JP2000249464A - Gas-liquid contact device, air liquefaction separation device, and gas separation method - Google Patents

Abstract

(57) [Problem] To provide a gas-liquid contact device capable of increasing a load amount. SOLUTION: In a gas-liquid contacting device 4a for causing a liquid to flow down along the surface of a filling material and to make the liquid come into contact with the gas while raising the gas, thin plates or tubes of various shapes which determine the flow direction of the liquid and the gas. And non-promoting type ordered packings A ₁ and A _2, which are stacked or arranged in the vertical direction, and coarsely distributing portions C ₁ and C for roughly distributing liquid.
₂ and precision dispensing units B ₁ , B ₂ for precise and even distribution of liquid
And at least one liquid distributor E ₁ , E ₂ .

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a gas-liquid contacting device for performing low-temperature distillation separation of a gas mixture by performing gas-liquid contacting, and more particularly to an air liquefaction separating device for liquefying and separating nitrogen, oxygen, argon and the like in air. TECHNICAL FIELD The present invention relates to a gas-liquid contact device used for air conditioning, an air liquefaction separation device using the same, and a gas separation method using the gas-liquid contact device.

[0002]

2. Description of the Related Art As a distillation column used in an air liquefaction separation apparatus or the like, there are a packed column, a tray column and the like. Of these, the packed tower can reduce the pressure loss as compared with the plate tower, and therefore can reduce the power cost. In addition, since the pressure loss is small, the operating pressure can be set low to increase the relative volatility between each component, and the tower length can be increased. This has the advantage that high-purity products, especially high-purity argon, can be produced. Have. Packed towers usually have a packing inside,
A tower provided with a gas-liquid contact part consisting of a liquid distributor and the like,
This type of structure is generically referred to herein as a gas-liquid contact device.

[0003] As the packing used in the above-mentioned gas-liquid contact device, a self-promoting-dispersion type structured packing is often used. As the self-promoting-dispersion type structured packing, for example, a metal plate made of aluminum or the like is appropriately bent, laminated and arranged with at least a part inclined with respect to the vertical direction, and the liquid obliquely fills the packing surface. One that is designed to be distributed while flowing (at an angle to the vertical). In some cases, the distribution of the liquid is promoted by providing irregularities or holes on the surface of the metal plate of the filler. As a specific example of the self-promoting-dispersion type structured packing, a self-promoting-promoting structured packing 7 shown in FIGS.
1, 81. Figure 6 shows the Japanese Patent Publication No. 57-3
No. 6009, and FIG. 7 is disclosed in Japanese Patent Application Laid-Open No. 54-16761. In addition, as a self-promoting distribution-type structured packing, Japanese Patent Publication No. 7-1
No. 13514 can be mentioned.

[0004] As a packing which is included in the category of the self-promoting-dispersion type structured packing, there is a packing disclosed in JP-A-50-11001, which is shown in FIGS. The packing shown here is composed of a plurality of thin plate lattices a, b, c, ..., each lattice a, b, c, ... is bent in a substantially zigzag manner and lattice planes A, B, C, ... ... Sheet strip 13'-1 inclined to
7 ', these strips 13' to 17 'are fillers which are joined together at bending points 18' and which form the plane intersections of the grid there. In order to produce this filling, a strip 28 'made of sheet metal or the like is cut into parallel strips 30' connected at a plurality of locations 29 '. In this case, the cutting line portions 31 ′ connecting the adjacent strips 30 ′ have the same length and are shifted with respect to the adjacent cutting line portions 31 ′ by half of this length. Thereafter, the strip 30 'is pulled apart.

[0005]

However, the gas-liquid contacting device of the packed tower type requires a higher tower design than the plate type of the same liquid load and gas load. However, there has been a problem that the construction cost increases.
Therefore, there has been a demand for a gas-liquid contact device capable of increasing the upper limits of the liquid load amount and the gas load amount of the filler and increasing the load without causing flooding. Further, an apparatus capable of setting a large increase / decrease range of the product amount has been desired. The present invention has been made in view of the above circumstances, and has as its object to provide a gas-liquid contact device capable of increasing a load amount.

[0006]

SUMMARY OF THE INVENTION The present inventors have conducted tests using Freon, which is a liquid having a viscosity similar to that of a liquefied product of air components such as nitrogen, oxygen, and argon.
Although the low-viscosity liquid such as the air component liquefied substance is likely to spread on the surface of the packing and high-efficiency gas-liquid contact is expected, when a gas-liquid contacting device having a self-distribution promoting type regular packing is used, Liquid is on the lower side (back side) of the inclined part of the filling
It has been found that the gas-liquid contact efficiency may be reduced due to the difficulty in flowing gas. The present invention has been made on the basis of the above findings, and as a filler, non-distributed sheets or tubes of various shapes that form the flow direction of the liquid and gas in the vertical direction are laminated or arranged in a state along the vertical direction. Gas-liquid contact, characterized in that it comprises at least one liquid distributor using a promoted structured packing and comprising a coarse distribution part for roughly distributing the liquid and a precision distribution part for precisely and evenly distributing the liquid. Device. Further, the present invention is characterized in that the specific surface area of the non-promoting-fluid-dispersion type structured packing is 350 m ² / m ³ or more. Further, the present invention is characterized in that the precise dispensing section for precisely and evenly distributing the liquid is made of a self-promoting-dispersion type structured packing. Further, the present invention is characterized in that the precision distributing section for precisely and evenly distributing the liquid is formed by stacking at least one self-promoting-dispersion type structured packing and a group of parallel flat plates in the column direction. And The parallel plate group may be made of metal. Further, the present invention is characterized in that the non-distribution promoting type structured packing comprises a group of thin metal plates or a group of metal tubes. The metal sheet is aluminum, an aluminum alloy,
Copper, copper alloy, various stainless steels and the like. Also one
Including the case of a plate-shaped wire mesh of 0 mesh or more. Further, the plate-shaped wire mesh includes a net formed by knitting a band-shaped plate. Further, the present invention is characterized in that the non-distribution promoting type structured packing comprises a group of various plastic thin plates or a group of tubes. Also, the present invention provides the non-distribution promoting type structured packing,
The cross-sectional shape of the flow path is square. At the same time that the cross-sectional shape of the flow path is polygonal including polygons of various shapes,
This includes the case where the cross-sectional shape is a rectangular shape such as a triangular bent waveform. Further, the present invention is characterized in that the cross-sectional shape of the non-distribution promoting type structured packing is triangular. Also,
The present invention is characterized in that the cross-sectional shape of the non-distribution promoting type structured packing is a square such as a square, a rectangle, a trapezoid, or a rhombus. Further, the present invention is characterized in that the cross-sectional shape of the non-distribution promoting structured packing is a hexagon.
Further, the present invention is characterized in that the non-distribution promoting type structured packing is constituted by a corrugated thin plate having a curved surface. Also, the present invention provides the non-distribution promoting type structured packing,
It is characterized by forming a flow path having a cross section of at least two of a triangle, a quadrangle, and a hexagon. Also, the present invention provides the non-distribution promoting type structured packing,
It is characterized by comprising a plurality of thin plates arranged via spacers. Further, the present invention is characterized in that the thin plate or the spacer is provided with at least one of irregularities, grooves, and holes. Further, the present invention is characterized in that at least one steam distributor for distributing steam is provided below the non-distribution promoting type structured packing. Further, the present invention is characterized in that the steam distributor is made of a self-promoting-dispersion type structured packing. Further, an air liquefaction / separation device of the present invention is characterized by using the above-mentioned gas-liquid contact device. Also, the gas separation method of the present invention is a gas separation method for separating a component of a gas mixture consisting of at least two components from other components using a gas-liquid contact device. Are arranged in such a manner that the flow of the mixture is vertical, and the specific surface area of the non-promoting-fluid-ordered structured packing is 350 m ² / used as is m ³ or more, 0.08
Under a pressure condition of ~ 0.4 MPa, the gas mixture and the liquefied product thereof are brought into contact with these liquids while flowing the gas mixture and the liquefied product in the non-distribution promoting type structured packing in opposition along the surface of the packing. The load of the gas and the liquid is set so that the density-corrected superficial velocity becomes 1.8 m / s (kg / m ³ ) ^1/2 or more. Further, the gas separation method of the present invention,
In a gas separation method for separating a component of a gas mixture consisting of at least two components from other components using a gas-liquid contact device, as the gas-liquid contact device, a thin plate or a sheet of various shapes that directs the flow of the mixture in a vertical direction The non-promoting-fluid-dispersion type structured packing composed of pipes is arranged so that the flow of the mixture is vertical, and the non-promoting-fluid-dispersion type structured packing having a specific surface area of 350 m ² / m ³ or more is used. .4-2.
Under a pressure condition of 0 MPa, the gas mixture and a liquefied product thereof are brought into contact with these liquids while flowing the gas mixture and the liquefied product in the non-distribution promoting type structured packing in opposition along the surface of the packing.
The load of the gas and liquid is adjusted to a density-corrected superficial velocity of 1.0
m / s (kg / m ³ ) ^1/2 or more.

