JP3662710B2 - Mixing equipment - Google Patents

Description

【００２３】
粒体には、重質油からガソリンを製造する流動接触分解装置に使用されている触媒を用いた。この触媒の平均粒径は６３ミクロン、カサ比重は０．８５ｇ／ｃｍ³である。また、ノズルから噴射する流体は原料油の代わりに常温の空気を用いた。
実験条件は実装置において６００℃の触媒に原料油を噴射して混合・気化が完了した瞬間で、反応はまだ起こっていない状況を想定して設定した。この設定に基づく実験条件は触媒供給量が５０ｋｇ／ｍｉｎから３５０ｋｇ／ｍｉｎ、空気供給量は２０ｍ³／ｈから１２０ｍ³／ｈまで変化させた。さらに空気は２段目および３段目、４段目の３ヶ所から注入し、それらの割合を種々変化させた。混合状態の観察はビデオ撮影および目視により行った。
その結果を以下に示す。
（１）触媒等量供給室（分配器）からの触媒は７本のスタンドパイプ（配管）にほぼ均等に流れることを確認した。
（２）トレイからの空気を供給しないで触媒等量供給室の分散用空気のみで触媒を落下させても２段の分散板の効果により、かなり良好な分散状態が得られた。
（３）トレイからの全空気供給量は多いほど分散状態は良くなる。
（４）全空気供給量一定においては４段目トレイから水平方向に噴射する空気量の割合を増加すると、それに伴い混合状態は良くなる。
【００２４】
（実施例２）
混合装置は図４に示す形態の二次元モデルを用い、透明塩ビで製作した。各部の寸法を実施例１のものと同一であるが厚みは１ｃｍである。
触媒供給量および空気供給量は実施例１とのモデルの断面積比から実施例１の１／１５とした。混合状態の観察は実施例１と同様にビデオ撮影および目視により行った。
その結果を以下に示す。
（１）触媒等量供給室からの触媒は７本のスタンドパイプにほぼ均等に流れることは実施例１と同様であった。但し、触媒等量供給室の流動層の液面からスタンドパイプに流れ込んだ触媒は触媒量が少ない場合にはスタンドパイプの外側に多く流れる傾向を示した。
（２）トレイからの空気を供給しないで触媒等量供給室の分散用空気にみで触媒を落下させた場合には２段の分散板の効果はあるものの分散状態は十分ではなかった。トレイからの空気供給量を増加すると、それに伴い混合状態は非常に良くなる。
（３）全空気供給量一定においては４段目トレイから水平方向に噴出する空気量の割合を増加すると、実施例１と同様に混合状態は良くなる。
（４）スタンドパイプからの触媒は分散板の上に落下するが、落下した触媒は分散板に２０度前後の安息角を持つ山型を形成する。本モデルの分散板は浅い皿型であり皿の内部に溜まった触媒はスタンドパイプから落下してくる触媒のクッションになっており衝撃がやわらいでいることが確認された。この現象はエロージョンに対して有利となる。
【００２５】
【発明の効果】
以上要するに本発明によれば、液体と固体粒子からなる粒体を迅速に均一混合することができる。
【図面の簡単な説明】
【図１】本発明の混合装置の一例を示す概略図である。
【図２】図１中のＡ−Ａ線矢視断面図である。
【図３】図１中のＢ−Ｂ線矢視断面図である。
【図４】本発明の混合器の要部を示す概略図である。
【図５】図４中のＣ−Ｃ線矢視断面図である。
【符号の説明】
１ 混合装置
２ 配管
３ 粒体分配器
４ 混合器
５ 分散板
６ 液体供給部[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a mixing apparatus for mixing a fluid such as heavy oil and high-temperature particles such as a catalyst for vaporizing the heavy oil.
[0002]
[Prior art]
Reaction systems in which a particulate solid is used as a catalyst or a heat medium and brought into contact with a reactant have been known for a long time. Among such reaction systems, some fluidized bed reactors use, for example, a dense fluidized bed (bubble fluidized bed) and a high speed moving bed (high speed fluidized bed). Among these, a high-speed moving bed is used for reactions that require a shorter contact time between the solid and the gas (short contact time reactions). Currently, an upflow type high-speed moving bed reactor called a riser is mainly used in a fluid catalytic cracking apparatus for producing gasoline using heavy oil or the like as a raw material oil. With this reactor, the contact time can be shortened with the improvement of the catalyst performance, thereby increasing the selectivity of a preferable product such as gasoline and suppressing an undesirable overdecomposition reaction.
