CN203955188U - For the feed distributor of ammonia oxidation reactor - Google Patents
For the feed distributor of ammonia oxidation reactor Download PDFInfo
- Publication number
- CN203955188U CN203955188U CN201420150619.6U CN201420150619U CN203955188U CN 203955188 U CN203955188 U CN 203955188U CN 201420150619 U CN201420150619 U CN 201420150619U CN 203955188 U CN203955188 U CN 203955188U
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- Prior art keywords
- distributor
- reactor
- feed
- ammonia
- header tube
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 144
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 72
- 230000003647 oxidation Effects 0.000 title claims abstract description 23
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 23
- 239000003054 catalyst Substances 0.000 claims abstract description 43
- 239000000203 mixture Substances 0.000 claims description 55
- 239000012530 fluid Substances 0.000 claims description 32
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 15
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 15
- 239000004215 Carbon black (E152) Substances 0.000 claims description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 6
- 229930195733 hydrocarbon Natural products 0.000 claims description 6
- 150000002430 hydrocarbons Chemical class 0.000 claims description 6
- 229920006395 saturated elastomer Polymers 0.000 claims description 6
- 239000001273 butane Substances 0.000 claims description 3
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- 239000001294 propane Substances 0.000 claims description 3
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 claims description 3
- 238000013461 design Methods 0.000 description 23
- 239000007789 gas Substances 0.000 description 20
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 16
- 238000000034 method Methods 0.000 description 12
- 238000003466 welding Methods 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 230000008439 repair process Effects 0.000 description 5
- 238000013459 approach Methods 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000005243 fluidization Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000001066 destructive effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005553 drilling Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 150000004767 nitrides Chemical class 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Abstract
The utility model relates to a kind of feed distributor for ammonia oxidation reactor.By disconnecting fast by air-tightness that accessory is attached to each section of distributor each other and the wall of reactor is convenient for changing the different portions section of the feed distributor using in commercial ammonia oxidation reactor.In addition, be changed to be conducive to the Uniform Flow by the feed gas of these parts at the diameter of these Duan Zhongzhi of distributor portion pipelines and the diameter that is attached to the feed nozzle of these arms.Distributor can be subdivided into the multiple feed distributor portion section of arranging for better reactor control.Finally, the end cap that is terminated at the far-end of distributor branch pipes pipeline can be provided with nozzle, for removing any ammoxidation catalyst that may not inadvertently arrive distributor inside.
Description
Technical field
The utility model relates to a kind of feed distributor for ammonia oxidation reactor.
Background technology
In the business of acrylonitrile is manufactured, propylene, ammonia and oxygen react according to following reaction scheme one:
CH
2=CH-CH
3?+?NH
3?+?3/2?O
2?→?CH
2=CH-CN+?3?H
2O
This process that is commonly referred to ammoxidation is at high temperature carried out with gas phase under the existence of suitable fluid bed ammoxidation catalyst.
Fig. 1 shows the typical ammonia oxidation reactor for carrying out this process.As shown in the drawing, reactor 10 comprises reactor wall 12, air grid 14, feed distributor (sparger) 16, cooling coil 18 and cyclone (cyclone) 20.In the normal operation period, plant air is filled with in reactor 10 by air intake 22, and the mixture of propylene and ammonia is filled with in reactor 10 by feed distributor 16.Both flows are all enough high, so that propylene and the ammonia catalytic ammoxidation to acrylonitrile occurs bed 24 fluidisations of the ammoxidation catalyst of inside reactor therein.
The product gas being produced by reaction exports 26 by reactor effluent and leaves reactor 10.Before doing like this, product gas is through cyclone 20, and cyclone 20 is removed any ammoxidation catalyst that these gases can be carried secretly, to turn back to catalyst bed 24 by dipleg (diplegs) 25.Ammoxidation is height heat release, therefore takes away excessive heat with cooling coil 18, thereby reaction temperature is remained on to proper level.
Propylene and ammonia can form explosive mixture with oxygen.But, under normal running temperature, carrying out prevent exploding in reactor 10 inside by the ammoniation catalyst of fluidisation, this catalyst is preferential catalytic ammoxidation reaction before blast can occur.Correspondingly, reactor 10 is designed and is operable to that to make the unique place that allows in the normal operation period plant air to contact propylene and ammonia be in the fluid bed of ammoxidation catalyst 24, and therefore only at the temperature height of catalyst when being enough to catalytic ammoxidation reaction.
For this reason, the traditional approach that propylene and ammonia are fed to reactor 10 uses such as at U.S. 5,256, the feed distributor system 16 shown in 810, and the disclosure of this patent is incorporated herein by reference.As shown in Fig. 1 of ' 810 patents and Fig. 2 (this two width figure is renumberd Fig. 2 and the Fig. 3 for the literature), feed distributor 16 is taked the form of a series of supply pipes or pipeline, it comprises main collector 30 and arm (lateral) 32, and arm 32 is attached to collector 30 and separates from collector 30.A series of prone feed nozzles 34 are limited in collector 30 and arm 34, and the mixture of propylene and ammonia was filled with by feed nozzle 34 in normal reaction device operating period.The number of arm 32 and feed nozzle 34 and spacing make to be roughly positioned with equably every square metre of approximately 10 to 30 feed nozzles altogether across the whole cross-sectional area of reactor 10.
