JP2018166482A - Fluid mixing device, gas processing equipment and waste disposal system - Google Patents

Abstract

To provide a fluid mixing device capable of supplying a second fluid into a device body at high efficiency, regulating a flow of a first fluid in the device body for forming a uniform flow, thereby mixing efficiently and in a uniform manner, the first fluid and second fluid in each part in the device body, and to provide gas processing equipment and waste disposal system comprising the above mentioned fluid mixing device.SOLUTION: A gas fermentation device (fluid mixing device) comprises: a container for storing a culture broth including a gas utilization bacterium; a circulation line connected to the container; and a pump provided in a midway of the circulation line for circulating the culture broth through the circulation line. In the container, plural fluid mixing parts 10 are provided along a vertical direction of the container so as to traverse the flow of teh culture broth. Each of the fluid mixing parts 10 comprises: plural open holes 10a which are formed of plural holes 11a of a plate-shaped part 11 and an inner space 12a of a corresponding cylindrical part 12; and one space 10b defined by the plate-shaped part 11 and the plural cylindrical parts 12.SELECTED DRAWING: Figure 2

Description

  The present invention relates to a fluid mixing device, a gas processing device, and a waste processing system.

  Synthetic reactions of organic substances and culturing of microorganisms are widely performed in liquids stored in containers. In the organic substance synthesis reaction, a raw material gas is supplied into a liquid (medium oil containing a catalyst), and the organic substance is synthesized from the raw material gas by the action of the catalyst (see, for example, Patent Document 1). Further, in the culture of microorganisms, a gas necessary for the growth of microorganisms is supplied into a liquid (culture solution) to propagate the microorganisms (for example, Patent Document 2).

  In order to improve the yield of organic substances and the growth rate of microorganisms, it is important to uniformly disperse the gas in the liquid. For this reason, in Patent Document 1, the raw material gas is supplied into the liquid as bubbles using a sparger arranged on the bottom side of the container. Furthermore, in patent document 2, stirring the liquid in a container is also performed using a stirring blade.

  However, when considering increasing the size (especially height) of the container, the current stirring method may form a uniform flow (uniform flow) of the liquid in the horizontal direction of the container. Can not. For this reason, even if gas is supplied as a bubble from the sparger, it is difficult to uniformly disperse the liquid in each part in the container.

  On the other hand, when supplying (injecting) the gas into the container, it is necessary to pressurize the gas, which requires pressurizing energy. In particular, when the gas is pressurized by a compressor or the like, the temperature of the gas rises due to the pressurization, so that the energy used for heating is lost. Moreover, the gas after pressurization may need to be cooled. For this reason, the cost required for installation of the cooling device and the cost required for its operation increase. Furthermore, the heat energy discarded by cooling the gas is wasted.

JP 2012-246232 A JP 2012-44943 A

  An object of the present invention is to supply the second fluid into the apparatus main body with high efficiency, and to arrange the flow of the first fluid in the apparatus main body to form a uniform flow, so that each part in the apparatus main body An object of the present invention is to provide a fluid mixing apparatus capable of mixing a first fluid and a second fluid efficiently and uniformly. Another object of the present invention is to provide a gas treatment device and a waste treatment system having such a fluid mixing device.

  Such an object is achieved by the present invention described below.

[1] The fluid mixing device of the present invention comprises:
An apparatus body for passing or storing the first fluid;
A flow generating mechanism for generating a flow of the first fluid in the apparatus body;
A second fluid supply mechanism for supplying a second fluid into the apparatus body;
One or more fluids provided in the apparatus body so as to cross the flow of the first fluid and mixing the first fluid and the second fluid when the second fluid passes through A mixing section,
The fluid mixing unit is closed at a plurality of through holes penetrating in the flow direction of the first fluid and downstream in the flow direction of the first fluid, and can temporarily store the second fluid. And a storage space.

  [2] In the fluid mixing device of the present invention, it is preferable that the first fluid is a liquid and the second fluid is a gas.

  [3] In the fluid mixing device of the present invention, it is preferable that the first fluid is a liquid and the second fluid is also a liquid.

  [4] In the fluid mixing apparatus of the present invention, it is preferable that the first fluid is a gas and the second fluid is a liquid.

  [5] In the fluid mixing apparatus of the present invention, it is preferable that the first fluid is a gas and the second fluid is also a gas.

  [6] In the fluid mixing device of the present invention, it is preferable that the fluid mixing unit includes a plurality of communication passages that connect the plurality of through holes and the storage space.

[7] In the fluid mixing device of the present invention, when the average cross-sectional area of the through hole is A [mm ² ] and the average cross-sectional area of the communication path is B [mm ² ], B / A is 0.01 It is preferable that it is -0.2.

  [8] In the fluid mixing device of the present invention, it is preferable that each through hole includes a portion whose cross-sectional area gradually decreases from the downstream side in the flow direction of the first fluid toward the upstream side.

  [9] In the fluid mixing device of the present invention, it is preferable that the distance between the openings on the downstream side in the flow direction of the first fluid in the adjacent through holes is 1 mm or less.

  [10] In the fluid mixing device of the present invention, it is preferable that the storage space is open upstream of the fluid mixing unit in the flow direction of the first fluid.

  [11] In the fluid mixing device of the present invention, it is preferable that the storage space is closed on the upstream side of the fluid mixing portion in the liquid flow direction.

  [12] In the fluid mixing device of the present invention, it is preferable that each through hole includes a portion whose cross-sectional area gradually decreases from the upstream side to the downstream side in the flow direction of the first fluid.

  [13] In the fluid mixing device of the present invention, it is preferable that the distance between the openings on the upstream side in the flow direction of the first fluid of the adjacent through holes is 1 mm or less.

  [14] In the fluid mixing apparatus of the present invention, it is preferable that the second fluid supply mechanism is configured to directly supply the second fluid to the storage space of the fluid mixing unit.

  [15] In the fluid mixing device of the present invention, when the fluid mixing unit is viewed from the downstream side in the flow direction of the first fluid, the ratio of the plurality of through holes to the fluid mixing unit is 1 to 50%. It is preferable that

  [16] In the fluid mixing device of the present invention, when the fluid mixing section is viewed from the upstream side in the flow direction of the first fluid, the ratio of the plurality of through holes to the fluid mixing section is 10 to 50%. It is preferable that

  [17] In the fluid mixing device of the present invention, it is preferable that the one or more fluid mixing units include a plurality of the fluid mixing units provided along the flow direction of the first fluid.

  [18] In the fluid mixing apparatus of the present invention, it is preferable that the apparatus main body is formed of a tubular body through which the first fluid passes.

  [19] In the fluid mixing device of the present invention, it is preferable that the device main body is constituted by a container for storing the first fluid.

[20] In the fluid mixing device of the present invention, the container includes a cylindrical body, a bottom that closes a lower end opening of the body, and a top that closes an upper end opening of the body.
The flow generation mechanism includes a line that connects the upper portion of the body portion and the bottom portion, and a pump that is provided in the middle of the line and that circulates the liquid. It is preferable that the liquid flow toward the upper side is generated.

[21] Further, the gas treatment device of the present invention comprises:
The fluid mixing device;
The container of the fluid mixing apparatus further includes a processing unit that processes an organic substance generated from the gas supplied as the second fluid.

[22] Further, the waste treatment system of the present invention includes:
The gas treatment device;
A gas generating unit connected to the container and configured to generate the gas by processing waste.