[0003]
[Problems to be solved by the invention]
In recent years, there has been a demand for further improvement of gasoline selectivity or light olefin selectivity, and the back-mixing phenomenon of the catalyst, which is a characteristic of the upflow type high-speed moving bed reactor, is the selectivity. Since it has an adverse effect on the improvement, down-flow type high-speed moving bed reactors that do not cause backmixing phenomenon are being studied.
The catalytic reaction time in a fluid catalytic cracker that uses existing upflow high-speed moving bed reactors to produce gasoline from heavy oil and other raw materials is several seconds, but it is a catalytic reaction for light olefins. It is necessary to shorten the time to about 0.1 to 1.5 seconds. In order to perform such a short contact time reaction, it is indispensable to quickly mix and vaporize the raw material oil and the catalyst at the reactor inlet. Furthermore, the catalyst circulation rate must be increased in order to compensate for the decrease in the conversion rate accompanying the shortening of the reaction time. Against this background, raw material oil and catalyst can be quickly mixed and vaporized at the reactor inlet, and gasoline is produced using heavy oil, etc. as raw material oil that has an existing upward flow type high-speed moving bed reactor. There is a demand for a feedstock / catalyst supply and mixing device that enables a catalyst circulation amount several times the catalyst circulation amount (cat / oil ratio 5 to 8) of the fluid catalytic cracking device.
Therefore, the present invention has been made in view of such circumstances, and an object of the present invention is to provide a mixing apparatus that can rapidly and uniformly mix particles composed of liquid and solid particles.
[0004]
[Means for Solving the Problems]
In order to achieve the above object, the mixing device of the present invention is a device that mixes liquid such as heavy oil and particles such as a catalyst that vaporizes the heavy oil, and the particles are arranged along the direction of gravity. A granular distributor that evenly distributes to a plurality of extending pipes, and below the granular distributor, the plurality of pipes extend through the upper part to the upper part inside, and the granular bodies extend from these pipes. Is provided with a mixer that drops inside, a dispersion plate that disperses particles falling from the pipe radially outward is provided inside the mixer and below each pipe. The liquid is sprayed on the outer periphery of the plurality of pipes in the vicinity of the outer periphery of the particle group falling from the pipes from the entire circumferential direction downward in the gravitational direction, and the particles dispersed by the dispersion plate are ejected. The liquid supply part which collides with the made liquid is provided.
[0005]
Further, the mixing device of the present invention is a device that mixes a fluid such as heavy oil and particles such as a catalyst that vaporizes the heavy oil, and a plurality of the particles extending along the direction of gravity. A granule distributor that distributes evenly to the pipes is provided, and below the granule distributor, the plurality of pipes extend through the upper part to the upper part inside, and the particles fall from the pipes to the inside. A dispersion plate that disperses the particles falling from the pipes radially outward is disposed inside the mixer and below each pipe, and the mixer drops from the pipe to the inside of the mixer. The liquid supply part which injects the said fluid over the circumferential direction whole area is provided in the outer periphery of the granular material group to perform.
[0006]
It is preferable that the fluid supply unit is an injector that injects a liquid using an injection medium such as steam or air. In addition, the liquid is at a high temperature of 300 ° C. or higher, and heat insulating means is provided in the fluid supply unit so as to surround the fluid supply unit in order to prevent the thermal effect of the high-temperature particles on the fluid to be ejected. preferable. Further, a dispersion plate that further disperses particles dispersed from the dispersion plates and falling below the dispersion plates inside the mixer may be provided at least at locations where the drop density of the particles is high. preferable.
[0007]
By the way, in order to carry out a short contact time reaction, it is indispensable to rapidly mix and vaporize, for example, raw material oil and granules (catalyst) at the reactor inlet. For that purpose, it is a precondition that the raw material oil is made into fine droplets (a sprayed body) and that the particles composed of the solid particles as a catalyst are uniformly dispersed. Next, uniform mixing with the spray body must take place. This uniform mixing is possible if there is a wide space, but it cannot be performed sufficiently in a limited space. For this reason, as a result of research and development to obtain alternative means, the following conclusions were reached.
