阅读说明：本技术 一种用于卧式反应器的气体分布器 (Gas distributor for horizontal reactor ) 是由 方晨辰 倪昊尹 刘英民 于 2020-05-29 设计创作，主要内容包括：本发明涉及一种用于卧式反应器的气体分布器,包括设于进气口处的锥形导流板以及设于锥形导流板与催化剂床层之间的开孔分布板,其中开孔分布板包括平行于反应器筒体轴向设置的水平分布板、沿宽度方向分别设于水平分布板两侧的倾斜分布板。与现有技术相比,本气体分布器可有效降低进口气体流速,减小高速气体对进口下方催化剂床层的冲击而造成的催化剂破碎粉化、床层塌陷等问题；有效提高大长径比卧式反应器轴向气体分布的均匀性。(The invention relates to a gas distributor for a horizontal reactor, which comprises a conical guide plate arranged at a gas inlet and an open pore distribution plate arranged between the conical guide plate and a catalyst bed layer, wherein the open pore distribution plate comprises a horizontal distribution plate arranged in parallel with the axial direction of a reactor barrel body and inclined distribution plates respectively arranged at two sides of the horizontal distribution plate along the width direction. Compared with the prior art, the gas distributor can effectively reduce the flow velocity of inlet gas and reduce the problems of catalyst crushing and pulverization, bed layer collapse and the like caused by the impact of high-speed gas on a catalyst bed layer below an inlet; effectively improving the axial gas distribution uniformity of the horizontal reactor with large length-diameter ratio.)

1. A gas distributor for a horizontal reactor, the gas distributor being arranged in the horizontal reactor, the horizontal reactor comprising a reactor barrel (5), a gas inlet (1) arranged on the reactor barrel (5), and a catalyst bed (6) arranged in the reactor barrel (5), characterized in that the gas distributor comprises:

the conical guide plate (2) is arranged at the gas inlet (1) and is used for uniformly diffusing gas to the periphery along the radial direction of the gas inlet (1); and

the perforated distribution plate (4) is arranged between the conical guide plate (2) and the catalyst bed layer (6) and used for enabling gas to be uniformly distributed along the axial direction of the reactor cylinder body (5), and comprises a horizontal distribution plate (403) which is parallel to the axial direction of the reactor cylinder body (5) and inclined distribution plates (402) which are respectively arranged at two sides of the horizontal distribution plate (403); and the horizontal distribution plate (403) and the inclined distribution plate (402) are respectively provided with a gas distribution hole.

2. The gas distributor for horizontal reactors according to claim 1, wherein the conical baffle (2) comprises a baffle (202) and an annular inclined plate (203);

the flow guide baffle (202) is vertical to the axial direction of the air inlet (1);

the annular inclined plate (203) is arranged on the edge of the flow guide baffle (202) along the circumferential direction.

3. The gas distributor for the horizontal reactor as claimed in claim 2, wherein the angle between the annular inclined plate (203) and the axial direction of the gas inlet (1) is 10-80 °.

4. The gas distributor for the horizontal reactor as claimed in claim 2, wherein the guide baffle (202) and the annular inclined plate (203) are provided with gas evacuation holes with a diameter of 1-100 mm.

5. The gas distributor for a horizontal reactor as claimed in claim 1, wherein the inclined distribution plate (402) is inclined at an angle of-75 ° to 75 ° with respect to the horizontal plane.

6. The gas distributor for the horizontal reactor according to claim 1, wherein the perforated distribution plate (4) is axially divided into a deceleration section (405), a flow guide section (406) and a diffusion section (404) which are sequentially connected along the reactor cylinder (5);

the deceleration section (405) is arranged opposite to the air inlet (1);

the flow guide section (406) and the diffusion section (404) are sequentially and symmetrically arranged at two sides of the deceleration section (405);

the aperture ratios of the gas distribution holes on the deceleration section (405), the flow guide section (406) and the diffusion section (404) are respectively 2-20%, 20-60% and 10-60%;

the flow guide section (406) is also provided with a plurality of flow guide sheets (401) which are vertically arranged on the horizontal distribution plate (403).

7. The gas distributor as claimed in claim 6, wherein the gas distribution holes comprise circular holes with a diameter of 1-150mm and a hole area of 100-5000mm²The rectangular holes and the strip-shaped holes with the length of 10-500mm and the width of 2-10 mm.