[0007]

1 and 2 show an air liquefaction / separation apparatus using an embodiment of a gas-liquid contacting apparatus according to the present invention. The air liquefaction separation device shown here is a high pressure column 2
, A low-pressure column 3 and a crude argon column 4. The high-pressure tower 2 is constituted by a gas-liquid contact device 2a. The low-pressure column 3 is composed of a gas-liquid contact device 3a. The gas-liquid contact device 3a is divided into contact areas 6 to 10 from the bottom to the top. The crude argon column 4 is constituted by a gas-liquid contact device 4a. A condenser 12 is provided near the bottom of the low-pressure column 3, and a crude argon column condenser 13 is provided above the crude argon column 4.

Hereinafter, the gas-liquid contact device 4a of the present embodiment constituting the crude argon column 4 will be described in detail. As shown in FIG. 2, the gas-liquid contact device 4a is accommodated in a cylindrical container that forms a column, toward the bottom side from the top side, provided with a precision distribution part B ₁ to the lower rough distribution part C ₁ Liquid distributor E
_1, a non-promoting-fluid-dispersion type structured packing A _1, and a liquid collector D,
Liquid distributor E provided with precision distribution section B ₂ below coarse distribution section C ₂
A _2, and a non-promoting-fluid-dispersion type structured packing A _2. Hereinafter, the liquid distributor E ₁ and the non-distribution promoting type regular packing A ₁ will be referred to as a liquid distribution / gas-liquid contact part F _1, and the liquid collector D, the liquid distributor E ₂ and the non-distribution promoting type regular packing will be described. The substance A ₂ is referred to as a liquid collection / distribution / gas-liquid contact section F ₂ .

The coarse distribution sections C ₁ and C ₂ coarsely distribute the descending liquid in order to make the descending liquid flow in the column uniform over the cross section of the tower. It is preferable to use the liquid dispersers shown in FIGS. 3 to 5 as the coarse distribution sections C ₁ and C ₂ . The liquid disperser 41 shown in FIG. 3 is called a channel type.
A distribution box 42 for primary dispersion provided in the shape of a rectangular parallelepiped provided in the radial direction of the tower, and a large number of rectangular boxes (cross-section) attached to the lower part of the distribution box 42 at intervals along the length direction of the distribution box 42. (Rectangular) secondary dispersion box 43. The distribution box 42 for primary dispersion is a box-like material having an upper opening,
Both ends are formed so as to reach near the inner wall of the tower, so that the descending liquid in the tower can be temporarily stored inside. Near the bottom of the distribution box 42, a distribution hole (not shown) for distributing the liquid in the distribution box 42 to the secondary dispersion box 43 is provided. The secondary dispersion box 43 is a box-like material arranged along the vertical direction, and is formed so that both ends reach the vicinity of the inner wall of the tower, and flows out from the distribution box 42 through a distribution hole provided at the bottom thereof. The liquid thus obtained can flow down in a state of being uniformly dispersed over the entire cross section of the tower.

A liquid disperser 51 shown in FIG. 4 is of a so-called chimney type, and includes a liquid receiving tray 52 provided along a horizontal plane and a plurality of cylindrical mounts mounted on the upper surface of the tray 52. A chimney 53 and a number of pipe-shaped branches 5 attached to the lower surface of the liquid tray 52;
4 is provided. The tray portion 52 is formed so that the peripheral portion reaches the inner wall of the tower, and is provided with a large number of distribution holes 52a over the entire surface. After the descending liquid is temporarily stored on the liquid receiving tray portion 52, the distribution liquid is distributed. Hole 52a, branch 54
(Pipes open at the upper and lower ends) and flow down in a uniformly dispersed state over the entire cross section of the tower. The upper and lower ends of the chimney 53 are open so that gas rising in the tower can pass above the liquid distributor 51 through the chimney 53.

The liquid disperser 61 shown in FIG. 5 is of a so-called spray type, and has a main pipe section 6 into which the descending liquid in the tower flows.
2 and a plurality of branch pipe portions 63 attached at intervals in the longitudinal direction of the main pipe portion 62. These main pipes 62
The branch 63 is formed so that both ends reach near the inner wall of the tower. The main pipe portion 62 is connected to a liquid receiving portion (not shown) for guiding the descending liquid in the tower into the main pipe portion 62 so that the descending liquid can be guided into the main pipe portion 62. The branch pipe section 63 is formed such that its internal space communicates with the internal space of the main pipe section 62, and the liquid in the main pipe section 62 flows into the branch pipe section 63. The branch pipe portion 63 has a large number of distribution holes 6 at intervals over the entire length direction.
3a is provided so that the liquid in the branch portion 63 flows down in a state of being uniformly dispersed through the distribution holes over the entire cross section of the tower.

[0012] The precision distributing sections B ₁ , B _{2 of the} gas-liquid contact device 4a
Is for precisely and evenly distributing the descending liquid flow roughly distributed by the coarse distribution sections C ₁ and C ₂ over the entire cross section of the column. Hereinafter, the structure of the precision distribution units B ₁ and B ₂ will be described. It is preferable to use a self-promoting-dispersion type structured packing as the precision distributing sections B ₁ and B ₂ . The self-promoting-dispersion type structured packing has a descending liquid stream and an ascending gas stream brought into gas-liquid contact on the surface of the structured packing, and the liquid stream and the gas stream are formed on the surface of the structured packing in a column axis. At the same time, the liquid flows and the gas flow are generated in a direction perpendicular to the main flow direction in the main flow direction along the direction, and the gas-liquid contact is performed while promoting the mixing of the two.・
This is a packing with a structure. A thin plate made of aluminum, copper, an alloy of aluminum and copper, stainless steel, various plastics, etc. is formed into various regular shapes, and this is formed into a block structure with a laminated structure. Also called an object. In the present invention, the case where the above-mentioned thin plate is a plate-like wire mesh of 10 mesh or more is also included.

Next, specific examples of the self-promoting-dispersion type structured packing are shown in FIGS. The self-promoting-dispersion type structured packing 71 shown in FIG. 6 is disclosed in Japanese Patent Publication No. 57-36009, in which a plurality of corrugated thin plates 72 made of aluminum or the like are arranged in parallel to the tower axis. Each of the thin plates 72 is laminated so as to be in contact with each other to form a block.
Of the corrugated grooves 73 are inclined with respect to the tower axis, and the adjacent corrugated thin plates 72 are arranged so that the directions in which the corrugated grooves 73 are formed intersect. Reference numeral 72a denotes a hole provided in the thin plate 72.