In other words, the droplets are refined to some extent by an injection nozzle or the like, and then the ejector is made to collide with the particles, and further refined by the impact force, and at the same time, uniformly mixed with the particles. .
[0008]
Therefore, the fluid is evenly distributed to the plurality of pipes, the particles falling from these pipes are dispersed by the dispersion plate, the dispersed particles collide with the injected liquid, and the liquid is further refined. Therefore, the solid-liquid contact can be efficiently performed, and the mixing of the particles and the liquid can be performed quickly and almost uniformly.
[0009]
DETAILED DESCRIPTION OF THE INVENTION
Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings.
In FIG. 1, reference numeral 1 denotes a mixing apparatus that mixes a fluid such as heavy oil and particles such as a catalyst that vaporizes the heavy oil.
This mixing apparatus 1 is provided with a particle distributor 3 that evenly distributes the particles to a plurality of pipes 2 extending along the direction of gravity, and the plurality of pipes below the particle distributor 3. 2 extends through the upper part to the upper part of the interior, and a mixer 4 is provided in which the particles fall from the pipes 2. Inside the mixer 4 and below the pipe 2, Dispersion plate 5 that disperses the falling particles radially outward is provided, and a fluid such as heavy oil or other fluid is injected into mixer 4 to mix the particles and liquid. The fluid supply part 6 to be provided is mainly provided.
[0010]
The particle distributor 3 may be configured in any way as long as it can distribute particles evenly to the plurality of pipes (stand pipes) 2. For example, in the example shown in FIG. 1, a fluidized bed is used. Is.
The fluidized bed furnace (catalyst equal amount supply chamber) 7 constituting the particle distributor 3 is formed in a vertical cross-sectional circular shape, a polygonal shape, a rectangular shape, etc., and in the illustrated example, it is formed in a cylindrical shape. Dispersers such as a perforated plate type disperser and a pipe grid type disperser, for example, a perforated plate 8 are provided below. Supply for supplying high-temperature particles (for example, high-temperature (450-700 ° C.) silica alumina catalyst particles having a solid particle diameter of 1 to 500 μm) onto the fluidized-bed dispersion plate 8 on the sidewall of the fluidized bed furnace 7. A tube 9 is connected. A fluidized gas supply pipe 10 is connected to the lower part of the fluidized bed furnace 7, and a fluid gas such as steam, air, or inert gas is supplied into the furnace 7 through the perforated plate 8, and the particles are fluidized. Thus, a fluidized bed 11 of granules is formed. A plurality of pipes 2 extending along the direction of gravity pass through the bottom of the fluidized bed furnace 7, and the tips of these pipes 2 further penetrate the perforated plate 8 and extend to the inner center of the fluidized bed furnace 7. Yes.
The number of these pipes 2 is not particularly limited, but preferably 3 to 30, and more preferably 3 to 7. The pipes 2 are arranged almost uniformly in the fluidized bed furnace 7. For example, as shown in FIG. 2, when there are seven pipes 2, six pipes are arranged at a predetermined interval (60 °) in the circumferential direction, and the remaining one pipe is arranged at the center. The diameter (diameter) of the pipe 2 is arbitrarily determined depending on the supply amount of particles, etc., but the diameter is increased when the supply amount of particles is large under the condition that the diameter of the reaction tube 12 and the number of the pipes 2 are constant. On the contrary, if it is small, it is of course possible to make it small. The cat / oil ratio of the catalyst circulation rate is preferably 5 to 50, more preferably 20 to 30. If the cat / oil ratio is less than 5, for example, the contact time between the catalyst and the feedstock oil is short, that is, the reaction cannot be performed sufficiently, and if it exceeds 50, problems such as pressure loss and erosion may occur.
[0011]
A mixer 4 is disposed below the fluidized bed furnace 7. The plurality of pipes 2 penetrate through the upper part of the mixer 4, and the lower ends of the pipes 2 extend upward in the interior. The fluid falls from the bottom to the bottom. The mixer (raw material catalyst mixing chamber) 4 is formed in, for example, a bowl-shaped cylindrical shape, and a reaction tube (vertical downflow reaction tube) 12 having the same diameter as the mixer 4 is connected to the lower part thereof.
