CN115738914A - Strong effect mixes formula fixed bed reactor in advance - Google Patents

Abstract

A strong pre-mixing type fixed bed reactor belongs to hydrogenation reaction equipment in the field of petrochemical industry, at least two groups of hydrogenation units are arranged in a reactor shell, and a catalytic reaction area is formed above each group of hydrogenation units; be provided with microbubble pre-mixing device in the entry pipeline, reaction oil gas rethread entry diffuser through microbubble pre-mixing device gets into in the reactor casing, is equipped with the cloth liquid subassembly of filtration in the below of entry diffuser, and the cloth liquid subassembly of filtration includes filter disc, defoaming dish and gas-liquid distribution dish. In the invention, the liquid phase enters the micro-bubble premixing device before entering the reactor, so that hydrogen is fully mixed with the liquid phase before entering the reactor to form a pseudo-homogeneous system of micro-bubbles, good initial distribution is formed at the inlet of the reactor, a good starting point is provided for the subsequent reaction in the whole reactor, the smooth proceeding of the whole reaction is ensured, and the problems of bias flow and coke generation caused by uneven distribution are avoided.

Description

Strong effect mixes formula fixed bed reactor in advance

Technical Field

The invention relates to a hydrogenation reaction in the field of petrochemical industry, in particular to a strong-effect premixing type fixed bed reactor.

Background

Under the large background that environmental regulations become stricter, standards for impurity content in various petroleum products are increasing day by day. The hydrogenation technology plays an important role in refinery production as an essential technology in the production process of clean fuels. The hydrogenation technology comprises hydrocracking, hydrofining and the like. Hydrogenation is exothermic reaction, most of domestic down-flow fixed bed reactor structures are adopted at present, uneven distribution of initial gas and liquid of a bed layer in the reaction process can cause hot spots, coking of catalysts, temperature runaway and the like in the reactor, and product quality and unsafe production are influenced, so that stable gas and liquid distribution is very important for improving the flow characteristic and the catalyst utilization rate in the reactor.

Since the line flow is from the direction perpendicular to the reactor and then from the top down into the reactor, and the gas phase enters the reactor separately, the gas-liquid mixing degree is poor, and good initial distribution is not formed at the inlet of the reactor.

Disclosure of Invention

In order to solve the problems of poor gas-liquid mixing and uneven distribution caused by the fact that the gas phase and the liquid phase of the existing fixed bed reactor are dispersed and enter the reactor, the invention provides a strong-effect premixing type fixed bed reactor, so that the oil phase and the gas phase are subjected to buffering mixing before entering the reactor to avoid the drift current phenomenon, and meanwhile, the gas phase enters the reactor stably along with the oil phase in a microbubble mode by using a microbubble strengthening theory, so that the problems of uneven gas-oil mixing and uneven initial distribution after entering the reactor are effectively solved.

The technical scheme adopted by the invention for solving the technical problems is as follows: a strong pre-mixing type fixed bed reactor is characterized in that an inlet pipeline and an outlet collector are respectively arranged at the top and the bottom of a reactor shell, at least two groups of hydrogenation units are arranged in the reactor shell, and a catalytic reaction area is formed above each group of hydrogenation units; the top of the reactor shell is provided with an inlet diffuser, a micro-bubble premixing device is arranged in the inlet pipeline, the reaction oil gas passing through the micro-bubble premixing device enters the reactor shell through the inlet diffuser, and a filtering liquid distribution component is arranged below the inlet diffuser and comprises a filtering disc, a defoaming disc and a gas-liquid distribution disc which are sequentially arranged from top to bottom; microbubble pre-mixing arrangement is including setting up two baffling buffer boards of corner orientation inlet pipeline incoming flow direction in the inlet pipeline, and has the clearance between the top of two baffling buffer boards and the inlet pipeline inner wall, forms the liquid phase overflow district between two baffling buffer boards, is provided with the microbubble generator of being connected with hydrogen source in this liquid phase overflow district.

As an optimization scheme of the strong premixing type fixed bed reactor, a liquid discharge hole is formed in the bottom of a baffling buffer plate close to the corner.

As another optimization scheme of the strong premixing type fixed bed reactor, the distance between the liquid discharge hole and the bottom of the baffling buffer plate is 5-10mm.

As another optimization scheme of the above strong premixing type fixed bed reactor, after the microbubble generator vertically penetrates through the inlet pipeline in the horizontal direction, the bubble emitting end of the microbubble generator is positioned in the liquid phase overflow area.

As another optimization scheme of the strong premixing type fixed bed reactor, the main body of the micro-bubble generator is made of a microporous material, and the pore diameter of the microporous material is 2 microns.