Conventionally, each feed nozzle 34 is fed guard shield 36 and surrounds, and charging guard shield 36 is taked the form of the short portion section of pipeline, and the internal diameter of this pipeline is the several times of the diameter of nozzle 34.Charging guard shield 34 can significantly slow down leaving before entering catalyst bed 24 speed of the gas that passes nozzle 10, and this has prevented the disintegration of original generable catalyst.
Plant air enters catalyst bed 24 (Fig. 1) conventionally after passing air grid 14, and air grid 14 is positioned at feed distributor 16 belows.As the well-known, air grid 14 is taked the form of continuous metal sheet conventionally, and it is limited to a series of airports or nozzle wherein.The diameter of air nozzle, through the mass flow of the plant air of air grid 14 and through the mass flow of propylene/ammonia mixture of feed distributor 16 through selecting, make ammoxidation catalyst in catalyst bed 24 in the normal operation period by the complete fluidisation of these gases.
Air nozzle is typically provided with its oneself protective atmosphere guard shield (not shown), and this guard shield is usually located at air grid 14 belows.In addition, in many cases, air nozzle in feed nozzle 34 and air grid 14 is with one-one relationship setting, and wherein each charging guard shield 36 is directly aimed at its corresponding air nozzle to promote to pass the mixing fast and fully of gas of these two kinds of different nozzles.Referring to U.S. 4,801,731.
Although propylene/ammonia feed system of this general type is respond well, there is some shortcoming in it really.For example, owing at high temperature continuing to be exposed to ammonia, form the metal of feed distributor 16 and pass in time and experience nitrogenize.As a result, each section of feed distributor 16 and sometimes whole feed distributor need to frequently be changed.Cost is very high for this, particularly because reactor in the time changing must dead halt.
The Second Problem being associated with this propylene/ammonia feed system is the inhomogeneities of operation.This not only adversely affects the productivity ratio of system, but also has caused inhomogeneous nitrogenize, and this has further increased the weight of nitrogenize problem.
Utility model content
According to the utility model, a kind of new feed distributor design is provided, it has significantly reduced these problems, and has roughly eliminated problem completely in some cases.
According to this new distributor designs feature, use air-tightness to disconnect fast accessory and the main header tube of distributor is attached to the wall of the reactor that main header tube passes, or the various pipelines that form feed distributor are connected to each other, or both.Due to this feature, when changing because excessive nitrogenize becomes if desired, change the required time of some or all of feed distributors and work and significantly reduce.
According to another feature of this new distributor designs, along with the entrance from feed distributor increases to the travel path of each feed nozzle, the relative diameter of feed nozzle 34 increases slightly.Due to this feature, become more approaching even feed nozzle through the mass flow containing ammonia incoming mixture of each feed nozzle.This causes again inside reactor between region, more to approach uniform operation, and this can maximize productivity ratio.This feature also by guaranteeing that the gas of correct flow flows through all the time distributor feed nozzle and carrys out minimum catalyst and flow backwards (back up), that is, is starting, is shutting down and the even pollution of catalyst to feed distributor during normal operating.
According to another feature of this new distributor designs, from its near-end to its far-end, (end that, is connected to main header tube from it is end away from main header tube to it) reduces the diameter of arm 32.Due to this feature, flow through the speed containing ammonia incoming mixture of these arms along the whole length of arm and especially enough high in its far-end maintenance, be purged to next feed nozzle 34 with any ammoxidation catalyst that can exist, to discharge from arm is inner by this feed nozzle.
According to this newly-designed another feature, feed distributor 16 is subdivided into multiple feed distributor portion section, and each section has its oneself ingress port for receiving containing ammonia charging from reactor is outside.Due to this feature, can realize reactor in interregional better control, because independent control system can be used to monitor individually and control the operation in each feed distributor portion section.
Therefore, the utility model provides a kind of improved distributor in one embodiment, for using containing ammonia incoming mixture from ammonia oxidation reactor outside by the reactor wall of reactor and to supply in the fluid bed of the ammoxidation catalyst of inside reactor, this improved distributor comprises: main header tube; Distributor entrance, it is communicated with main header tube fluid, and this distributor entrance is attached to reactor wall rigidly; And multiple branch road distributor pipelines, it is communicated with main collector distributor pipeline fluid, this branch road distributor pipeline limits feed nozzle for propylene/ammonia incoming mixture is entered in the fluid bed of ammoxidation catalyst, and wherein distributor entrance disconnects fast accessory by means of air-tightness and is attached to rigidly reactor wall.
In another embodiment, the utility model provides a kind of improved distributor, for using containing ammonia incoming mixture from ammonia oxidation reactor outside by the reactor wall of reactor and to supply in the fluid bed of the ammoxidation catalyst of inside reactor, this improved distributor comprises: main header tube; Distributor entrance, it is communicated with main header tube fluid; And multiple branch road distributor pipelines, it is communicated with main collector distributor pipeline fluid, this branch road distributor pipeline limits feed nozzle for entering in the fluid bed of ammoxidation catalyst containing ammonia incoming mixture, and wherein at least some in branch road distributor pipeline disconnect fast accessory by corresponding air-tightness and are attached to main header tube.