Dispersing plates 5 for dispersing particles falling from the pipes 2 radially outward are provided at the center of the mixer 4 and below the pipes 2. These dispersing plates 5 may be any one that is arranged on the same horizontal plane and disperses the falling particles radially outward, for example, a circle having a diameter equal to or larger than the diameter of the lower end of the pipe 2. A plate, a disc whose central portion is recessed below the outer peripheral edge, a dish-like disc, a cone, and the like.
Below these dispersion plates 5, a plurality of dispersion plates 13 are provided on the same horizontal plane to further disperse particles dispersed from the dispersion plate 5 and falling downward. The dispersive plates 13 are arranged at least at locations where the drop density of the granules is high. For example, it is provided at a position corresponding to between the upper dispersion plates 5. These lower dispersion plates 13 may be the same as or different from the upper dispersion plate 5. Although the number of stages of the dispersion plates 5 and 13 is set to two in the illustrated example, the number of stages is not particularly limited. However, if the number of stages is too large, the mixing efficiency increases, but conversely the pressure loss increases. It is desirable to use steps.
[0012]
A fluid supply unit 6 for injecting a fluid such as raw oil such as heavy oil is provided on the outer peripheral portion of the pipe 2 in the mixer 4. The fluid supply unit 6 injects the fluid so as to surround the entire outer periphery of the particle group (for example, a columnar fluid group) falling from the pipe 2, and if it is injected in this way, how is it configured? May be. The injection angle is 0 ° (parallel to the horizontal direction) to 90 ° (lower in the direction of gravity), 90 ° in the example of FIG. 1 and 0 ° in FIG. That is, the fluid supply unit 6 shown in FIG. 1 ejects liquid from the entire circumference in the vicinity of the particles falling from the pipes 2 downward in the gravitational direction, and is dispersed by the dispersion plates 5 and 13. It is comprised so that the granulated body and the jet liquid may collide.
[0013]
The fluid supply unit 6 shown in FIG. 4 is ejected at an ejection angle of 0 °, that is, parallel to a horizontal plane, and ejects a fluid, for example, a liquid using a spray medium (gas, steam, etc.). An example of an injection nozzle is shown.
As shown in FIG. 4, the fluid supply unit 6 is also provided with a heat insulating means 14. Between the upper pipes 2 in the mixer 4 and between the pipes 2 and the inner wall of the mixer, a heat insulating steam tray 15, a spray steam tray 16, and a feed oil tray 17 are stacked from above so as to be stacked along the direction of gravity. An insulating spray steam tray 18 is provided. The plurality of pipes 2 have a structure that penetrates these trays 15, 16, 17, and 18. A cylindrical space (clearance) 19 is provided along the axial direction so as to surround the pipe 2 on the outer periphery of the pipe 2, and the upper portion of the space 19 communicates with the heat insulating steam tray 15. Insulation steam flows downward along the pipe 2 to insulate the high-temperature pipe 2 from the raw material oil.
A heat insulating partition plate 20 that extends in the horizontal direction is provided below the heat insulating spray steam tray 18 (a position that is also below the lower end portion of the pipe 2). The partition plate 20 faces the lower end of the pipe 2. It is formed as follows. That is, the partition plate 20 is a disc provided with a circular opening (an opening through which particles from the pipe 2 can pass) in a portion corresponding to the pipe 2. A clearance 21 is provided between the partition plate 20 and the adiabatic spray steam tray 18, and steam from the adiabatic spray steam tray 18 flows radially inward through the clearance 21, so that the inside of the high-temperature mixer 4 and the raw oil Insulation with is to be performed. The heat insulation means 14 is comprised by this heat insulation and the said heat insulation. The heat insulating means 14 may be configured in any way as long as the raw material oil can be insulated from the high-temperature pipe 2 or the like.