FIG. 7 shows a thin plate 82 which is a constituent unit of the self-promoting-dispersion type structured packing 81 disclosed in Japanese Patent Application Laid-Open No. 54-16676. This thin plate 82 is formed into a corrugated shape. The feature is that the groove 83 is formed, and the thin plate 82 is further provided with a minute corrugated groove (fold) 84 formed at a predetermined angle with respect to the corrugated groove 83. Reference numeral 82a denotes a hole formed in the thin plate 82.

FIGS. 8 and 9 show another example of the self-promoting-dispersion type structured packing, which is described in Japanese Patent Application Laid-Open No. 58-11001. The self-promoting-fluid-dispersion type structured packing shown here was developed for the purpose of distributing a liquid so as to obtain a liquid surface as large as possible for substance and heat exchange, and a plurality of thin plate lattices a, b, and c,
.., each of the lattices a, b, c,... Being composed of thin strips 13 ′ to 17 ′ that are bent in a zigzag shape and inclined to lattice planes A, B, C,. , These thin strips 13'-1
7 'is a packing which is joined together at a bending point 18' and forms a planar crossing point of the grid thereat, wherein the strips 13'-17 'extending in the flow direction are connected at the crossing point 18'. , Crossing point 1 through thin strips 13'-17 '
Liquid phase 23 'flowing down to 8' is at least partially crossing 1
It is characterized in that it is formed so as to be guided to adjacent thin strips 13 'to 17' via 8 '. At the intersection 18 ', notches 2 are formed at the outer edges of the thin strips 13' to 17 '.
0 ′ and 21 ′ are formed. Notches 20 'and 21'
In the direction in which the thin strips 13 ′ to 17 ′ extend in a zigzag manner, the width s of the thin strips 13 ′ to 17 ′ is longer than the width s of the thin strips 13 ′ to 17 ′. It is formed deeper than half. In addition, thin strip 1
3'-17 'are stacked directly on each other.

A hole and / or a side notch can be formed between the intersections 18 'of the thin strips 13' to 17 '. Further, holes and / or side cutouts can be alternately formed in the thin strips of the thin strips 13 'to 17' which are successively formed in a zigzag shape.

As shown in FIG. 10, the above-mentioned filling material is formed by cutting a plurality of parallel strips 3 connected at a plurality of locations 29 ′ by making a cut in a thin metal strip 28 ′.
0 'is formed, a diamond-shaped hole 32' is provided in the cut portion 31 ', and a diamond-shaped lattice obtained by stretching the metal strip 28' in a direction 33 'which is a direction perpendicular to the strip 30'. Can be manufactured by laminating a plurality of thin plate lattices and forming a block shape.

This filling has the advantage that a large filling surface can be obtained with little material cost. This advantage derives from the lamella structure of the grid, that is to say that the lamella is a lamella with a large surface compared to the material costs.

Next, the structure of the non-promoting-dispersion type structured packings A ₁ and A ₂ will be described. Non-distribution-promoting structured packing is
The liquid flow descending in the tower and the ascending gas flow oppose each other along its surface, and the gas-liquid contact is performed without promoting the mixing of the liquid flow and the gas flow in the cross-sectional direction perpendicular to the tower axis. A packing having a shape and a structure, in which a number of thin plates, tubes, and the like that determine the flow direction of the liquid and the gas are arranged in parallel with the main flow direction (the tower axis direction). The thin plate,
As the material of the tube, aluminum, copper, an alloy of aluminum and copper, stainless steel, various plastics, and the like can be used. Among them, it is particularly preferable to use a metal that can be easily formed. The main flow refers to a liquid flow descending and a gas flow rising along the direction of the tower axis in the column, and the mass flow generated at the interface between the liquid flow and the gas flow (that is, the boundary layer) on the surface of the packing material. It refers to the flow in the tower axis direction relative to the flow.

Specific examples of the non-promoting-dispersion type structured packings A ₁ and A ₂ are shown in FIGS. The non-promoting-dispersion type structured packing 91 shown in FIGS. 11 to 13 is formed by laminating a plurality of laminated thin plates 92 with a wiper band 95. The thin plate 92 is formed by bending a thin plate made of the above metal, plastic, or the like, and forming a plurality of parallel grooves 93 at intervals. The groove 93 is formed so as to gradually decrease in width in the depth direction, and includes an inclined portion 93a inclined with respect to the base 94, and a bottom 93b parallel to the base 94. The thin plates 92 are stacked such that the bases 94 and the grooves 93 face each other. For this reason, in the non-distribution-promoting structured packed material 91, the gap between the thin plates 92, that is, the space defined by the two opposing grooves 93 or the two bases 94 has a cross section of 6.
It has a square shape. This space becomes a flow path 96 for a rising gas and a descending liquid during a distillation operation described later. The non-distribution promoting type structured packing 91 is provided in the column such that the thin plate 92 is parallel to the tower axis (vertical) direction which is the main flow direction.

The non-promoting-dispersion type structured packing 10 shown in FIG.
1 is a thin plate group in which a plurality of triangular bent plates 102 formed by bending a thin plate made of the above metal, plastic or the like to form a triangular wave via a plate-shaped spacer 103 made of metal, plastic, or the like, They are fixed to each other by a wiper band 95. In the non-distribution promoting type structured packing 101 shown here, the uppermost portion 102a of the triangular bent plate 102
However, the position of the triangular bent plate 102 is determined so as to be located near the lowermost portion 102b of the adjacent triangular bent plate 102. In the non-distribution promoting type structured packing 101, a triangular wave-shaped triangular bent plate 102 is laminated via a plate-shaped spacer 103. Curved plate 102 and spacer 1
03, a multiplicity of triangular channels 106
Becomes The triangular bent plate 102 may be formed so that the cross-sectional shape of the flow path 106 becomes an equilateral triangle, or may be formed so as to become an isosceles triangle or an inequilateral triangle.

Non-distribution promoting type structured packing 11 shown in FIG.
1 is that the position of the triangular bent plate 102 is determined so that the uppermost portion 102a of the triangular bent plate 102 and the lowermost portion 102b of the adjacent triangular bent plate 102 are separated from each other. It is different from the ordered packing 101. Also in the non-distribution promoting type structured packing 111, the gap between the triangularly bent plate 102 and the spacer 103 becomes a large number of triangular cross-sectional channels 116 divided by the triangularly bent plate 102 and the spacer 103.

The non-promoting-dispersion type structured packing 12 shown in FIG.
1 is a triangularly bent plate 102 in the non-distribution promoting type structured packing 101 shown in FIG.
Are laminated. This non-distribution promoting type structured packing 1
In 21, similarly to the filling 101, the position of the triangular bent plate 102 is determined such that the uppermost portion 102 a of the triangular bent plate 102 is located near the lowermost portion 102 b of the adjacent triangular bent plate 102. Therefore, the gap between the triangularly bent plates 102 becomes a flow path 126 having a quadrangular cross section, which is a shape obtained by combining two flow paths 106 having a triangular cross section. In this case, the triangular bent plate 102 can be formed such that the cross-sectional shape of the flow channel 126 is various shapes such as a square, a rectangle, a trapezoid, and a rhombus.

The non-distribution promoting structured packing 12 shown in FIG.
Reference numeral 1 'designates the position of the triangular plate 102 such that the uppermost portion 102a of the triangular plate 102 and the lowermost portion 102b of the adjacent triangular plate 102 are separated from each other.
A plurality of spacers (not shown) can be interposed between the triangular bent plates 102 at intervals in the tower axis direction.