In yet another embodiment, the utility model provides a kind of improved distributor, for using containing ammonia incoming mixture from ammonia oxidation reactor outside by the reactor wall of reactor and to supply in the fluid bed of the ammoxidation catalyst of inside reactor, this improved distributor comprises: main header tube; Distributor entrance, it is communicated with main header tube fluid; And multiple branch road distributor pipelines, it is communicated with main collector distributor pipeline fluid, each branch road distributor pipeline limits feed nozzle for entering in the fluid bed of ammoxidation catalyst containing ammonia incoming mixture, wherein feed nozzle has at least two kinds of different sizes, wherein less feed nozzle is positioned at more close distributor porch, and larger nozzle is positioned at further from distributor porch, depend on that propylene/ammonia incoming mixture is from the distributor entrance distance to each nozzle by distributor of advancing.
In yet another embodiment, the utility model provides a kind of improved distributor, for using from ammonia oxidation reactor outside by the reactor wall of reactor and to supplying ammonia incoming mixture in the fluid bed of the ammoxidation catalyst of inside reactor, this improved distributor comprises: main header tube; Distributor entrance, it is communicated with main header tube fluid; And multiple branch road distributor pipelines, each branch road sparger tube road has the near-end that is communicated with main header tube fluid and the far-end away from main header tube, each branch road distributor pipeline is also defined for and will enters the feed nozzle in the fluid bed of ammoxidation catalyst containing ammonia incoming mixture, and wherein the diameter of at least some in branch road distributor pipeline reduces to its far-end from its near-end.
In yet another embodiment, the utility model provides a kind of improved distributor, for using containing ammonia incoming mixture from ammonia oxidation reactor outside by the reactor wall of reactor and to supply in the fluid bed of the ammoxidation catalyst of inside reactor, this improved distributor comprises: main header tube; Distributor entrance, it is communicated with main header tube fluid; And multiple branch road distributor pipelines, it is communicated with main collector distributor pipeline fluid, this branch road distributor pipeline limits feed nozzle for entering in the fluid bed of ammoxidation catalyst containing ammonia incoming mixture, wherein improved distributor is made up of the multiple feed distributor portion section that is arranged in inside reactor, each feed distributor portion section has its oneself distributor entrance, for from reactor outside, the system of the branch road distributor pipeline of its oneself main header tube and its oneself receives containing ammonia charging.
Brief description of the drawings
By understanding better the utility model with reference to the following drawings, in the accompanying drawings:
Fig. 1 is schematic diagram, and it shows the reactor portion section for the preparation of the conventional ammonia oxidation reactor of acrylonitrile;
Fig. 2 is plane, and it shows the downside of the conventional sparger system of the ammonia oxidation reactor of Fig. 1;
Fig. 3 is the cutaway view intercepting along the line 3-3 of Fig. 2, and Fig. 3 shows the feed nozzle and the charging guard shield being associated of the conventional sparger system of Fig. 2;
Fig. 4 is cutaway view, and the main header tube that shows the feed distributor of commercial ammonia oxidation reactor penetrates and be connected to the mode of the sidewall of reactor;
Fig. 5 is the cutaway view that is similar to Fig. 4, shows a feature of the present utility model, and wherein the main header tube of feed distributor penetrates and disconnect fast connector and be connected to by means of air-tightness the sidewall of reactor;
Fig. 6 is the side view that the air-tightness of Fig. 5 disconnects connector fast;
Fig. 7 is the cutaway view that is similar to Fig. 2, shows another feature of the present utility model, and wherein distributor branch pipes pipeline disconnects connector and be connected to the main header tube of distributor fast by means of air-tightness;
Fig. 8 is plane, and the air-tightness that illustrates in greater detail Fig. 7 disconnects connector fast;
Fig. 9 A and Fig. 9 B are according to the sectional view of the distributor branch pipes pipeline of another feature use of the present utility model, how show the diameter of this arm along with the distance apart from distributor header tube increases and reduces;
Figure 10 A, Figure 10 B and Figure 10 C are the sectional elevations of the distributor branch pipes pipeline of Fig. 9, and how the diameter that further shows this arm increases and to reduce with the distance apart from distributor header tube;
Figure 11 A, Figure 11 B, Figure 11 C and Figure 11 D are according to the vertical cutaway view of the distributor branch pipes end cap of another feature use of sparger system of the present utility model; And
Figure 12 is plane, and it shows another feature of the present utility model, and wherein the feed distributor of acrylonitrile reactor is subdivided into multiple feed distributor portion section.
Detailed description of the invention
Definition
As used herein, " fluid connection " refers to and is effective to allow identical liquid or steam to be sent to connection or the pipeline in another region from a region.
As used herein, " fixing releasedly " refers to non-being welded to connect that allows object to disconnect by non-destructive mode.For example, fix and can refer to bolt, crab-bolt, the flange being spirally connected and their combination releasedly.
As used herein, " containing ammonia incoming mixture " refers to ammonia and blend saturated and/or undersaturated C3 to C4 hydrocarbon.Saturated and/or undersaturated C3 to C4 hydrocarbon can comprise propane, propylene, butane, butylene and their mixture.
Disconnect fast connector
As described above, the subject matter running in the operation of commercial acrylonitrile reactor be feed distributor due to form its metal nitrogenize and pass and lost efficacy in time.In order to address this problem, propose by for example at U.S. 3,704 690, the anti-nitro-alloy shown in U.S. 4,401,153, U.S. 5,110,584 and EP 0 113 524 manufactures distributor.Regrettably, due to distinctive some problem of fluid catalyst ammoxidation reaction with and cost reason, proved this solution in commercial acrylonitrile reactor use be unsuccessful.
