CN113244801A - Multi-fluid mixing equipment - Google Patents
Multi-fluid mixing equipment Download PDFInfo
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- CN113244801A CN113244801A CN202110542783.6A CN202110542783A CN113244801A CN 113244801 A CN113244801 A CN 113244801A CN 202110542783 A CN202110542783 A CN 202110542783A CN 113244801 A CN113244801 A CN 113244801A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
- B01F25/40—Static mixers
- B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
- B01F25/43—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction
- B01F25/431—Straight mixing tubes with baffles or obstructions that do not cause substantial pressure drop; Baffles therefor
- B01F25/4314—Straight mixing tubes with baffles or obstructions that do not cause substantial pressure drop; Baffles therefor with helical baffles
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
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Abstract
The invention discloses multi-fluid mixing equipment which comprises a shell, a heat exchange tube bundle, a fluid distributor, a main fluid mixer, an auxiliary fluid mixer and a central tube, wherein the heat exchange tube bundle is arranged in the shell; the fluid distributor is positioned at one end of the shell and comprises a pipeline, a cavity upper cover and a cavity lower cover, an inner cavity is formed by the cavity upper cover and the cavity lower cover, the pipeline is communicated with the inner cavity, and the cavity lower cover is provided with a small hole; the central tube is inserted into the shell from the top end of the fluid distributor to the other end close to the shell; the main fluid mixer comprises a first flow guide pipe, the first flow guide pipe is coaxially arranged with the central pipe and forms an annular gap with the central pipe, and a first vortex sheet is arranged on the inner wall of the first flow guide pipe; the auxiliary fluid mixer comprises a second flow guide pipe positioned in the shell, the second flow guide pipe is coaxially arranged with the central pipe and forms an annular gap with the central pipe, and a second rotational flow sheet is arranged on the inner wall of the second flow guide pipe; a fluid inlet is provided at the other end of the housing. The multi-fluid mixing equipment has good fluid distribution effect and low flow resistance.
Description
Technical Field
The present invention relates to a multi-fluid mixing apparatus, in particular to a multi-fluid mixing apparatus suitable for use in a fixed bed reactor.
Background
In the industrial process, equipment for mixing various fluids exists, for example, a fixed bed reactor is provided with cold air and hot fluid, the hot fluid is a main fluid, the cold air is used for adjusting the temperature of a bed layer, the cold air and the hot fluid are uniformly mixed through a gas mixing device in the reactor and then enter a catalyst bed layer for reaction, and the phenomenon that the reaction effect is influenced by the fact that the gas which is not uniformly mixed enters the catalyst bed layer is avoided. At present, gas mixing equipment is mostly annular distributing pipe, dendritic distributing pipe, grid formula distributor etc. but all can't adapt to the requirement of different operating modes better.
CN203440099U discloses a gas mixing distributor, which comprises a quench gas distributor and a syngas diversion baffle plate, wherein the quench gas distributor comprises a straight pipe and an annular pipe provided with vent holes, and a cylindrical syngas diversion baffle plate is arranged below the annular pipe. The gas mixing distributor enables the cold shock gas and the synthesis gas to be uniformly mixed, and enables the mixed fluid to be uniformly distributed on the cross section of the catalyst basket in the axial flow catalyst basket, so that the catalyst can achieve better conversion rate and utilization rate and the effect of reducing the pressure drop of a catalyst bed layer. The gas mixing distributor is simple in structure, but because the cold shock gas distributor adopts a ring pipe structure, the cold shock gas quantity changes along with the changes of production load and operation conditions, so that the uniformity of the cold shock gas quantity from the vent holes is poor; and the cold shock gas distributor and the synthesis gas diversion baffle belong to two parts, concentric constraint cannot be realized, different expansion amounts are generated due to the temperature difference of the cold shock gas and the synthesis gas, and the mixing effect of the cold shock gas and the synthesis gas is reduced.