8. The gas distributor for the horizontal reactor as claimed in claim 6, wherein the velocity reduction section (405), the flow guide section (406) and the diffuser section (404) each comprise a plurality of distribution unit plates which are sequentially detachably connected in parallel with the axial direction of the reactor cylinder (5);

the distribution unit plate comprises a horizontal sub plate and inclined sub plates arranged on two sides of the horizontal sub plate;

the plurality of horizontal sub-plates are sequentially connected to form a horizontal distribution plate (403), and the plurality of inclined sub-plates are sequentially connected to form an inclined distribution plate (402);

the gas distribution holes are formed in the horizontal sub-plate and the inclined sub-plate.

9. The gas distributor for a horizontal reactor as claimed in claim 6, wherein the height of the guide vanes (401) is 5-100mm, and the included angle between the guide vanes (401) and the radial plane of the reactor barrel (5) is-75 ° to 75 °.

Technical Field

The invention belongs to the technical field of coal chemical industry and petrochemical industry, and relates to a gas distributor for a horizontal reactor.

Background

Aiming at the characteristics of China fossil resources of 'less oil, gas and more coal' and the current development trend of 'large scale, low energy consumption, high efficiency and low pollution' of coal chemical industry, the fixed bed reactor develops towards the aims of enlarging the productivity of a single machine, improving a process route and reducing the emission pollution. For example, as the capacity of the coal-to-ethylene glycol project is continuously expanded, the capacity of a single fixed bed reactor for synthesizing dimethyl oxalate is correspondingly improved. The traditional vertical fixed bed reactor is difficult to meet the requirement of capacity expansion, and the horizontal reactor can adapt to the requirement of single large-scale production.

At present, chinese patents CN1035201140B and CN106475018A disclose gas distributors suitable for vertical fixed bed reactors, respectively, which mainly improve the uniformity of gas flow in the top head of the reactor.

Different from the axial symmetry structure of a vertical fixed bed reactor, the length-diameter ratio of the horizontal reactor in the flow direction is far less than 1, and the gas flow section is changed from the circular shape of the vertical reactor to the rectangular shape of the horizontal reactor, so that the influence of the inlet gas distributor on the normal operation of the horizontal reactor is larger. The uniformity of the inlet gas flow determines the uniformity of the reaction within each channel of the reactor, which in turn leads to the uniformity of the exothermic (endothermic) heat of reaction, ultimately affecting the efficiency and safety of the reactor. To date, patents directed to gas distributors for large-scale horizontal fixed bed reactors are very rare, but there is a necessary trend to develop large-scale horizontal fixed bed reactors.

Disclosure of Invention

The invention aims to provide a gas distributor for a horizontal reactor, which aims to improve the flow uniformity of gas in the axial direction of the horizontal reactor and avoid the problem of bed collapse caused by the impact of high-speed gas on a catalyst bed below an inlet.

The purpose of the invention can be realized by the following technical scheme:

a gas distributor for a horizontal reactor, the gas distributor being disposed in the horizontal reactor, the horizontal reactor comprising a reactor barrel, a gas inlet disposed in the reactor barrel, and a catalyst bed disposed in the reactor barrel, the gas distributor comprising:

the conical guide plate is arranged at the air inlet and used for enabling the gas to be uniformly diffused to the periphery along the radial direction of the air inlet; and

the perforated distribution plate is arranged between the conical guide plate and the catalyst bed layer, is used for enabling gas to be uniformly distributed along the axial direction of the reactor cylinder body, and comprises a horizontal distribution plate arranged parallel to the axial direction of the reactor cylinder body and inclined distribution plates respectively arranged on two sides of the horizontal distribution plate along the width direction; and the horizontal distribution plate and the inclined distribution plate are provided with gas distribution holes.

As a preferable technical scheme, the inclined distribution plates are symmetrically arranged at two sides of the horizontal distribution plate.

As the preferred technical scheme, a supporting beam is further arranged in the reactor barrel, and the perforated distribution plate is mounted on the supporting beam through bolts so as to be convenient and reliable to mount and dismount.

Furthermore, the conical guide plate comprises a guide baffle and an annular inclined plate;

the flow guide baffle is arranged in the axial direction perpendicular to the gas inlet and is used for avoiding the problem of bed layer collapse caused by direct impact of high-speed gas on a catalyst bed layer;

the annular inclined plate is circumferentially distributed on the edge of the flow guide baffle plate, so that gas can be uniformly diffused around the annular inclined plate.

As a preferable technical scheme, the flow guide baffle occupies 1/10-1/8 of the cross section area of the air inlet.