As another optimization scheme of the strong premixing type fixed bed reactor, the heights of the two baffle buffer plates are 1/4-3/4 of the inner diameter of the inlet pipe.

As another optimization scheme of the strong premixing type fixed bed reactor, the heights of the two baffle buffer plates are different.

As another optimization scheme of the strong premixing type fixed bed reactor, the height of the baffle buffer plate close to the corner is higher than that of the other baffle buffer plate.

As another optimization scheme of the strong premixing type fixed bed reactor, the distance between the two baffle buffer plates is 500-1200mm.

As another optimization scheme of the strong premixing type fixed bed reactor, the corners are arc-shaped, and the high ends of the corners are in contact with the baffle buffer plates.

As another optimization scheme of the strong premixing type fixed bed reactor, the vertical distance between the baffle buffer plate close to the corner and the central axis of the reactor shell is 500-800mm.

As another optimization scheme of the strong premixing type fixed bed reactor, the hydrogenation unit comprises a catalyst grid, a hydrogenation pipeline, a hydrogen cooling box, an even distributor and a gas-liquid distribution disc from top to bottom.

As another optimization scheme of the strong premixing type fixed bed reactor, the catalyst grid comprises a support plate with fine slits distributed on the surface, and a plurality of supporting beams protruding upwards are distributed on the support plate.

As another optimization scheme of the strong premixing type fixed bed reactor, the hydrogenation pipeline comprises a cold hydrogen inlet pipe and an annular pipeline arranged around a cold hydrogen box, and a plurality of downward hydrogen nozzles are distributed on the annular pipeline.

As another optimization scheme of the strong premixing type fixed bed reactor, the hydrogen cooling tank is arranged on a horizontal partition plate in the reactor shell, and the horizontal partition plate enables oil gas to accumulate on the horizontal partition plate to form an oil gas liquid layer surrounding the hydrogen cooling tank; the cold hydrogen case is including setting up urceolus on horizontal baffle and the apron that is in the urceolus top, and forms oil gas entering gap between urceolus top and the apron bottom surface, is provided with the inner tube in the bottom surface of apron, and has the clearance between inner tube bottom and the horizontal baffle, forms the baffling circumferential weld between inner tube and the urceolus, the center of urceolus is provided with the oil gas export that link up horizontal baffle.

As another optimization scheme of the strong premixing type fixed bed reactor, the uniform distributor is positioned below an oil gas outlet of the hydrogen cooling tank and is formed by surrounding a rectangular bottom wall with through holes densely distributed on the surface and four side walls surrounding the edge of the rectangular bottom wall, and the top ends of the four side walls are zigzag overflow areas.

As another optimization scheme of the highly effective premixed fixed bed reactor, the inlet diffuser comprises a cylinder and a flow crushing plate arranged below an oil gas outlet of the cylinder, an overflow weir is arranged in the cylinder, the overflow weir is a circular truncated cone-shaped cylinder with an arc-shaped surface, the small diameter end of the overflow weir faces the oil gas inlet direction, a baffling baffle is arranged, and a side channel is arranged between the baffling baffle and the overflow weir; the surface of the overflow weir is uniformly distributed with a plurality of overflow slits along the circumferential direction, the side wall of the overflow weir is divided into a recent flow area close to the incoming flow direction of the inlet pipeline and a far flow area far away from the incoming flow direction of the inlet pipeline, and a plurality of liquid outlet holes are arranged between the overflow slits on the far flow area.

The invention is mainly characterized in that: the invention sets micro-bubble pre-mixing device in the inlet pipeline to pre-mix the oil phase and gas phase, uses micro-bubble air inlet device and baffle buffer board to buffer the oil phase in the micro-bubble pre-mixing device, and the liquid phase enters into the reactor, and the inlet pipeline before entering into the reactor is buffered by two layers of baffle buffer boards, to prevent the liquid phase with high flow speed from bias flow phenomenon due to centrifugal force effect when entering into the reactor. Meanwhile, the two layers of baffle buffer plates can form a certain liquid layer between the buffer plates, so that a place is provided for the generation of micro bubbles. The gas phase entering the reactor generates micro-bubbles in the liquid layers of the two baffling buffer plates through the micro-bubble gas inlet device, and the liquid phase and the gas phase can form good initial distribution when entering the reactor and stably enter the reactor.

When the oil-gas separator is used, oil gas enters the upper part of the reactor from the inlet pipeline, before the oil gas enters the inlet of the reactor, liquid phase, namely the oil, firstly meets the first baffling buffer plate, the baffling buffer plate performs the buffer blocking effect on the liquid phase, the buffered liquid phase bypasses the first baffling buffer plate and further collides with the second baffling buffer plate at the position, close to the reactor, of the inlet pipe, and the second baffling buffer plate mainly plays a role in liquid accumulation overflowing on the liquid phase. The liquid phase forms a certain liquid level between the two buffer plates to provide a liquid phase environment for the micro-bubble generator. The gas phase enters the inlet pipe through a microbubble generator vertical to the inlet pipe, passes through a metal sintering pipe of the microbubble generator, and is mixed with the liquid phase in a microbubble mode through the cutting action of the liquid phase to enter the reactor.