CN208471554U discloses a gas mixing distributor, and this technique has improved on the basis of CN203440099U, through set up the baffle on the ring pipe, makes synthetic gas and partial cold shock velocity of flow slow and flow direction change formation spiral flow air current, and then makes the mixed effect of cold shock gas and synthetic gas better. The gas mixing distributor improves the mixing effect of the cold shock gas and the synthetic gas from the vent holes, but the main structure is similar to the CN203440099U structure, and different expansion amounts generated by temperature difference cannot be overcome, so that the mixing effect of the cold shock gas and the synthetic gas is reduced.
CN106000240A discloses a cold hydrogen box for a hydrogenation reactor, which comprises a cold hydrogen distributor, a mixing box, and a liquid coarse distribution disc, wherein the cold hydrogen distributor is dendritic or annular, so as to solve the problems of insufficient mixing of cold hydrogen and reaction products and uneven temperature reduction of material flow, improve the conversion efficiency of the reaction, and prolong the service life of the catalyst. The cold hydrogen distributor only adopts a dendritic or annular structure, hydrogen flows flow along the axial direction of the reactor through the small holes, the phenomenon of uneven distribution of the small holes caused by the change of hydrogen load can not be overcome, in order to further improve the mixing effect, the mixed fluid flows along the circumferential direction in a staggered way by adopting the mixing box, and the operation pressure drop is high.
Disclosure of Invention
The invention aims to overcome the defects of a mixing distributor (distributor) in the prior art, and provides multi-fluid mixing equipment with a reasonable structure, wherein the path of fluid passing through the multi-fluid mixing equipment is short, the fluid mixing effect is good, and the utilization rate and the reaction conversion rate of a catalyst are improved; and the flow resistance is low, which is beneficial to reducing the energy consumption of the system.
The purpose of the invention is realized by the following technical scheme:
a multifluid mixing apparatus comprising a housing 5, a heat exchange tube bundle 6 mounted within the housing, characterized in that: the device also comprises a fluid distributor 1, a main fluid mixer 2, an auxiliary fluid mixer 3 and a central pipe 4; the fluid distributor 1 is positioned at one end of the shell; the fluid distributor 1 comprises a pipeline 11, a cavity upper cover 12 and a cavity lower cover 13, an inner cavity is formed by the cavity upper cover 12 and the cavity lower cover 13, the pipeline 11 is communicated with the inner cavity, the cavity lower cover 13 is provided with small holes 14, and a C fluid enters the inner cavity of the fluid distributor through the pipeline and then enters the cavity formed by the fluid distributor and the shell through the small holes; the central tube 4 is inserted into the shell from the top end of the fluid distributor 1 to be close to the other end of the shell; the main fluid mixer 2 comprises a first guide pipe 21 fixed by the fluid distributor 1, the first guide pipe 21 is coaxially arranged with the central pipe 4 and forms an annular gap with the central pipe 4, and a first cyclone sheet 22 is arranged on the inner wall of the first guide pipe 21; the auxiliary fluid mixer 3 comprises a second flow guide pipe 31 positioned in the shell, the diameter of the second flow guide pipe 31 is smaller than that of the first flow guide pipe 21, the second flow guide pipe 31 is coaxially arranged with the central pipe 4 and forms an annular gap with the central pipe 4, a second vortex sheet 32 is arranged on the inner wall of the second flow guide pipe 31, and the outlet end of the second flow guide pipe 31 is positioned in a cavity formed by the fluid distributor 1 and the shell; the other end of the shell 5 is provided with a fluid inlet 7 communicated with an annular gap between the second flow guide pipe 31 and the central pipe 4, fluid A enters the auxiliary fluid mixer 3 through the annular gap between the central pipe 4 and the second flow guide pipe 31, and enters a cavity formed by the fluid distributor 1 and the shell in a swirling manner from the outlet end of the second flow guide pipe 31 through the flow guide of the second flow guide pipe 31 and the swirling action of the second swirling sheet 32.
The diameters of the central tube 4, the first flow duct 21 and the second flow duct 31 are determined by the A, B, C fluid volume flow rate.
