CN104941522A - Feeding distributor designed for ammonia oxidation reactor - Google Patents
Feeding distributor designed for ammonia oxidation reactor Download PDFInfo
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- CN104941522A CN104941522A CN201410124814.6A CN201410124814A CN104941522A CN 104941522 A CN104941522 A CN 104941522A CN 201410124814 A CN201410124814 A CN 201410124814A CN 104941522 A CN104941522 A CN 104941522A
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- pipeline
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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
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
- B01J4/004—Sparger-type elements
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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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
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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
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C253/00—Preparation of carboxylic acid nitriles
- C07C253/24—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
- C07C253/26—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
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- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
Different parts of a feeding distributor used in a commercial ammonia oxidation reactor are conveniently replaced through attaching and connecting all parts of the distributor to each other and to the wall of the reactor by using airtight quick disconnecting accessories. In addition, the diameters of branch pipelines in the parts of the distributor and the diameters of feeding nozzles attached and connected to the branch pipelines are changed, so that feeding gases passing through the parts can favorably and uniformly flow. The distributor can be subdivided into a plurality of feeding distributor parts for better controlling the reactor. Finally, end covers of which the ends are connected to the far ends of the branch pipelines of the distributor can be provided with nozzles which are used for removing any ammonia oxidation catalyst possibly and unintentionally reaching into the distributor.
Description
Background technology
In the business of acrylonitrile manufactures, 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 being 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, to make bed 24 fluidisation of the ammoxidation catalyst of inside reactor, propylene and the ammonia catalytic ammoxidation to acrylonitrile occur wherein.
The product gas produced by reaction exports 26 by reactor effluent and leaves reactor 10.Before doing so, product gas is through cyclone 20, and any ammoxidation catalyst that these gases can be carried secretly removed by cyclone 20, to turn back to catalyst bed 24 by dipleg (diplegs) 25.Ammoxidation is high exothermic heat, therefore uses cooling coil 18 to take away excessive heat, thus reaction temperature is remained on proper level.
Propylene and ammonia can form explosive mixture with oxygen.But at normal operating temperatures, prevent blast 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 to make the unique place allowing plant air to contact propylene and ammonia in the normal operation period be in the fluid bed of ammoxidation catalyst 24 with operating into, and therefore only catalyst temperature height to be enough to catalytic ammoxidation reaction time.
For this reason, traditional approach propylene and ammonia being fed to reactor 10 uses such as at U.S. 5, and 256, the feed distributor system 16 shown in 810, the disclosure of this patent is incorporated herein by reference.As shown in Fig. 1 and Fig. 2 (this two width figure is by Fig. 2 and Fig. 3 renumberd as the literature) of ' 810 patents, feed distributor 16 takes the form of a series of supply pipe 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 nozzle 34 is limited in collector 30 and arm 34, and the mixture of propylene and ammonia is filled with by feed nozzle 34 during the operation of normal reaction device.The number of arm 32 and feed nozzle 34 and spacing make the whole cross-sectional area across reactor 10 be positioned with every square metre of about 10 to 30 feed nozzles altogether roughly equably.
Usually, each feed nozzle 34 is fed guard shield 36 and surrounds, and the form of the short portion section of pipeline taked by charging guard shield 36, and the internal diameter of this pipeline is the several times of the diameter of nozzle 34.Charging guard shield 34 make the speed of the gas passing nozzle 10 can leave enter catalyst bed 24 before significantly slow down, this prevent the disintegration of original generable catalyst.
Plant air enters catalyst bed 24 (Fig. 1) usually after passing air grid 14, and air grid 14 is positioned at below feed distributor 16.As the well-known, air grid 14 takes the form of continuous print metal sheet usually, and it is limited to a series of airport wherein or nozzle.The mass flow of the diameter of air nozzle, the mass flow through the plant air of air grid 14 and the propylene/ammonia mixture through feed distributor 16, through selecting, makes the 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 below air grid 14.In addition, in many cases, feed nozzle 34 is arranged with one-one relationship with the air nozzle in air grid 14, wherein each charging guard shield 36 air nozzle of directly aiming at its correspondence with promote to pass the gas of these two kinds different nozzles fast and mix fully.See U.S. 4,801,731.
Although the propylene of this general type/ammonia feed system is respond well, there is some shortcoming in it really.Such as, owing at high temperature continuing to be exposed to ammonia, the metal forming feed distributor 16 is passed in time and experiences nitrogenize.As a result, feed distributor 16 each section and sometimes whole feed distributor need frequently to be changed.Cost is very high for this, particularly because the reactor when changing must dead halt.