Simultaneously, U.S. 5,256,810 described a kind of for roughly eliminating the method for nitrogenize of distributor of commercial acrylonitrile reactor, the method is by using custom-designed blanket insulation to make the temperature of the ammonia of distributor inside keep enough low, to prevent nitrogenize.But due to cost and somewhat complex design, it is not satisfied that this solution is also proved to be.
According to this feature of the present utility model, the distributor designs that distributor this problem that passing was lost efficacy in time due to nitride metal can be changed each section of distributor and whole distributor as a whole by employing quickly and easily solves.Although still need acrylonitrile reactor to shut down in the time carrying out this replacing, compare conventional practice, realizing the time that this replacing spends shortens greatly.As a result, with regard to loss production time and human cost, significantly reduce for the totle drilling cost that solves this nitrogenize problem in continuous foundation.
Fig. 4, Fig. 5 and Fig. 6 show a feature of the present utility model, and wherein this distributor nitrogenize problem solves by using air-tightness to disconnect fast the outer wall that the entrance of sparger system is connected to ammonia oxidation reactor by connector.In the specific embodiment shown in these accompanying drawings, the end of main collector 30 is directly attached to the wall 40 of reactor 10.Therefore,, in this design, this collector end forms the entrance 31 of distributor portion section 16.In other design, intermediate duct can be used to distributor entrance 31 to be connected to collector 30.For convenient, in connection with the reactor design shown in Fig. 4, Fig. 5 and Fig. 6, this feature of the present utility model is described.But, should be appreciated that this feature and advantage thereof are applicable to other reactor design comparably, such as the design that for example wherein distributor entrance 31 separates by intermediate duct with main collector 30.
As shown in Figure 4, the usual manner that the distributor entrance 31 of feed distributor 16 is attached to the wall 40 of reactor 10 is by welding.Correspondingly, in the time that main header tube 30 need to be replaced, must adopt weld repairs method, wherein tightly be cut off by welding around the part reactor wall 40 of main header tube 30, the opening forming thus in shell of reactor 12 is by welding to repair with suitable patch, and new main header tube 30 is also arranged in the reactor wall 40 of repairing by welding.This needs the on-the-spot manpower of significant quantity and additional material, and this is with high costs.
According to this feature of the present utility model, the air-tightness that this problem is used for the main header tube 30 to be attached to reactor wall 40 by employing disconnects fast connector design and avoids.The example of such connector is shown in Fig. 5 and Fig. 6, there is shown " manhole " 42 with cylindrical sleeve 44 forms, the first side of cylindrical sleeve 44 is for good and all welded to the periphery 46 that is formed at the permanent opening 48 in reactor wall 40 with air tight manner.The opposite side of cylindrical sleeve 44 or the second side carrying flange 50, flange 50 is defined for a series of through holes of receiving therein bolt 52.Meanwhile, the hoop 54 of smooth circular slab form is permanently welded to the outside of main header tube 30 with air tight manner.In addition the hoop 54 a series of through holes 56 that also limit corresponding to the through hole in the flange 50 of manhole 42.
Utilize this structure, main header tube 30 can be fixed to releasedly simply to the reactor wall 40 of reactor 10 by the hoop of main header tube 30 54 being screwed to the flange 50 of manhole 42 with air tight manner.In an identical manner, can by hoop 54 is gone to be spirally connected from flange 50, main header tube 30 be separated with reactor wall 40 simply.Correspondingly, due to excessive nitrogenize becomes the replacing of disabled existing main collector 30 can be by simply going to be spirally connected and being spirally connected again process and simply and easily realizing.Owing to not needing Site Welding, so this replacing program implements much easier compared with the weld repairs method of carrying out routinely and cost is lower.
Fig. 2, Fig. 7 and Fig. 8 show another feature of the present utility model, wherein use air-tightness to disconnect fast connector to solve the problem of distributor branch pipes nitrogenize.As shown in Figure 2, be by welding by the usual manner that props up pipeline (or " arm ") 32 and be attached to main header tube (or " collector ") 30.Correspondingly, in the time that each arm 32 need to be replaced due to excessive nitrogenize, adopt weld repairs method, wherein old arm separates with main header tube 30 by welding or other suitable cutting technique, and new arm is arrived to main header tube 30 by weld attachment.This also needs the on-the-spot manpower of significant quantity, and this is with high costs.
According to this feature of the present utility model, the air-tightness that this problem is used for each arm 32 to be attached to main header tube 30 by employing disconnects fast connector design and avoids.This is shown in Fig. 7 and Fig. 8, and the air-tightness there is shown for each arm 32 being connected to the main header tube 30 of sparger system 16 disconnects connector 60 fast.Although these accompanying drawings show each arm and be directly connected to main header tube 30, should be appreciated that one or more in these arms can for example be connected to main header tube 30 by means of intermediate duct (not shown) indirectly.
