CN118718903A - Multilayer fluidized bed reactor - Google Patents
Multilayer fluidized bed reactor Download PDFInfo
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- CN118718903A CN118718903A CN202411226628.3A CN202411226628A CN118718903A CN 118718903 A CN118718903 A CN 118718903A CN 202411226628 A CN202411226628 A CN 202411226628A CN 118718903 A CN118718903 A CN 118718903A
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Abstract
The application relates to the technical field of fluidized beds, in particular to a multi-layer fluidized bed reactor, which comprises: the cylinder body is cylindrical; the inside of the cylinder is divided into a reaction chamber and a gas supply chamber by a wind distribution plate; air holes are uniformly distributed on the air distribution plate; the reaction chamber is divided into a first layer of reaction chamber and a second layer of reaction chamber by the horizontal baffle plate, the first layer of reaction chamber is divided into a plurality of reaction chambers by the first vertical baffle plate, and the second layer of reaction chamber is divided into a plurality of reaction chambers by the second vertical baffle plate; the air supply cavities are in one-to-one correspondence with the reaction cavities in one layer of reaction chamber. Each reaction cavity in the one-layer reaction chamber can be used as a loosening chamber and a fluidization chamber in turn, and the air supply cavity corresponds to the reaction cavity in the one-layer reaction chamber one by one, so that the air speed of each reaction cavity can be conveniently and independently controlled, the material can be controlled to alternately pass through the loosening chamber and the fluidization chamber, and the technical problem that a fluidization dead zone is easy to form in certain areas of a general fluidized bed reactor, and the fluidized bed reactor cannot normally run is solved.
Description
Technical Field
The application relates to the technical field of fluidized beds, in particular to a multi-layer fluidized bed reactor.
Background
The fluidized bed reactor is an important chemical equipment, uses gas to make solid particles in suspension motion state by means of granular solid layer, and makes gas-solid phase reaction process, after completing a reaction period, the produced product is transferred into the following treatment unit in gas phase form. The fluidized bed reactor can realize continuous input and output of solid materials.
In a general fluidized bed reactor, a reaction chamber is divided into a plurality of reaction chambers by a baffle plate, materials enter from one end of the reaction chamber and are discharged from the other end of the reaction chamber through each chamber, so that the reaction time is increased, and the reaction rate is improved.
However, after a general fluidized bed reactor is operated for a certain time, the accumulation of materials in each chamber is increased, so that a fluidization dead zone is formed in certain areas, the fluidized bed reactor cannot normally operate, the reaction conversion rate is low, and the production cost is increased.
Disclosure of Invention
The application aims to at least solve one of the technical problems that after a general fluidized bed reactor is operated for a certain time, the fluidized dead zone is formed in certain areas due to the fact that materials in each chamber are accumulated and increased, the fluidized bed reactor cannot be operated normally, the reaction conversion rate is low, and the production cost is increased.
Therefore, the application provides a multilayer fluidized bed reactor, wherein each reaction cavity in one layer of reaction chamber can be used as a loosening chamber and a fluidization chamber alternately, and an air supply cavity corresponds to each reaction cavity in one layer of reaction chamber one by one, so that the air speed of each reaction cavity can be conveniently and independently controlled, the material can be controlled to alternately pass through the loosening chamber and the fluidization chamber, the accumulation of the material in each chamber is avoided, and the technical problems that a fluidization dead zone is easy to form in certain areas of a general fluidized bed reactor, and the fluidized bed reactor cannot normally operate are solved.
According to an embodiment of the present application, there is provided a multi-layered fluidized bed reactor including: the cylinder body is cylindrical; the inside of the cylinder is divided into a reaction chamber and a gas supply chamber by a wind distribution plate; air holes are uniformly distributed on the air distribution plate; the reaction chamber is divided into a first layer of reaction chamber and a second layer of reaction chamber by the horizontal baffle, the first layer of reaction chamber is divided into a plurality of reaction chambers by the first vertical baffle, the second layer of reaction chamber is divided into a plurality of reaction chambers by the second vertical baffle, and the reaction chambers are sequentially communicated from the first layer of reaction chamber to the second layer of reaction chamber; the material inlet is arranged on the side wall of the first reaction cavity of the first layer of reaction chamber, and the material outlet is arranged on the side wall of the last reaction cavity of the second layer of reaction chamber; the air supply chamber is divided into a plurality of air supply chambers by a third vertical baffle, and the positions of the air supply chambers are in one-to-one correspondence with the reaction chambers in one layer of reaction chamber; the gas inlets are respectively communicated with the gas supply cavity.