The inhomogeneities run with the Second Problem that this propylene/ammonia feed system is associated.The productivity ratio of this not only adversely influential system, but also result in uneven nitrogenize, this has increased the weight of nitrogenize problem further.
Summary of the invention
According to the present invention, provide the design of a kind of new feed distributor, it significantly reduces these problems, and roughly completely eliminate problem in some cases.
According to a feature of this new distributing device design, use air-tightness to disconnect the wall that the main header tube of distributor is attached to the reactor that main header tube is passed by accessory fast, or the various pipelines forming feed distributor are connected to each other, or both.Due to this feature, when replacing becomes if desired due to excessive nitrogenize, change the time needed for some or all of feed distributor and work significantly minimizing.
According to another feature of this new distributing device design, along with the travel path from the entrance of feed distributor to each feed nozzle increases, the relative diameter of feed nozzle 34 increases slightly.Due to this feature, becoming feed nozzle closer to evenly containing the mass flow of ammonia incoming mixture through each feed nozzle.This causes again inside reactor between zones closer to uniform operation, and this makes productivity ratio to maximize.This feature also by guaranteeing that the gas of correct flow flows through distributor feed nozzle all the time and carrys out minimum catalyst and flow backwards (back up), that is, startup, shut down and even during normal operating catalyst to the pollution of feed distributor.
According to another feature of this new distributing device design, the diameter of arm 32 reduces from its near-end to its far-end (that is, from the end that it is connected to main header tube to its end away from main header tube).Due to this feature, flow through these arms containing ammonia incoming mixture speed along arm whole length and especially its far-end keep enough high, next feed nozzle 34 is purged to, so that by this feed nozzle from arm internal discharge with any ammoxidation catalyst that can exist.
According to this another feature newly-designed, feed distributor 16 is subdivided into multiple feed distributor portions section, each section have its oneself ingress port for from reactor external reception containing ammonia charging.Independent control system due to this feature, can realize to reactor in interregional better control, because can be used to the operation in each feed distributor portion of monitor and forecast individually section.
Therefore, the present invention provides a kind of distributor of improvement in one embodiment, use containing in ammonia incoming mixture for supply at the reactor wall by reactor outside from ammonia oxidation reactor and in the fluid bed of the ammoxidation catalyst of inside reactor, the distributor of this improvement comprises: main header tube; Distributor inlet, it is communicated with main header tube fluid, and this distributor inlet is attached to reactor wall rigidly; And multiple branch road distributor pipeline, itself and main collector distributor fluid communication, this branch road distributor pipeline limits feed nozzle for entering in the fluid bed of ammoxidation catalyst by propylene/ammonia incoming mixture, and wherein distributor inlet disconnects accessory fast by means of air-tightness and is attached to reactor wall rigidly.
In another embodiment, the invention provides a kind of distributor of improvement, use containing in ammonia incoming mixture for supply at the reactor wall by reactor outside from ammonia oxidation reactor and in the fluid bed of the ammoxidation catalyst of inside reactor, the distributor of this improvement comprises: main header tube; Distributor inlet, it is communicated with main header tube fluid; And multiple branch road distributor pipeline, itself and main collector distributor fluid communication, this branch road distributor pipeline limits feed nozzle for entering in the fluid bed of ammoxidation catalyst containing ammonia incoming mixture, and wherein the ducted at least some of branch road distributor disconnects attachment to main header tube fast by corresponding air-tightness.
In yet another embodiment, the invention provides a kind of distributor of improvement, use containing in ammonia incoming mixture for supply at the reactor wall by reactor outside from ammonia oxidation reactor and in the fluid bed of the ammoxidation catalyst of inside reactor, the distributor of this improvement comprises: main header tube; Distributor inlet, it is communicated with main header tube fluid; And multiple branch road distributor pipeline, itself and main collector distributor fluid communication, 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 closer to distributor inlet place, and larger nozzle is positioned at further from distributor inlet place, depend on that propylene/ammonia incoming mixture is advanced through the distance of distributor to each nozzle from distributor inlet.
In yet another embodiment, the invention provides a kind of distributor of improvement, for supplying in ammonia incoming mixture in the fluid bed of the ammoxidation catalyst of inside reactor use from the outside reactor wall by reactor of ammonia oxidation reactor, the distributor of this improvement comprises: main header tube; Distributor inlet, it is communicated with main header tube fluid; And multiple branch road distributor pipeline, 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 the feed nozzle that will enter containing ammonia incoming mixture in the fluid bed of ammoxidation catalyst, and wherein the diameter of the ducted at least some of branch road distributor reduces from its near-end to its far-end.