Furthermore, the axial included angle between the annular inclined plate and the air inlet is 10-80 degrees, the included angle is too small, the effect of uniform diffusion of gas cannot be achieved, and the loss of the pressure drop of the gas entering the air reactor is too large due to the overlarge included angle, so that the integral resistance of the reactor is increased.

As a preferred technical scheme, the conical guide plate further comprises a conical guide plate support beam arranged between the annular inclined plate and the side wall of the air inlet, and the conical guide plate is fixed at the air inlet through the conical guide plate support beam.

Furthermore, the guide baffle and the annular inclined plate are both provided with gas-dredging holes with the diameter of 1-100 mm; the gas dredging hole is used for eliminating the gas negative pressure backflow phenomenon below the conical guide plate, so that the conical guide plate is prevented from vibrating due to high-speed gas vortex, the pressure loss of the reactor is reduced, and the flowing uniformity of gas below the gas inlet is improved.

Further, the included angle between the inclined distribution plate and the horizontal plane is-75 degrees to 75 degrees. When the upper gas distribution area in the reactor cylinder is too small and the distance between the horizontal distribution plate and the upper cylinder wall of the reactor cylinder is too small, a downward-inclined distribution plate (-75-0 degrees) is selected for increasing the area of the perforated distribution plate and enhancing the effect of the gas distributor; in other cases, the distribution plate is inclined upwards (0-75 deg.).

Furthermore, the perforated distribution plate is axially divided into a deceleration section, a flow guide section and a diffusion section which are sequentially connected along the reactor cylinder;

the speed reduction section is arranged opposite to the air inlet;

the flow guide section and the diffusion section are sequentially and symmetrically arranged at two sides of the speed reduction section;

the aperture ratios of the gas distribution holes on the deceleration section, the flow guide section and the diffusion section are respectively 2-20%, 20-60% and 10-60%;

the flow guide section is also provided with a plurality of flow guide sheets which are vertically arranged on the horizontal distribution plate, so that the gas can uniformly flow through the distribution plate.

Preferably, the aperture ratio of the horizontal distribution plate is different from the aperture ratio of the inclined distribution plate, the aperture ratio of the horizontal distribution plate is higher than that of the inclined distribution plate in the deceleration section, and the aperture ratio of the inclined distribution plate is higher than that of the horizontal distribution plate in the diversion section and the diffusion section, so that the gas can uniformly pass through the whole distributor.

Further, the gas distribution holes comprise round holes with the aperture of 1-150mm and the hole area of 100-5000mm²The rectangular holes and the strip-shaped holes with the length of 10-500mm and the width of 2-10 mm.

As a preferable technical scheme, the openings in the decelerating section are round holes which are arranged in a regular triangle, and the openings in the flow guide section and the diffusing section are rectangular holes or strip-shaped holes which are arranged in a diamond shape.

The speed reduction section is arranged opposite to the gas inlet, and the gas flow velocity at the position is larger because the speed reduction section is closer to the gas inlet, so that the aperture ratio of the speed reduction section is set to be 2-20% and the aperture form of circular holes arranged in a regular triangle is adopted to guide a small amount of gas to uniformly enter the catalyst bed layer at a low speed after passing through the speed reduction section in order to avoid the direct impact action of high-speed gas flow on the catalyst bed layer; the main airflow which does not enter the catalyst bed layer is diffused around in a radial shape after passing through the deceleration section, and because the gas vortex can be generated due to the limitation of the space above the distribution plate, the gas vortex can be destroyed by the flow deflector on the flow guide section, and the gas above the gas distribution plate is further guided to flow uniformly, so that part of the airflow changes the direction and flows through the distribution plate of the flow guide section to enter the catalyst bed layer. The diffusion section guides the residual gas to uniformly flow through the distribution plate and enter the catalyst bed layers at two sides of the reactor. The opening rates of the flow guide section and the diffusion section are 20-60% and 10-60%, respectively, and the opening forms are rectangular holes or strip-shaped holes arranged in a diamond shape.

Furthermore, the deceleration section, the flow guide section and the diffusion section respectively comprise a plurality of distribution unit plates which are parallel to the axial direction of the reactor cylinder and are sequentially detachably connected; each distribution unit plate can be detachably connected with a clip structure or a bolt structure through a common clamping groove;

the distribution unit plate comprises a horizontal sub plate and inclined sub plates arranged on two sides of the horizontal sub plate;

the plurality of horizontal sub-plates are sequentially connected to form a horizontal distribution plate, and the plurality of inclined sub-plates are sequentially connected to form an inclined distribution plate;

the gas distribution holes are formed in the horizontal sub-plate and the inclined sub-plate.