Alternatively, the height of the first layer of reaction chambers is the same as the height of the second layer of reaction chambers.
Optionally, the aperture ratio of the air holes on the air distribution plate is 6% -16%, and the thickness of the air distribution plate is 1-5 mm.
Optionally, the first vertical baffle and the second vertical baffle are respectively provided with a communication notch, the communication notches are arranged in a staggered way up and down, and the communication notch is used for communicating the reaction cavity.
Optionally, the ratio of the height of the communicating gap to the height of the reaction cavity is 0.2-0.35.
Optionally, the material inlet and the material outlet are on an extension line of the diameter of the same cylinder.
Optionally, the material inlet and the material outlet are cylindrical, the diameters of the material inlet and the material outlet are equal, and the ratio of the diameter of the material inlet to the diameter of the cylinder is 0.1-0.3.
Optionally, a layer of reaction chamber is uniformly divided into 4 reaction chambers by 2 first vertical baffles which are orthogonally arranged, wherein the 4 reaction chambers are respectively a reaction chamber I, a reaction chamber II, a reaction chamber III and a reaction chamber IV; the two-layer reaction chamber is uniformly divided into 4 reaction chambers by 2 second vertical baffles which are orthogonally arranged, namely a V-shaped reaction chamber, a VI-shaped reaction chamber, a VII-shaped reaction chamber and a VIII-shaped reaction chamber; the reaction chamber I, the reaction chamber II, the reaction chamber III, the reaction chamber IV, the reaction chamber V, the reaction chamber VI, the reaction chamber VII and the reaction chamber VIII are communicated in sequence; the material inlet is arranged on the side wall of the No. I reaction cavity, and the material outlet is arranged on the side wall of the No. VIII reaction cavity.
Optionally, the air supply chamber is evenly divided into 4 air supply chambers by 2 third vertical baffles that the quadrature set up, and the position of air supply chamber respectively with I No. reaction chamber, II No. reaction chamber, III No. reaction chamber, IV No. reaction chamber one-to-one.
Optionally, the material inlet is positioned at the middle position of the outer circumference of the No. I reaction chamber in the horizontal direction, and the material inlet is positioned at the top of the No. I reaction chamber in the vertical direction; the material outlet is positioned at the middle position of the outer circumference of the VIII-type reaction cavity in the horizontal direction, and the material outlet is positioned at the bottom of the VIII-type reaction cavity in the vertical direction.
One of the above technical solutions has at least the following advantages or beneficial effects:
The present application provides a multi-layered fluidized bed reactor comprising: the cylinder body is cylindrical; the inside of the cylinder is divided into a reaction chamber and a gas supply chamber by a wind distribution plate; air holes are uniformly distributed on the air distribution plate; the reaction chamber is divided into a first layer of reaction chamber and a second layer of reaction chamber by the horizontal baffle, the first layer of reaction chamber is divided into a plurality of reaction chambers by the first vertical baffle, the second layer of reaction chamber is divided into a plurality of reaction chambers by the second vertical baffle, and the reaction chambers are sequentially communicated from the first layer of reaction chamber to the second layer of reaction chamber; the material inlet is arranged on the side wall of the first reaction cavity of the first layer of reaction chamber, and the material outlet is arranged on the side wall of the last reaction cavity of the second layer of reaction chamber; the air supply chamber is divided into a plurality of air supply chambers by a third vertical baffle, and the positions of the air supply chambers are in one-to-one correspondence with the reaction chambers in one layer of reaction chamber; the gas inlets are respectively communicated with the gas supply cavity. Each reaction chamber in the one deck reaction chamber can be used as loosening chamber, fluidization chamber in proper order, and the air feed chamber corresponds with the reaction chamber one-to-one in the one deck reaction chamber, and the gas velocity of each reaction chamber of convenient individual control can control the material and pass through in the loosening chamber with the fluidization chamber in turn, has avoided the material to produce in each cavity to cumulate and has increased, has solved general fluidized bed reactor and has formed the fluidization dead zone in some regions easily, the unable normal operating technical problem of fluidized bed reactor.