In yet another embodiment, the invention provides a kind of distributor of improvement, use containing in ammonia incoming mixture for supply at the reactor wall by reactor outside from ammonia oxidation reactor and in the fluid bed of the ammoxidation catalyst of inside reactor, the distributor of this improvement comprises: main header tube; Distributor inlet, it is communicated with main header tube fluid; And multiple branch road distributor pipeline, itself and main collector distributor fluid communication, this branch road distributor pipeline limits feed nozzle for entering in the fluid bed of ammoxidation catalyst containing ammonia incoming mixture, the distributor wherein improved is made up of the multiple feed distributor portions section being arranged in inside reactor, each feed distributor portion section has its oneself distributor inlet, for the system acceptance of, its oneself main header tube outside from reactor and its oneself branch road distributor pipeline containing ammonia charging.
Accompanying drawing explanation
The present invention can be understood better by referring to the following drawings, in the accompanying drawings:
Fig. 1 is schematic diagram, it illustrates the reactor section section of the conventional ammonia oxidation reactor for the preparation of acrylonitrile;
Fig. 2 is plane, it illustrates the downside of the conventional sparger system of the ammonia oxidation reactor of Fig. 1;
Fig. 3 is the sectional view intercepted along the line 3-3 of Fig. 2, the feed nozzle that Fig. 3 shows the conventional sparger system of Fig. 2 and the charging guard shield be associated;
Fig. 4 is sectional view, and the main header tube showing the feed distributor of commercial ammonia oxidation reactor penetrates and is connected to the mode of the sidewall of reactor;
Fig. 5 is the sectional view being similar to Fig. 4, shows a feature of the present invention, and wherein the main header tube of feed distributor penetrates and disconnects by means of air-tightness the sidewall that connector is connected to reactor fast;
Fig. 6 is the side view that the air-tightness of Fig. 5 disconnects connector fast;
Fig. 7 is the sectional view being similar to Fig. 2, shows another feature of the present invention, and wherein distributor branch pipes pipeline disconnects by means of air-tightness the main header tube that connector is connected to distributor fast;
Fig. 8 is plane, and the air-tightness illustrating in greater detail Fig. 7 disconnects connector fast;
Fig. 9 A and Fig. 9 B is the sectional view of the distributor branch pipes pipeline according to another feature use of the present invention, and how the diameter showing this arm increases along with the distance apart from distributor header tube and to reduce;
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 further illustrating this arm increases with the distance apart from distributor header tube and to reduce;
Figure 11 A, Figure 11 B, Figure 11 C and Figure 11 D are the vertical sectional views of the distributor branch pipes end cap used according to another feature of sparger system of the present invention; And
Figure 12 is plane, it illustrates another feature of the present invention, and wherein the feed distributor of acrylonitrile reactor is subdivided into multiple feed distributor portions 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 that the non-solder allowing object to be disconnected by non-destructive mode is connected.Such as, fixingly releasedly bolt, crab-bolt, the flange be spirally connected and their combination can be referred to.
As used herein, " containing ammonia incoming mixture " refers to ammonia and blend that is 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.
Quick disconnection connector
As described above, the subject matter run in the operation of commercial propylene nitrile reactor is that feed distributor passes inefficacy in time owing to forming the nitrogenize of its metal.In order to address this problem, propose by such as at U.S. 3,704,690, U.S. 4,401,153, the anti-nitro-alloy shown in U.S. 5,110,584 and EP 0 113 524 manufacture distributor.Regrettably, due to fluid catalyst ammoxidation reaction some problem distinctive and its cost reason, proved that this solution is unsuccessful for using in commercial propylene nitrile reactor.
Simultaneously, U.S. 5,256, the 810 a kind of methods describing nitrogenize for roughly eliminating the distributor in commercial propylene nitrile reactor, the method makes the temperature of the ammonia of distributor inside keep enough low, to prevent nitrogenize by using custom-designed blanket insulation.But due to cost and somewhat complex design, this solution is also proved to be not satisfied.
According to this feature of the present invention, inefficacy passed in time by distributor this problem due to nitride metal enables each section of distributor and whole distributor as a whole be solved by the distributor designs changed quickly and easily by adopting.Although still need acrylonitrile reactor to shut down when 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 solving this nitrogenize problem in continuous foundation.
Fig. 4, Fig. 5 and Fig. 6 show a feature of the present invention, and wherein the outer wall that the entrance of sparger system is connected to ammonia oxidation reactor solves by using air-tightness to disconnect connector fast by this distributor nitrogenize problem.In specific embodiment in the 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 inlet 31 to be connected to collector 30.Conveniently, this feature of the present invention is described the reactor design shown in composition graphs 4, Fig. 5 and Fig. 6.But, should be appreciated that this feature and advantage thereof are applicable to the design of other reactor comparably, such as the such as wherein design that is separated by intermediate duct with main collector 30 of distributor inlet 31.