[0014]
On the outer periphery of the clearance 19 provided on the outer periphery of the pipe 2, a cylindrical raw material oil (liquid) spray chamber 22 is provided along the axial direction so as to surround the clearance 19. The upper part of the spray chamber 22 communicates with the spray steam tray 16 so that steam as a spray medium flows in the spray chamber 22 from the upper side to the lower side at a high speed. A large number of injection nozzles (injection holes) 23 are provided on the side wall of the spray chamber 22 with the raw material oil tray 17 so that the raw material oil is injected from the raw material oil tray 17 into the spray chamber 22 and mixed with steam. The raw material oil collides with the partition plate 21 and becomes a spray body, and this spray body is sprayed on the outer periphery of the granule from the pipe 2 in parallel to the horizontal direction over the entire circumferential direction. . The spray angle of the spray body is 0 ° (parallel to the horizontal direction) to 90 ° (downward in the direction of gravity), preferably 0 ° to 45 °, and can be changed by changing the angle of the partition plate 21. In the illustrated example, the spray angle is 0 °. Further, as shown in FIG. 5, a plurality of injection nozzles 23 are disposed on the side wall at predetermined intervals in the circumferential direction so that the raw material oil is sprayed over the entire spray chamber, and the number of spray nozzles 23 is sprayed. If raw material oil is sprayed on the whole chamber 22, it will be decided arbitrarily. The number of stages of the injection nozzle 23, that is, the number of stages provided at a predetermined interval in the height direction (two stages in the illustrated example) is not particularly limited, but is preferably 1 to 6 stages, and more preferably 1 to 3.
[0015]
Now, a case where raw material oil (heavy oil) and high-temperature (450 to 700 ° C.) silica-alumina catalyst particles are mixed using the mixing apparatus 1 will be described.
The catalyst particles are continuously supplied from the supply pipe 9 onto the perforated plate 8 in the fluidized bed furnace 7, where they are fluidized by a fluid gas to form a fluidized bed 11 of catalyst particles. By forming the fluidized bed 11 as described above, even if excessive particles are supplied to a part, the particles are dispersed in a small part while fluidizing, and the horizontal particle density is made uniform.
When the bed height of the fluidized bed 11 increases, some of the particles overflow the upper end of the pipe 2 and overflow into the respective pipes 2 from the entire circumferential direction. Thus, when the density of the particles in the horizontal direction becomes uniform and the bed height of the fluidized bed 11 rises in this state, almost equal amounts of particles flow into each pipe 2. The particles will be distributed uniformly.
[0016]
The particles that have entered the pipe 2 fall down in the pipe 2 and reach the mixer 4 from the lower end opening of the pipe 2.
In the mixer 4, the particles from the pipe 2 fall below it. Since the dropping is continuously performed, although depending on the amount of particles, it falls in a substantially cylindrical shape, and almost all of the dropped particles hit the dispersion plate 5 and are dispersed radially outward. For example, when the dispersion plate 5 is a disk or a dish, as shown by a dotted line in FIG. 4, the dispersion plate 5 has a mountain (conical shape) having an angle of repose of, for example, about 20 degrees, on which particles are formed. When dropped, the particles move radially outward on the mountain slope. Further, when a disc or a dish whose central portion is recessed below the outer peripheral edge portion is used as the dispersion plate 5, the catalyst particles accumulated at the center of the dispersion plate serve as a cushion for the falling catalyst, and the impact of the drop is exerted. Since it becomes soft, it is advantageous to erosion.
Thus, since the particles are dropped from the plurality of pipes 2 and dispersed in the radial direction by the dispersion plate 5 corresponding to each pipe, the particles can be dispersed well.
[0017]
On the other hand, in the case shown in FIG. 1, the raw material oil is injected from the fluid supply unit 6 in the vicinity of the outer periphery of the particle group falling from the pipe 2 and downward in the gravitational direction from the entire circumferential direction. At this time, since the fluid supply unit 6 is provided with a heat insulating means 14 as shown in FIG. 4, the injected raw material oil is insulated from the heat of the catalyst particles at a high temperature (450 to 700 ° C.). The oil is injected without caulking.
In this way, the raw material oil is injected so as to surround the outer periphery of the falling particle group, so that the particles collide with the dispersion plate 5 and are dispersed radially outward to collide with the heavy oil. Since the heavy oil is further refined and scattered, the dispersion of the raw material oil is improved. Thereby, mixing of particle | grains and raw material oil can be performed almost uniformly rapidly. Further, the contact efficiency between the particles and the raw material oil is improved, and the raw material oil can be sufficiently vaporized. Further, when the dispersion plates 5 and 13 are provided in a plurality of stages, the particles are dispersed again, and the dispersed particles and heavy oil collide (contact), so that the contact efficiency between the particles and heavy oil is improved. In addition to the improvement, the mixing of particles and heavy oil becomes even better. Then, the mixture moves downward in the reaction tube 12.