  According to the present invention, the second fluid is supplied into the apparatus main body with high efficiency, and the flow of the first fluid in the apparatus main body is adjusted to form a uniform flow. The first fluid and the second fluid can be mixed efficiently and uniformly.

It is a side view which shows typically the gas fermenter using the fluid mixing apparatus of this invention. It is a fragmentary sectional perspective view which shows one structural example of the fluid mixing part with which the gas fermenter of FIG. 1 is provided. It is a fragmentary sectional view which shows the fluid mixing part of FIG. It is a fragmentary sectional view showing other examples of composition of a fluid mixing part. It is a fragmentary sectional perspective view which shows the other structural example of a fluid mixing part. It is a fragmentary sectional view which shows the fluid mixing part of FIG. It is a fragmentary sectional view showing other examples of composition of a fluid mixing part. It is a block diagram showing an embodiment of a waste disposal system of the present invention. It is a figure which shows typically the structure of the drying part, gasifier, heat exchanger, and distiller which the waste disposal system of FIG. 8 has. FIG. 8 is a diagram schematically illustrating a cross section of the fluid mixing unit illustrated in FIG. 7 in order to perform simulation in the example. It is a figure which shows the structure for performing a simulation with a comparative example.

Hereinafter, a fluid mixing device, a gas treatment device, and a waste treatment system of the present invention will be described in detail based on preferred embodiments shown in the accompanying drawings.
<Gas fermenter>
First, a gas fermenter using the fluid mixing apparatus of the present invention will be described.

  FIG. 1 is a side view schematically showing a gas fermenter using the fluid mixing apparatus of the present invention, and FIG. 2 is a partial cross-sectional perspective view showing one configuration example of a fluid mixing unit provided in the gas fermenter of FIG. 3 is a partial cross-sectional view showing the fluid mixing section of FIG. 2, FIG. 4 is a partial cross-sectional view showing another configuration example of the fluid mixing section, and FIG. 5 is a partial cross-section showing another configuration example of the fluid mixing section. FIG. 6 is a partial cross-sectional view showing the fluid mixing unit in FIG. 5, and FIG. 7 is a partial cross-sectional view showing another configuration example of the fluid mixing unit.

  In addition, in FIG.3, FIG.4, FIG.6 and FIG. 7, the production | generation state of the bubble in a fluid mixing part is shown. Moreover, in FIG. 2 to FIG. 7, hatching indicating a cross section is omitted so as not to make it difficult to see the drawings.

  A gas fermenter (culture container) 6 shown in FIG. 1 includes a container (device main body) 61 that stores a culture solution (first fluid) containing gas-assimilating bacteria (microorganisms), and a circulation connected to the container 61. A line 62 and a pump 63 provided in the middle of the circulation line 62 for circulating the culture solution through the circulation line 62 are provided. That is, the gas fermenter 6 is a type of fermenter that stirs the culture solution by circulating the culture solution itself.

  The container 61 includes a cylindrical body 611 arranged with the longitudinal direction as a vertical direction, a bottom 612 that closes the lower end opening of the body 611, and a top 613 that closes the upper end opening of the body 611. The circulation line 62 is connected to the upper portion and the bottom portion 612 of the trunk portion 611. By the operation of the pump 63, a culture fluid flow is generated in the container 61 from the bottom side (lower side) to the top side (upper side). Accordingly, in this embodiment, the circulation line 62 and the pump 63 constitute a flow generation mechanism that generates a flow of the culture solution (liquid) in the container 61.

  The container 61 is provided with a line for supplying a culture solution and gas-assimilating bacteria (not shown), a gas line 202 for supplying gas into the culture solution (inside the container 61), and a gas-assimilating bacterium, as described later. A liquid line 301 for discharging the culture solution after the operation is connected. Therefore, in the present embodiment, a gas supply mechanism (second fluid) for supplying gas (second fluid) into the container 61 by the gas line 202 and a pump (not shown) provided in the middle of the gas line 202. Fluid supply mechanism).

  In such a gas fermenter 6, the culture solution and the gas-assimilating bacteria are supplied and stored in the container 61. Next, by operating the pump 63, a flow of the culture solution from the lower side to the upper side is generated in the container 61 to stir the culture solution. While maintaining this state, gas (raw material gas) is supplied into the container 61 via the gas line 202. Thereby, gas-assimilating bacteria are cultured in a culture solution, and an organic substance is produced | generated from gas by the fermentation action.

  In the present embodiment, the flow direction of the culture solution is a direction from the lower side to the upper side of the container 61. Accordingly, “upstream side in the flow direction of the culture medium” corresponds to the lower side of the container 61, and “downstream side in the flow direction of the culture liquid” corresponds to the upper side of the container 61.

  In the container 61 (body 611), a plurality of fluid mixing units 10 are provided along the vertical direction of the container 61 (flow direction of the culture solution) and across the flow of the culture solution. As shown in FIG. 2, each fluid mixing part 10 includes a plate-like part 11 having a plurality of holes 11a and a plurality of cylindrical parts provided on the lower surface of the plate-like part 11 so as to surround each hole 11a. 12.

  With such a configuration, each fluid mixing unit 10 includes a plurality of through holes 10a configured by the plurality of holes 11a and the corresponding internal space 12a of the cylindrical portion 12. Therefore, each through hole 10a penetrates in the vertical direction of the fluid mixing unit 10 (the flow direction of the culture solution).

  The fluid mixing unit 10 includes a single space 10 b defined by the plate-like part 11 and the plurality of cylindrical parts 12. Therefore, the space 10b is closed on the upper side of the fluid mixing unit 10 and opened on the lower side. This space 10 b functions as a storage space for temporarily storing the gas supplied into the container 61.

  As shown in FIG. 3, when the culture solution passes through the fluid mixing unit 10, it is necessary to pass through the elongated through hole 10a. At this time, the culture solution has a passage resistance, and its flow is adjusted. (Rectified). As a result, a uniform culture fluid flow (uniform flow) is generated in the horizontal direction in the container 61.

  The passage resistance increases the load of the pump 63, and the increase in the load can be changed to heat due to the viscosity of the culture solution (first fluid) or to heat due to friction with the fluid mixing unit 10. In addition, it is used when bubbles are generated in the fluid mixing unit 10 by entraining gas, and is used to generate a vortex under the fluid mixing unit 10 after passing through the fluid mixing unit 10. Alternatively, it may be used to guide low pressure gas to the high pressure medium side.

  On the other hand, the gas supplied into the container 61 is received in the space 10b and spreads in the surface direction (horizontal direction) of the fluid mixing unit 10 and stored. When an amount of gas exceeding the volume of the space 10b is stored in the space 10b, the gas receives a shearing force from the culture solution and is gradually released from the space 10b into the culture solution as a valve.

  The generated gas bubbles (hereinafter simply referred to as “bubbles”) ride on the flow of the rectified culture solution (uniform flow), pass through each through-hole 10a, and move upward toward the container 61. Move. That is, the gas becomes bubbles when passing through the fluid mixing unit 10 and is dispersed (mixed) in the culture solution.

  By using such a fluid mixing unit 10, the bubbles can be uniformly dispersed in the horizontal direction of the container 6. In addition, by using a plurality of fluid mixing units 10, even when some of the bubbles move together toward the upper side of the container 6, the fluid mixing units 10 located on the upper side may be combined. Thus, the bubbles that are coarsened by coalescence due to the above-described action can be divided again into fine bubbles.

  Thereby, it is possible to uniformly disperse the bubbles in the culture solution in each part in the container 6. Moreover, microbubbles are easy to dissolve in the culture solution. For this reason, the gas-assimilating bacterium can efficiently generate gas from the gas using the gas.