As shown in Figure 4, the usual manner distributor inlet 31 of feed distributor 16 being attached to the wall 40 of reactor 10 is by welding.Correspondingly, when main header tube 30 needs to be replaced, weld repairs method must be adopted, wherein tightly be cut off around the part reactor wall 40 of main header tube 30 by welding, the opening formed thus in shell of reactor 12 is by repairing with the welding of suitable patch, and new main header tube 30 is also arranged on by welding in the reactor wall 40 repaired.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 invention, this problem is avoided by adopting the air-tightness being used for main header tube 30 being attached to reactor wall 40 to disconnect connector design fast.The example of such connector illustrates in fig. 5 and fig., there is shown " manhole " 42 with cylindrical sleeve 44 form, the first side of cylindrical sleeve 44 is for good and all welded to the periphery 46 of the permanent opening 48 be formed in reactor wall 40 in a gastight 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 receiving bolt 52 wherein.Meanwhile, the hoop 54 of smooth circular slab form is permanently welded to the outside of main header tube 30 in a gastight manner.In addition, a series of through holes 56 that 54 also limit the through hole in the flange 50 corresponding to manhole 42 are bound round.
Utilize this structure, main header tube 30 can be fixed in a gastight manner releasedly the reactor wall 40 of reactor 10 simply by the flange 50 hoop 54 of main header tube 30 being screwed to manhole 42.In an identical manner, main header tube 30 can be separated with reactor wall 40 simply by being gone to be spirally connected from flange 50 by hoop 54.Correspondingly, the replacing becoming disabled existing main collector 30 due to excessive nitrogenize is by simply going to be spirally connected and be spirally connected process and simply and easily realize.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 invention, wherein use air-tightness to disconnect the problem that connector solves distributor branch pipes nitrogenize fast.As shown in Figure 2, be by welding by the usual manner propping up pipeline (or " arm ") 32 and be attached to main header tube (or " collector ") 30.Correspondingly, when each arm 32 needs to be replaced due to excessive nitrogenize, adopt weld repairs method, wherein old arm is separated with main header tube 30 by welding or other suitable cutting technique, and by new arm by weld attachment to main header tube 30.This also needs the on-the-spot manpower of significant quantity, and this is with high costs.
According to this feature of the present invention, this problem is avoided by adopting the air-tightness being used for each arm 32 being attached to main header tube 30 to disconnect connector design fast.This illustrates in figures 7 and 8, and the air-tightness that there is shown the main header tube 30 for each arm 32 being connected to sparger system 16 disconnects connector 60 fast.Although these accompanying drawings show each arm be directly connected to main header tube 30, to should be appreciated that in these arms one or more such as can 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 (namely, when connected and the together parts removed when connecting and being disconnected) be designed specifically to and join connector each other to by means of only mechanical means (that is, not using welding or adhesive).Air-tightness disconnects connector fast and is also designed to keep tight seal under the high temperature conditions, and it is that described hot conditions runs into during being the temperature cycles such as occurred during the normal operating of typical commercial ammonia oxidation reactor and when when such reactor start-up and shutdown.The example being applicable to the commercially available connector of this purposes is the Grayloc intermetallic endoporus sealing clamp connector that can derive from Grayloc Products (Houston, Texas).Another example being applicable to the commercially available connector of this purposes is the Techlok clamp connector of the Vector group that can derive from Freudenberg Oil & Gas Technologies (Houston, Texas).Another example being applicable to the commercially available connector of this purposes is the G-Lok that can derive from Australasian Fittings & Flanges (Osborne Park, WA, Australia)
?clamp connector.It is not too desirable that conventional flange connects for this application, because they are easy to leak due to the temperature cycles during reactor operation.
Fig. 8 shows the structure that typical air-tightness disconnects connector 60 fast, comprises the mode that arm 30 is interconnected to main header tube 30 by this connector.As shown in the figure, connector 60 is by receive hub 64 and 66 and the clamp assembly 62 kept together is formed, and hub 64 and 66 is carried on arm 32 and the end faced by collector joint 72 68 and 70.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 engagement hub 64 and 66 hermetically, thus is formed gas-tight seal between arm 32 and collector 30.