The non-promoting-fluid-dispersion type structured packing 13 shown in FIG.
Reference numeral 1 denotes a laminate in which a plurality of corrugated plates 132 formed by bending a thin plate made of the above-mentioned metal, plastic, or the like to form a corrugated surface are laminated, and these are fixed to each other by a wiper band 95. The corrugated plate 132 has a shape in which a concave portion and a convex portion are curved in an arc-shaped cross section. In the non-distribution promoting type structured packing 131 shown here, the top 1
The position of the corrugated sheet 132 is determined such that the position 32a is located near the lowermost part 132b of the adjacent corrugated sheet 132.

The non-distribution promoting structured packing 14 shown in FIG.
1 is the one in which the spacers 103 are arranged between the corrugated plates 132 in the above-mentioned non-distribution promoting type structured packing 131.

The non-distribution promoting type structured packing 15 shown in FIG.
1 is different from the non-distribution promoting type structured packing 141 in that the corrugated plate 152 is formed in a corrugated shape having a flat plate portion 152a substantially perpendicular to the spacer 103 and a curved plate portion 152b.

The non-promoting-dispersion type structured packing 16 shown in FIG.
1 is a cylindrical tube 1 made of the above metal, plastic, etc.
A group of tubes 62 are fixed to each other by a wiper band 95. This non-distribution promoting type structured packing 1
In 61, the inside of the pipe 162 becomes a flow path 166a having a circular cross section. Further, a portion defined by the outer peripheral surface of the pipe 162 becomes a flow path 166b. The shape of the tube 162 is not limited to the above, and a tube having a cross section of an ellipse, or a polygon such as a triangle or a quadrangle can also be used.

The non-promoting-fluid-dispersion type structured packing 17 shown in FIG.
1 is the above-mentioned non-distribution promoting type structured packing 91 shown in FIGS. 11 to 13 and the non-distribution promoting type structured packing 111 shown in FIG.
And a flow path 96 having a hexagonal cross section.
, And two types of flow paths 116 having a triangular cross section.

These non-distribution promoting type structured packings 91, 10
1, 111, 121, 121 ', 131, 141, 15
When installing 1, 161 and 171 in the tower, the bent shapes of the plates 92, 102, 132 and 152 constituting them are all vertical, and the spacer 103 and the pipe 162
Is parallel to the tower axis (vertical) direction, which is the main flow direction, in all parts.

In the packing shown in FIGS. 14, 15, 19, 20, and 22, the spacer 103 extends from the upper end to the lower end of one packing block longitudinal section as long as the relative position of the thin plate can be determined. It is not necessary that the material be partially inserted between the thin plates to function as a spacer. The thickness of the spacer 103 is 0.2
０．５0.5 mm.

Further, at least one of irregularities, grooves, and holes may be formed in the thin plate and the spacer constituting the non-distribution promoting type structured packing to improve the gas-liquid contact efficiency. 23 and 24 show specific examples.
Shown in FIG. 23A shows a non-distribution promoting type structured packing 91.
This shows a configuration in which a hole 92a is provided in a thin plate 92 similar to that used in the above. FIG. 23B shows a configuration in which unevenness 92 b is provided on a thin plate 92. FIG.
(C) shows a configuration in which a groove 92c is provided in the thin plate 92. FIG. 24 (a) shows the non-distribution promoting type structured packing 11
A spacer 103 similar to that used for
3 shows a configuration provided with 3a. FIG. 24 (b)
This shows a configuration in which irregularities 103b are provided on the spacer 103. FIG. 24C shows that the groove 103 c is formed in the spacer 103.
FIG. Also, two or more of these irregularities, grooves, and holes can be formed on the thin plate and the spacer.

The specific surface area of the non-promoting-dispersion type structured packing is desirably 350 m ² / m ³ or more, preferably 500 m ² / m ³ or more. This specific surface area is 350 m ² / m ³
If it is less than this, the gas-liquid contact efficiency is reduced, the distillation efficiency is reduced, and the purity of the product is reduced. The thickness of the thin plate or tube is preferably 0.1 to 2.0 mm in consideration of structural strength.

Returning to FIG. 2, a further description will be given. Gas-liquid contact device 4
The liquid collector D of (a) is for collecting descending liquid in the tower, and includes a plurality of inclined plates 181 for collecting descending liquid.

A gas-liquid contact device 2a constituting the high pressure column 2,
The gas-liquid contact device 3a constituting the low-pressure tower 3 can have the same configuration as the gas-liquid contact device 4a. Further, the gas-liquid contact apparatus 2a, 3a, as the 4a, not limited to the above configuration, it is also possible to use a liquid distribution · vapor-liquid contact portion F ₁ consisting of a liquid distributor E ₁ and packing A ₁ Tokyo. Furthermore, gas-liquid contact apparatus 2a, 3a, 4a is liquid distributing and the lower gas-liquid contact portion F _1, the liquid collector D, liquid distributor E _2, and a liquid collecting dispensed consisting packing A ₂ · the gas-liquid contact part F ₂ may be provided with plurality.

Each of the sections 6 to 9 of the gas-liquid contact device 3a includes one or more of the above-mentioned liquid collection / distribution / gas-liquid contact portions F
₂ can be used. It is not necessary to provide the liquid collector D in the area 10 which is the area closest to the top of the tower. That is, the nearest zone 10 to the top of the column, liquid distribution, consisting of a liquid distributor E ₁ and packing A ₁
It can be used gas-liquid contact portion F _1. In addition to the above configuration, the bottom of each column, may be taking into account the distribution of the rising gas, providing the precise distribution part B _1.

As described above, the self-promoting-dispersion type structured packing can be used for the precision distribution sections B ₁ and B ₂ . For example, precise liquid distribution can be performed by providing one or more layers of the filler having the shape shown in FIGS. The detailed structure, features and effects of this type of packing are described in JP-A-58-11.
001. As described above, this filler can be suitably used for a liquid distributor and a precision dispenser, but it can be of course suitably used for an ordinary gas-liquid contact device.

Next, using the air liquefaction and separation apparatus shown in FIGS. 1 and 2, each component in the raw material air, which is a gas mixture containing nitrogen, oxygen and argon, is separated from other components by liquefaction and separation. As an example, an embodiment of the gas separation method of the present invention will be described. In the example shown, the gas-liquid contact device 2a, as 3a, similarly to the gas-liquid contact apparatus 4a shown in FIG. 2, a liquid distribution · vapor-liquid contact portion F _1, the liquid collecting distributing and gas-liquid contact portion F _The one having the structure provided with ₂ shall be used. In addition, non-distribution promoting type structured packing A
₁ and A ₂ are non-distribution promoting type structured packings 91, precision distribution sections B ₁ and B ₂ are self-distribution promoting type structured packings 71, and coarse distribution sections C ₁ and C ₂ are liquid dispersers 41. Shall be.

First, feed air is supplied to the lower part of the high-pressure column 2 through the pipe 1. The feed air is usually about 0.6
After being compressed to MPa, impurities such as water and carbon dioxide are removed by a pretreatment device using an adsorbent such as silica, alumina gel, or molecular sieve, and cooled to a predetermined temperature by a main heat exchanger, the high pressure column 2 Supplied to The raw material air supplied into the high-pressure column 2 rises in the high-pressure column 2 as a rising gas, contacts a descending liquid described later in the gas-liquid contact device 2a, and is subjected to distillation.
It is separated into nitrogen gas (low boiling component) at the top of the column and oxygen-enriched liquid air (high boiling component) at the bottom of the column. At this time, the internal pressure of the high-pressure column 2 is controlled, for example, by the non-distribution promoting type structured packing A ₁ , A ₂
When the specific surface area is 500 m ² / m ³ , 0.4 to 2.
0 MPa, in which case the density corrected superficial velocity is 1.0 m / s (kg / m ³ ) ^1/2 or more, for example, 1.0 m / s (kg / m ³ ) ^1/2.
１1.6 m / s (kg / m ³ ) ^1/2 .