Drawings
In order to more clearly illustrate the technical solution of the present application, the drawings that are needed in the embodiments will be briefly described below, and it will be obvious to those skilled in the art that other drawings can be obtained from these drawings without inventive effort.
FIG. 1 shows a schematic structural view of a multi-layered fluidized bed reactor according to an embodiment of the present application;
FIG. 2 shows an exploded view of a multi-layered fluidized bed reactor provided in an embodiment of the present application;
FIG. 3 illustrates a front view of a multi-layered fluidized bed reactor provided in accordance with an embodiment of the present application;
FIG. 4 shows a top view of a multi-layered fluidized bed reactor provided by an embodiment of the present application;
FIG. 5 illustrates a cross-sectional view taken along line A-A in FIG. 3 provided by an embodiment of the present application;
Fig. 6 shows a cross-sectional view along line B-B in fig. 4 provided by an embodiment of the present application.
Reference numerals illustrate:
1. Top cap, 2, barrel, 21, air feed chamber, 211, third vertical baffle, 22, one deck reaction chamber, 221, first vertical baffle, 23, two deck reaction chamber, 231, second vertical baffle, 24, air distribution plate, 25, horizontal baffle, 3, material inlet, 4, material outlet, 5, gas inlet.
Detailed Description
The application will be better explained by the following detailed description of the embodiments with reference to the drawings. References herein to "upper", "lower", "inner", "outer" and the like are made to the orientation of fig. 1. The position of the top cover 1 relative to the gas inlet 5 is defined as "up"; the position of the first vertical barrier 221 with respect to the cylinder 2 is defined as "inside".
As mentioned above, fluidized bed reactors, also called ebullated bed reactors, refer to devices in which a gas undergoes a chemical reaction in an ebullated bed of solid material or catalyst. In such devices, the gas vigorously agitates the solid particulate material at a flow rate that acts like a boiling liquid and exhibits certain characteristics of the liquid, such as fluid pressure against the walls, ability to overflow, and viscosity. The working principle is mainly based on the gas-solid fluidization technology, and when the gas passes through the bed layer at a higher flow rate, the solid particles in the bed are driven to move so as to suspend in the flowing main flow for reaction. In this state, the solid particles are blown up by the fluid to be in a suspension state, and can move up, down, left and right and flip as if the liquid is boiling.
In a typical fluidized bed reactor, the reaction chamber is divided into a plurality of reaction chambers by baffles, and usually only one reaction chamber can be used as a loosening chamber, and the other reaction chambers are used as fluidization chambers.
The loosening chamber is mainly used for carrying out preliminary loosening treatment on materials so as to facilitate the subsequent fluidization process. In fluidized bed apparatus, a loosening chamber is usually located before the fluidization chamber, and by means of a specific mechanical or air flow, a relative motion is generated between the material particles, so that the agglomeration state of the particles is destroyed, and the looseness of the material is increased.
The fluidization chamber is a core part for carrying out reaction, and the material particles are suspended and in a fluidization state by introducing reaction gas, and the contact and collision frequency among the material particles is greatly increased in the fluidization state, so that the heat and mass transfer processes among the materials are promoted, and the efficiency of operations such as drying, mixing, reaction and the like is improved.
The material needs to pass through a plurality of fluidization chambers, and the pressure of the reaction gas is reduced after the reaction, so that the material can be piled up, and a loosening chamber is not arranged between the plurality of fluidization chambers to loosen the material.
Therefore, after a general fluidized bed reactor is operated for a certain time, the accumulation of materials in each chamber is increased, so that a fluidization dead zone is formed in certain areas, the fluidized bed reactor cannot be operated normally, the reaction conversion rate is low, and the production cost is increased.