By using air-tightness to disconnect connector 60 fast, each arm 32 can simply by being spirally connected or going to be spirally connected clamp assembly 62 and be fixed to main header tube 30 and remove from main header tube 30.Correspondingly, the replacing becoming disabled existing arm 32 due to excessive nitrogenize is by simply going to be spirally connected and be spirally connected process and simply and easily realize.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.
Various aspects described herein can be used for the reactor with various sizes diameter.In preferred at one, reactor can have from about 2 to about 12, about 5 to about 12 meters on the other hand, on the other hand about 8 to about 12 meters and the external diameter of about 9 to about 11 meters on the other hand.
Variable feed nozzle size
According to another feature of this new distributing device design, along with the travel path from the entrance of feed distributor to each feed nozzle increases, the diameter of feed nozzle 34 increases slightly.
When being advanced through distributor 16 containing ammonia incoming mixture, the heat trnasfer from the hot gas of distributor outside causes the temperature of the incoming mixture of distributor inside to increase.As a result, the temperature leaving the incoming mixture of each feed nozzle is different, specifically depends on how long the time of incoming mixture before leaving in distributor has.Specifically, the temperature of the incoming mixture of the feed nozzle be positioned at further from distributor inlet place is left hotter in the temperature of incoming mixture leaving the feed nozzle be positioned at closer to distributor inlet.In this context, " further from " and " closer to " should be understood to represent with regard to the length of travel path further from closer to distributor inlet, this travel path starts from distributor inlet place and ends at incoming mixture leaves distributor specific feed nozzle by it.
In the ammonia oxidation reactor of routine, the diameter of feed nozzle 34 (Fig. 3) is all identical.As a result, the density of the incoming mixture left by the feed nozzle 34 be positioned at further from distributor inlet place is less than the density of the incoming mixture that the feed nozzle 34 by being positioned at closer to distributor inlet place leaves, because density and temperature are inversely proportional to.This causes again the mass flow containing ammonia incoming mixture left by the feed nozzle 34 be positioned at further from distributor inlet place to be less than the mass flow of the incoming mixture that the feed nozzle 34 by being positioned at closer to distributor inlet place leaves, precondition is that other condition is identical, because mass flow is directly proportional to density.Regrettably, cause on the whole lower than the reactor performance of the best by the shortage of this uniformity of the mass flow of each feed nozzle, because the amount (that is, the gross mass of unit interval) containing ammonia incoming mixture entering the bed 24 of ammoxidation catalyst is less than in the region of feed nozzle closer to this entrance in the reactor area of feed nozzle further from distributor inlet.
According to this feature of the present invention, this problem is overcome by the size changing distributor feed nozzle 34, and those feed nozzles be wherein positioned at further from distributor inlet place are greater than those feed nozzles be positioned at closer to distributor inlet place." 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 about 0.5 to about 2.5, on the other hand about 1 to about 2 and on the other hand about 1.5 to about 2.
Although the nozzle with different size can be used in specific acrylonitrile reactor, but it has been found that, use has from about 2 to about 10 kinds of different sizes, about 2 to about 8 kinds of different sizes on the other hand, about 2 to about 6 kinds of different sizes on the other hand, about 2 to about 4 kinds of different sizes on the other hand, about 3 to about 6 kinds of different sizes on the other hand, about 3 to about 4 kinds of different sizes on the other hand, about 4 to about 8 kinds of different sizes on the other hand, about 4 to about 6 kinds of different sizes on the other hand, about 5 to about 6 kinds of different sizes on the other hand, about 5 to about 7 kinds of different sizes on the other hand, and the nozzle (specifically depending on the diameter of reactor) of about 5 to about 8 kinds of different sizes is enough to overcome the problems referred to above in most of acrylonitrile reactor with uneven charging on the other hand.On the other hand, the external diameter of 2 to about 5 meters if reacting appliance is had an appointment, so feed nozzle has about 3 to about 4 kinds of different sizes.On the other hand, if reactor has the diameter exceeding about 5 to about 12 meters, so feed nozzle has about 5 to about 8 kinds of different sizes.Therefore, such as, use there are three kinds of different sizes nozzle usually for have about 8 to 12 feet (~ 2.4 to ~ 3.7 meters) diameter " small-sized " acrylonitrile reactor be enough.On the other hand, the nozzle with five or six kind of different size is used to 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 propylene nitrile reactor the size (cross-sectional area) of feed nozzle 34 at 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 use in conjunction with this feature of the present invention.In other words, in given acrylonitrile reactor, the average nozzle size of all feed nozzles will corresponding to these values.
With regard to the difference of jet size, in the set of nozzles for specific ammonia oxidation reactor, maximum nozzle and the ratio of minimum nozzle on cross-sectional area can be as small as 1.02 and large to 1.35.The size with middle-sized feed nozzle is easily determined by calculating and/or normal experiment.