[0018]
When the fluid supply unit 6 is configured as shown in FIG. 4, steam from the spray steam tray 16 flows into the spray chamber 22 and flows from the top to the bottom at high speed. The raw material oil is injected from the injection nozzle 23 into the spray chamber 22 through the raw material oil tray 17 and mixed with the steam, which collides with the heat insulating partition plate 21 and becomes the spray body. The spray body is sprayed along with the steam from the heat insulating / spraying steam tray 18 on the outer periphery of the granule from the pipe 2 in parallel in the horizontal direction over the entire circumferential direction. That is, the raw material oil is sprayed on the catalyst particle group (cylindrical particles) falling from the pipe 2 at a right angle to the dropping direction.
The sprayed raw material oil collides with the particles, becomes finer, scatters in the vicinity of the outer periphery of the falling particles, and falls downward. Then, the particles are dispersed radially outward by the dispersion plate 5 and collide with the refined raw material oil, and the raw material oil is further refined and scattered, so that the dispersion of the raw material oil is further improved. Further, the contact efficiency between the particles and the heavy oil is further improved. Further, when a gas (steam) is injected together with the raw material oil, the steam promotes the diffusion of the particles, so that the dispersed state of the particles becomes even better.
[0019]
Accordingly, the catalyst particles are evenly distributed to the plurality of pipes 2 and the particles falling from the pipes 2 are dispersed by the dispersion plate 5 and the dispersed particles collide with the raw material oil, so that the raw material oil is refined and scattered. In addition, the mixing of the particles and the raw material oil can be performed quickly and almost uniformly, and the catalyst particles and the raw material oil can be efficiently contacted. Further, the catalyst particles are evenly distributed to the plurality of pipes 2, the particles of each pipe 2 are dispersed and the particles and heavy oil are mixed, and the mixing of the particles and the raw material oil is performed quickly and substantially uniformly. The present invention can also be applied when the proportion of particles is large (particle weight / liquid weight up to 50).
Furthermore, since the short contact time reaction can be performed in a shorter time and the reaction can be made uniform, for example, the contact reaction time can be shortened to about 0.1 to 1.5 seconds. Thereby, when manufacturing gasoline, it is possible to further suppress an unfavorable overdecomposition reaction, and it is possible to manufacture gasoline with higher quality.
As a result, the mixing apparatus of the present invention has an existing upward flow type high-speed moving bed reactor and has a catalyst circulation rate (cat / oil ratio of 5) of a fluid catalytic cracking apparatus that manufactures gasoline using heavy oil or the like as a feedstock. Cat / oil ratio up to 50 with a catalyst circulation amount several times that of ~ 8) is possible.
[0020]
【Example】
Examples of the present invention will be described below, but the present invention is not limited thereto.
[0021]
(Example 1)
A mixing apparatus having the form shown in FIG. 4 was used, and the mixing apparatus was made of transparent PVC. The main dimensions are shown in Table 1.
[0022]
[Table 1]

[0023]
As the granule, a catalyst used in a fluid catalytic cracking apparatus for producing gasoline from heavy oil was used. This catalyst has an average particle size of 63 microns and a specific gravity of 0.85 g / cm ³ . The fluid ejected from the nozzle was air at normal temperature instead of raw material oil.
The experimental conditions were set on the assumption that the reaction had not yet occurred at the moment when the raw material oil was injected into the catalyst at 600 ° C. in the actual apparatus and mixing and vaporization were completed. The experimental conditions based on this setting were such that the catalyst supply rate was changed from 50 kg / min to 350 kg / min, and the air supply rate was changed from 20 m ³ / h to 120 m ³ / h. Furthermore, air was injected from three places, the second stage, the third stage, and the fourth stage, and their ratios were variously changed. The mixed state was observed by video shooting and visual observation.
The results are shown below.
(1) It was confirmed that the catalyst from the catalyst equivalent supply chamber (distributor) flows almost evenly into the seven stand pipes (piping).
(2) Even if the catalyst was dropped only with the dispersion air in the catalyst equivalent supply chamber without supplying air from the tray, a fairly good dispersion state was obtained due to the effect of the two-stage dispersion plate.
(3) The greater the total air supply from the tray, the better the dispersion state.