Air-tightness disconnect fast connector 60 be the parts that wherein coordinate (, in the time connecting and together and the parts of removing in the time that connection is disconnected) specialized designs only becomes by mechanical means (, do not use and weld or adhesive) to join connector each other to.Air-tightness disconnects fast connector and is also designed to keep tight seal under hot conditions, and described hot conditions is for example run into during the temperature cycles occurring during the normal operating of typical commercial ammonia oxidation reactor and when when such reactor start-up and shutdown that.Be applicable to this purposes commercially available connector be exemplified as the Grayloc intermetallic endoporus sealing clamp connector that can derive from Grayloc Products (Houston, Texas).Another of the commercially available connector of applicable this purposes is exemplified as the Techlok fixture connector of the Vector group that can derive from Freudenberg Oil & Gas Technologies (Houston, Texas).Another of the commercially available connector of applicable this purposes is exemplified as the G-Lok that can derive from Australasian Fittings & Flanges (Osborne Park, WA, Australia)
?fixture connector.It is not too desirable for this application that conventional flange connects, because they are owing to being easy to leakage in the temperature cycles of reactor operating period.
Fig. 8 shows typical air-tightness and disconnects fast the structure of connector 60, comprises that this connector is interconnected to arm 30 mode of main header tube 30.As shown in the figure, connector 60 is formed by the clamp assembly 62 of hub 64 and 66 being received and keep together, and hub 64 and 66 is carried on the end of facing 68 and 70 of arm 32 and collector joint 72.When time in position by bolt 73, clamp assembly 62 causes metallic packing ring (not shown) to be fixed between hub 64 and 66 and engage hub 64 and 66 hermetically, thereby between arm 32 and collector 30, forms gas-tight seal.
By using air-tightness to disconnect fast connector 60, each arm 32 can be fixed to main header tube 30 by the clamp assembly 62 that is spirally connected or goes to be spirally connected simply and remove from main header tube 30.Correspondingly, due to excessive nitrogenize becomes the replacing of disabled existing arm 32 can be by simply going to be spirally connected and being spirally connected again process and realizing simply and easily.Owing to not needing Site Welding, this replacing program implements much easier compared with the weld repairs method of carrying out routinely and cost is lower.
Described various aspects can be used for having the reactor of various sizes diameter herein.One preferred aspect, reactor can have from approximately 2 to approximately 12, approximately 5 to approximately 12 meters on the other hand, approximately 8 to approximately 12 meters and the external diameter of approximately 9 to approximately 11 meters on the other hand on the other hand.
Variable feed nozzle size
According to another feature of this new distributor designs, along with the entrance from feed distributor increases to the travel path of each feed nozzle, the diameter of feed nozzle 34 increases slightly.
When containing ammonia incoming mixture while advancing by distributor 16, cause the temperature of the incoming mixture of distributor inside to increase from the heat transmission of the hot gas of distributor outside.As a result, the temperature of leaving the incoming mixture of each feed nozzle is different, specifically depends on how long incoming mixture time in distributor before leaving has.Particularly, leave that to be positioned at the temperature further from the incoming mixture of the feed nozzle of distributor porch hotter in the temperature of incoming mixture of leaving the feed nozzle that is positioned at more close distributor entrance.In this context, " further from " and " more close " should be understood to represent with regard to the length of travel path further from more close distributor entrance, this travel path starts from distributor porch and ends at incoming mixture and leaves the specific feed nozzle of distributor by it.
In conventional ammonia oxidation reactor, the diameter of feed nozzle 34 (Fig. 3) is all identical.As a result, be less than the density of the incoming mixture that the feed nozzle 34 by being positioned at more close distributor porch leaves by being positioned at the density of the incoming mixture leaving further from the feed nozzle 34 of distributor porch, because density and temperature are inversely proportional to.This cause again by be positioned at leave further from the feed nozzle 34 of distributor porch be less than the mass flow of the incoming mixture that the feed nozzle 34 by being positioned at more close distributor porch leaves containing the mass flow of ammonia incoming mixture, precondition is that other condition is identical, because mass flow is directly proportional to density.Regrettably, this inhomogeneity shortage of the mass flow by each feed nozzle causes on the whole lower than best reactor performance, because entering the amount (, the gross mass of unit interval) containing ammonia incoming mixture of the bed 24 of ammoxidation catalyst is less than in the region of more close this entrance of feed nozzle in the reactor area of distributor entrance at feed nozzle.
According to this feature of the present utility model, this problem overcomes by the size that changes distributor feed nozzle 34, is wherein positioned at further from those feed nozzles of distributor porch and is greater than those feed nozzles that are positioned at more close distributor porch." size ", " larger " and " less " refer to the cross-sectional area of nozzle opening in this context.In this respect, the ratio of the number of the feed nozzle of reactor external diameter and different size is approximately 0.5 to approximately 2.5, on the other hand approximately 1 to approximately 2 and on the other hand approximately 1.5 to approximately 2.