Preferably, one end of the central tube 4 close to the fluid inlet 7 is closed, at least one distribution tube is arranged on the tube wall of the central tube 4 close to the closed end, the distribution tube passes through an annular gap between the central tube 4 and the second flow guide tube 31, and the fluid B flows through the central tube 4 to the other end of the multi-fluid mixing device and then enters the tube side of the heat exchange tube bundle through the distribution tube.
Preferably, the housing 5 comprises a cylinder and a sealing head arranged at one end of the cylinder.
Preferably, the number of the pipes 11 is at least 1. When the number of the pipelines 11 is at least 2, the pipelines 11 are uniformly distributed on the cavity upper cover 12.
Preferably, the upper cover 12 of the cavity is a seal head; the cavity lower cover 13 is in a circular truncated cone shape, and the inclination angle (alpha) between the cavity lower cover 13 and the horizontal plane is 15-75 degrees, preferably 30-60 degrees, so that the fluid in the inner cavity of the fluid distributor 1 enters the cavity formed by the fluid distributor and the shell at a certain angle.
Preferably, the diameter of the small hole 14 is 1-25 mm, preferably 5-10 mm.
Preferably, the first cyclone plate 22 is installed on the inner wall of the first flow guide pipe 21; the second swirl plate 32 is arranged on the inner wall of the second flow guide pipe 31 near the outlet end.
The elevation angle of the first cyclone plate 22 and the horizontal plane is 15-75 degrees, preferably 30-45 degrees; the number of the first cyclone pieces 22 is 4-36, preferably 8-16. The elevation angle of the second vortex sheet 32 and the horizontal plane is 15-75 degrees, preferably 30-45 degrees; the number of the second rotational flow sheets 32 is 2-24, preferably 4-12.
Further preferably, the first and second vanes 22, 32 are oriented in the same direction, and the number of the first vanes 22 is not less than the number of the second vanes 32.
By adopting the multi-fluid mixing device, the fluid C (generally cold fluid) enters the inner cavity of the fluid distributor 1 through the pipeline 11, and the space of the inner cavity is far higher than the sectional area of the pipeline, so that the fluid C has lower flow velocity in the inner cavity, and enters the cavity formed by the fluid distributor 1 and the shell at a certain angle after passing through the small hole 14 formed in the lower cover 13 of the cavity; the fluid B flows through the central pipe 4 to the other end of the multi-fluid mixing device, is distributed to the tube pass of the heat exchange tube bundle, and is mixed with the fluid A after heat exchange; fluid A enters the auxiliary fluid mixer 3 through the annular gap between the central pipe 4 and the second flow guide pipe 31, the fluid A leaves the auxiliary fluid mixer 3 through the flow guide of the second flow guide pipe 31 and the rotational flow effect of the second rotational flow sheet 32, the fluid A is mixed with the fluid B and the fluid C through heat exchange in a cavity formed by the fluid distributor 1 and the shell through the rotational flow effect of the auxiliary fluid mixer 3, A, B, C mixed fluid after primary rotational flow enters the main fluid mixer 2, and the flow guide of the first flow guide pipe 21 and the rotational flow effect of the first rotational flow sheet 22 are realized, so that the effects of high-efficiency uniform mixing and low flow resistance of various fluids are realized.
Typically, A, B, C are independent fluids, but A, B, C may be the same fluid, but the temperatures are not all the same.