  Here, the average diameter of the generated bubbles is preferably about 100 to 1,500 μm, and more preferably about 300 to 1,000 μm. The diameter of the bubble can be controlled by appropriately setting, for example, the average cross-sectional area of the through-holes 10a, the shape of each through-hole 10a, the pressure of the supplied gas, the flow rate (circulation speed) of the culture solution, and the like. .

  In the present embodiment, a supply path 611 a that penetrates the body 611 is formed in the body 611 of the container 61 at a position corresponding to the fluid mixing unit 10. A gas line 202 is connected to the container 61 so as to communicate with the supply path 611a, and the gas is directly supplied to the space 10b of the fluid mixing unit 10.

  The gas may be supplied to a position below the fluid mixing unit 10 and away from the fluid mixing unit 10 without being supplied directly to the space 10 b of the fluid mixing unit 10. However, by adopting a configuration in which the gas is directly supplied to the space 10b of the fluid mixing unit 10, it becomes easier to use the shearing force generated by the culture solution flowing toward the upper side of the container 61, and bubbles can be generated more efficiently. .

  In the present embodiment, the boundary between the plate-like portion 11 and each cylindrical portion 12 is rounded. That is, each through-hole 10a has a portion (cross-sectional area gradually decreasing portion) where the cross-sectional area (cross-sectional area in the horizontal direction) gradually decreases from the upper side to the lower side at the upper end portion thereof. Thereby, the flow of the culture solution in the vicinity of the upper end opening of each through hole 10a becomes smooth.

  Furthermore, it is more preferable that the two cylindrical portions 12 and the plate-like portions 11 are streamlined (see FIG. 7). Thereby, almost no passage resistance of the culture solution can be generated on the upper side of the fluid mixing unit 10, and the generation of the vortex can be prevented or suppressed. In addition, the boundary part of the plate-shaped part 11 and the cylindrical part 12 may not be round, but may be angular.

  Moreover, when the fluid mixing part 10 is seen from the upper side, the ratio (occupancy ratio) of the plurality of through holes 10a to the fluid mixing part 10 is not particularly limited, but is preferably about 1 to 50%, More preferably, it is about 50%, and more preferably about 20-40%. By setting the occupation ratio within the above range, regardless of the constituent material of the fluid mixing unit 10, the mechanical strength of the fluid mixing unit 10 is sufficiently ensured, while the bubble generation efficiency and the uniform dispersibility in the culture medium are increased. Can be increased.

  The shape of each through-hole 10a (the shape seen from the upper side or the lower side) is not particularly limited. For example, a circular shape, an elliptical shape, a triangular shape, a quadrangular shape, a hexagonal shape such as a hexagonal shape, a star shape, etc. It can be an irregular shape or the like. In addition, the shape of each through-hole 10a may be the same, or may differ.

The average cross-sectional area of the through hole 10a (the average value of the cross-sectional area in the horizontal direction) is not particularly limited, is preferably from about ² 50～1,000Mm, and more preferably about ² 100~800mm . By setting the average cross-sectional area of the through-hole 10a within the above range, it is possible to prevent the culture solution from passing through the fluid mixing unit 10 from becoming unnecessarily high and to prevent the culture solution from foaming vigorously.

  Moreover, although the length of each through-hole 10a (thickness of the fluid mixing part 10) is based also on the constituent material of the fluid mixing part 10, it is preferable that it is about 1-100 mm, and it is about 5-75 mm. More preferred. By setting the length of each through-hole 10a within the above range, the bubble generation efficiency can be sufficiently increased.

  Examples of the constituent material of the fluid mixing unit 10 include metal materials such as stainless steel, aluminum alloy, and titanium alloy, ceramic materials such as alumina, and plastic materials such as polycarbonate, polyethylene, polypropylene, and vinyl chloride. These can be used alone or in combination of two or more. In addition, although the said metal material is preferable from a viewpoint which has corrosion resistance, when a culture solution (1st fluid) is a liquid which has reducibility (liquid with a small oxidation-reduction potential), another metal material is used. You can also.

  In addition, the fluid mixing unit 10 is, for example, one of a forging method, a casting method, a compacting method, an extrusion molding method, a compression molding method, an injection molding method, etc. alone or in combination of two or more methods. Can be manufactured.

  In the configuration shown in the figure, the plate-like portion 11 and the cylindrical portion 12 are integrally formed. However, these members are manufactured as separate bodies, for example, by welding, brazing, fusion, adhesion, or the like. You may make it join mutually.

  In addition, the manufacturing cost of the fluid mixing unit 10 can be reduced by configuring the fluid mixing unit 10 with a plastic molded product (not a machined product but a die-cut product). At this time, the fluid mixing unit 10 may be configured by a half (part) divided into two on the plane of symmetry, and each half may be manufactured by die cutting. Thereby, the fluid mixing part 10 can be manufactured by die cutting at a lower cost.

  Further, in this case, the two halves may be joined by bonding, but may be joined by fitting (inserting), and abutting (the two halves are simply in contact with each other). May be assembled. When assembling the two halves by butting, only one type of mold (die) for producing the halves needs to be prepared, so investment in the production facility for the fluid mixing unit 10 can be reduced.

  In particular, when the fluid mixing unit 10 having the configuration shown in FIGS. 4, 6, and 7 to be described later is manufactured, since the communication passage 121 for releasing the gas is provided, the two halves are bonded with high adhesion. Even if not joined, the fluid mixing part 10 can fully exhibit its function by joining by fitting or assembly by butting.

  In the gas fermenter 6 having the above-described configuration, the number of the fluid mixing units 10 is appropriately set according to the size of the container 61 and is not particularly limited. In the embodiment, the height is preferably about 1 to 5 pieces per 1 m, and more preferably about 1 to 3 pieces. Thereby, both the rectifying action of the culture solution and the uniform dispersibility of the bubbles in the culture solution are sufficiently exhibited.

The capacity of the container 61 is not particularly limited, but is preferably about 1 × 10 ⁻² to 1 × 10 ⁴ m ³ , and more preferably about 5 × 10 ^{−1 to} 5 × 10 ² m ^3. preferable. In particular, the height of the container 61 is preferably about 1 to 30 m, and more preferably about 5 to 20 m. The gas production | generation apparatus of this invention can be used especially preferably for the gas fermenter 6 provided with such a large sized container 61. FIG.

  In the present embodiment, gas is supplied to the fluid mixing unit 10 located on the lowermost side, but in addition to the fluid mixing unit 10 located on the lowermost side, the fluid mixing unit at an arbitrary position 10 may be configured to supply gas, or may be configured to supply gas to all the fluid mixing units 10. Moreover, what is necessary is just to provide multiple fluid mixing parts 10 as needed, and you may make it provide only one.

<< Other structural examples of fluid mixing section >>
Each fluid mixing unit 10 may be configured as shown in FIGS. 4 to 7 instead of the configuration shown in FIGS. 2 and 3. Hereinafter, another configuration example of the fluid mixing unit 10 will be described.

  The fluid mixing unit 10 illustrated in FIG. 4 is the same as the fluid mixing unit 10 illustrated in FIGS. 2 and 3 except that the fluid mixing unit 10 includes a communication path (pinhole) 121 communicating with the plurality of through holes 10a and the space 10b. Each communication path 121 is formed so as to penetrate each cylindrical portion 12 in the thickness direction (horizontal direction).