Compared with the prior art, the invention has the following beneficial effects:

1) In the invention, the liquid phase firstly enters the micro-bubble premixing device before entering the reactor, and passes through the double-layer baffling buffer plate, so that the liquid phase is buffered and forms a liquid layer, and the bias flow phenomenon of high-speed fluid at the end socket is reduced; then, a microbubble generator is utilized to form hydrogen microbubbles, the hydrogen microbubbles are premixed with a liquid phase, hydrogen is fully mixed with the liquid phase before entering the reactor, a pseudo-homogeneous system of the microbubbles is formed, good initial distribution is formed at an inlet of the reactor, a good starting point is provided for the subsequent reaction in the whole reactor, the smooth proceeding of the whole reaction is ensured, and the problems of bias flow and coke generation and the like caused by uneven distribution are avoided;

2) According to the cold hydrogen box in the hydrogenation unit, the baffling circular seam is formed by the outer cylinder and the inner cylinder arranged on the cover plate, so that oil gas and hydrogen gas overflowing into the cold hydrogen box can be fully mixed in the baffling circular seam and then discharged from the oil gas outlet; the saw-toothed overflow area of the side wall of the uniform distributor below the oil gas outlet provides more stable overflow due to the saw-toothed shape with stable height difference, and plays a role in dynamic adjustment;

3) The overflow weir with a special structure is arranged in the inlet diffuser, so that oil gas can be buffered and rectified on the overflow weir, the problem of serious oil gas flow deflection at the inlet is effectively solved, and the phenomenon of uneven distribution of the inner section of the reactor is avoided; the overflow weir is a circular truncated cone-shaped cylinder with an arc-shaped surface, so that fluid can uniformly overflow along the circumferential direction, and the distribution of the circular section of the reactor is more uniform; because the overflow weir is provided with the overflow seams and the uneven liquid outlet holes which are uniformly distributed along the circumferential direction, the oil gas can enter the reactor through the overflow seams and the liquid outlet holes, but the liquid outlet holes are distributed on one side away from the incoming flow direction, and the liquid outlet holes are not arranged on the other side, so that the oil gas from a pipeline can be further prevented from deviating, the phenomenon of uneven overflow is avoided, the unavoidable deviation phenomenon entering the reactor is completely improved, and meanwhile, the simple structure can reduce the cost and the pressure drop as much as possible; the baffling baffle arranged in the inlet diffuser can ensure that oil gas entering the reactor cannot directly impact the reactor to cause unstable cross-section distribution of the reactor, and meanwhile, the baffling baffle exceeds the top of the overflow weir to form a flange, so that oil gas backflow is prevented, the oil gas can be guided into the bell-mouth overflow weir, the oil gas overflowing from the overflow weir is further baffled, and the oil gas overflowing is ensured to be uniform and stable; the arrangement of the flow crushing plate can lead oil gas flowing down from the center of the inlet diffuser to generate vertical impact so as to carry out baffling diffusion, change gas-liquid axial flow into radial flow, and then evenly distribute on the catalyst bed layer after radially impacting with gas-liquid material flows flowing out of other gas-liquid distributors in a plug flow mode.

Drawings

FIG. 1 is a schematic view of the overall structure of the present invention;

FIG. 2 is a schematic diagram of the configuration of the microbubble premixing device in the inlet line;

FIG. 3 is a top view of FIG. 2;

FIG. 4 is a schematic diagram of the structure of a hydrogenation unit;

FIG. 5 is a schematic top view of a catalyst grid;

FIG. 6 is a schematic diagram of the structure of a hydrogenation line and a cold hydrogen tank;

FIG. 7 is a schematic structural view of a homogenizer;

FIG. 8 is a schematic view of the inlet diffuser structure;

reference numerals: 1. reactor shell 101, inlet pipe 102, outlet collector 103, catalytic reaction zone 104, filter tray 105, defoaming tray 106, gas-liquid distribution tray 107, horizontal partition 108, corner 2, micro-bubble generator 3, baffle buffer plate 301, gap 302, liquid drain hole 4, liquid phase overflow zone 5, catalyst grid 501, support plate 502, slit 503, support beam 6, hydrogenation pipe 601, cold hydrogen inlet pipe 602, ring pipe 603, hydrogen nozzle 7, cold hydrogen tank 701, outer cylinder 702, cover plate 703, support rod 704, inner cylinder 705, oil gas inlet slit 706, baffle ring slit 707, oil gas outlet 8, distributor 801, rectangular bottom wall 802, side wall 803, zigzag overflow zone 804, connector 9, inlet diffuser 901, cylinder 902, overflow weir 903, overflow zone 904, baffle 905, side channel 906, overflow slit, baffle plate 907, liquid drain hole 908; A. a microbubble premixing device, a hydrogenation unit and a hydrogenation unit.