Although can use the nozzle with different size in specific acrylonitrile reactor, but it has been found that, use has from approximately 2 to approximately 10 kinds of different sizes, approximately 2 to approximately 8 kinds of different sizes on the other hand, approximately 2 to approximately 6 kinds of different sizes on the other hand, approximately 2 to approximately 4 kinds of different sizes on the other hand, approximately 3 to approximately 6 kinds of different sizes on the other hand, approximately 3 to approximately 4 kinds of different sizes on the other hand, approximately 4 to approximately 8 kinds of different sizes on the other hand, approximately 4 to approximately 6 kinds of different sizes on the other hand, approximately 5 to approximately 6 kinds of different sizes on the other hand, approximately 5 to approximately 7 kinds of different sizes on the other hand, and the nozzle (specifically depending on the diameter of reactor) of approximately 5 to approximately 8 kinds of different sizes is enough to overcome the problems referred to above in most of acrylonitrile reactors with inhomogeneous charging on the other hand.On the other hand, the external diameter of 2 to approximately 5 meters if reacting appliance is had an appointment, feed nozzle has approximately 3 to approximately 4 kinds of different sizes so.On the other hand, if reactor has the diameter that exceedes approximately 5 to approximately 12 meters, feed nozzle has approximately 5 to approximately 8 kinds of different sizes so.Therefore, for example, the nozzle that use has three kinds of different sizes is enough for " small-sized " acrylonitrile reactor of the diameter with about 8 to 12 feet (~ 2.4 to ~ 3.7 meters) conventionally.On the other hand, use have five or the nozzle of six kind of different size be more suitable for having " large-scale " acrylonitrile reactor of about 26 to 32 feet (~ 7.9 to ~ 9.7 meters) or larger diameter.
Generally speaking, in commercial acrylonitrile reactor the size of feed nozzle 34 (cross-sectional area) 15 to 80mm
2, more commonly 20 to 60mm
2scope in, specifically depend on the size of reactor and the density of feed nozzle, that is, the number of the feed nozzle 34 of every square meter of reactor cross section.This identical jet size design also can be used in conjunction with this feature of the present utility model.In other words, in given acrylonitrile reactor, the average nozzle size of all feed nozzles will be worth corresponding to these.
With regard to the difference of jet size, in the maximum nozzle of nozzle in groups for specific ammonia oxidation reactor and minimum nozzle, the ratio on cross-sectional area can be as small as 1.02 and greatly to 1.35.The size with middle-sized feed nozzle can easily be determined by calculating and/or normal experiment.
In this regard, using the object of the feed nozzle 34 with different size is the mass flow that approaches as far as possible uniform incoming mixture in order to realize between feed nozzle.In given sparger system, through the mass flow of the incoming mixture of any specific feed nozzle, mainly based on its density, density is again mainly based on its temperature.Correspondingly, for having the estimating temperature of incoming mixture that the specific dimensions of middle-sized specific nozzle can pass this feed nozzle by reference and easily definite, this estimating temperature again can be by actual measurement or easily definite by suitable heat transfer calculations.
Utilize this feature, become more approaching even feed nozzle through the mass flow containing ammonia incoming mixture of each feed nozzle.This causes again inside reactor between region, more to approach uniform operation, and this can maximize productivity ratio.In this respect, in approximately 5% of the mass flow of mass flow what its nozzle in office by any feed nozzle, on the other hand in approximately 4%, on the other hand in approximately 3%, on the other hand in approximately 2%, on the other hand in approximately 1%, on the other hand in approximately 0.5%, on the other hand approximately 0.25% and on the other hand in approximately 0.1%.
This feature is also by guaranteeing that the gas of correct flow flows through all the time distributor feed nozzle and is minimized in startup, shuts down and the even pollution (catalyst reverse flow) of catalyst to feed distributor during normal operating.
There is the arm of ever-reduced diameter
According to another feature of this new distributor designs, from its near-end to its far-end, (end that, is connected to collector 30 from it is opposed end away from collector 30 to it) reduces the diameter of branch road distributor pipeline or " arm " 32.
In conventional acrylonitrile reactor, the diameter of branch road distributor pipeline 32 is identical along the whole length of pipeline.Should design, the flow of the incoming mixture by pipeline significantly reduces to its far-end from its near-end, leaves pipeline by the feed nozzle 34 of the length location along pipeline because enter many incoming mixtures of near-end.As a result, the speed of the incoming mixture of these pipe interiors pipeline far-end or near too slow, to such an extent as to any ammoxidation catalyst that can be present in there is not had to remarkable impact.
According to this feature of the present utility model, this problem is avoided by the diameter that reduces branch road distributor pipeline or " arm " 32 from its near-end to its far-end.Fig. 9 A, Fig. 9 B, Figure 10 A, Figure 10 B and Figure 10 C show this feature of the present utility model.As shown in these figures, the diameter of arm 32 progressively reduces to its far-end 39 from its near-end 37.
Utilize this feature, speed containing ammonia incoming mixture can keep enough high along the whole length of pipeline, be purged to next feed nozzle 34 so that can not inadvertently pollute any ammoxidation catalyst of sparger system 16 inside, here, catalyst will discharge together with flowing through the feeding gas of this feed nozzle.Although also use in design early for this mechanism of removing catalyst, the far-end of arm or near the speed of feeding gas too slow in these designs, to such an extent as to any catalyst purge that there can not be existed is to next feed nozzle.According to this feature of the present utility model, this problem is by reducing the diameter of arm to avoid to its far-end from its near-end.Result is, keeps enough high in the speed of the feeding gas of these arm pipe interiors, arrives next available feed nozzle with any catalyst purge that can be present in there, even at the far-end of pipeline.Using ever-reduced diameter to make suitably high speed is even also possible at the far-end of pipeline, also avoids speed and/or the pressure drop unacceptably high in the proximal end of pipeline simultaneously.
Although Fig. 9 A, Fig. 9 B, Figure 10 A, Figure 10 B and Figure 10 C show arm 32 and have three independent portion's sections of different-diameter, should be appreciated that according to the utility model and can use any different-diameter that facilitates number.Generally speaking, the size of different-diameter and number be selected as keeping in all distributor pipelines (, collector 30 and all arms 32) approximately 10 to 30, the preferred gas velocity of 15 to 25 meter per seconds.