  Here, the flow rate (flow velocity) of the culture solution is faster near the inner surface than the central axis of the cylindrical portion 12 or the vicinity thereof. For this reason, the pressure in the cylindrical part 12 becomes lower near the inner surface than the central axis of the cylindrical part 12 or the vicinity thereof. Therefore, by providing the communication path 121 that penetrates the cylindrical portion 12 in the thickness direction, the gas stored in the space 12b can be efficiently discharged as bubbles through the through hole 10a via the communication path 121. .

  For this reason, the pressure of the gas supplied into the container 61 from the gas line 202 can be reduced. That is, the cost required for gas compression can be reduced. Therefore, the overall cost required for culturing gas-utilizing bacteria (producing organic substances) can also be kept low.

When the average cross-sectional area of the through hole 10a is A [mm ² ] and the average cross-sectional area of the communication passage 121 (average value of the cross-sectional area in the vertical direction) is B [mm ² ], B / A is 0.01 to It is preferably about 0.2, more preferably about 0.05 to 0.15. Thereby, the discharge efficiency of the gas to the through-hole 10a via the communicating path 121 can be improved, and the bubble generation efficiency can be further improved.

Specific values of the average cross-sectional area B of the communication passage 121 is not particularly limited, is preferably from about ² 0.1 to 50 mm, and more preferably ² about 1 to 30 mm. By setting the average cross-sectional area B of the communication passage 121 within the above range, the efficiency of gas discharge to the through hole 10a via the communication passage 121 can be further increased.

  The fluid mixing unit 10 shown in FIGS. 5 and 6 is the same as the fluid mixing unit 10 shown in FIG. 4 except that it further includes a plate-like part 13 having a plurality of holes 13a. The plate-like portion 13 is disposed so as to face the plate-like portion 11 so that each hole 13 a corresponds to each hole 11 a of the plate-like portion 11.

  In the configuration shown in the figure, the plate-like portion 11, the cylindrical portion 12 and the plate-like portion 13 are integrally formed. However, these members are manufactured as separate bodies, for example, welding, brazing, and melting. You may make it mutually join by adhesion | attachment, adhesion | attachment, etc.

  Therefore, in this embodiment, each through-hole 10a is comprised by the hole 11a of the plate-shaped part 11, the internal space 12a of the cylindrical part 12, and the hole 13a of the plate-shaped part 13. FIG. In addition, the space 10 b is closed below the fluid mixing unit 10.

  With this configuration, no pressure is applied to the gas in the space 12b from below the fluid mixing unit 10 by the culture solution. For this reason, the pressure required to supply the gas into the container 61 (space 10b) can be greatly reduced.

  In the present embodiment, the boundary portion between the plate-like portion 13 and the tubular portion 12 is also rounded. That is, each through-hole 10a has a portion (cross-sectional area gradually decreasing portion) where the cross-sectional area gradually decreases from the lower side toward the upper side at the lower end thereof. Thereby, the flow of the culture solution into each through hole 10a becomes smooth. In addition, the boundary part of the plate-shaped part 13 and the cylindrical part 12 may not be round, but may be angular.

  Further, when the fluid mixing unit 10 is viewed from the lower side, the ratio (occupation ratio) of the plurality of through holes 10a to the fluid mixing unit 10 is not particularly limited, but is preferably about 10 to 50%, More preferably, it is about ˜40%. By setting the occupation ratio within the above range, regardless of the constituent material of the fluid mixing unit 10, the culture solution is directed from the lower side to the upper side while sufficiently securing the mechanical strength of the fluid mixing unit 10. Can pass smoothly.

  The occupation ratio of the through holes 10a when the fluid mixing section 10 is viewed from the lower side may be the same as or different from the occupation ratio of the through holes 10a when the fluid mixing section 10 is viewed from the upper side. Good. For example, by making the occupation ratio of the through hole 10a when the fluid mixing section 10 is viewed from the lower side larger than the occupation ratio of the through hole 10a when the fluid mixing section 10 is viewed from the upper side, the fluid mixing section 10 is The speed of the culture solution passing through can be increased.

The fluid mixing unit 10 shown in FIG. 7 is the same as the fluid mixing unit 10 shown in FIGS. 5 and 6 except that the radius of curvature of the boundary between the cylindrical part 12 and the plate-like parts 11 and 13 is different.
Specifically, as shown in FIG. 7, the vertical cross-sectional shape (the cross-sectional shape in the vertical direction) of the portion that defines the space 10b of the fluid mixing unit 10 is streamlined on the upper side and the lower side, respectively. .

  In such a configuration, when no gas is supplied into the culture solution via the communication path 121, the flow resistance when the culture solution passes through the through hole 10a becomes extremely low due to the above streamline effect, and the rectification action of the culture solution. I can not expect. However, in this embodiment, since the gas is supplied to the culture solution via the communication path 121, the culture solution works on the gas, thereby increasing the passage resistance of the through-hole 10a of the culture solution and rectifying action. Occurs.

  In particular, in this embodiment, under the influence of the streamline, the vortex of the culture solution does not occur or is very unlikely to occur between the upper openings of the adjacent through holes 10a. For this reason, coalescence of the generated bubbles can be prevented. In addition, the vortex of the culture solution is hardly generated between the openings on the lower side of the adjacent through holes 10a. For this reason, it is possible to prevent a disturbance in the flow of the culture solution.

  In this case, the separation distance between the upper openings of the adjacent through-holes 10a is preferably 1 mm or less (including 0 mm), and more preferably 0.8 mm or less. Thereby, coalescence of gas bubbles can be reliably prevented.

  Similarly, the separation distance between the lower openings of adjacent through holes 10a is preferably 1 mm or less (including 0 mm), and more preferably 0.8 mm or less. Thereby, it can prevent suitably that disorder arises in the flow of a culture solution.

  In the present embodiment, the vertical cross-sectional shape of the portion defining the space 10b of the fluid mixing unit 10 is streamlined on the upper side (downstream side) and the lower side (upstream side), but only one of them is It may be streamlined. When only one of the upper side and the lower side is streamlined, it is particularly effective to make the upper side streamlined for the reasons described above.

  In addition, the gas fermenter 6 is replaced with the fermenter of the type which stirs a culture solution by circulating the culture solution itself, For example, the fermenter of the type which stirs a culture solution with a stirring plate, Aeration of supplied gas It is good also as a fermenter etc. of the type which stirs a culture solution with the water flow accompanying a bubble flow produced in 1).

<Gas treatment equipment and waste treatment system>
Next, a gas processing apparatus and a waste processing system having the gas fermenter 6 as described above will be described.
FIG. 8 is a block diagram showing an embodiment of the waste treatment system of the present invention, and FIG. 9 is a schematic diagram of the configuration of the drying section, gasification furnace, heat exchanger, and distiller included in the waste treatment system of FIG. FIG.

  A waste treatment system 1 shown in FIG. 8 includes a waste treatment apparatus and a gas treatment apparatus connected to the waste treatment apparatus. In the present embodiment, the waste disposal apparatus includes a drying unit 2 and a gasification furnace 3. The gas processing apparatus includes a heat exchanger 4, a gas purification unit 5, a gas fermenter 6 shown in FIG. 1, a distiller 7, an offgas combustion furnace 8, and a waste liquid fermenter 9.

  The drying unit 2 is an apparatus for drying waste containing water (hereinafter also referred to as “hydrated waste”), and is provided in the drying chamber 21 and the drying chamber 21 as shown in FIG. A conveyor (conveying mechanism) 22 that conveys waste toward the gasification furnace 3 is provided.

  Here, examples of the waste include plastic waste, garbage, municipal waste (MSW), waste tires, biomass waste, and the like. One of these is used alone or two or more are combined. Can be used.