Detailed Description

The technical solution of the present invention will be further described in detail with reference to the following embodiments, and the parts of the present invention not illustrated in the following embodiments should be understood as the technologies known or should be known to those skilled in the art, such as the structure of the microbubble generator, the structure of the outlet collector, the structure and installation of the gas-liquid distribution plate, etc.

Example 1

A strong premixing type fixed bed reactor is disclosed as shown in figure 1, comprising a reactor shell 1, wherein an inlet pipeline 101 and an outlet collector 102 are respectively arranged at the top and the bottom of the reactor shell 1, the inlet pipeline 101 is used for introducing reaction oil gas into the reactor shell, the inlet pipeline 101 is generally horizontal, but the fixed bed reactor shell 1 is vertical, therefore, the inlet pipeline 101 is bent downwards when being introduced to the top of the reactor shell 1 so as to enter the reactor shell 1, at the moment, a corner 108 of the inlet pipeline 101 is formed, the horizontal section of the inlet pipeline 101 extends in a direction generally called as an incoming flow direction, the outlet collector 102 intercepts a small amount of catalyst or dust, and simultaneously the reacted oil gas is collected and discharged through a discharge pipeline, a wire mesh is wrapped outside the outlet collector 102, at least two groups of hydrogenation units B are arranged in the reactor shell 1, two groups, generally 2-3 groups are shown in figure 1, a catalytic reaction zone 103 is formed above each group of hydrogenation units B, and catalyst particles for reaction are filled in the reactor shell; the top of the reactor shell 1 is provided with an inlet diffuser 9, oil gas in the inlet pipeline 101 enters the reactor shell 1 through the inlet diffuser 9, and the inlet diffuser 9 mainly plays a role in rapidly diffusing the mixed bubble flow to the cross section of the whole reactor, so that the central flow and the back-mixed flow are avoided, and the initial distribution function is achieved; a micro-bubble premixing device A is arranged in the inlet pipeline 101, the reaction oil gas passing through the micro-bubble premixing device A enters the reactor shell 1 through the inlet diffuser 9, and a filtering liquid distribution component is arranged below the inlet diffuser 9 and comprises a filtering disc 104, a defoaming disc 105 and a gas-liquid distribution disc 106 which are sequentially arranged from top to bottom; microbubble pre-mixing arrangement A is including setting up two baffling buffer plates 3 of corner 108 orientation inlet pipeline 101 incoming flow direction in inlet pipeline 101, and has clearance 301 between the top of two baffling buffer plates 3 and the inlet pipeline 101 inner wall, forms liquid phase overflow district 4 between two baffling buffer plates 3, is provided with the microbubble generator 2 of being connected with hydrogen source in this liquid phase overflow district 4.

The filter disc 104 is installed below the bias flow preventing diffuser A, and can be in the form of a cylinder filter, a grating disc filter, a groove type filter disc and the like, wherein the filter disc needs to ensure a large opening area and a large filter gap, so that raw oil can be effectively filtered to remove impurity components in the raw oil, and the pressure drop of the reactor is reduced; a defoaming disc 105 is arranged below the filter disc 104, and the defoaming disc 105 is of a metal wire mesh structure and is used for removing foams generated by the reaction of hydrogen and oil phase; the gas-liquid distribution disc 106 is arranged below the defoaming disc 105, the gas-liquid distribution disc 106 is generally arranged above a catalyst bed layer of the reactor and is generally directly arranged on a boss arranged on the inner wall of the reactor shell 1, the gas-liquid distribution disc 106 is composed of a porous plate and a plurality of distributors, the gas-liquid distribution is realized through the distributors, the distributors are tubular gas-liquid distributors with simple structures, and the aperture ratio of the gas-liquid distribution disc 106 is generally 10-50%.

