsorbent includes coal raw material activated carbon and coconut shell raw material activated carbon. 5. The mixed gas supply apparatus according to claim 1, wherein the phase difference adjusting means includes a difference in aspect ratio of each packed tower. 6. The mixed gas supply apparatus according to claim 1, wherein the phase difference adjusting means includes a difference in shape of an adsorbent packed in each packed tower. The mixed gas supply device according to claim 1, wherein the phase difference adjusting means includes a difference in pipe extension of a parallel pipe section. 8. The mixed gas supply apparatus according to claim 7, further comprising means for arbitrarily adjusting the pipe extension of some of the branch pipes. The mixed gas supply apparatus according to claim 1 or 2, wherein two or more phase difference adjusting means according to any one of claims 1 to 8 are combined. The mixed gas supply apparatus according to claim 1, wherein the mixed gas is a fuel gas. The mixed gas supply device according to claim 10, wherein the fuel gas is a city gas mainly composed of methane. A calorific value adjustment comprising the mixed gas supply device according to claim 10 or 11, wherein the calorific value of fuel gas or city gas after passing through the parallel pipe section can be adjusted within a predetermined range. apparatus. In the mixed gas supply apparatus according to any one of claims 1 to 11, when the cycle of the composition variation cycle of the mixed gas passing through each branch pipe is the same,
A composition fluctuation adjusting method for a mixed gas supply apparatus, wherein the phase of a composition fluctuation cycle of a mixed gas passing through some branch pipes is adjusted to be delayed by π radians with respect to the phase of other branch pipes. The mixed gas supply apparatus according to claim 10 or 11,
In the mixed gas supply apparatus, wherein one or both of the phase difference and the flow rate ratio are controlled so that the calorific value of the fuel gas or the city gas whose gas composition changes with time is adjusted within a predetermined range. The calorific value adjustment method.

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