(4) If the total air supply amount is constant, increasing the ratio of the amount of air sprayed horizontally from the fourth tray will improve the mixing state.
[0024]
(Example 2)
The mixing apparatus was made of transparent PVC using a two-dimensional model having the form shown in FIG. The dimensions of each part are the same as those in Example 1, but the thickness is 1 cm.
The catalyst supply amount and the air supply amount were set to 1/15 of Example 1 from the cross-sectional area ratio of the model with Example 1. The mixed state was observed by video shooting and visual observation in the same manner as in Example 1.
The results are shown below.
(1) The catalyst from the catalyst equivalent supply chamber flowed almost evenly through the seven stand pipes as in Example 1. However, the catalyst which flowed into the stand pipe from the fluid surface of the fluid bed of the catalyst equal amount supply chamber tended to flow largely outside the stand pipe when the catalyst amount was small.
(2) When the catalyst was dropped only by the dispersion air in the catalyst equivalent supply chamber without supplying air from the tray, the dispersion state was not sufficient although the effect of the two-stage dispersion plate was obtained. As the amount of air supplied from the tray is increased, the mixing state becomes very good accordingly.
(3) When the total air supply amount is constant, if the ratio of the amount of air ejected horizontally from the fourth tray is increased, the mixed state is improved as in the first embodiment.
(4) The catalyst from the standpipe falls on the dispersion plate, but the dropped catalyst forms a mountain shape having an angle of repose of about 20 degrees on the dispersion plate. The dispersion plate of this model was a shallow dish type, and the catalyst accumulated inside the dish was a cushion of the catalyst falling from the stand pipe, and it was confirmed that the impact was soft. This phenomenon is advantageous for erosion.
[0025]
【The invention's effect】
In short, according to the present invention, particles composed of liquid and solid particles can be rapidly and uniformly mixed.
[Brief description of the drawings]
FIG. 1 is a schematic view showing an example of a mixing apparatus of the present invention.
FIG. 2 is a cross-sectional view taken along line AA in FIG.
3 is a cross-sectional view taken along line BB in FIG.
FIG. 4 is a schematic view showing a main part of the mixer of the present invention.
5 is a cross-sectional view taken along the line CC in FIG.
[Explanation of symbols]
DESCRIPTION OF SYMBOLS 1 Mixing apparatus 2 Piping 3 Granule distributor 4 Mixer 5 Dispersion plate 6 Liquid supply part

Claims (5)

In an apparatus for mixing a liquid such as heavy oil and particles such as a catalyst for vaporizing the heavy oil,
A granule distributor is provided for evenly distributing the granules into a plurality of pipes extending in the direction of gravity, and the plurality of pipes pass through the upper part below the granule distributor and are internally upward. And a dispersion plate that disperses the particles falling from the pipe radially outwardly inside the mixer and below each pipe. And, on the outer periphery of the plurality of pipes in the mixer, in the vicinity of the outer periphery of the particle group falling from the pipes, and spraying the liquid from the entire circumferential direction downward in the gravitational direction, A mixing apparatus comprising a liquid supply unit that collides the particles dispersed by the dispersion plate with the jetted liquid. In an apparatus for mixing a fluid such as heavy oil and particles such as a catalyst for vaporizing the heavy oil,
A granule distributor is provided for evenly distributing the granules into a plurality of pipes extending in the direction of gravity, and the plurality of pipes pass through the upper part below the granule distributor and are internally upward. And a dispersion plate that disperses the particles falling from the pipe radially outwardly inside the mixer and below each pipe. A mixing apparatus, characterized in that a liquid supply unit for ejecting the fluid over the entire circumferential direction is provided on the outer periphery of a particle group falling from a pipe inside the mixer. The apparatus according to claim 1, wherein the fluid supply unit is an injector that injects a liquid using an injection medium such as steam or air. The granule is at a high temperature of 300 ° C. or higher, and the fluid supply unit is provided with a heat insulating means so as to surround the fluid supply unit so as to prevent a thermal effect of the high temperature granule on the fluid to be ejected. Item 4. The apparatus according to any one of Items 1 to 3. A dispersion plate that further disperses particles dispersed from the dispersion plates and falling downwardly inside the mixer and below the dispersion plates is provided at least at locations where the drop density of the particles is high. The apparatus according to any one of 1 to 4.

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