The nitrogen gas separated at the top of the high-pressure column 2 is extracted from the high-pressure column 2 through a pipe 12a and introduced into the main condenser 12, where it is cooled and liquefied. The liquid is returned into the high-pressure column 2 through the pipes 12b and 12c and becomes a descending liquid (reflux liquid) flowing down the high-pressure tower 2, and the remaining part is led out of the tower through the pipe 23.

Hereinafter, a process in which distillation proceeds by contact between the descending liquid and the rising gas in the high-pressure column 2 will be described. First, the descending liquid is temporarily stored in the primary dispersion distribution box 42 of the coarse distribution section C ₁ , and is passed through the distribution holes.
Reached, is temporarily stored in the dispersion box 43, it flows down uniformly dispersed in the lower state (roughness distributed state) the rough distribution part C ₁ over the entire cross section of the column through the distribution hole provided in the bottom thereof .

Next, the descending liquid reaches the precision dispensing section B ₁ ,
Here, it spreads on the surface of the thin plate 72 of the self-distribution promoting type structured packing 71, and flows down below the self-distribution promoting type structured packing 71 in a more precise and evenly distributed state. At this time, the descending liquid comes into contact with the gas rising in the column, mass transfer is performed between gas and liquid, and distillation proceeds.

Next, the descending liquid reaches the non-promoting-dispersion type structured packing A ₁ (filling 91) and flows down the surface of the thin plate 92. At this time, the descending liquid flows down the surface of the thin plate 92 along the thin plate 92, and in this process, the descending liquid comes into contact with the gas rising in the tower.

In the gas-liquid contact device 2a shown here, as described above, the thin plate 92 of the filler 91 is moved in the main flow direction (vertical direction).
Since it is arranged along the flow of the descending liquid in the packing A ₁ is intended to all along in this direction. Therefore, the flow of the descending liquid is not disturbed, and the liquid flow is smooth and uniform over the entire surface of the thin plate 92. Therefore,
Prevents the rising gas flow path from becoming narrow due to the turbulence of the descending liquid flow, secures a sufficient rising gas flow path, suppresses the increase in pressure loss due to the increase in rising gas flow resistance, and does not cause flooding Distillation can be performed. In addition, the descending liquid flowing on the surface of the thin plate easily spreads over the entire thin plate, a large gas-liquid contact area is secured, and efficient distillation is performed. On the other hand, in the gas-liquid contact device using only the self-promoting-dispersion type structured packing, at least a part of the thin plate is inclined with respect to the main flow direction (vertical direction). In addition, the descending liquid does not easily flow on the back side of the inclined portion, and the gas-liquid contact area becomes insufficient, so that the efficiency of distillation may be reduced.

The descending liquid having passed through the non-distribution promoting type structured packing A ₁ is collected in the liquid collector D and introduced into the coarse distribution section C ₂ where the flow is homogenized and then self-distributed. The promoted structured packing B ₂ flows further downward through the non-distributed promoted structured packing A ₂ and reaches the bottom of the column. Also in the non-promoting-dispersion type structured packing A ₂ , the descending liquid flows smoothly and uniformly over the surface of the thin plate 92, so that distillation is performed without flooding in the high-pressure column 2. Also, the distillation efficiency is kept high.

A part of the liquid nitrogen led out of the high-pressure column 2 through the line 23 is introduced into the low-pressure column 3 as reflux liquid nitrogen through the valve 24 and the line 25, and the descending liquid descends in the low-pressure column 3. Becomes The other part is led out of the system through line 22 as product liquid nitrogen (LN ₂ ).

The oxygen-enriched liquid air separated at the bottom of the high-pressure column 2 is led out of the high-pressure column 2 through a line 15 and partly introduced into a crude argon column condenser 13 through a line 16, After being exchanged with the gas or liquid in the condenser 13 and heated and partially vaporized, the gas or liquid is introduced into an intermediate portion of the low-pressure column 3 (between the top and the bottom) through the pipe line 31, and descends in the low-pressure column 3. It becomes liquid or rising gas. The other part of the oxygen-enriched liquefied air derived from the high-pressure column 2 is introduced into the intermediate portion of the low-pressure column 3 through a pipe 17, a valve 18, and a pipe 19, and becomes a descending liquid or a rising gas in the low-pressure tower 3. .

The descending liquid and the ascending liquid introduced into the low pressure column 3
The gas is exchanged in each section 6 to 10 of the gas-liquid contact device 3a.
And gas is distilled, and oxygen gas and liquid
As the oxygen is separated, it is separated into nitrogen gas at the top of the tower.
It is. The internal pressure of the low-pressure column 3 is, for example, a non-distribution promoting pressure in the low-pressure column 3.
Hexagonal regular packing A₁, A_TwoHas a specific surface area of 500m^Two/ M^Threeso
In some cases, 0.08 to 2.0 MPa, preferably 0.08 to 2.0 MPa.
8 to 0.4 MPa, and in this case,
Degree corrected superficial velocity is 1.8 m / s (kg / m^Three)^1/2Less than
Above, preferably 1.8 to 2.5 m / s (kg / m ^Three)^1/2
It can be set so that

Each section 6 of the gas-liquid contact device 3a in the low pressure column 3
Also at 10 to 10, since the descending liquid flows smoothly and uniformly over the thin plate surface of the packing materials A ₁ and A ₂ , distillation is performed in the low-pressure column 3 without flooding. Also, the distillation efficiency is kept high.

The nitrogen gas separated at the top of the low-pressure column 3 is led out of the system as product nitrogen gas (GN ₂ ) through a pipe 21. The oxygen gas separated at the bottom of the low-pressure column 3 passes through a pipe 32 to a product oxygen gas (GO ₂
) Is derived outside the system. The gas in the upper part of the low-pressure column 3 is discharged out of the system through a pipe 20 as waste nitrogen gas (WG).

The gas in the low-pressure tower 3 at a position slightly below the position where the pipe 31 is connected to the low-pressure tower 3 passes through the pipe 2
6, is supplied to the lower part of the crude argon column 4. The gas supplied into the crude argon column 4 is distilled in the gas-liquid contact device 4a constituting the crude argon column 4, and the crude argon gas is separated at the top of the column. This crude argon gas is supplied through line 3
3, is led out from the top of the crude argon column 4, introduced into the condenser 13, and passed through the above-described line 16 to the condenser 13.
The liquid is cooled and liquefied by heat exchange with the oxygen-enriched liquefied air introduced into the reactor, and then returned to the upper part of the crude argon column 4 as a reflux liquid through lines 34 and 35. Part of the liquefied crude argon led out of the condenser 13 through the pipe 34 is led out of the system as liquefied crude argon (LAr) through the pipe 29. The liquid separated at the bottom of the crude argon column 4 is passed through line 2
It is returned to the low pressure column 3 through 7, 28. When the equivalent number of theoretical plates of the crude argon column 4 is set to be large, the pump 14 is connected to the lines 27 and 28 in order to return the bottom liquid to the low-pressure column 3.
Can be installed in

In the gas-liquid contacting device 4a in the crude argon column 4, the descending liquid flows smoothly and uniformly over the thin plate surface of the packing materials A ₁ and A ₂ , so that flooding occurs in the crude argon column 4. Distillation takes place without. Also, the distillation efficiency is kept high.

In recent years, a case has been adopted in which the crude argon column 4 is set to the number of theoretical plates almost as before, and a deoxidizing column is installed to remove oxygen in the crude argon. In this case, the above effect can be obtained by using a deoxidation tower having the same configuration as that shown in FIG.