In order to solve at least one of the technical problems in the prior art or related art, the present application provides a multi-layered fluidized bed reactor comprising: the cylinder body is cylindrical; the inside of the cylinder is divided into a reaction chamber and a gas supply chamber by a wind distribution plate; air holes are uniformly distributed on the air distribution plate; the reaction chamber is divided into a first layer of reaction chamber and a second layer of reaction chamber by the horizontal baffle, the first layer of reaction chamber is divided into a plurality of reaction chambers by the first vertical baffle, the second layer of reaction chamber is divided into a plurality of reaction chambers by the second vertical baffle, and the reaction chambers are sequentially communicated from the first layer of reaction chamber to the second layer of reaction chamber; the material inlet is arranged on the side wall of the first reaction cavity of the first layer of reaction chamber, and the material outlet is arranged on the side wall of the last reaction cavity of the second layer of reaction chamber; the air supply chamber is divided into a plurality of air supply chambers by a third vertical baffle, and the positions of the air supply chambers are in one-to-one correspondence with the reaction chambers in one layer of reaction chamber; the gas inlets are respectively communicated with the gas supply cavity. Each reaction chamber in the one deck reaction chamber can be used as loosening chamber, fluidization chamber in proper order, and the air feed chamber corresponds with the reaction chamber one-to-one in the one deck reaction chamber, and the gas velocity of each reaction chamber of convenient individual control can control the material and pass through in the loosening chamber with the fluidization chamber in turn, has avoided the material to produce in each cavity to cumulate and has increased, has solved general fluidized bed reactor and has formed the fluidization dead zone in some regions easily, the unable normal operating technical problem of fluidized bed reactor.
A multi-layered fluidized bed reactor according to some embodiments provided herein is described below with reference to the accompanying drawings.
Referring to fig. 1 to 6, an embodiment of the first aspect of the present application provides a multi-layered fluidized bed reactor, comprising: the cylinder body 2, the cylinder body 2 is cylindrical; the inside of the cylinder 2 is divided into a reaction chamber and a gas supply chamber 21 by a wind distribution plate 24; the air holes are uniformly distributed on the air distribution plate 24; the reaction chamber is divided into a first layer of reaction chamber 22 and a second layer of reaction chamber 23 by a horizontal baffle 25, the first layer of reaction chamber 22 is divided into a plurality of reaction chambers by a first vertical baffle 221, the second layer of reaction chamber 23 is divided into a plurality of reaction chambers by a second vertical baffle 231, and the reaction chambers are sequentially communicated from the first layer of reaction chamber 22 to the second layer of reaction chamber 23; the material inlet 3 is arranged on the side wall of the first reaction cavity of the first layer of reaction chamber 22, and the material outlet 4 is arranged on the side wall of the last reaction cavity of the second layer of reaction chamber 23; the air supply chamber 21 is divided into a plurality of air supply chambers by a third vertical baffle 211, and the positions of the air supply chambers are in one-to-one correspondence with the reaction chambers in the layer of reaction chambers 22; the gas inlets 5 are respectively communicated with the gas supply cavities.
The cylinder body 2 is cylindrical, the lower layer is an air supply chamber 21, and the upper layer is a reaction chamber; the reaction chamber is divided into two layers, the lower layer is a first layer of reaction chamber 22, the upper layer is a second layer of reaction chamber 23, and the first layer of reaction chamber 22 and the second layer of reaction chamber 23 are divided into a plurality of reaction chambers. The material enters the reaction chamber from the material inlet 3, the gas enters from the gas inlet 5, the number of the gas supply chambers is the same as that of the reaction chambers in the reaction chamber 22 of one layer, and each reaction chamber in the reaction chamber 22 of one layer is provided with an independent gas source for supplying gas, so that each reaction chamber in the reaction chamber 22 of one layer can be used as a loosening chamber or a fluidization chamber, for example: the first reaction chamber is used as a loosening chamber, the second reaction chamber is used as a fluidization chamber, and the third reaction chamber is used as a loosening chamber, so that the steps are alternately performed; or the first reaction chamber and the last reaction chamber in the layer of reaction chambers 22 are used as loosening chambers, the other reaction chambers are used as fluidization chambers, etc. The design can control materials to pass through the loosening chamber and the fluidization chamber alternately in sequence, so that the accumulation of materials in each chamber is avoided, and the technical problem that a fluidization dead zone is easy to form in certain areas of a general fluidized bed reactor and the fluidized bed reactor cannot normally operate is solved.