When the oil phase is applied to a hydrogenation reactor, the liquid phase is an oil phase, oil gas enters an inlet at the top of the hydrogenation reactor from an inlet pipeline 101, before entering the inlet of the reactor, the oil phase firstly meets a first baffling buffer plate 3, the baffling buffer plate 3 performs a buffering and blocking effect on the oil phase, the oil phase after buffering further flows in the inlet pipeline 101 from a gap 301 at the top of the first baffling buffer plate 3 and collides with a second baffling buffer plate 3 at a position close to the reactor, and the second baffling buffer plate 3 mainly plays a liquid loading overflowing effect on the oil phase; the oil phase forms a liquid phase overflow area 4 between the two buffer plates, and accumulates a certain liquid level to provide a liquid phase environment for the micro-bubble generator 2. The gas phase (i.e., hydrogen gas) enters the inlet line 101 through the microbubble generator 2 perpendicular to the inlet line 101, and the microbubble generator 2 extends into the liquid layer of the liquid phase overflow area 4. The gas phase is mixed with the oil phase in the form of microbubbles by the microbubble generator 2, and the gas phase is mixed with the oil phase in the form of microbubbles and enters the reactor together by the cutting action of the oil phase. The baffling buffer plate 3 can weaken the wall flow effect of the fluid entering the reactor, and improve the initial distribution of gas-liquid two-phase flow in the head sealing section of the reactor; meanwhile, the micro-bubble generator 2 is additionally arranged, so that gas and liquid can be mixed in a micron level before entering the reactor, the original gas and liquid phases are respectively continuous phases and become pseudo-homogeneous phases, and the contact area of the gas and the liquid and the mixing uniformity are greatly increased.

The above is the basic implementation of the present invention, and further improvements, optimizations and limitations can be made on the above, so as to obtain the following embodiments:

example 2

This embodiment is an improved scheme based on embodiment 1, and the main structure thereof is the same as embodiment 1, and the improvement point is that: as shown in fig. 2 and 3, the bottom of the baffle buffer plate 3 near the corner 108 is provided with a drain hole 302, and the baffle buffer plate 3 far away from the corner 108 is not provided with a drain hole, and the drain hole 302 is used for draining oil layer accumulated in the liquid phase overflow area 4 when the equipment is stopped; the distance between the drain hole 302 and the bottom of the baffle buffer plate 3 is generally 5-10mm.

In this embodiment, the corner 108 is curved and the high end of the corner contacts the baffle 3 to ensure that the oil layer flowing out of the drainage hole 302 flows along the inner wall of the curved corner 108 to the inlet diffuser 9 during shutdown.

Example 3

The present embodiment is another modified scheme based on embodiment 1, and the main structure of the present embodiment is the same as that of embodiment 1, and the improvement point is that: as shown in fig. 3, after the micro-bubble generator 2 vertically penetrates through the side surface of the inlet pipeline 101 in the horizontal direction, the bubble emitting end is located in the liquid phase overflow area 4, the axial direction of the micro-bubble generator 2 forms an included angle of 90 ° with the direction of the inlet pipeline, and finally the micro-bubble generator is vertically immersed in the oil phase; the length of the microbubble generator 2 in the inlet line 101 is typically 400mm.

In the present embodiment, the main body of the microbubble generator 2 is made of a microporous material with a pore size of 2 μm, and the specific structure thereof is found in a microbubble generator for enhancing the hydrogenation process with the application number of 201410081189.1 previously applied by the applicant.

Example 4

The present embodiment is another modified scheme based on embodiment 1, and the main structure of the present embodiment is the same as that of embodiment 1, and the improvement point is that: as shown in FIG. 2, the heights of the two baffle buffer plates 3 are generally 1/4-3/4 of the inner diameter of the inlet pipe 1, and preferably 1/2 of the inner diameter of the inlet pipe 1.

In addition, the heights of the two baffle buffer plates 3 can be the same or different, when the heights of the two baffle buffer plates 3 are different, the height of the baffle buffer plate 3 close to the corner 108 is higher than that of the other baffle buffer plate 3;

the distance between the two baffle buffer plates 3 is generally 500-1200mm, for example, 500mm, 600mm, 700mm, 800mm, 900mm, 1000mm, 1100mm, 1200mm, and the like, preferably 800mm, and the thickness of the two baffle buffer plates 3 is generally 5-10mm, preferably 5mm;

the baffle buffer plates 3 near the corners 108 are at a vertical distance of 500-800mm, preferably 500mm, from the central axis of the reactor shell 1.