Another object of the present invention is to provide an ammonia synthesis reactor, comprising an outer cylinder and an inner member, wherein an annular space is formed between the outer cylinder and the inner member; the internal member comprises a first radial basket 51, a second radial basket 53 and a third radial basket 55 which are sequentially arranged from top to bottom, wherein ammonia synthesis catalysts are respectively filled in the first radial basket 51, the second radial basket 53 and the third radial basket 55 to form a first catalytic bed, a second catalytic bed and a third catalytic bed, a multi-fluid mixing device provided by the invention is arranged in the first radial basket 51 to serve as an upper interlayer heat exchanger 52, a lower interlayer heat exchanger 54 is arranged in the second radial basket 54, a central pipe 4 of the upper interlayer heat exchanger 52 extends into the lower interlayer heat exchanger 54, an outlet of the central pipe 4 is positioned at the near bottom end of the lower interlayer heat exchanger 54, and a second guide pipe 31 of the upper interlayer heat exchanger 52 is communicated with the top end of the lower interlayer heat exchanger 54; the upper interlayer heat exchanger 52 is provided with a downcomer 58, one end of the downcomer 58 extends out of the upper interlayer heat exchanger 52 to the outside of the first radial basket 51, and the other end extends to the lower end of the upper interlayer heat exchanger 52; and a radial flow gas distributor and a radial flow gas collector are arranged in the third radial basket, and a gas outlet pipe 56 is arranged at the bottom of the high-pressure outer cylinder.
Compared with the prior art, the invention has the beneficial effects that:
the fluid distributor, the main fluid mixer and the auxiliary fluid mixer of the multi-fluid mixing device are concentrically arranged by the central pipe, so that the fluid distributor, the main fluid mixer and the auxiliary fluid mixer are coaxially arranged into an organic whole, the manufacturing precision of the device is high, the central positioning of each flow channel is not influenced by different temperatures of the fluid to generate deviation, the adverse influence caused by different expansion amounts of parts due to the change of the temperature of the fluid can be overcome, the processing and manufacturing precision is high, and the uniformity of fluid mixing is improved.
The main fluid mixer and the auxiliary fluid mixer have the same direction of the rotational flow sheets, the number of the rotational flow sheets of the main fluid mixer is higher than that of the rotational flow sheets of the auxiliary fluid mixer, so that the fluid can realize two times of homodromous rotational flow mixing in a smaller space, the mixed fluid spirally rises (or falls), the fluid has the function of mutual entrainment, the mixing strength and the mixing effect of the fluid are improved, and the pressure drop of the fluid is reduced.
The multi-fluid mixing device has the advantages of wide application range, large operation elasticity, good fluid distribution effect, low flow resistance and safe and reliable operation, and is suitable for occasions where various fluids are uniformly mixed, in particular to a gas phase reactor in the field of chemical industry.
Drawings
FIG. 1 is a schematic structural view of a multi-fluid mixing apparatus of the present invention;
FIG. 2 is a schematic view of a fluid distributor;
FIG. 3 is a schematic diagram of the structure of the main fluid mixer
FIG. 4 is a schematic structural view of the auxiliary fluid mixer;
FIG. 5 is a schematic diagram of the structure of an ammonia synthesis reactor employing the multi-fluid mixing apparatus of example 1;
FIG. 6 is a schematic diagram of the structure of an ammonia synthesis reactor employing a cold quench distributor (CN 203440099U).
In the figure: 1-a fluid distributor; 2-main fluid mixer; 3-an auxiliary fluid mixer; 4-a central tube; 5-a shell; 6-a heat exchange tube bundle; 7-a fluid inlet; 11-a pipeline; 12-upper cover of cavity; 13-a lower cover of the cavity; 14-a small hole; 21-a first draft tube; 22-a first spinning disk; 31-a second draft tube; 32-a second spinning disk; 51-a first radial basket; 52-upper interlayer heat exchanger; 53-a second radial basket; 54-lower-level intermediate heat exchanger; 55-a third radial basket; 56-air outlet pipe; 57-a quench distributor; 58-down comer.
Detailed Description
The technical solution of the present invention is further explained by the following embodiments.