When a certain reaction cavity is used as a loosening chamber, air, nitrogen or other protective gases are introduced into the corresponding gas inlets 5, and the relative movement among the material particles is generated by controlling the speed of the gases, so that the aggregation state of the particles is damaged, and the looseness of the materials is increased; when a certain reaction cavity is used as a fluidization chamber, the corresponding gas inlet 5 is filled with reaction gas, so that the material particles are suspended and are in a fluidization state. In the fluidized state, the materials move up and down along the baffle channel in the reaction chamber, and a plurality of reaction chambers are arranged in the first-layer reaction chamber 22 and the second-layer reaction chamber 23, so that the path of the materials in the fluidized bed is prolonged, the reaction time of the materials and the gas is prolonged, and the reaction efficiency is improved.
It is understood that the number of reaction chambers in the first layer of reaction chamber 22 may be the same as or different from the number of reaction chambers in the second layer of reaction chamber 23; the reaction chambers in the first layer reaction chamber 22 and the second layer reaction chamber 23 can be uniformly arranged or unevenly arranged, and can be correspondingly and optimally arranged according to different materials.
In an exemplary embodiment, as shown in fig. 2, a layer of reaction chambers 22 is uniformly divided into 4 reaction chambers, i, ii, iii and iv, by 2 first vertical baffles 221 arranged orthogonally; the two-layer reaction chamber 23 is uniformly divided into 4 reaction chambers by 2 second vertical baffles 231 which are orthogonally arranged, namely a V-shaped reaction chamber, a VI-shaped reaction chamber, a VII-shaped reaction chamber and a VIII-shaped reaction chamber; the reaction chamber I, the reaction chamber II, the reaction chamber III, the reaction chamber IV, the reaction chamber V, the reaction chamber VI, the reaction chamber VII and the reaction chamber VIII are communicated in sequence; the material inlet 3 is arranged on the side wall of the No. I reaction chamber, and the material outlet 4 is arranged on the side wall of the No. VIII reaction chamber.
The 2 first vertical baffles 221 orthogonally disposed refer to 2 first vertical baffles 221 being perpendicular, and the 2 first vertical baffles 221 intersect at a middle point, that is, the 2 first vertical baffles 221 orthogonally disposed may uniformly separate a layer of reaction chambers 22, i.e., the size of the reaction chambers No. i, no. ii, no. iii, and No. iv are the same. Similarly, the size of the V-shaped reaction chamber, the VI-shaped reaction chamber, the VII-shaped reaction chamber and the VIII-shaped reaction chamber are the same. The IV reaction chamber is arranged right below the V reaction chamber, and a notch is arranged on the horizontal baffle 25, so that the IV reaction chamber is communicated with the V reaction chamber. The design structure is simple, the reaction cavity is uniformly arranged, the reaction gas can be uniformly distributed in the cavity, and the partial gas concentration is prevented from being too high or too low, so that the uniformity of the reaction is ensured.
In an exemplary embodiment, as shown in fig. 5, the air supply chamber 21 is uniformly divided into 4 air supply chambers by 2 third vertical baffles 211 which are orthogonally arranged, and the positions of the air supply chambers are respectively in one-to-one correspondence with the reaction chambers No. i, no. ii, no. iii and No. iv. The 4 air supply cavities are uniformly arranged, so that the control of the gas flow can be facilitated, the gas can be ensured to be uniformly distributed in the cavity, the local gas concentration is prevented from being too high or too low, and the uniformity of the reaction is ensured.
In an exemplary embodiment, the material inlet 3 is located at a middle position of the outer circumference of the reaction chamber I in the horizontal direction, and the material inlet 3 is located at the top of the reaction chamber I in the vertical direction; the material outlet 4 is positioned at the middle position of the outer circumference of the VIII-type reaction cavity in the horizontal direction, and the material outlet 4 is positioned at the bottom of the VIII-type reaction cavity in the vertical direction.
The material inlet 3 is located in the middle of the outer circumference of the No. i reaction chamber in the horizontal direction, that is, the axial direction of the material inlet 3 is 45 ° with the first vertical baffle 221 disposed in 2 orthogonal directions, as shown in fig. 4, so that the material can be ensured to enter the No. i reaction chamber uniformly and efficiently. The material inlet 3 is located the top of I reaction chamber in vertical orientation, and as shown in FIG. 3, the material can fall down under the effect of gravity after getting into I reaction chamber, and the gas in the gas supply chamber is from blowing down upwards, can make the material fully mix with gas in the short time after getting into I reaction chamber.