Example 5

The present embodiment is another modified scheme based on embodiment 1, and the main structure of the present embodiment is the same as that of embodiment 1, and the improvement point is that: as shown in fig. 4, the hydrogenation unit B comprises a catalyst grid 5, a hydrogenation pipeline 6, a cold hydrogen box 7, an equilizer 8 and a gas-liquid distribution disc 106 from top to bottom;

the catalyst grid 5 is used for supporting a catalyst bed layer, and has a main bearing function, as shown in fig. 5, the catalyst grid comprises a support plate 501 with thin slits 502 distributed on the surface, the width of the thin slits 502 is smaller than the particle size of catalyst particles, so that oil gas can pass through, but the catalyst particles cannot pass through, generally, the grid thin slits 502 are smaller than the catalyst size by more than 0.2mm, a plurality of upwards-protruding support beams 503 are distributed on the support plate 501, the support beams 503 are used for supporting the catalyst layer, and the thickness and the height of the support beams 503 are different, and the height is gradually reduced from the center to the edge;

when the reaction oil material needs to be supplemented with cold hydrogen after passing through the catalyst bed layer, the matching of the hydrogenation pipeline 6 and the cold hydrogen box 7 is needed, and the functions of the two are that cold hydrogen is provided for the reaction to reduce the temperature of the reaction raw material, and hydrogen needed by the reaction is supplemented; as shown in fig. 6, the hydrogenation pipeline 6 includes a cold hydrogen inlet pipe 601 and an annular pipeline 602 disposed around the cold hydrogen tank 7, and a plurality of downward hydrogen nozzles 603 are distributed on the annular pipeline 602, low-temperature hydrogen enters the annular pipeline 602 along the cold hydrogen inlet pipe 601 and is ejected along the hydrogen nozzles 603, the hydrogen nozzles 603 eject hydrogen downward, in order to pre-mix the hydrogen with oil gas that has not entered the cold hydrogen tank 7, the hydrogen ejected from the hydrogen nozzles 603 is ejected in the form of micro bubbles, and can be rapidly mixed with oil liquid for heat exchange, and maintain the flowing state of the mixed gas-liquid flow, and the oil-gas mixture passing through the cold hydrogen tank 7 is again distributed through the gas-liquid distribution plate 106;

as shown in fig. 6, the cold hydrogen tank 7 is arranged on a horizontal partition 107 in the reactor shell 1, and the horizontal partition 107 makes the oil gas accumulate thereon to form an oil gas liquid layer surrounding the cold hydrogen tank 7; the hydrogen cooling box 7 comprises an outer cylinder 701 arranged on the horizontal partition 107 and a cover plate 702 positioned above the outer cylinder 701, an oil gas inlet gap 705 is formed between the top of the outer cylinder 701 and the bottom surface of the cover plate 702, the cover plate 702 is also circular and the size of the cover plate is far larger than that of the outer cylinder 701, a plurality of support rods 703 are arranged around the outer cylinder 701, the bottoms of the support rods 703 are connected with the horizontal partition 107, and the top of the support rods is connected with the bottom of the cover plate 702, so that the cover plate 702 is supported and fixed above the outer cylinder 701; an inner cylinder 704 is arranged on the bottom surface of the cover plate 702, a gap is reserved between the bottom of the inner cylinder 704 and the horizontal partition plate 107, a baffling annular seam 706 is formed between the inner cylinder 704 and the outer cylinder 701, and an oil gas outlet 707 penetrating through the horizontal partition plate 107 is arranged in the center of the outer cylinder 701;

as shown in fig. 7, the distributor 8 is located below the oil gas outlet 707 of the cold hydrogen tank 7, and is enclosed by a rectangular bottom wall 801 with through holes densely distributed on the surface and four side walls 802 surrounding the edges of the rectangular bottom wall 801, the four side walls 802 are fixed below the horizontal partition 107 through a plurality of connecting pieces 804, and the top ends of the four side walls 802 are zigzag overflow areas 803.

Example 6

The present embodiment is another modified scheme based on embodiment 1, and the main structure of the present embodiment is the same as that of embodiment 1, and the improvement point is that: the inlet diffuser 9 may be any one of the existing inlet diffusers, or may be an inlet diffuser having a structure, as shown in fig. 8, including a cylinder 901 fixed on the top of the reactor housing 1, and a flow breaking plate 907 disposed below the oil and gas outlet of the cylinder 901, where the flow breaking plate 907 is actually already in the reactor housing 1, an overflow weir 902 is disposed in the cylinder 901, an overflow area 903 is formed between the outer side wall of the overflow weir 902 and the inner side wall of the cylinder 901, the overflow weir 902 is a circular truncated cone-shaped cylinder with an arc-shaped surface, the small diameter end of the overflow weir 902 faces the oil and gas inlet direction, and is provided with a baffle 904, and a side passage 905 is provided between the baffle 904 and the overflow weir 902; a plurality of overflow slits 906 are uniformly distributed on the surface of the overflow weir 902 along the circumferential direction of the overflow weir 902, the side wall of the overflow weir 902 is divided into a recent flow area close to the incoming flow direction of the inlet pipeline 101 and a far flow area far away from the incoming flow direction of the inlet pipeline 101, and a plurality of liquid outlet holes 908 are arranged between the overflow slits 906 on the far flow area;