In the gas-liquid contact devices 2a, 3a and 4a,
The thin plates of various shapes constituting the non-distribution promoting type structured packings A ₁ and A ₂ are arranged so that their shapes are along the main flow direction (vertical direction), so that a sufficient ascending gas flow path is secured. At the same time, the flow of the descending liquid on the surface of the thin plate (or tube) is smooth and uniform over the entire surface of the thin plate. Therefore, while suppressing the increase in pressure loss due to the increase in the flow resistance of the rising gas, preventing the occurrence of flooding, the gas-liquid contacting device using a self-dispersion promoting type structured packing having an inclined portion has a sufficient gas-liquid contacting device. It is possible to secure a contact area and perform efficient distillation. Therefore, the liquid load and the gas load can be set large without causing flooding.

For example, in a conventional gas-liquid contact device using a packing having a specific surface area of 500 m ² / m ³ (self-distribution promoting type structured packing), the density-corrected superficial velocity is 1.6 m.
/ S (kg / m ³ ) ^1/2 or less (internal pressure of 0.08 to 0.4
MPa) or 1.0 m / s (kg /
m ³ ) ^1/2 or less (when the column internal pressure is 0.4 MPa or more)
On the other hand, in the gas-liquid contact devices 2a, 3a and 4a, the density-corrected superficial superficial velocity of each tower was set to 1.
8 m / s (kg / m ³ ) ^1/2 or more (internal pressure 0.08 to 0.
4 MPa) or 1.0 m / s (kg / m ³ ) ^1/2 or more (internal pressure of 0.4 to 2.0 MPa).

For this reason, the gas-liquid contact devices 2a, 3a, 4a
By using, the height of the tower can be designed low, and the cost required for manufacturing and constructing the device can be kept low. Further, since the upper limit of the load is high, the production amount of the product can be greatly increased or decreased.

In general, in a packed column, flooding tends to occur more easily as the column internal pressure is higher, and it has been difficult to apply the packed column to a high-pressure column of an air liquefaction / separation apparatus having a double distillation column. On the other hand, since the gas-liquid contact device 2a can set a high load even under a high pressure, it can be applied to a high-pressure column.
Therefore, the air liquefaction / separation apparatus in which the gas-liquid contacting device 2a is applied to the high-pressure column 2 has a lower power cost and product purity than the apparatus in which a plate column inferior in pressure loss to the packed column is applied to the high-pressure column. It is excellent in point.

[0058] In order to further improve the function of the precise distribution part B _1, B _2, precise distribution part B _1, as B _2, at least the promoting-fluid-dispersion type structured packing above, and a parallel plate group Structures laminated one by one in the tower axis direction can be used. FIG. 25 and FIG. 26 show examples of the parallel plate group. The parallel flat plate group 85 shown in FIG. 25 includes a plurality of flat plates 85a arranged in parallel with each other and at intervals. These flat plates 85a are arranged along the tower axis direction. Each flat plate 85a is formed so that the end in the direction perpendicular to the tower axis reaches near the inner wall of the tower, and each flat plate 85a has a spacer (not shown) having a thickness equal to the distance between them. They are fixed to each other in a sandwiched state. The thickness of the flat plate 85a is preferably 0.5 to 5 mm in consideration of structural strength. Each flat plate 8
The interval of 5a is preferably set to 3 to 10 mm in consideration of the liquid dispersion density. The flat plate 85a is preferably made of metal, but may be made of plastic. Although the shape and material of the spacer are not particularly limited, the size, for example, the length in the horizontal direction and the length in the tower axis direction is a range in which the strength of the structure can be maintained so as not to greatly hinder the flow of the liquid film on the flat plate. The smaller the better.

When the above-mentioned parallel plate group is provided below the self-promoting-dispersion type structured packing as the precision distributing sections B ₁ and B ₂ , the precise distribution is performed within the self-promoting-dispersion type structured packing. The supplied liquid is supplied to a group of parallel plates placed below and flows down while forming a liquid film of uniform thickness on the surface of each plate, so that the flow rate of the liquid is parallel to each plate and perpendicular to the tower axis. Uniform over various directions. As a result, a more precisely distributed liquid is supplied to the non-distribution promoting type structured packings A ₁ and A ₂ .

In order to more surely increase the liquid spray density on the non-distribution promoting type structured packings A ₁ and A ₂ , a plurality of flat plates constituting the parallel flat plate group are provided at the lower edge thereof in the width direction of the flat plates. Protrusions can also be formed. The width direction refers to a direction parallel to the flat plate and perpendicular to the tower axis. FIG. 26 shows a parallel plate group 86 formed with the protruding portions. The lower edge portion 86b of the flat plate 86a constituting the parallel plate group 86 shown here.
Has a large number of V-shaped protrusions 86c over the entire width direction.
Are formed. The pitch of these projections 86c is 3 to
It is preferably 10 mm.

As shown in FIG. 26, when a plurality of projections 86c are formed on the lower edge portion 86b as the flat plates constituting the parallel plate group, the liquid flowing near the projections 86c flows down. It gathers near the tip of the projection 86c and flows down from this tip. For this reason, the liquid flowing down on the surface of the flat plate 86a reaches the lower edge 86b and then reaches the lower edge 8b.
6b, and the flow rate of the liquid can be prevented from being biased in the width direction of the flat plate. Therefore, more precise liquid distribution becomes possible.

Normally, non-partitioning-promoting structured packing does not have the function of positively distributing the vapor stream. For this reason,
In order to maximize the distillation performance, at least one steam distributor for distributing the ascending steam in the apparatus should be provided below the non-distribution-enhanced structured packing in consideration of the distribution of the steam flow. preferable. As the vapor distributor, it is preferable to use a self-promoting-dispersion type structured packing, for example, those shown in FIGS.

When the self-promoting-dispersion type structured packing is used as a vapor distributor, mist (fine droplets) is generated below the packing, and the mist collides with the thin plate surface of the packing to cause a liquid flow. , The effect of preventing entrainment is obtained. Further, in the gas-liquid contact device of the present invention, since the non-distribution promoting type structured packing is used with a high load for both the vapor and the liquid, the self-distribution promoting type structured packing used in the precision distribution section and the like is used to avoid flooding. It is preferable to use one having a specific surface area equal to or smaller than that of the non-distribution promoting type structured packing.

[0064]

EXAMPLES Hereinafter, the effects of the present invention will be clarified by showing examples.
To (Example 1) Distillation using the air liquefaction separation apparatus shown in FIG.
A computer simulation of the operation was performed. High pressure tower
2. Gas-liquid contact devices 2a and 4a in the crude argon column 4
Is applied from the top to the bottom as shown in Fig. 2.
And the liquid distributor E₁And non-distribution promoting type structured packing A₁And liquid
Body collector D and liquid distributor E_TwoAnd non-distribution promoting rule filling
Thing A_TwoIt is assumed that a material having Also low
Each of the sections 6 to 9 of the gas-liquid contact device 3a of the pressure tower 3 collects liquid.
Distribution / gas-liquid contact part F_TwoIn the area 10, the liquid distribution
Gas-liquid contact part F₁Was used. Non-distribution-promoting rules
Filling A₁, A_TwoAs the regular packing 91,
Distribution-promoting structured packing B₁, B_TwoAs a regular packing 71
Used, coarse distribution section C₁, C_TwoUse liquid disperser 41
I decided that. For gas-liquid contactor 4a in crude argon column 4
Non-distribution promoting type structured packing A ₁, A_TwoSpecific surface area
Is 500m^Two/ M^ThreeWas assumed. The pressure in the tower is about 0.1M
Pa, oxygen concentration in feed argon is about 90%
Was. As a result of the simulation, the filling height and steam obtained
The relationship between the oxygen concentrations in the phases is shown by the solid line in FIG. The figure
Medium, the filling height of 0 m indicates the bottom of the tower.

(Comparative Example 1) In the gas-liquid contact device 4a,
Example ₁ was replaced by a device having the same configuration as the device shown in FIG. 1 except that the same area of the self-distribution promoting structured packing was used instead of the non-distribution promoting structured packing A ₁ and A ₂ . A computer simulation was performed when a similar distillation operation was attempted. The result is indicated by a broken line in FIG.