The material outlet 4 is located at the middle position of the outer circumference of the VIII-type reaction chamber in the horizontal direction, namely, the axial direction of the material outlet 4 is 45 degrees with the second vertical baffle 231 which is orthogonally arranged, so that the arrangement is beneficial to ensuring that the material can be uniformly and efficiently discharged. The material outlet 4 is positioned at the bottom of the VIII reaction cavity in the vertical direction, so that the material moves from top to bottom in the VIII reaction cavity, is easier to discharge, and can avoid accumulation and increase of the material.
In an exemplary embodiment, the height of the first layer of reaction chambers 22 is the same as the height of the second layer of reaction chambers 23. This is designed to ensure uniformity of distribution of the material in the first and second reaction chambers 22, 23, and when the material flows from the first reaction chamber 22 into the second reaction chamber 23, the flow path and velocity of the material may be more uniform due to the high uniformity, which helps to reduce local accumulation or blockage of the material during the flow process, thereby ensuring uniform distribution of the material throughout the reaction process.
In an exemplary embodiment, as shown in FIG. 5, the air holes in the air distribution plate 24 have an open area of 6% -16% and the air distribution plate 24 has a thickness of 1-5 mm. The aperture ratio of the air holes refers to the ratio of the sum of the areas of all the air holes on the air distribution plate 24 to the effective area of the air distribution plate 24, for example, the aperture ratio of the air holes on the air distribution plate 24 is 6%; or the aperture ratio of the air holes on the air distribution plate 24 is 10%; or the aperture ratio of the air holes on the air distribution plate 24 is 16%, so that more air holes are formed on the air distribution plate 24, the air flow passing through the air distribution plate 24 can be more uniformly distributed in the reaction cavity, the dead angle and vortex phenomenon of the air flow can be reduced, and the fluidization effect and the reaction efficiency of the materials can be improved. The air distribution plate 24 may be made of 316 or 304 stainless steel, and has a thickness in the range of 1-5 mm, for example, the air distribution plate 24 has a thickness of 1 mm; or the thickness of the air distribution plate 24 is 2 mm; or the thickness of the air distribution plate 24 is 3.5 mm; or the thickness of the air distribution plate 24 is 5mm, so that the air distribution plate 24 can maintain enough mechanical strength to bear various forces in the reaction process, and the pressure is reduced when the thickness of the air distribution plate 24 is thinner.
In an exemplary embodiment, as shown in fig. 6, the first vertical baffle 221 and the second vertical baffle 231 are respectively provided with a communication notch, and the communication notches are staggered up and down and are used for communicating with the reaction chamber. The material moves up and down along the first vertical baffle 221 and the second vertical baffle 231 in the reaction cavity, and the communicating notches are staggered up and down, so that the path of the material in the reaction cavity is prolonged, the reaction time of the material and the gas is prolonged, and the reaction efficiency is improved.
In an exemplary embodiment, the ratio of the height of the communication gap to the height of the reaction chamber is 0.2-0.35. For example, the ratio of the height of the communicating gap to the height of the reaction chamber is 0.2; or the ratio of the height of the communicating gap to the height of the reaction cavity is 0.25; or the ratio of the height of the communicating gap to the height of the reaction chamber is 0.35, so that the mixture of the material and the gas is stirred more strongly when passing through the first vertical baffle 221 and the second vertical baffle 231, and the reaction is more sufficient. The height of the communicating gap is too high, and the gas and the materials can be backmixed, so that the distribution time of the materials in the reaction cavity is uneven; the height of the communicating gap is too low, and materials are easy to block when passing through the vertical baffle plate, so that the reaction process is influenced.
In an exemplary embodiment, as shown in fig. 4, the material inlet 3 and the material outlet 4 are on an extension of the diameter of the same cylinder 2. I.e. the phase angle of the material inlet 3 and the material outlet 4 is 180 deg., so that the design can maximally utilize the space to enable the material to form the longest flow path in the equipment, thereby increasing the contact and mixing opportunity between the material and the gas and helping to improve the reaction efficiency.