In this regard, the object with the feed nozzle 34 of different size is used to be to realize between feed nozzle as far as possible close to the mass flow of uniform incoming mixture.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, specific dimensions for having middle-sized specific nozzle is easily determined by the estimating temperature with reference to the incoming mixture through this feed nozzle, and this estimating temperature is easily determined by actual measurement or by suitable heat transfer calculations again.
Utilize this feature, becoming feed nozzle closer to evenly containing the mass flow of ammonia incoming mixture through each feed nozzle.This causes again inside reactor between zones closer to uniform operation, and this makes productivity ratio to maximize.In this respect, by about 5% of the mass flow of the mass flow of any one feed nozzle what its nozzle in office, on the other hand in about 4%, on the other hand in about 3%, on the other hand in about 2%, on the other hand in about 1%, on the other hand in about 0.5%, on the other hand about 0.25% and on the other hand in about 0.1%.
This feature also by guarantee the gas of correct flow flow through distributor feed nozzle to be all the time minimized in startup, shut down and even during normal operating catalyst to the pollution (catalyst reverse flow) of feed distributor.
There is the arm of ever-reduced diameter
According to another feature of this new distributor designs, the diameter of branch road distributor pipeline or " arm " 32 reduces from its near-end to its far-end (that is, from the end that it is connected to collector 30 to its opposed end away from collector 30).
In the acrylonitrile reactor of routine, the diameter of branch road distributor pipeline 32 is identical along the whole length of pipeline.Should design, significantly be reduced to its far-end from its near-end by the flow of the incoming mixture of pipeline, because the many incoming mixtures entering near-end leave pipeline by the feed nozzle 34 of locating along the length of pipeline.As a result, the incoming mixture of these pipe interiors speed pipeline far-end or near too slow, to such an extent as on any ammoxidation catalyst that can be present in there, not there is remarkable impact.
According to this feature of the present invention, this problem is avoided by the diameter reducing 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 invention.As shown in these figures, the diameter of arm 32 progressively reduces from its near-end 37 to its far-end 39.
Utilize this feature, speed containing ammonia incoming mixture can keep enough high along the whole length of pipeline, next feed nozzle 34 is purged to make any ammoxidation catalyst that not inadvertently can pollute sparger system 16 inside, here, catalyst discharges together with the feeding gas flowing through this feed nozzle.Although also use in design comparatively early for this mechanism of removing catalyst, arm far-end or near the speed of feeding gas too slow in the 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 invention, this problem is by reducing the diameter of arm from its near-end to its far-end to avoid.As a result, keep enough high in the speed of the feeding gas of these arm pipe interiors, so that any catalyst purge of there can be present in next available feed nozzle, even at the far-end of pipeline.Use ever-reduced diameter to make suitably high speed also be even possible at the far-end of pipeline, also avoid in the unacceptably high speed in the proximal end of pipeline and/or pressure drop simultaneously.
Although Fig. 9 A, Fig. 9 B, Figure 10 A, Figure 10 B and Figure 10 C show arm 32 have the independent portion's section of three of different-diameter, should be appreciated that and can use any different-diameter facilitating number according to the present invention.Generally speaking, the size of different-diameter and number are selected as the gas velocity keeping about 10 to 30, preferably 15 to 25 meter per seconds in all distributor pipelines (that is, collector 30 and all arms 32).
Described various aspects can be used for the reactor with various sizes diameter herein.In preferred at one, reactor can have from about 2 to about 12, about 5 to about 12 meters on the other hand, on the other hand about 8 to about 12 meters and the external diameter of about 9 to about 11 meters on the other hand.
Prop up pipe end-cap
In the optional preferred embodiment realizing above feature of the present invention, far-end 39 termination being configured with a pipeline 32 of ever-reduced diameter has the end cap (see Figure 11) penetrated by one or more feed nozzle 34.As mentioned above, the ever-reduced feature of this diameter guarantee its far-end or near flow through the feeding gas of arm 32 speed keep relatively high.By having the arm 32 of less far-end 39 by end cap 90 termination comprising one or more feed nozzle, can guarantee that this speed keeps enough high, to make can be present in this far-end or neighbouring any ammoxidation catalyst maintenance movement, so that it blows out arm eventually through feed nozzle 34.Figure 11 A and Figure 11 B shows 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 shows 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 reduced makes wherein catalyst can become the dead space be trapped to minimize, but may manufacturing cost higher.