Example 1
As shown in fig. 1-4, a multi-fluid mixing device comprises a housing 5, a heat exchange tube bundle 6 mounted in the housing, a fluid distributor 1, a primary fluid mixer 2, a secondary fluid mixer 3, a central tube 4; the shell 5 comprises a cylinder body and a seal head arranged at one end of the cylinder body, the seal head is provided with a fluid inlet 7, the other end of the shell 5 is provided with a fluid distributor 1, and the fluid distributor 1 and the shell form a cavity; the fluid distributor 1 comprises a pipeline 11, a cavity upper cover 12 and a cavity lower cover 13, wherein the cavity upper cover 12 is a seal head, the cavity lower cover 13 is in a circular truncated cone shape, the inclination angle (alpha) of the cavity lower cover 13 and the horizontal plane is 45 degrees, an inner cavity is formed by the cavity upper cover 12 and the cavity lower cover 13, the pipeline 11 is communicated with the inner cavity, the cavity lower cover 13 is provided with small holes 14, a fluid C enters the inner cavity of the fluid distributor through the pipeline and then enters the cavity formed by the fluid distributor and the shell through the small holes at a certain angle; the central tube 4 is inserted into the shell from the top end of the fluid distributor 1 to be close to the other end of the shell, one end of the central tube 4 close to the fluid inlet 7 is closed, at least one distribution tube is arranged on the tube wall of the central tube 4 close to the closed end, the distribution tube penetrates through an annular gap between the central tube 4 and the second guide tube 31, and the fluid B flows through the central tube 4 to be redistributed to the tube pass of the heat exchange tube bundle at the other end of the multi-fluid mixing device; the main fluid mixer 2 comprises a first guide pipe 21, the first guide pipe 21 is fixed by the fluid distributor 1, and the first guide pipe 21 is coaxially arranged with the central pipe 4 and forms an annular gap with the central pipe 4; a first cyclone sheet 22 is arranged in an annular gap between the first draft tube 21 and the central tube 4; the auxiliary fluid mixer 3 comprises a second guide pipe 31 positioned in the shell, the outlet end of the second guide pipe 31 is positioned in a cavity formed by the fluid distributor 1 and the shell, the second guide pipe 31 and the central pipe 4 are coaxially arranged and form an annular gap with the central pipe 4, and the annular gap between the second guide pipe 31 and the central pipe 4 is communicated with the fluid inlet 7 so that the fluid A enters the annular gap between the central pipe 4 and the second guide pipe 31; a second swirl plate 32 having the same direction as the first swirl plate 22 is installed in the annular space between the second flow tube 31 and the central tube 4 near the outlet end of the second flow tube 31.
The number of the pipelines 11 is 2, and the 2 pipelines 11 are symmetrically distributed.
The diameter of the first draft tube 21 is larger than that of the second draft tube 31.
The diameter of the small hole 14 is 10 mm.
First spinning disk 22 fix on the inner wall of first honeycomb duct 21, the angle of elevation of first spinning disk 22 and horizontal plane is 45, and the quantity of first spinning disk 22 is 16.
The second spinning disk 32 fix on the inner wall of second honeycomb duct 31, the angle of elevation 60 of second spinning disk 32 and horizontal plane, the quantity of second spinning disk 32 is 8.
By adopting the multi-fluid mixing device of the embodiment, the fluid C (generally a cold fluid) enters the inner cavity of the fluid distributor 1 through the pipeline 11, and the space of the inner cavity is far higher than the sectional area of the pipeline, so that the fluid C with lower flow velocity in the inner cavity enters the cavity formed by the fluid distributor 1 and the shell at a certain angle after passing through the small hole 14 (the hole flow velocity is generally 15-45 m/s) formed in the lower cover 13 of the cavity; the fluid B flows through the central pipe 4 to the other end of the multi-fluid mixing equipment and is distributed to the tube pass of the heat exchange tube bundle for heat exchange; fluid A enters the auxiliary fluid mixer 3 through the annular gap between the central pipe 4 and the second flow guide pipe 31, the fluid A leaves the auxiliary fluid mixer 3 through the flow guide of the second flow guide pipe 31 and the rotational flow effect of the second rotational flow sheet 32, the fluid A is mixed with the fluid B and the fluid C through heat exchange in a cavity formed by the fluid distributor 1 and the shell, A, B, C mixed fluid after primary rotational flow enters the main fluid mixer 2, and the flow guide of the first flow guide pipe 21 and the rotational flow effect of the first rotational flow sheet 22 are realized, so that the effects of high-efficiency uniform mixing and low flow resistance of various fluids are realized.