In an exemplary embodiment, the material inlet 3 and the material outlet 4 are cylindrical, the diameters of the material inlet 3 and the material outlet 4 are equal, and the ratio of the diameter of the material inlet 3 to the diameter of the cylinder 2 is 0.1-0.3. The ratio of the diameter of the material inlet 3 to the barrel 2 reflects the size of the material inlet 3 relative to the volume of the entire barrel 2, which directly affects the flow rate and distribution of the material as it enters the barrel 2 and the mixing and reaction effects of the material within the barrel 2. The range of 0.1-0.3 is a reasonable interval obtained through practical experience and theoretical calculation, for example, the ratio of the diameter of the material inlet 3 to the diameter of the cylinder 2 is 0.1; or the ratio of the diameter of the material inlet 3 to the diameter of the cylinder 2 is 0.2; or the ratio of the diameter of the material inlet 3 to the diameter of the cylinder 2 is 0.3, and too large a diameter of the material inlet 3 may cause gas to flow out of the material inlet 3, and too small a diameter may cause slow feeding rate and easy accumulation after entering the reaction chamber.
In an exemplary embodiment, the top of the cylinder 2 is provided with a top cover 1, and the top cover 1 is usually designed to be detachable for the convenience of maintenance and repair of the inside of the cylinder 2. When it is necessary to clean the inside of the cylinder 2, replace the internal parts or perform other maintenance work, the top cover 1 can be conveniently opened for operation.
In the description of the present application, it should be understood that the terms "first," "second," and the like are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present application, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
In the present application, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium; may be a communication between two elements or an interaction between two elements. The specific meaning of the above terms in the present application can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present application, unless expressly stated or limited otherwise, a first feature is "on" or "under" a second feature, which may be in direct contact with the first and second features, or in indirect contact with the first and second features via an intervening medium. Moreover, a first feature "above," "over" and "on" a second feature may be a first feature directly above or obliquely above the second feature, or simply indicate that the first feature is higher in level than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is level lower than the second feature.
In the description of the present specification, the terms "one embodiment," "some embodiments," "example embodiments," "examples," "specific examples," or "some examples," etc., refer to a particular feature, structure, material, or characteristic described in connection with the embodiment or example as being included in at least one embodiment or example of the application. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.
While embodiments of the present application have been shown and described above, it will be understood that the above embodiments are illustrative and not to be construed as limiting the application, and that alterations, modifications, substitutions and variations may be made in the above embodiments by those skilled in the art within the scope of the application.
Claims (10)
1. A multi-layered fluidized bed reactor, comprising: the cylinder body (2), the said cylinder body (2) is cylindrical;
the inside of the cylinder body (2) is divided into a reaction chamber and an air supply chamber (21) by an air distribution plate (24); the air holes are uniformly distributed on the air distribution plate (24);
The reaction chamber is divided into a first layer of reaction chamber (22) and a second layer of reaction chamber (23) by a horizontal baffle plate (25), the first layer of reaction chamber (22) is divided into a plurality of reaction chambers by a first vertical baffle plate (221), the second layer of reaction chamber (23) is divided into a plurality of reaction chambers by a second vertical baffle plate (231), and the reaction chambers are sequentially communicated from the first layer of reaction chamber (22) to the second layer of reaction chamber (23);
The material inlet (3) is arranged on the side wall of the first reaction cavity of the first-layer reaction chamber (22), and the material outlet (4) is arranged on the side wall of the last reaction cavity of the second-layer reaction chamber (23);
the gas supply chambers (21) are divided into a plurality of gas supply chambers by third vertical baffles (211), and the positions of the gas supply chambers are in one-to-one correspondence with the reaction chambers in the layer of reaction chambers (22);
The gas inlets (5) are respectively communicated with the gas supply cavities.
2. A multi-layer fluidized bed reactor according to claim 1, characterized in that the height of the one-layer reaction chamber (22) is the same as the height of the two-layer reaction chamber (23).
3. A multilayer fluidized bed reactor according to claim 1, characterized in that the opening ratio of the air holes in the air distribution plate (24) is 6% -16%, and the thickness of the air distribution plate (24) is 1-5 mm.