As shown in FIG. 27, in the gas-liquid contact device 4a,
It can be seen that by using the non-promoting-fluid-dispersion type structured packings A ₁ and A ₂ , the required filling height is about 60% as compared with the case of using the self-promoting-fluid-dispersion type structured packing.

Next, the following test was conducted to compare the pressure loss between the case where the non-promoting-dispersion type structured packing was used and the case where the self-promoting-promoting structured packing was used. (Example 2) The following test was conducted using a distillation column which is a gas-liquid contact device shown in FIG. This distillation column (inner diameter 208m
m, made of transparent vinyl chloride) is provided with a coarse distribution section C ₃ , a fine distribution section B ₃ , and a non-distribution promoting type structured packing A ₃ from the top to the bottom. The crude distributor C _3, used was the same as that shown in FIG. The precision distribution section B ₃ has a specific surface area of 500 m ² / m ³ and a height of 10
0 mm self-distribution promoting type structured packing with 2 elements,
A parallel plate group 85 (height 50 m) similar to that shown in FIG.
m) and a parallel plate group 86 (height: 50 mm) similar to that shown in FIG. 26 were sequentially stacked from the top.
At this time, the two parallel flat plate groups 85 and 86 were arranged such that the parallel flat plates 85a and 86a constituting each group had a positional relationship perpendicular to each other. Non-distribution-promoting structured packing A
_{As 3} , the same one as shown in FIG. 15 (specific surface area 375 m ² / m ³ , height 600 mm) was used. The total height of the precision dispensing section B ₃ and the non-distribution promoting structured packing A ₃ is 900 mm.

As the fluid, CFC 11 having the same viscosity as that of air was used, the density-corrected superficial velocity was changed under the conditions of a pressure of 130 kPa and total reflux, and the coarse distribution section C ₃ and the precision distribution section B _{3 were used.}
And the pressure loss of the sum of non-promoting-fluid-dispersion type structured packing A ₃ was measured.

Comparative Example 2 For comparison, a distillation column of a type using a self-promoting-dispersion type structured packing as a packing,
That is, using a distillation column provided below the coarse distribution section C ₃ with 5 elements (500 m ² / m ³ , 5 elements of self-promoting-dispersion type structured packing having a height of 207 mm (total filling height of 1035 mm))
The test was performed. The promoting-fluid-dispersion type structured packing, was used and what the same type used in precision dispensing portion B ₃ of the distillation column shown in Figure 28. In the same manner as in Example 2, as the fluid, Freon 11 having the same viscosity as air was used, and the density-corrected superficial velocity was changed under all reflux conditions, and the pressure loss was measured under each condition.

FIG. 29 is a graph showing the pressure loss per unit height with respect to the density superficial velocity. As can be seen from this figure, the pressure loss in the case of using a non-distribution promoting type structured packing as the packing (Example 2) is higher than the pressure loss in the case of using a self-promoting type structured packing (Comparative Example 2). Is also obviously small. Further, in Comparative Example 2, when the density corrected superficial superficial velocity becomes about 1.8 m / s (kg / m ³ ) ^1/2 or more, the pressure loss starts to increase sharply. Such a phenomenon did not occur even at the density corrected superficial velocity. From these test results, the distillation column of the type used in Example 2 can be designed to have a smaller column diameter than the type used in Comparative Example 2, and the cost required for manufacturing and constructing the apparatus can be kept low. It turns out that it becomes possible.

Next, a comparison was made between the liquid distribution with and without the precision distribution section in the distillation column. (Example 3) As an example in which a precision distribution section is provided in a distillation column, a chlorofluorocarbon having a viscosity similar to that of air is used as a fluid in the same manner as in Example 2 by using the distillation column of Example 2 shown in FIG. 11
Was used to observe the state of dispersion of the liquid under each condition. Also,
The video of the flow of the liquid in the tower and the state of liquid distribution were taken. (Comparative Example 3) As an example in which a precision distribution section is not provided in a distillation column,
A test similar to that of Example 3 was performed using the same distillation column as that used in Example 3 except that it did not have a precision distribution unit.

FIGS. 30 and 31 show a pressure of 130 kP.
a, Liquid load is 2m / s (kg / m ³ ) ^{1/2 in} gas load conversion
5 is a photograph of the state of fluid flowing down from the lower end of the non-promoting-dispersion type structured packing of the distillation columns of Example 3 and Comparative Example 3, respectively. According to FIG. 30, in the case where there is a precision distribution unit (Example 3), droplets are flowing down in a streak form from each flow path in which the packing is formed, and these droplets are uniformly distributed throughout the tower. Can be confirmed. On the other hand, when the precision distribution unit was not provided (Comparative Example 3)
FIG. 31 shows that the droplets are clearly biased, as shown in FIG.

[0073]

As described above, in the gas-liquid contact device according to the present invention, thin plates or tubes having various shapes that determine the flow direction of the liquid and gas are vertically stacked or arranged along the vertical direction. It comprises a non-distribution promoting type structured packing, and at least one liquid distributor, wherein the liquid distributor comprises a coarse distribution section for roughly distributing the liquid and a precision distribution section for precisely and evenly distributing the liquid. In the liquid distribution section, firstly, the descending liquid is uniformly dispersed throughout the tower section, and then the non-distribution promotion is performed by laminating or arranging thin plates or tubes in a shape that makes the flow vertical in the vertical direction. By performing gas-liquid contact in the regular packing layer, a sufficient ascending gas flow path is ensured, and the flow of the descending liquid on the packing surface is smooth and uniform throughout the top, bottom, left and right of the thin plate It is. That is, the entire surface of the packing is effectively used. For this reason, it is possible to suppress an increase in pressure loss due to an increase in flow resistance of the rising gas, prevent occurrence of flooding, secure a sufficient gas-liquid contact area, and perform efficient distillation. Therefore, the liquid load and the gas load can be set large. Further, the height of the tower can be designed to be low, and the cost required for manufacturing and constructing the device can be kept low. Furthermore, it is possible to greatly increase or decrease the production amount of the product.

[Brief description of the drawings]

FIG. 1 is a schematic configuration diagram of an air liquefaction / separation device using one embodiment of a gas-liquid contact device of the present invention.

FIG. 2 is a schematic configuration diagram showing an example of a gas-liquid contact device used in the air liquefaction / separation device shown in FIG.

FIG. 3 is a perspective view showing an example of a coarse distribution unit used in the gas-liquid contact device shown in FIG.

FIG. 4 is a perspective view showing another example of the coarse distribution unit used in the gas-liquid contact device shown in FIG.

FIG. 5 is a perspective view showing still another example of the coarse distribution section used in the gas-liquid contact device shown in FIG.

6 is a perspective view showing an example of a self-promoting-dispersion type structured packing used as a precision dispensing section in the gas-liquid contact device shown in FIG. 2;

FIG. 7 is a perspective view showing another example of a self-promoting-dispersion type structured packing used as a precision dispensing section in the gas-liquid contact device shown in FIG. 2;

8 is a front view showing still another example of the self-promoting-dispersion type structured packing used as a precision dispensing section in the gas-liquid contact device shown in FIG.

FIG. 9 is a sectional view of the self-promoting-fluid-dispersion type structured packing shown in FIG.

FIG. 10 is an explanatory diagram for explaining a method for producing the self-promoting-dispersion type structured packing shown in FIG. 8;

11 is a perspective view showing an example of a non-distribution promoting type structured packing used in the gas-liquid contact device shown in FIG.

FIG. 12 is a cross-sectional view showing the non-promoting-dispersion type structured packing shown in FIG. 11;

FIG. 13 is a perspective view showing a thin plate constituting the non-distribution promoting type structured packing shown in FIG. 11;

14 is a cross-sectional view showing another example of the non-distribution promoting type structured packing used in the gas-liquid contact device shown in FIG.