Multiple feed distributor portions section
According to another feature of this new distributing device design, feed distributor 16 is subdivided into multiple feed distributor portions section, each section have its oneself ingress port for from reactor external reception containing ammonia charging.
In all typical commercial ammonia oxidation reactors as shown in Figure 2, use single feed distributor system 16, wherein the collector 30 of single horizontal orientation is all arms 32 feed of 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 (namely this distributor designs is used for larger acrylonitrile reactor, there is the reactor of the diameter being greater than about 6 meters (~ 20 feet)) in time, can become very large, because unstripped gas enters an only end of collector 30 and therefore must march to the other end to arrive the arm being attached to there always by the difference between the shortest travel path experienced in distributor containing ammonia feeding gas and most long row inbound path.As a result, leave the temperature of the incoming mixture of each feed nozzle 34, density and therefore mass flow can marked change between feed nozzle, specifically depend on the position that feed nozzle is residing in sparger system.As mentioned above, this deviation in temperature, density and mass flow can cause the sizable problem in the uniformity two of reactor performance and nitrogenize.
In order to solve this problem, propose distributor inlet 31 is moved to the position far above collector 30 and utilizes suitable pipeline to join distributor inlet 31 center of collector 30 to.Idea is because feeding gas is transported to the center of collector 30 instead of a place only in its end, so this feeding gas by collector 30 to all arms 32 and by the flowing of all arms 32 by than original situation closer to evenly.But the problem of the method is that the additional line needed for center distributor inlet 31 being connected to collector 30 is passed in time and becomes by nitrogenize, this due to above pointed reason be very disadvantageous.
According to this feature of the present invention, feed distributor 16 is divided into multiple feed distributor portions section, wherein each distributor portion section be provided with its oneself distributor inlet 31 for from reactor external reception containing ammonia charging.Each distributor portion section is also provided with its oneself control system, can control the flowing containing ammonia incoming mixture in each distributor portion section individually.In addition, the distributor inlet 31 of each distributor portion section be positioned at the horizontal plane place that limited by collector 30 or near.Preferably, distributor inlet 31 and this horizontal plane of each distributor portion section vertically spaced apart be no more than 10 feet, no more than 5 feet.
This feature of distributor designs of the present invention is shown in Figure 12, the figure illustrates and is relative to each other arranged in four of inside reactor separately and independently feed distributor portion sections 100,102,104 and 106 with relation side by side substantially.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 top of the other.As further shown in Figure 12, each in distributor portion section 100,102,104 and 106 comprises distributor inlet 110,112,114 and 116 respectively, and all distributor inlet are all connected to the common feed header tube (not shown) being positioned at reactor 10 outside.In addition, the independent control valve 120,122,124 and 126 being connected to control system (not shown) is provided.
Utilize this feature, each independent distributor portion section can by the amount (mass flow) containing ammonia incoming mixture controlling individually to adjust by this distributor portion section feeding.This allows even better to control reactor on the whole, because each region of reactor can be controlled individually.This enables again each region by " adjustment " to mate other region, thus realizes optimum performance on whole reactor.
Various aspects described herein can be used for the reactor with various sizes diameter.In preferred at one, reactor can have from about 2 to about 12, about 5 to about 12 meters on the other hand, on the other hand about 8 to about 12 meters and the external diameter of about 9 to about 11 meters on the other hand.
Although foregoing describes only concrete examples more of the present invention, should be appreciated that and can carry out many amendments without departing from the spirit and scope of the present invention.All amendments are like this intended to be included in the scope of the present invention that is only limited by the appended claims.
Claims (17)
1. a distributor, it is effective to from the outside reactor wall by described reactor of ammonia oxidation reactor and supplies ammonia incoming mixture in the fluid bed of the ammoxidation catalyst of described inside reactor, and described distributor comprises: main header tube; Distributor inlet, it is communicated with described main header tube fluid; And multiple branch road distributor pipeline, each branch road sparger tube road has the near-end that is communicated with described main header tube fluid and the far-end away from described main header tube, each branch road distributor pipeline is also defined for the feed nozzle that will enter containing ammonia incoming mixture in the fluid bed of ammoxidation catalyst, wherein, the diameter of the ducted at least some of described branch road distributor reduces from its near-end to its far-end.
2. distributor according to claim 1, it is characterized in that, the ducted at least some of described branch road distributor is divided at least three portion's sections, wherein, in portion's section of the proximal end of described branch road distributor pipeline, there is major diameter, in portion's section of the far-end of described branch road distributor pipeline, there is minor diameter, and the portion's section in the middle of these described sections has and is less than described major diameter and the mid diameter being greater than described minor diameter.