Example 2
As shown in FIG. 5, a typical ammonia synthesis reactor, using the multi-fluid mixing device of example 1 for gas mixing, other components are known, and the skilled person will be able to carry out this solution based on the solution of the present example and the common general knowledge in the art. The ammonia synthesis reactor consists of a high-pressure outer cylinder and an internal part, and an annular gap is formed between the high-pressure outer cylinder and the internal part; the internal parts comprise a first radial basket 51, a second radial basket 53 and a third radial basket 55 which are sequentially arranged from top to bottom, wherein ammonia synthesis catalysts are respectively filled in the first radial basket 51, the second radial basket 53 and the third radial basket 55 to form a first catalytic bed, a second catalytic bed and a third catalytic bed, an upper interlayer heat exchanger 52 (multi-fluid mixing equipment in embodiment 1) and a lower interlayer heat exchanger 54 (conventional heat exchanger) are respectively arranged in the first radial basket 51 and the second radial basket 54, a central pipe 4 (two ends of the central pipe 4 are open or one end of the central pipe extending into the lower interlayer heat exchanger 54 is closed, a distribution hole is formed in the pipe wall close to the closed end) of the upper interlayer heat exchanger 52 extends into the lower interlayer heat exchanger 54, the outlet of the central pipe is positioned at the near bottom end of the lower interlayer heat exchanger 54, and a second guide pipe 31 of the upper interlayer heat exchanger 52 is communicated with the top end of the lower interlayer heat exchanger 54; the upper interlayer heat exchanger 52 is provided with a downcomer 58, one end of the downcomer 58 extends out of the upper interlayer heat exchanger 52 to the outside of the first radial basket 51, and the other end extends to the lower end of the upper interlayer heat exchanger 52, so that fluid at the top of the reactor enters the tube side of the upper interlayer heat exchanger 52 to exchange heat with hot gas after the reaction of the first catalyst bed; and a radial flow gas distributor and a radial flow gas collector are arranged in the third radial basket, and a gas outlet pipe 56 is arranged at the bottom of the high-pressure outer cylinder.
f1Main line gas, f0Cold shock gas, f2The process gas composition is hydrogen nitrogen (hydrogen content is 70-75%, nitrogen content is 24-26%, ammonia content is 2-3%, and the rest is a small amount of inert gases such as methane, argon and the like1Main line gas, f0Cold shock gas, f2The temperature of the process gas is the same and ranges from 165 ℃ to 170 ℃.
f1The main line gas enters an annular gap between the high-pressure outer cylinder and the internal part from the bottom of the ammonia synthesis tower reactor, rises to the top of the reactor, enters the tube pass of the upper interlayer heat exchanger 52 through the downcomer 58, and exchanges heat with the hot gas after the reaction of the first catalyst bed; f. of2The process gas enters the central tube 4 from the top of the ammonia synthesis tower reactor, enters the tube pass of the lower-layer interlayer heat exchanger 54, exchanges heat with hot gas after the reaction of a second catalytic bed, then rises through the annular gap between the second guide tube 31 of the upper-layer interlayer heat exchanger 52 and the central tube 4, and finally leaves the auxiliary fluid mixer through the second cyclone sheet; cold air secondary line f for regulating zero meter temperature0The cold shock gas pipeline 11 enters the cavity of the fluid distributor, and then is distributed through the small holes of the lower cover of the cavity and exchanges heat with the f1Main line gas mixing, mixed f0、f1Gas and heat exchanged f from auxiliary fluid mixer2The process gas is mixed and enters a main fluid mixer, and f is enabled to be mixed through the rotational flow mixing action of a first rotational flow sheet0、f1、f2Gas is mixed evenly, three paths f after mixing0、f1、f2The gas enters a first catalytic bed in sequence to carry out ammonia synthesis reaction; the hot gas after reaction sequentially passes through the shell pass of the upper interlayer heat exchanger 52 and f1The main gas exchanges heat and then enters the second catalystFluidized bed reaction, shell pass and f of the lower inter-layer heat exchanger 542The process gas exchanges heat, enters the third catalytic bed for reaction, and finally leaves the reactor through the gas outlet pipe 56. The temperature and the flow of the process gas at the inlet of the reactor are regulated, so that the ammonia synthesis reaction is ensured to be in a better working state.