  The gasification furnace (gas generation unit) 3 is a furnace that processes waste (hereinafter also referred to as “dry waste”) after being dried in the drying unit 2. In this gasification furnace 3, dry waste (carbon source) is partially oxidized (incomplete combustion) to generate a gas (synthetic gas) containing carbon monoxide as a main component.

  The generated gas may contain other gas components such as hydrogen, water vapor, carbon dioxide, nitrogen, and oxygen in addition to carbon monoxide. A gas having such a composition is easily generated by partially oxidizing the waste as described above.

  The partial oxidation of the dry waste in the gasification furnace 3 may be performed while supplying air, but is preferably performed while supplying a gas having a higher oxygen concentration than that of air (high oxygen concentration gas). . By using the high oxygen concentration gas, the temperature of the gas generated by the partial oxidation of the dry waste can be further increased, and higher-temperature superheated steam can be generated by the heat exchanger 4.

  In this case, the high oxygen concentration gas may be supplied from a gas line connected to a branch gas line 204a, which will be described later, or supplied from another gas line directly connected to the gasification furnace 3 different from the branch gas line 204a. You may make it do.

  The heat exchanger (superheated steam generation unit) 4 is an apparatus that generates superheated steam using heat generated when the waste is partially oxidized in the gasification furnace 3. The heat exchanger 4 shown in FIG. 9 includes a coiled pipe 41 disposed in the gasification furnace 3, and the steam passing through the pipe 41 is heated by the heat in the gasification furnace 3 to generate superheated steam. Become.

According to this heat exchanger 4, superheated steam can be generated easily and efficiently with a simple configuration. The superheated steam is preferably superheated steam (H ₂ O gas) containing water vapor as a main component, but may contain other gas components.

  Further, the heat exchanger 4 may be a type of heat exchanger provided independently from the gasification furnace 3. As this type of heat exchanger, for example, jacket type heat exchanger, immersion coil type heat exchanger, double tube type heat exchanger, thrombon type heat exchanger, shell and tube type heat exchanger, plate type heat exchanger Examples include exchangers, bayonet heat exchangers, and the like.

  The steam discharge port (the lower end portion (one end portion) of the pipe 41) of the heat exchanger 4 is connected to the steam supply port of the drying chamber 21 via the steam line 101. The superheated steam generated in the heat exchanger 4 is supplied into the drying chamber 21 by a pump (not shown) and directly contacts the hydrated waste conveyed by the conveyor 22. Thereby, the water (water | moisture content) contained in a hydrous waste evaporates, and a hydrous waste dries.

  Here, since the superheated steam has high heat conductivity, it is possible to efficiently dry the hydrated waste as compared with the case where hot air (heated air) is used. In addition, if superheated steam is used, generation of hydrogen chloride or the like can be suppressed during the drying of hydrous waste, so that adverse effects such as surface corrosion on each part of the waste treatment system 1 through which superheated steam passes can be reduced. it can.

  Moreover, the temperature of the superheated steam used for drying the hydrous waste is not particularly limited, but is preferably about 120 to 800 ° C, and more preferably about 200 to 400 ° C. By using the superheated steam in the above temperature range, the drying efficiency of the hydrated waste can be further increased, and the generation amount of hydrogen chloride or the like that adversely affects each part of the waste treatment system 1 can be further reduced.

  The temperature of the superheated steam can be appropriately set within the above temperature range depending on the water content of the water-containing waste. That is, when the water content of the hydrous waste is high, the temperature of the superheated steam can be set to a relatively high temperature, and when the water content of the hydrous waste is low, the temperature of the superheated steam can be set to a relatively low temperature.

  At this time, the temperature of the superheated steam used for drying the hydrated waste is reduced to a low temperature steam having a lower temperature. Moreover, low temperature steam comes to contain the water (water vapor | steam) removed from the water-containing waste, and becomes near a saturated state compared with superheated steam. It should be noted that the water content of the hydrous waste is extremely large, and the low temperature steam is almost saturated when it is transported to the gasification furnace 3 without completely drying the hydrous waste. Moreover, the temperature of the low temperature steam at this time is about 100-200 degreeC normally.

  A steam discharge port of the drying chamber 21 is connected to a steam supply port of the distiller 7 via a steam line 102. The steam line 103 branched from the middle of the steam line 102 is connected to the steam supply port of the heat exchanger 4 (the upper end portion (the other end portion) of the pipe 41). Thereby, a part of low temperature steam is supplied to the distiller 7, and the heat is utilized for distillation. On the other hand, the remainder of the low-temperature steam is supplied to the heat exchanger 4 (pipe 41) and reused to generate superheated steam.

  Note that a valve (not shown) is provided at or near the branch portion between the steam line 102 and the steam line 103 so that the supply amount of the low-temperature steam to the distiller 7 and the heat exchanger 4 can be adjusted. ing.

  The gas exhaust port of the gasification furnace 3 described above is connected to the gas supply port of the gas purification unit 5 through the gas line 201, and the gas exhaust port of the gas purification unit 5 is further connected through the gas line 202. It is connected to the gas supply port of the gas fermenter 6. The gas generated in the gasification furnace 3 is supplied to a gas fermenter 6 as shown in FIG. 1 after passing through a gas purification unit 5 by a pump (not shown).

In the gas fermenter (organic substance generation unit) 6, as described above, the gas assimilating bacteria are cultured in the culture solution, and an organic substance is generated from the gas by the fermentation action.
The culture solution is a liquid containing main component water and nutrients (for example, vitamins, phosphoric acid, etc.) dissolved or dispersed in the water. The composition of such a culture solution is prepared so that gas-assimilating bacteria can grow well.

  Examples of the organic substance include ethanol, 2,3-butanediol, acetic acid, lactic acid, isoprene and the like, and an organic substance containing ethanol is preferable. Ethanol with high concentration (99.5 vol% or more) can be used as fuel ethanol, and can be used as an additive for raw materials such as cosmetics, beverages, chemical substances, fuel (jet fuel), foods, etc. The versatility is extremely high.

Examples of the gas-assimilating bacteria include Clostridium bacteria, Moorella bacteria, Acetobacterium bacteria, Carboxydocella bacteria, Rhodopseudomonas bacteria, Eubacterium, Butyribacterium, Oligotropha, Bradyrhizobium, aerobic hydrogen-oxidizing bacteria such as Ralsotonia Can be mentioned.
Among the gas-assimilating bacteria as described above, a bacterium having a high ability to produce a target organic substance is selected and used.

  For example, gas-assimilating bacteria with high ethanol-producing ability include Clostridium autoethanogenum, Clostridium ljungdahlii, Clostridium aceticum, Clostridium carboxidivorans , Moorella thermoacetica, Acetobacterium woodii and the like.

  The temperature of the culture solution (culture temperature) is preferably about 30 to 45 ° C, more preferably about 33 to 42 ° C. More preferably, it is about 36.5-37.5 degreeC. The culture time can be preferably about 24 hours to 300 days in continuous culture, more preferably about 5 days to 300 days in continuous culture.

  Moreover, although the normal pressure may be sufficient as the pressure in the gas fermenter 6, Preferably it is about 10-300 kPa (gauge pressure), More preferably, it can be about 20-200 kPa (gauge pressure). By setting the pressure in the gas fermenter 6 within the above range, it is possible to further increase the reactivity of the gas-assimilating bacteria while suppressing an increase in equipment cost due to excessive pressure load.