Described various aspects can be used for having the reactor of various sizes diameter herein.One preferred aspect, reactor can have from approximately 2 to approximately 12, approximately 5 to approximately 12 meters on the other hand, approximately 8 to approximately 12 meters and the external diameter of approximately 9 to approximately 11 meters on the other hand on the other hand.
Prop up pipe end-cap
In the optional optimal way of realizing above feature of the present utility model, far-end 39 terminations that are configured with a pipeline 32 of ever-reduced diameter have the end cap (referring to Figure 11) being penetrated by one or more feed nozzles 34.As mentioned above, the ever-reduced feature of this diameter guarantee its far-end or near flow through arm 32 feeding gas speed keep relatively high.Comprise that by use end cap 90 terminations of one or more feed nozzles have the arm 32 of less far-end 39, can guarantee that this speed keeps enough high, to make being present in this far-end or near any ammoxidation catalyst maintenance movement, so that it finally blows out arm by feed nozzle 34.Figure 11 A and Figure 11 B show circular in configuration, and a figure has the feed nozzle 34 of location placed in the middle, and another figure has the feed nozzle 34 of reduction.Figure 11 C and Figure 11 D show flat configuration, and a figure has the feed nozzle 34 of location placed in the middle, and another figure has the feed nozzle 34 of reduction.The feed nozzle configuration reducing makes wherein catalyst can become the dead space being trapped to minimize, but may manufacturing cost higher.
Multiple feed distributor portion section
According to another feature of this new distributor designs, feed distributor 16 is subdivided into multiple feed distributor portion section, and each section has its oneself ingress port for receiving containing ammonia charging from reactor is outside.
In all ammonia oxidation reactors of typical commercial as shown in Figure 2, use single feed distributor system 16, all arms 32 feed that wherein collector 30 of single horizontal orientation is system.In the great majority of these systems, as shown in Fig. 2 and Fig. 4 further, the entrance 31 of distributor 16 is arranged in the sidewall of reactor 10 in the horizontal plane substantially the same with collector 30.
When (this distributor designs is used for larger acrylonitrile reactor, there is the reactor of the diameter that is greater than approximately 6 meters (~ 20 feet)) in time, can become very large by the difference between the shortest travel path and the longest travel path that experience containing ammonia feeding gas in distributor, because unstripped gas enters an only end of collector 30 and therefore must march to the other end to arrive the arm that is attached to there always.As a result, leave the temperature, density of the incoming mixture of each feed nozzle 34 and therefore mass flow can marked change between feed nozzle, specifically depend on feed nozzle residing position in sparger system.As mentioned above, this deviation in temperature, density and mass flow can cause the sizable problem aspect the uniformity two of reactor performance and nitrogenize.
In order to address this problem, propose distributor entrance 31 move to far above the position of collector 30 and utilize suitable pipeline to join distributor entrance 31 to collector 30 center.Idea is because feeding gas is transported to collector 30 center instead of a place in its end only, so this feeding gas by collector 30 to all arms 32 and flowing more approaching the situation than original even by all arms 32.But the problem of the method is distributor entrance 31 to be connected to the required additional line in collector 30 center pass in time and become and be nitrided, this is because above pointed reason is very disadvantageous.
According to this feature of the present utility model, feed distributor 16 is divided into multiple feed distributor portion section, and wherein the sub-portion of each distributor section is provided with its oneself distributor entrance 31 for receiving containing ammonia charging from reactor is outside.Each distributor portion section is also provided with its oneself control system, to can control individually the flowing containing ammonia incoming mixture in each distributor portion section.In addition, the distributor entrance 31 of each distributor portion section be positioned at the horizontal plane place that limited by collector 30 or near.Preferably, the distributor entrance 31 of each distributor portion section and this horizontal plane vertically spaced apart be no more than 10 feet, be more preferably no more than 5 feet.
This feature of distributor designs of the present utility model is shown in Figure 12, the figure illustrates relative to each other with relation side by side substantially and is arranged in four of inside reactor separately and feed distributor portion section 100,102,104 and 106 independently.In this context, " side by side " should be understood to represent that each distributor portion section is arranged in substantially the same height at inside reactor, instead of is arranged to one on another top.As further shown in Figure 12, each in distributor portion section 100,102,104 and 106 comprises respectively distributor entrance 110,112,114 and 116, and all distributor entrances are all connected to the common feed header tube (not shown) that is positioned at reactor 10 outsides.In addition, provide the independent control valve 120,122,124 and 126 that is connected to control system (not shown).
Utilize this feature, each independent distributor portion section can be controlled to adjust the amount (mass flow) containing ammonia incoming mixture by this distributor portion section feeding individually.This allows on the whole reactor even better to be controlled, because each region of reactor can be controlled individually.This makes again each region can be by " adjustment " to mate other region, thereby realizes optimum performance on whole reactor.
Described various aspects can be used for having the reactor of various sizes diameter herein.One preferred aspect, reactor can have from approximately 2 to approximately 12, approximately 5 to approximately 12 meters on the other hand, approximately 8 to approximately 12 meters and the external diameter of approximately 9 to approximately 11 meters on the other hand on the other hand.