FIG. 15 is a sectional view showing still another example of the non-distribution promoting type structured packing used in the gas-liquid contact device shown in FIG. 2;

FIG. 16 is a cross-sectional view showing still another example of the non-distribution promoting type structured packing used in the gas-liquid contact device shown in FIG. 2;

FIG. 17 is a cross-sectional view showing still another example of the non-distribution promoting type structured packing used in the gas-liquid contact device shown in FIG. 2;

FIG. 18 is a cross-sectional view showing still another example of the non-distribution promoting type structured packing used in the gas-liquid contact device shown in FIG.

FIG. 19 is a cross-sectional view showing still another example of the non-distribution promoting type structured packing used in the gas-liquid contact device shown in FIG.

20 is a cross-sectional view showing still another example of the non-distribution promoting type structured packing used in the gas-liquid contact device shown in FIG.

21 is a cross-sectional view showing still another example of the non-distribution promoting type structured packing used in the gas-liquid contact device shown in FIG.

22 is a cross-sectional view showing still another example of the non-distribution promoting type structured packing used in the gas-liquid contact device shown in FIG.

FIG. 23 is a perspective view showing a modification of the non-distribution promoting type structured packing shown in FIGS.

24 is a perspective view showing a modification of the non-distribution promoting type structured packing shown in FIG.

FIG. 25 is a perspective view showing an example of a parallel plate group used in the gas-liquid contact device of the present invention.

FIG. 26 is a perspective view showing another example of the parallel flat plate group used in the gas-liquid contact device of the present invention.

FIG. 27 is a graph showing a result of simulating a distillation operation using the gas-liquid contact device shown in FIG. 2 as an example.

FIG. 28 is a diagram showing the internal structure of an example of the gas-liquid contact device of the present invention.

FIG. 29 is a graph showing experimental results, in which the horizontal axis represents the density-corrected superficial velocity, and the vertical axis represents the pressure loss per unit height.

FIG. 30 is a photograph of the fluid flowing down from the lower end of the packing when an example of the gas-liquid contact device of the present invention is used.

FIG. 31 is a photograph of the fluid flowing down from the lower end of the packing when the gas-liquid contact device of the comparative example is used.

[Explanation of symbols]

2 ... High pressure tower, 2a, 3a, 4a ... Gas-liquid contact device, 3 ...
・ Low pressure tower, 4 ・ ・ ・ Argon tower, 41, 51, 61 ・ ・ ・ Liquid disperser, 91, 101, 111, 121, 131, 14
1, 151, 161: non-distribution promoting type structured packing, 9
2, 102, 132, 152 ... thin plate, 96, 106,
116, 126, 166a, 166b...
..Pipes, A ₁ , A ₂ , A ₃ ...
B ₁ , B ₂ , B _3: precision distributing unit, C ₁ , C ₂ , C _3: coarse distributing unit, E ₁ , E _2: liquid distributor, 85, 86 ... parallel plate group

 ────────────────────────────────────────────────── ─── Continuing on the front page (72) Inventor Hiroshi Kawakami F-term in Nippon Oxide Co., Ltd. 1-16-7 Nishishinbashi, Minato-ku, Tokyo 4D047 AA08 AB01 AB02 AB04 DA06 DA12 EA00 4G075 AA03 BB05 BB07 BD13 CA02 CA03 CA05 DA01 EB09 EE02 EE12 EE22 EE32 EE33 EE34 EE36 FB02

Claims (18)

[Claims] 1. A gas-liquid contacting device for causing a liquid to flow down along the surface of a filling material and for bringing the liquid into contact with the gas while raising the gas, wherein the filling material has a vertical flow direction of the liquid and gas. Using non-promoting-type regular packing in which thin plates or tubes of various shapes to be formed are laminated or arranged along the vertical direction, a coarse distribution section for roughly distributing the liquid, and a precision for precisely and evenly distributing the liquid A gas-liquid contact device comprising at least one liquid distributor including a distributor. 2. The non-promoting-dispersion type structured packing having a specific surface area of 3
^2. The gas-liquid contact device according to claim 1, wherein the gas-liquid contact device is 50 m ² / m ³ or more. 3. The gas-liquid contact device according to claim 1, wherein the precision distributing section for precisely and evenly distributing the liquid is made of a self-promoting-dispersion type structured packing. 4. The precision dispensing unit for distributing the liquid precisely and evenly is characterized in that at least one self-promoting-fluid-dispersion type structured packing and a group of parallel flat plates are laminated in the column direction. The gas-liquid contact device according to claim 1. 5. The gas-liquid contact device according to claim 1, wherein the non-distribution promoting type structured packing comprises a group of thin metal plates or a group of metal tubes. 6. The gas-liquid contact device according to claim 1, wherein the non-distribution promoting type structured packing has a rectangular cross-sectional shape. 7. The gas-liquid contact device according to claim 1, wherein the cross-sectional shape of the non-distribution promoting type structured packing is triangular. 8. The gas-liquid contact device according to claim 1, wherein the cross-sectional shape of the non-distribution promoting type structured packing is a square such as a square, a rectangle, a trapezoid, or a rhombus. 9. The gas-liquid contact device according to claim 1, wherein the non-distribution promoting type structured packing has a hexagonal cross section. 10. The gas-liquid contact device according to claim 1, wherein the non-distribution promoting type structured packing comprises a wavy thin plate having a curved surface. 11. The method according to claim 1, wherein the non-distribution promoting structured packing forms a flow path having a cross-sectional shape of at least two of a triangle, a square, and a hexagon. Gas-liquid contact device. 12. The gas-liquid contact device according to claim 1, wherein the non-distribution promoting type structured packing is composed of a plurality of thin plates arranged via spacers. 13. The unevenness of the thin plate or the spacer,
The gas-liquid contact device according to any one of claims 1 to 12, wherein at least one of a groove and a hole is provided. 14. Under the non-distribution promoting structured packing,
The gas-liquid contact device according to any one of claims 1 to 13, wherein at least one steam distributor for distributing steam is provided. 15. The steam distributor according to claim 1, wherein the steam distributor is made of a self-promoting-dispersion type structured packing.
5. The gas-liquid contact device according to 4. 16. An air liquefaction separation device using the gas-liquid contact device according to claim 1. 17. A gas separation method for separating a component of a gas mixture composed of at least two components from other components using a gas-liquid contact device, wherein the gas-liquid contact device directs a flow of the mixture in a vertical direction. It has a non-promoting-fluid-dispersion type structured packing composed of thin plates or tubes of various shapes, and has a specific surface area of 350 m ² / m ³ or more. Under the pressure conditions described above, the gas mixture and the liquefied product thereof are brought into contact with the liquid while flowing the gas mixture and the liquefied product in the non-distribution promoting type structured packing opposite to each other along the surface of the packing. A gas separation method, wherein a load is set so that a density-corrected superficial velocity becomes 1.8 m / s (kg / m ³ ) ^1/2 or more. 18. A gas separation method for separating a component of a gas mixture comprising at least two components from other components using a gas-liquid contact device, wherein the gas-liquid contact device directs a flow of the mixture in a vertical direction. It has a non-promoting-fluid-dispersion type structured packing composed of thin plates or tubes of various shapes, and has a specific surface area of 350 m ² / m ³ or more of 0.4 to 2.0 MPa. Under the pressure conditions described above, the gas mixture and the liquefied product thereof are brought into contact with the liquid while flowing the gas mixture and the liquefied product in the non-distribution promoting type structured packing opposite to each other along the surface of the packing. A gas separation method comprising setting a load so that a density-corrected superficial velocity becomes 1.0 m / s (kg / m ³ ) ^1/2 or more.