In the present embodiment, the gas purification unit 5 is provided in the previous stage (upstream side) of the gas fermenter 6. The gas purification unit 5 performs a process for increasing the amount of components necessary for the growth of gas-utilizing bacteria contained in the gas, a process for removing components that adversely affect the gas-utilizing bacteria, a humidification process, a drying process, and the like. It is a device to perform.
By using the gas that has passed through the gas refining unit 5 in the gas fermenter 6, it is possible to further improve the production efficiency of the organic substance by the gas assimilating bacteria.

  In addition, the gas purification part 5 should just be provided as needed, and may be abbreviate | omitted. That is, the gas discharge port of the gasification furnace 3 may be directly connected to the gas supply port of the gas fermenter 6 via the gas line 201.

  The number of gas fermenters 6 installed is not limited to one, but may be two or more (multistage (series) or parallel). By connecting two or more gas fermenters 6 in multiple stages (in series), the gas remaining in the upstream (upstream side) gas fermenter 6 is further converted into organic substances in the downstream (downstream side) gas fermenter 6. Can be used for generation. In this case, the organic material generated in the preceding gas fermenter 6 and the organic material generated in the subsequent gas fermenter 6 may be the same or different.

  When two or more gas fermenters 6 are connected in series, I: a design in which the culture fluid flow is in series and the gas flow is parallel, and II: the culture fluid flow in parallel and the gas flow in parallel. And III: a design in which both the culture fluid flow and the gas flow are in series. In the case of design III, the culture fluid flow and the gas flow may be in opposite directions (opposite flow), or the culture fluid flow and the gas flow may be in the same direction (parallel flow).

  A gas discharge port of the gas fermenter 6 is connected to a gas supply port of the off-gas combustion furnace 8 through a gas line 203. The exhaust gas (mainly nitrogen) remaining in the gas fermenter 6 is supplied to the off-gas combustion furnace 8 by a pump or pressure gradient (not shown).

  The off-gas combustion furnace 8 is a device that burns exhaust gas. The exhaust gas after being burned in the off-gas combustion furnace 8 is discharged (released) into the atmosphere after passing through a predetermined filter, for example. The off-gas combustion furnace 8 may be provided as necessary and may be omitted. Further, superheated steam may be generated by the waste heat of the off-gas combustion furnace 8.

  The liquid discharge port of the gas fermenter 6 is connected to the liquid supply port of the distiller (concentration unit) 7 via the liquid line 301. In the gas fermenter 6, an organic substance is generated from the gas in the culture solution, and the culture solution containing the organic substance is supplied to the distiller 7 by a pump (not shown).

  In addition, you may make it provide the solid-liquid separation part which removes gas utilization bacteria from a culture solution in the middle of the liquid line 301, for example. Such a solid-liquid separation unit includes, for example, a filter such as a ceramic membrane filter, a multi-plate wave filter, a screw press machine, a roller press machine, a belt screen machine, a vibration sieve machine, a vacuum dehydrator, a pressure dehydrator (filter press machine). ), Belt press machine, screw press machine, centrifugal concentration dehydrator (screw decanter machine), multiple disk dehydrator, and the like.

  The distiller 7 is an apparatus that distills and concentrates an organic substance by utilizing the difference between the boiling point of the organic substance and the boiling points of other components. As shown in FIG. 9, the distiller 7 of the present embodiment is provided outside the container 71, a plurality of trays (perforated plates) 72 and a coiled pipe 73 provided in the container 71, and the container 71. And a capacitor 74.

  A reflux liquid 710 is accommodated at the bottom of the container 71, and a pipe 73 is disposed so as to be immersed in the reflux liquid 710. Further, a steam line 102 is connected to the lower end (one end) of the pipe 73, and low-temperature steam is supplied to the pipe 73. At this time, the reflux liquid 710 is heated using the heat of low-temperature steam passing through the pipe 73. Thereby, the reflux liquid 710 evaporates and becomes a vapor | steam.

A steam line 104 is connected to the upper end (other end) of the pipe 73. The low temperature steam that has passed through the pipe 73 and the steam line 104 is discharged (released) into the atmosphere after passing through a predetermined filter, for example.
Note that a liquid having a boiling point higher than that of the organic substance (eg, water) can be used for the reflux liquid 710.

  The plurality of trays 72 are arranged at substantially equal intervals along the vertical direction (height direction) of the container 71. Further, a liquid line 301 is connected to a liquid supply port provided in the middle of the container 71 in the vertical direction, and a culture solution is supplied from the gas fermenter 6 into the container 71. When the culture solution supplied into the container 71 flows down along the tray 72, it comes into contact with the vapor of the reflux solution 710, and the components including the organic substance in the culture solution also evaporate.

  A steam outlet provided at the top of the container 71 is connected to the condenser 74 via a recovery line 741. The condenser 74 is a device that recovers and cools the vapor (particularly, vapor of the organic substance) in the container 71. The condenser 74 collects and cools the vapor of the organic substance, and a concentrated liquid of the organic substance is obtained.

  Although the temperature in the still 7 (container 71) at the time of distillation of this organic substance is not specifically limited, It is preferable that it is 100 degrees C or less, and it is more preferable that it is about 70-95 degreeC. By setting the temperature in the distiller 7 within the above range, it is possible to more reliably separate the necessary organic material from other components, that is, distillation of the organic material.

  Further, the pressure in the distiller 7 (container 71) during distillation of the organic substance may be normal pressure, but is preferably less than atmospheric pressure, and is about 60 to 95 kPa (gauge pressure). More preferred. By setting the pressure in the distiller 7 within the above range, it is possible to improve the separation efficiency of the organic substance, and thus improve the yield of the concentrated liquid of the organic substance.

  The liquid discharge port of the condenser 74 is connected to a liquid supply port provided in the upper part of the container 71 through a reflux line 742. Further, a liquid line 302 branched from the reflux line 742 is connected to the reflux line 742.

  With this configuration, a part of the concentrate is returned into the container 71 by a pump (not shown), and the remaining part of the concentrate is recovered as a final product. By returning a part of the concentrated liquid into the container 71 and using the concentrated liquid as a part of the reflux liquid 710 for distillation, the concentration of the organic substance in the concentrated liquid can be further increased.

  A valve (not shown) is provided at or near the branch portion between the reflux line 742 and the liquid line 302 so that the amount of the concentrated liquid returned to the container 71 and the amount of the concentrated liquid recovered can be adjusted. It has become.

  A gas line 204 is connected to the gas discharge port of the capacitor 74. The gas line 204 is branched into two branch gas lines 204a and 204b on the way, one branch gas line 204a is connected to the gas supply port of the gasification furnace 3, and the other branch gas line 204b is connected to the gas line 203. Connected in the middle of

  Here, when the organic substance is distilled, a gas containing oxygen or air dissolved in the culture solution is generated. By supplying such gas as exhaust gas to the gasification furnace 3 and the off-gas combustion furnace 8, the exhaust gas generated by the distiller 7 is effectively used for partial oxidation of waste and combustion of the exhaust gas generated by the gas fermenter 6. can do.

  In the present embodiment, the concentrating unit (processing unit for processing the organic substance) is configured by the distiller 7, but is provided with another processing unit instead of or together with the distiller 7. May be. In the case where the concentrating unit includes another processor together with the distiller 7, the other processor is provided, for example, downstream of the distiller 7 (downstream side, that is, in the middle of the liquid line 302). By using a concentration unit including another processor together with the distiller 7, the concentration of organic matter in the concentrate can be further increased.