the baffling baffle 904 is fixed at the small-diameter end of the overflow weir 902 through a plurality of baffle support legs, the number of the baffle support legs is 2-6, on one hand, the baffling baffle 904 cannot block fluid, on the other hand, the baffling baffle can bear the impact of the fluid under the condition of using less support pieces, so that the fluid is prevented from being uneven, and a side channel 905 is formed between the baffle support legs; the distance between the baffle 904 and the small diameter end of the weir 902 is generally 100mm; the baffling plate 904 is a circular thin plate and is coaxial with the small-diameter end of the overflow weir 902, the diameter of the baffling plate is slightly larger than that of the small-diameter end of the overflow weir 902 and is generally 50-100mm larger, so that the edge of the baffling plate exceeds the small-diameter end of the overflow weir 902 to form a flange for preventing oil gas from flowing back;

the overflow slit 906 is positioned at the middle upper part of the overflow weir 902, the length direction of the overflow slit 906 is parallel to a generatrix of the overflow weir 902, the length of the overflow slit 902 is generally 200-350mm, and the width of the overflow slit 902 is generally 10-30mm;

a plurality of liquid outlet holes 908 are arranged among the overflow slits 906 on the far-coming flow area in a row, the number of the liquid outlet holes is 2-5, and the aperture is generally 15-30mm, such as 15mm, 20mm, 25mm, 30mm and the like;

the flow crushing plate 907 is fixed at the bottom of the cylinder 901 through a plurality of flow crushing plate support legs, a fluid channel is formed among the flow crushing plate support legs, the number of the flow crushing plate support legs is generally 4 uniformly arranged, fluid is not blocked as far as possible on the premise of ensuring the strength, and the fluid channel is formed among the flow crushing plate support legs;

the flow crushing plate 907 is connected below the cylinder 901, because oil gas flows down from the center of the cylinder 901, the diameter of the flow crushing plate 907 is slightly smaller than the inner diameter of the cylinder 901 and is generally 5-10mm smaller than the inner diameter of the cylinder 901, on one hand, an inlet diffuser can be ensured to smoothly enter the reactor, on the other hand, materials and space can be saved, and the distance between the flow crushing plate 907 and the bottom of the cylinder 901 is generally 200mm;

the flow crushing plate 907 is a circular flat plate, and two circles of through holes are arranged on the surface of the circular flat plate around the center, are positioned on the outer side of the surface of the flow crushing plate 907, are respectively 12 and 18 in number, and have an aperture of 30mm generally;

a positioning groove matched with the reactor shell 1 is arranged on the side wall of the cylinder 901, so that when the cylinder 901 is arranged at the top of the reactor shell 1, the boundary of a far flow area and a near flow area on the inner overflow weir 902 is vertical to the incoming flow direction; the cylinder 901 is cylindrical, the wall thickness of the tube can be 5-8mm, such as 5mm, 5.5mm, 6mm, 6.5mm, 7mm, 7.5mm, 8mm, etc., the cylinder 901 is determined according to the inlet diameter of the actual reactor, the outer diameter is 10-30mm smaller than the inlet diameter of the reactor matched with the cylinder, the height is generally 1000mm, and the wall thickness is 5-8mm, such as 5mm, 5.5mm, 6mm, 6.5mm, 7mm, 7.5mm, 8mm, etc.

Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.

Claims (17)

1. A strong premixing type fixed bed reactor is characterized in that an inlet pipeline (101) and an outlet collector (102) are respectively arranged at the top and the bottom of a reactor shell (1), at least two groups of hydrogenation units (B) are arranged in the reactor shell (1), and a catalytic reaction area (103) is formed above each group of hydrogenation units (B); the top of reactor shell (1) is provided with inlet diffuser (9), its characterized in that: a micro-bubble premixing device (A) is arranged in the inlet pipeline (101), reaction oil gas passing through the micro-bubble premixing device (A) enters the reactor shell (1) through an inlet diffuser (9), and a filtering liquid distribution component is arranged below the inlet diffuser (9) and comprises a filtering disc (104), a defoaming disc (105) and a gas-liquid distribution disc (106) which are sequentially arranged from top to bottom; microbubble pre-mixing arrangement (A) including set up in inlet pipeline (101) corner (108) towards two baffling buffer boards (3) of inlet pipeline (101) incoming flow direction, and have clearance (301) between the top of two baffling buffer boards (3) and inlet pipeline (101) inner wall, form liquid phase overflow district (4) between two baffling buffer boards (3), be provided with microbubble generator (2) of being connected with hydrogen source in this liquid phase overflow district (4).

2. The strong premixing type fixed bed reactor as claimed in claim 1, wherein: the bottom of a baffling buffer plate (3) close to the corner (103) is provided with a liquid discharge hole (302).