4. The multi-layer fluidized bed reactor according to claim 1, wherein the first vertical baffle plate (221) and the second vertical baffle plate (231) are respectively provided with communication notches, the communication notches are arranged in a vertically staggered manner, and the communication notches are used for communicating with the reaction chamber.
5. A multi-layered fluidized bed reactor according to claim 4, wherein the ratio of the height of the communicating gap to the height of the reaction chamber is 0.2 to 0.35.
6. A multi-layer fluidized bed reactor according to claim 1, characterized in that the material inlet (3) and the material outlet (4) are on the same extension of the diameter of the cylinder (2).
7. A multi-layer fluidized bed reactor according to claim 1, characterized in that the material inlet (3) and the material outlet (4) are cylindrical, the diameter of the material inlet (3) and the material outlet (4) is equal, and the ratio of the diameter of the material inlet (3) to the diameter of the cylinder (2) is 0.1-0.3.
8. A multilayer fluidized bed reactor according to claim 1, characterized in that the one layer of reaction chambers (22) is evenly divided into 4 reaction chambers, i reaction chamber, ii reaction chamber, iii reaction chamber and iv reaction chamber, by 2 first vertical baffles (221) arranged orthogonally;
The two-layer reaction chamber (23) is uniformly divided into 4 reaction chambers by 2 second vertical baffles (231) which are orthogonally arranged, namely a V-shaped reaction chamber, a VI-shaped reaction chamber, a VII-shaped reaction chamber and a VIII-shaped reaction chamber;
The reaction cavity I, the reaction cavity II, the reaction cavity III, the reaction cavity IV, the reaction cavity V, the reaction cavity VI, the reaction cavity VII and the reaction cavity VIII are sequentially communicated;
the material inlet (3) is arranged on the side wall of the No. I reaction cavity, and the material outlet (4) is arranged on the side wall of the No. VIII reaction cavity.
9. A multilayer fluidized bed reactor according to claim 8, wherein the gas supply chambers (21) are uniformly divided into 4 gas supply chambers by 2 third vertical baffles (211) which are orthogonally arranged, and the positions of the gas supply chambers are respectively in one-to-one correspondence with the reaction chambers No. i, no. ii, no. iii and No. iv.
10. A multilayer fluidized bed reactor according to claim 8, wherein the material inlet (3) is located at a middle position of the outer circumference of the reaction chamber No. i in the horizontal direction, and the material inlet (3) is located at the top of the reaction chamber No. i in the vertical direction; the material outlet (4) is positioned at the middle position of the outer circumference of the VIII-type reaction cavity in the horizontal direction, and the material outlet (4) is positioned at the bottom of the VIII-type reaction cavity in the vertical direction.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10204513A (en) * | 1997-01-17 | 1998-08-04 | Kobe Steel Ltd | Fluidized bed type reduction method, fluidized bed type reduction reactor and fluidized bed type reduction reaction apparatus |
| KR20020016024A (en) * | 2000-08-24 | 2002-03-04 | 이구택 | Fluidized bed reactor |
| CN103868327A (en) * | 2014-01-01 | 2014-06-18 | 杨胜妹 | Multilayer fluidized bed |
| CN104096518A (en) * | 2013-04-08 | 2014-10-15 | 中国科学院大连化学物理研究所 | Multi-chamber fluidized bed reactor |
| CN117205846A (en) * | 2023-10-17 | 2023-12-12 | 东北大学 | Fluidized reactor for magnetizing reduction of refractory iron ore |
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2024
- 2024-09-03 CN CN202411226628.3A patent/CN118718903A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10204513A (en) * | 1997-01-17 | 1998-08-04 | Kobe Steel Ltd | Fluidized bed type reduction method, fluidized bed type reduction reactor and fluidized bed type reduction reaction apparatus |
| KR20020016024A (en) * | 2000-08-24 | 2002-03-04 | 이구택 | Fluidized bed reactor |
| CN104096518A (en) * | 2013-04-08 | 2014-10-15 | 中国科学院大连化学物理研究所 | Multi-chamber fluidized bed reactor |
| CN103868327A (en) * | 2014-01-01 | 2014-06-18 | 杨胜妹 | Multilayer fluidized bed |
| CN117205846A (en) * | 2023-10-17 | 2023-12-12 | 东北大学 | Fluidized reactor for magnetizing reduction of refractory iron ore |
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