  Examples of such a treatment device include a treatment device including a zeolite dehydration membrane, a treatment device that removes a low-boiling substance having a lower boiling point than an organic material, a treatment device that removes a high-boiling material having a higher boiling point than an organic material, and an ion exchange membrane. The processor etc. which contain are mentioned, One of these can be used individually or in combination of 2 or more.

  Further, the liquid discharge port provided in the lower part of the container 71 is connected to the waste liquid fermenter 9 through the liquid line 303. A part of the reflux liquid 710 in the container 71 is supplied to the waste liquid fermenter 9 as a waste liquid by a pump (not shown).

  The waste liquid fermenter (waste liquid processing part) 9 is an apparatus for processing the waste liquid by the fermentation action of methane fermentation bacteria. Specifically, first, the culture solution and the methane fermentation bacteria are supplied and accommodated in the waste liquid fermenter 8 via a line (not shown). In this state, the waste liquid is supplied into the waste liquid fermenter 9 while stirring the culture liquid. As a result, the methane-fermenting bacteria are cultured in the culture solution, and from the substance (for example, carbohydrate, protein, etc.) generated by the gas-utilizing bacteria dead or gas-utilizing bacteria contained in the waste liquid by the fermentation action. The gas containing methane as a main component is generated.

As the waste liquid fermenter 9, a fermenter similar to the gas fermenter 6 can be used.
Note that the gas containing methane as a main component produced in the waste liquid fermenter 9 can be used as a fuel gas for partially oxidizing dry waste in the gasification furnace 3 by performing a predetermined treatment.

  In the present embodiment, the waste liquid processing unit is configured by the waste liquid fermenter 9, but may be provided with another processing device instead of the waste liquid fermenter 9. Examples of other processing devices include a filter, a diffuser that diffuses moisture into the atmosphere by an evaporation method, and a concentrator that concentrates waste liquid by an evaporation method. In addition, the waste liquid fermenter (waste liquid processing unit) 9 may be provided as necessary and may be omitted.

  According to the waste treatment system 1 as described above, the superheated steam is generated using the heat generated when the dry waste is partially oxidized in the gasification furnace 3, and the superheated steam generates the superheated steam in the drying unit 2. The water-containing waste is dried, and the heat of the low-temperature steam after being used for drying the water-containing waste is also used for concentration (distillation) of the organic substance in the distiller 7.

  That is, when the heat generated in the gasification furnace 3 is used for both the drying of the hydrous waste and the concentration of the organic substance, when different heat sources are used for the drying of the hydrous waste and the concentration of the organic substance. In comparison, the amount of energy required can be reduced.

  Further, when hot air (non-condensable gas) is used for drying the hydrous waste, the water vapor generated from the hydrous waste is mixed with the non-condensable gas, so that it is difficult to condense even if the temperature is lowered. For this reason, it is extremely difficult to use as a heat source for the still 7. On the other hand, when superheated steam is used to dry the hydrous waste, the low-temperature steam after being used to dry the hydrous waste is almost saturated, and the heat of condensation is effectively used as a heat source for the distiller 7. Can do.

  In other words, when generating superheated steam, the latent heat input to obtain the steam can be recovered without waste, so the amount of energy required is lower than when hydrated waste is dried using hot air. Become.

  In addition, the water-containing waste is usually dried without reducing the pressure in the drying chamber 21. For this reason, the water-containing waste can be continuously dried in the drying unit 2. Therefore, the waste treatment system 1 can be particularly preferably used for the treatment of waste generated in large quantities.

In addition, you may make it utilize the heat | fever of low temperature steam with the gas fermenter 6 besides using with the distiller 7. FIG.
In this case, for example, the pipe 63 is spirally wound around the body 611 of the container 61 or the pipe 63 is provided in the container 61 so as to be immersed in the culture solution, and the vapor line 102 or the vapor line 104 is provided at one end thereof. Connected.

  When the steam line 102 is connected, the pipe 63 is supplied with the low-temperature steam after passing through the drying unit 2, and the heat is used for culturing gas-assimilating bacteria. When the steam line 104 is connected, the pipe 63 is supplied with low-temperature steam after passing through the drying unit 2 and further passing through the distiller 7, and the residual heat is used for culturing gas-assimilating bacteria. Used.

  Furthermore, the heat of the low temperature steam may be used in the waste liquid fermenter 9. In this case, the waste liquid fermenter 9 can have the same configuration as the gas fermenter 6. Further, the heat of the low temperature steam may be used in two or three of the distiller 7, the gas fermenter 6 and the waste liquid fermenter 9.

  As mentioned above, although the fluid mixing apparatus, gas processing apparatus, and waste disposal system of this invention were demonstrated, this invention is not limited to these. For example, the fluid mixing device, the gas treatment device, and the waste treatment system of the present invention may have other arbitrary configurations, or may be replaced with an arbitrary configuration that exhibits the same function.

  In the fluid mixing apparatus of the present invention, two or more of the fluid mixing sections as described above can be used in combination. For example, the lowermost fluid mixing unit can be configured as shown in FIG. 7, and the other fluid mixing unit can be configured as shown in FIG. 3, FIG. 5, or FIG.

  In the fluid mixing device of the present invention, the flow direction of the liquid may be a horizontal direction or a direction inclined with respect to the vertical direction (vertical direction).

  Furthermore, the fluid mixing device of the present invention can be used not only for a gas fermenter but also for a reactor that synthesizes an organic substance from gas by the action of a catalyst. In this case, for example, a medium oil containing a metal catalyst is preferably used as the liquid.

  In addition, it cannot be overemphasized that the fluid mixing apparatus of this invention may be used only for the production | generation (manufacture) of a bubble. For example, bubbles generated using a physiological saline (liquid) containing carbohydrates, phospholipids, and the like can be used as a contrast agent during ultrasonic contrast by being injected into a living body.

  Moreover, in the fluid mixing apparatus of the present invention, the apparatus main body can be formed of a tubular body that allows the first fluid to pass therethrough instead of the container that stores the first fluid. In this case, the same operation and effect as in the above embodiment can be obtained.

  Furthermore, in the embodiment, the first fluid is a liquid and the second fluid is a gas (gas). However, the present invention is not limited to this, and the first fluid is a liquid. A combination in which the fluid is also a liquid, a combination in which the first fluid is a gas, a combination in which the second fluid is a liquid, a combination in which the first fluid is a gas, and a second fluid is also a gas.

  In particular, when the same kind of fluid is used as the first fluid and the second fluid, the fluid mixing portion has a remarkable function as a current plate that can change the passage resistance.

  Next, specific examples of the present invention will be described. Note that the present invention is not limited to the following specific examples.

(Example)
By changing the flow rate of the liquid (first fluid) and the flow rate of the gas (second fluid), a change in the substantial passage resistance of the liquid passing through the fluid mixing unit was simulated.
FIG. 10 is a diagram schematically showing a cross section of the fluid mixing section shown in FIG. In FIG. 10, the liquid is flowing upward from below.

Port 0 indicates the vicinity of the lower opening of the through hole 10a, and port 2 indicates the vicinity of the upper opening of the through hole 10a. Port 1 indicates a portion where the through hole 10a has a reduced diameter, and port 2 indicates a communication path 121 that connects the through hole 10a and the space 10b. Normally, S ₀ = S ₂ , but S ₀ > S ₂ may be satisfied, or S ₀ <S ₂ may be satisfied.