3. The strong premixing type fixed bed reactor as claimed in claim 2, wherein: the distance between the liquid discharge hole (302) and the bottom of the baffling buffer plate (3) is 5-10mm.

4. The strong premixing type fixed bed reactor as claimed in claim 1, wherein: the microbubble generator (2) vertically penetrates through the inlet pipeline (101) in the horizontal direction, and then the bubble emitting end of the microbubble generator is positioned in the liquid phase overflow area (4).

5. The strong premixing type fixed bed reactor as claimed in claim 1, wherein: the main body of the micro-bubble generator (2) is made of a microporous material, and the pore diameter of the microporous material is 2 mu m.

6. The strong premixing type fixed bed reactor as claimed in claim 1, wherein: the height of the two baffle buffer plates (3) is 1/4-3/4 of the inner diameter of the inlet pipe (1).

7. The strong premixing type fixed bed reactor as claimed in claim 1, wherein: the heights of the two baffle buffer plates (3) are different.

8. The strong premixed fixed bed reactor according to claim 7, wherein: the height of the baffle buffer plate (3) close to the corner (108) is higher than that of the other baffle buffer plate (3).

9. The strong premixing type fixed bed reactor as claimed in claim 1, wherein: the distance between the two baffle buffer plates (3) is 500-1200mm.

10. The strong premixing type fixed bed reactor as claimed in claim 1, characterized in that: the corner (108) is arc-shaped, and the high end of the corner is contacted with the baffle buffer plate (3).

11. The strong premixing type fixed bed reactor as claimed in claim 1, wherein: the vertical distance between the baffle buffer plate (3) close to the corner (108) and the central axis of the reactor shell (1) is 500-800mm.

12. The strong premixing type fixed bed reactor as claimed in claim 1, wherein: the hydrogenation unit (B) comprises a catalyst grid (5), a hydrogenation pipeline (6), a cold hydrogen box (7), an even distributor (8) and a gas-liquid distribution disc (106) from top to bottom.

13. The strongly premixed fixed-bed reactor according to claim 12, wherein: the catalyst grid (5) comprises a supporting plate (501) with fine slits (502) distributed on the surface, and a plurality of supporting beams (503) are distributed on the supporting plate (501).

14. The strongly premixed fixed-bed reactor according to claim 12, wherein: the hydrogenation pipeline (6) comprises a cold hydrogen inlet pipe (601) and an annular pipeline (602) arranged around the cold hydrogen tank (7), and a plurality of downward hydrogen nozzles (603) are distributed on the annular pipeline (602).

15. The strongly premixed fixed-bed reactor according to claim 12, wherein: the hydrogen cooling tank (7) is arranged on a horizontal partition plate (107) in the reactor shell (1), and oil gas is accumulated on the horizontal partition plate (107) to form an oil gas liquid layer surrounding the hydrogen cooling tank (7); the cold hydrogen case (7) is including setting up urceolus (701) on horizontal baffle (105) and apron (702) that is in urceolus (701) top, and forms oil gas entering gap (705) between urceolus (701) top and apron (702) bottom surface, is provided with inner tube (704) at the bottom surface of apron (702), and has the clearance between inner tube (704) bottom and horizontal baffle (105), forms baffling circumferential weld (706) between inner tube (704) and urceolus (701), the center of urceolus (701) is provided with oil gas export (707) that link up horizontal baffle (107).

16. The strong premixed fixed bed reactor according to claim 12, wherein: the uniform distributor (8) is positioned below an oil gas outlet (707) of the cold hydrogen box (7) and comprises a rectangular bottom wall (801) with the surface densely distributed with through holes and four side walls (802) surrounding the edges of the rectangular bottom wall (801) in a surrounding mode, and the top ends of the four side walls (802) are provided with sawtooth-shaped overflow areas (803).

17. The strongly premixed fixed-bed reactor according to claim 12, wherein: the inlet diffuser (9) comprises a cylinder body (901) and a flow crushing plate (907) arranged below an oil gas outlet of the cylinder body (901), an overflow weir (902) is arranged in the cylinder body (901), the overflow weir (902) is a circular truncated cone-shaped cylinder body with an arc-shaped surface, the small-diameter end of the overflow weir (902) faces the direction of the oil gas inlet, a baffling baffle (904) is arranged, and a side channel (905) is arranged between the baffling baffle (904) and the overflow weir (2); the surface of the overflow weir (902) is evenly distributed with a plurality of overflow slits (906) along the circumference, the side wall of the overflow weir (902) is divided into a near flow area close to the incoming flow direction of the inlet pipeline (101) and a far flow area far away from the incoming flow direction of the inlet pipeline (101), and a plurality of liquid outlet holes (908) are arranged between the overflow slits (906) on the far flow area.

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