As shown in FIG. 6, the reactor is also a typical ammonia synthesis reactor, but the difference is that the gas mixing is carried out by using a quench distributor 57(CN203440099U) of a ring-shaped distribution pipe mixing structure, the quench distributor is a ring-shaped distribution pipe, small holes are arranged on the ring pipe, and the quench distributor is of a split structure. f. of1The main line gas enters the annular space between the high-pressure outer cylinder and the internal part from the bottom of the ammonia synthesis tower reactor, rises to the top of the reactor, then enters the bottom of the upper interlayer heat exchanger through a downcomer and comes from the f after heat exchange2The process gas is mixed and enters the tube pass of the upper interlayer heat exchanger to exchange heat with hot gas after the reaction of the process gas and the first catalyst bed; f. of2The process gas enters from the top of the reactor of the ammonia synthesis tower, enters the tube pass of the lower-layer intermediate heat exchanger through the central tube, exchanges heat with the hot gas after the reaction of the second catalyst bed, and the heat exchanged f2The process gas enters the bottom of the upper interlayer heat exchanger and f1Mixing the main line gas and entering a tube pass of the upper interlayer heat exchanger; cold air secondary line f for regulating zero meter temperature0The cold shock gas enters the annular distribution pipe and is distributed through the small holes of the annular distribution pipe and then exchanges heat with the gas f1、f2Mixing the gases, and mixing the three paths f0、f1、f2The gas enters a first catalytic bed in sequence to carry out ammonia synthesis reaction; the reacted hot gas passes through the shell side heat exchange of the upper interlayer heat exchanger 52 in sequence, enters the second catalytic bed for reaction, passes through the shell side heat exchange of the lower interlayer heat exchanger 54, enters the third catalytic bed for reaction, and finally leaves the reactor through the gas outlet pipe 56.
TABLE 1 Ammonia Synthesis reactor operating parameters
As can be seen from table 1, under the condition that the specifications, operating pressures, ammonia yields, and other parameters of the ammonia synthesis reactor are substantially the same, the temperature distribution of each section of bed of the ammonia synthesis reactor using the multi-fluid mixing apparatus of the present invention is good, and the temperature difference is small, such as 2 ℃ of the temperature difference at the inlet of the first bed (4.4 ℃ in the conventional structure) and 7.6 ℃ of the maximum temperature difference at the outlet of the first bed (17.9 ℃ in the conventional structure); because the reaction temperature is well distributed, the net value of ammonia is higher, the resistance of the reactor is lower, the total flow of the inlet of the reactor is lower, and the energy conservation and consumption reduction of the system are facilitated.
Claims (10)
1. A multi-fluid mixing apparatus comprising a housing (5), a heat exchanger tube bundle (6) mounted within the housing, characterized in that: the device also comprises a fluid distributor (1), a main fluid mixer (2), an auxiliary fluid mixer (3) and a central pipe (4); the fluid distributor (1) is positioned at one end of the shell and comprises a pipeline (11), a cavity upper cover (12) and a cavity lower cover (13), an inner cavity is formed by the cavity upper cover (12) and the cavity lower cover (13), the pipeline (11) is communicated with the inner cavity, and the cavity lower cover (13) is provided with a small hole (14); the central tube (4) is inserted into the shell from the top end of the fluid distributor (1) to be close to the other end of the shell; the main fluid mixer (2) comprises a first guide pipe (21) fixed by the fluid distributor (1), the first guide pipe (21) and the central pipe (4) are coaxially arranged and form an annular gap with the central pipe (4), and a first spinning disk (22) is arranged on the inner wall of the first guide pipe (21); the auxiliary fluid mixer (3) comprises a second guide pipe (31) positioned in the shell, the diameter of the second guide pipe (31) is smaller than that of the first guide pipe (21), the second guide pipe (31) and the central pipe (4) are coaxially arranged and form an annular gap with the central pipe (4), a second vortex sheet (32) is arranged on the inner wall of the second guide pipe (31), and the outlet end of the second guide pipe (31) is positioned in a cavity formed by the fluid distributor (1) and the shell; the other end of the shell (5) is provided with a fluid inlet (7) communicated with the annular gap between the second guide pipe (31) and the central pipe (4).