Furthermore, the height of the flow deflector is designed within the range of 5-100mm according to the size and the flow of the reactor, the flow deflector is arranged above the perforated distribution plate, and the included angle between the flow deflector and the radial plane of the reactor cylinder is-75 degrees, so that the gas is distributed to the flow guide section and the diffusion section in proportion.

As the preferred technical scheme, the width of each flow deflector on the flow guide section and the included angle between the flow deflector and the axial direction of the reactor barrel are different.

The working principle is as follows: gas materials enter a cylinder body of the horizontal reactor from a gas inlet, are uniformly diffused to the periphery through a conical guide plate and flow to an open pore distribution plate, the flow rate of high-speed gas is reduced and the flow direction is changed through a deceleration section, a small amount of gas flow passes through gas distribution holes on the deceleration section and enters a catalyst bed layer, and a main body of gas flow diffuses to the periphery and enters a flow guide section; the guide section is provided with a plurality of guide vanes, the gas vortex above the perforated distribution plate is damaged by the guide vanes, and one part of the gas above the perforated distribution plate is further guided to uniformly flow into the diffusion section according to the proportion, and the other part of the gas passes through the gas distribution holes on the guide section to enter the catalyst bed layer; the diffusion section has a high opening rate, and ensures that gas uniformly flows into the catalyst bed layers on two sides of the reactor.

Compared with the prior art, the invention has the following characteristics:

1) the gas distributor can effectively reduce the flow velocity of inlet gas and reduce the problems of catalyst crushing and pulverization, bed collapse and the like caused by the impact of high-speed gas on a catalyst bed below the gas inlet;

2) compared with the conventional conical guide plate structure only comprising the annular inclined plate, the guide baffle plate can effectively avoid the problem of bed layer collapse caused by direct impact of high-speed gas on a catalyst bed layer; meanwhile, the gas distributing function of the gas distributing holes formed in the flow guide baffle is stronger than that of the gas distributing holes in the annular inclined plate, so that the negative pressure backflow phenomenon of the gas below the conical flow guide plate can be eliminated, the gas flowing uniformity of the speed reduction section is improved, and a small part of the fluid is guided to pass through the horizontal distribution plate of the speed reduction section and enter the catalyst bed layer;

3) the flow uniformity of the gas in the axial direction of the reactor is improved, so that the gas can be uniformly distributed in each channel filled with the catalyst, the uniformity of chemical reaction in a catalyst bed is facilitated, and the control and regulation of industrial production are more accurate and rapid;

4) the horizontal fixed bed reactor is suitable for horizontal fixed bed reactors with any capacity scale, the number and arrangement of distribution unit plates with different opening rates and opening forms in the opening distribution plate can be correspondingly combined according to the axial length of the horizontal reactor and the number of gas inlets, and the requirement of uniform distribution of gas flow velocity is met;

5) the gas distributor is suitable for any gas with flow characteristics, the shape, the size and the arrangement of the openings of the sectional detachable opening distribution plate and the inclination angle of the annular inclined plate of the conical guide plate can be adjusted according to the flowing viscosity, the compressibility, the pressure and the like of the gas, and the requirement of uniform distribution of the gas flow speed is met;

6) the sectional detachable perforated distribution plate is convenient and reliable to assemble and disassemble, the problem that the space at the upper part of a catalyst bed layer in a fixed bed reactor is insufficient is solved, and sufficient operation space is provided for filling the catalyst.

Drawings

FIG. 1 is a schematic view of a gas distributor for a horizontal reactor according to the present invention;

FIG. 2 is a schematic view of a conical baffle;

FIG. 3 is a schematic view of an open-cell distribution plate;

FIG. 4 is a sectional view taken along line A-A of FIG. 3;

the notation in the figure is:

1-air inlet, 2-conical guide plate, 201-conical guide plate support beam, 202-guide baffle, 203-annular inclined plate, 3-support beam, 4-perforated distribution plate, 401-guide plate, 402-inclined distribution plate, 403-horizontal distribution plate, 404-diffusion section, 405-deceleration section, 406-guide section, 5-reactor barrel and 6-catalyst bed layer.

Detailed Description

The invention is described in detail below with reference to the figures and specific embodiments. The present embodiment is implemented on the premise of the technical solution of the present invention, and a detailed implementation manner and a specific operation process are given, but the scope of the present invention is not limited to the following embodiments.