Although only described concrete examples more of the present utility model above, should be appreciated that in the situation that not departing from spirit and scope of the present utility model and can carry out many amendments.All such amendments are intended to be included in the scope of the present utility model being only limited by the appended claims.
Claims (14)
1. the feed distributor for ammonia oxidation reactor, its be effective to from ammonia oxidation reactor outside by the reactor wall of described reactor and to supply in the fluid bed of the ammoxidation catalyst of described inside reactor containing ammonia incoming mixture, described distributor comprises: main header tube; Distributor entrance, it is communicated with described main header tube fluid, and described distributor entrance is attached to described reactor wall rigidly; And multiple branch road distributor pipelines, it is communicated with described main collector distributor pipeline fluid, described branch road distributor pipeline limits feed nozzle for entering in the fluid bed of ammoxidation catalyst containing ammonia incoming mixture, wherein, described distributor entrance disconnects fast accessory by means of air-tightness and is attached to rigidly described reactor wall.
2. distributor according to claim 1, it is characterized in that, described reactor wall limits permanent opening, and further wherein, described air-tightness disconnects fast accessory and comprises the cylindrical sleeve with the first side and second side relative with described the first side, wherein, the first side of described cylindrical sleeve is permanently welded to the periphery of described permanent opening with air tight manner, described air-tightness disconnects fast accessory and also comprises the outside hoop that is permanently welded to described main header tube with air tight manner, wherein, described hoop is fixed to the second side of described cylindrical sleeve releasedly.
3. feed distributor according to claim 1, is characterized in that, described is the blend of ammonia and saturated and/or undersaturated C3 to C4 hydrocarbon containing ammonia incoming mixture.
4. feed distributor according to claim 3, is characterized in that, the group that the described blend of ammonia and saturated and/or undersaturated C3 to C4 hydrocarbon selects free propane, propylene, butane, butylene and their mixture to form.
5. feed distributor according to claim 1, is characterized in that, described reactor external diameter is 2 to 12 meters.
6. feed distributor according to claim 1, is characterized in that, described reactor external diameter is 8 to 12 meters.
7. feed distributor according to claim 1, is characterized in that, described reactor external diameter is 9 to 11 meters.
8. the feed distributor for ammonia oxidation reactor, its be effective to from ammonia oxidation reactor outside by the reactor wall of described reactor and to supply in the fluid bed of the ammoxidation catalyst of described inside reactor containing ammonia incoming mixture, described distributor comprises: main header tube; Distributor entrance, it is communicated with described main header tube fluid; And multiple branch road distributor pipelines, it is communicated with described main collector distributor pipeline fluid, described branch road distributor pipeline limits feed nozzle for entering in the fluid bed of ammoxidation catalyst containing ammonia incoming mixture described, wherein, at least some in described branch road distributor pipeline disconnect fast accessory by corresponding air-tightness and are attached to described main header tube.
9. feed distributor according to claim 8, it is characterized in that, described main header tube comprises the multiple collector joints for being attached to corresponding branch road distributor pipeline, and further, wherein, each air-tightness disconnects fast accessory and comprises metallic packing ring and clamp assembly, and described clamp assembly is configured to described metallic packing ring to be fixed between corresponding collector joint and the end of facing of branch road distributor pipeline with air tight manner.
10. feed distributor according to claim 8, is characterized in that, described ammonia incoming mixture is the blend of ammonia and saturated and/or undersaturated C3 to C4 hydrocarbon.
11. feed distributors according to claim 10, is characterized in that, the group that the described blend of ammonia and saturated and/or undersaturated C3 to C4 hydrocarbon selects free propane, propylene, butane, butylene and their mixture to form.
12. feed distributors according to claim 8, is characterized in that, described reactor external diameter is 2 to 12 meters.
13. feed distributors according to claim 8, is characterized in that, described reactor external diameter is 8 to 12 meters.
14. feed distributors according to claim 8, is characterized in that, described reactor external diameter is 9 to 11 meters.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420150619.6U CN203955188U (en) | 2014-03-31 | 2014-03-31 | For the feed distributor of ammonia oxidation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420150619.6U CN203955188U (en) | 2014-03-31 | 2014-03-31 | For the feed distributor of ammonia oxidation reactor |
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| Publication Number | Publication Date |
|---|---|
| CN203955188U true CN203955188U (en) | 2014-11-26 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201420150619.6U Expired - Lifetime CN203955188U (en) | 2014-03-31 | 2014-03-31 | For the feed distributor of ammonia oxidation reactor |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104941523A (en) * | 2014-03-31 | 2015-09-30 | 英尼奥斯欧洲股份公司 | Feeding distributor designed for ammonia oxidation reactor |
| WO2019096065A1 (en) * | 2017-11-14 | 2019-05-23 | 中国石油化工股份有限公司 | Fluid distributor, reaction device, and application thereof |
-
2014
- 2014-03-31 CN CN201420150619.6U patent/CN203955188U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104941523A (en) * | 2014-03-31 | 2015-09-30 | 英尼奥斯欧洲股份公司 | Feeding distributor designed for ammonia oxidation reactor |
| WO2019096065A1 (en) * | 2017-11-14 | 2019-05-23 | 中国石油化工股份有限公司 | Fluid distributor, reaction device, and application thereof |
| US11571673B2 (en) | 2017-11-14 | 2023-02-07 | China Petroleum & Chemical Corporation | Fluid distributor, reaction device and application thereof |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20141126 |