2. The multi-fluid mixing apparatus according to claim 1, wherein: the one end that center tube (4) is close to fluid inlet (7) seal, set up an at least distributing pipe at the pipe wall that center tube (4) is close to the closed end, distributing pipe pass the annular space between center tube (4) and second honeycomb duct (31).
3. The multi-fluid mixing apparatus according to claim 1, wherein: the upper cover (12) of the cavity is a seal head; the cavity lower cover (13) is in a circular truncated cone shape, and the inclination angle of the cavity lower cover (13) and the horizontal plane is 15-75 degrees.
4. The multi-fluid mixing apparatus according to claim 3, wherein: the inclination angle between the cavity lower cover (13) and the horizontal plane is 30-60 degrees.
5. The multi-fluid mixing apparatus according to claim 1, wherein: the diameter of the small hole (14) is 1-25 mm, preferably 5-10 mm.
6. The multi-fluid mixing apparatus according to claim 1, wherein: the second cyclone plate (32) is arranged on the inner wall of the second flow guide pipe (31) close to the outlet end.
7. The multi-fluid mixing apparatus according to claim 1, wherein: the elevation angle of the first rotational flow sheet (22) and the horizontal plane is 15-75 degrees; the number of the first rotational flow sheets (22) is 4-36; the elevation angle of the second rotational flow sheet (32) and the horizontal plane is 15-75 degrees; the number of the second rotational flow plates (32) is 2-24.
8. The multi-fluid mixing apparatus according to claim 7, wherein: the elevation angle of the first rotational flow sheet (22) and the horizontal plane is 30-45 degrees; the number of the first rotational flow sheets (22) is 8-16; the elevation angle of the second rotational flow sheet (32) and the horizontal plane is 30-45 degrees; the number of the second rotational flow plates (32) is 4-12.
9. The multi-fluid mixing apparatus according to claim 7 or 8, wherein: the direction of first spinning disk (22) and second spinning disk (32) is unanimous, and the quantity of second spinning disk (32) is no less than to the quantity of first spinning disk (22).
10. An ammonia synthesis reactor comprises an outer cylinder and an inner part, wherein an annular space is formed between the outer cylinder and the inner part; the internal member comprises a first radial basket (51), a second radial basket (53) and a third radial basket (55) which are sequentially arranged from top to bottom, wherein the first radial basket (51), the second radial basket (53) and the third radial basket (55) are respectively filled with ammonia synthesis catalysts to form a first catalytic bed, a second catalytic bed and a third catalytic bed; a radial flow gas distributor and a radial flow gas collector are arranged in the third radial basket, and a gas outlet pipe (56) is arranged at the bottom of the outer cylinder; the method is characterized in that: arranging a multi-fluid mixing device as claimed in claim 1 in said first radial basket (51) as an upper inter-layer heat exchanger (52), arranging a lower inter-layer heat exchanger (54) in said second radial basket (54), wherein the central pipe (4) of the upper inter-layer heat exchanger (52) extends into the lower inter-layer heat exchanger (54) and the outlet of the central pipe (4) is located at the near bottom end of the lower inter-layer heat exchanger (54), and the second flow guide pipe (31) of the upper inter-layer heat exchanger (52) is communicated with the top end of the lower inter-layer heat exchanger (54); a descending pipe (58) is arranged on the upper interlayer heat exchanger (52), one end of the descending pipe (58) extends out of the upper interlayer heat exchanger (52) to the outside of the first radial basket (51), and the other end of the descending pipe extends to the lower end of the upper interlayer heat exchanger (52).
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