Here, the flow rate of the fluid in each port is represented by F _n = S _n × V _n (n = 0, 1, 2, 3). Moreover, the pressure of each port is represented by P _n (n = 0, 1, 2, 3). The change in the passage resistance was calculated by obtaining the pressures of port 0, port 1 and port 2 under the conditions of S ₀ = 10 cm ² , S ₁ = 0.5 cm ² and V ₀ = 0.1 m / s.

Tables 1 and 2 are graphs showing the pressure of the port 0 and the port 1 based on the pressure P _{2 of the} port 2, and the horizontal axis represents the flow rate F _{0 of the} liquid flowing through the port ₀ and the supply from the port 3. The ratio (F ₃ / F ₀ ) with the flow rate F _{3 of} the gas to be performed is shown. Table 1 shows a case where the ratio F ₃ / F ₀ is small, and Table 2 shows a case where the ratio F ₃ / F ₀ is large. The volume change due to the pressure change was ignored.

As is apparent from Tables 1 and 2, in the range of F ₃ / F ₀ <0.01, it can be seen that P ₁ -P ₂ is a negative value, and gas is drawn from port 3 to port 1. Even in the range of F ₃ / F ₀ ≧ 0.01, P ₁ −P ₂ <P ₀ −P ₂ (that is, P ₁ <P ₀ ), and the gas is supplied to the port 3 at a pressure lower than P _0. It can be seen that injection into port 1 is possible. Therefore, the compression energy of the supplied gas can be reduced by using the fluid mixing section shown in FIG.

  According to such a fluid mixing unit, by providing a plurality of through holes and giving passage resistance to the liquid, it is possible to reduce unevenness in the flow of the liquid in a direction perpendicular to the direction (horizontal direction). A uniform flow of liquid can be formed. At this time, due to an increase in the passage resistance of the liquid, it is necessary to impart additional energy to the liquid in order to pass through the liquid mixing unit. As shown in Tables 1 and 2, the additional energy is Since it is used as gas injection energy, energy loss can be suppressed.

  Similar results are also obtained in the fluid mixing section shown in FIGS. In addition, in the fluid mixing part shown in FIG. 4, although the suppression effect of energy loss becomes a little low, sufficient rectification effect is acquired.

(Comparative example)
As shown in FIG. 11, the bubble distribution state was simulated in a configuration in which two current plates are arranged and a ring sparger is arranged near the upper side of the current plate located below.
Each rectifying plate was a perforated plate in which holes with a diameter of 5 mm were arranged in a triangle with a pitch of 10 mm, and the ring sparger was a ring-shaped tube with holes with a diameter of 0.5 mm formed at a pitch of 5 mm.
In the comparative example, as shown in FIG. 11, a uniform flow of liquid is not formed, and bubbles are not uniformly dispersed in the liquid (bubbles are unevenly distributed in the liquid). Moreover, the effect of suppressing energy loss cannot be obtained.

DESCRIPTION OF SYMBOLS 1 Waste disposal system 2 Drying part 21 Drying room 22 Conveyor 3 Gasifier 4 Heat exchanger 41 Piping 5 Gas refinement part 6 Gas fermenter 61 Container 611 Body part 611a Supply path 612 Bottom part 613 Top part 62 Circulation line 63 Pump 7 Distillation Vessel 71 container 710 reflux liquid 72 tray 73 piping 74 condenser 741 recovery line 742 reflux line 8 off-gas combustion furnace 9 waste liquid fermenter 10 fluid mixing part 10a through hole 10b space 11 plate-like part 11a hole 12 cylindrical part 12a internal space 13 plate 13a Hole 101 Steam line 102 Steam line 103 Steam line 104 Steam line 201 Gas line 202 Gas line 203 Gas line 204 Gas line 204a Branch gas line 204b Branch gas line 301 Liquid line 302 Liquid line 302 Liquid line

Claims (22)

An apparatus body for passing or storing the first fluid;
A flow generating mechanism for generating a flow of the first fluid in the apparatus body;
A second fluid supply mechanism for supplying a second fluid into the apparatus body;
One or more fluids provided in the apparatus body so as to cross the flow of the first fluid and mixing the first fluid and the second fluid when the second fluid passes through A mixing section,
The fluid mixing unit is closed at a plurality of through holes penetrating in the flow direction of the first fluid and downstream in the flow direction of the first fluid, and can temporarily store the second fluid. A fluid mixing device comprising a storage space.   The fluid mixing apparatus according to claim 1, wherein the first fluid is a liquid and the second fluid is a gas.   The fluid mixing apparatus according to claim 1, wherein the first fluid is a liquid and the second fluid is also a liquid.   The fluid mixing apparatus according to claim 1, wherein the first fluid is a gas and the second fluid is a liquid.   The fluid mixing apparatus according to claim 1, wherein the first fluid is a gas and the second fluid is also a gas.   The fluid mixing device according to any one of claims 1 to 5, wherein the fluid mixing unit includes a plurality of communication passages that connect the plurality of through holes and the storage space. The B / A is 0.01 to 0.2, where A [mm ² ] is the average cross-sectional area of the through holes and B [mm ² ] is the average cross-sectional area of the communication path. Fluid mixing device.   8. The fluid mixing device according to claim 1, wherein each through hole includes a portion whose cross-sectional area gradually decreases from a downstream side to an upstream side in the flow direction of the first fluid.   The fluid mixing device according to claim 8, wherein a separation distance between openings on the downstream side in the flow direction of the first fluid of the adjacent through holes is 1 mm or less.   The fluid mixing device according to any one of claims 1 to 8, wherein the storage space is opened upstream of the fluid mixing unit in the flow direction of the first fluid.   The fluid mixing device according to claim 1, wherein the storage space is closed on an upstream side of the fluid mixing unit in the liquid flow direction.   The fluid mixing device according to claim 11, wherein each of the through holes includes a portion whose cross-sectional area gradually decreases from the upstream side to the downstream side in the flow direction of the first fluid.   The fluid mixing device according to claim 12, wherein a distance between openings on the upstream side in the flow direction of the first fluid in the adjacent through holes is 1 mm or less.   The fluid mixing device according to claim 1, wherein the second fluid supply mechanism is configured to directly supply the second fluid to the storage space of the fluid mixing unit.   The ratio of the plurality of through holes to the fluid mixing part is 1 to 50% when the fluid mixing part is viewed from the downstream side in the flow direction of the first fluid. The fluid mixing device as described.   The ratio of the plurality of through holes to the fluid mixing part is 10 to 50% when the fluid mixing part is viewed from the upstream side in the flow direction of the first fluid. The fluid mixing device as described.   The fluid mixing device according to any one of claims 1 to 16, wherein the one or more fluid mixing units include a plurality of the fluid mixing units provided along a flow direction of the first fluid.   The fluid mixing device according to any one of claims 1 to 17, wherein the device main body is configured by a tubular body that allows the first fluid to pass therethrough.   The fluid mixing device according to any one of claims 1 to 17, wherein the device main body includes a container that stores the first fluid. The container includes a cylindrical body, a bottom that closes a lower end opening of the body, and a top that closes an upper end opening of the body.
The flow generation mechanism includes a line that connects the upper portion of the body portion and the bottom portion, and a pump that is provided in the middle of the line and that circulates the liquid. The fluid mixing device of claim 19, wherein the fluid mixing device is configured to generate a flow of the liquid from the top to the top. A fluid mixing device according to claim 19 or 20,
A gas processing apparatus comprising: a processing unit configured to process an organic substance generated from the gas supplied as the second fluid in the container of the fluid mixing apparatus. A gas treatment device according to claim 21,
A waste treatment system comprising: a gas generation unit that is connected to the container and generates the gas by processing the waste.