3. distributor according to claim 1 and 2, is characterized in that, the size of diameter and number are effective to the gas velocity keeping about 10 to about 30 meter per seconds in all distributor pipelines.
4. distributor according to claim 1 and 2, is characterized in that, the entrance of each distributor portion section is located at the At The Height in 10 feet of the plane limited by the main header tube of described distributor portion section.
5. distributor according to claim 1, is characterized in that, the distal end with the branch road distributor pipeline of ever-reduced diameter is connected to the end cap penetrated by one or more feed nozzle.
6. distributor according to claim 1, is characterized in that, described reactor external diameter is about 2 to about 12 meters.
7. distributor according to claim 1, is characterized in that, described reactor external diameter is about 8 to about 12 meters.
8. distributor according to claim 1, is characterized in that, described reactor external diameter is about 9 to about 11 meters.
9., for the method by being supplied to ammonia oxidation reactor containing ammonia incoming mixture, described method comprises:
Ammonia incoming mixture is supplied from ammonia oxidation reactor outside by the reactor wall of described reactor and to the fluid bed of the ammoxidation catalyst of described inside reactor by distributor,
Wherein, described distributor comprises: main header tube; Distributor inlet, it is communicated with described main header tube fluid; And multiple branch road distributor pipeline, each branch road sparger tube road has the near-end that is communicated with described main header tube fluid and the far-end away from described main header tube, each branch road distributor pipeline is also defined for the feed nozzle that will enter containing ammonia incoming mixture in the fluid bed of ammoxidation catalyst, wherein, the diameter of the ducted at least some of described branch road distributor reduces from its near-end to its far-end.
10. method according to claim 9, it is characterized in that, the ducted at least some of described branch road distributor is divided at least three portion's sections, wherein, in portion's section of the proximal end of described branch road distributor pipeline, there is major diameter, in portion's section of the far-end of described branch road distributor pipeline, there is minor diameter, and the portion's section in the middle of these sections has and is less than described major diameter and the mid diameter being greater than described minor diameter.
11. methods according to claim 9 or 10, it is characterized in that, the size of diameter and number are effective to remain valid for catalyst purge being gone out the gas velocity outside described branch road distributor pipeline.
12. methods according to claim 9 or 10, it is characterized in that, the size of diameter and number effectively for keeping the gas velocity of about 10 to about 30 meter per seconds in all distributor pipelines.
13. methods according to claim 9 or 10, it is characterized in that, the entrance of each distributor portion section is located at the At The Height in 10 feet of the plane limited by the main header tube of described distributor portion section.
14. methods according to claim 1, is characterized in that, the distal end with the described branch road distributor pipeline of ever-reduced diameter is connected to the end cap penetrated by one or more feed nozzle.
15. distributors according to claim 1, is characterized in that, described reactor external diameter is about 2 to about 12 meters.
16. distributors according to claim 1, is characterized in that, described reactor external diameter is about 8 to about 12 meters.
17. distributors according to claim 1, is characterized in that, described reactor external diameter is about 9 to about 11 meters.
Priority Applications (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410124814.6A CN104941522B (en) | 2014-03-31 | 2014-03-31 | Feed distributor for ammonia oxidation reactor designs |
| EA201691968A EA032715B1 (en) | 2014-03-31 | 2015-03-24 | Feed sparger design for an ammoxidation reactor |
| PCT/US2015/022216 WO2015153196A1 (en) | 2014-03-31 | 2015-03-24 | Feed sparger design for an ammoxidation reactor |
| SA516371960A SA516371960B1 (en) | 2014-03-31 | 2016-09-29 | Ammoxidation Reactor Feed Sparger with Narrowing Laterals |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410124814.6A CN104941522B (en) | 2014-03-31 | 2014-03-31 | Feed distributor for ammonia oxidation reactor designs |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104941522A true CN104941522A (en) | 2015-09-30 |
| CN104941522B CN104941522B (en) | 2018-03-30 |
Family
ID=52875268
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410124814.6A Active CN104941522B (en) | 2014-03-31 | 2014-03-31 | Feed distributor for ammonia oxidation reactor designs |
Country Status (4)
| Country | Link |
|---|---|
| CN (1) | CN104941522B (en) |
| EA (1) | EA032715B1 (en) |
| SA (1) | SA516371960B1 (en) |
| WO (1) | WO2015153196A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108472615A (en) * | 2015-12-14 | 2018-08-31 | 特殊设计和工程局卡塔利扎托尔股份公司 | For to С3To С5The system that paraffin hydrocarbon carries out dehydrogenation |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109772234B (en) * | 2017-11-14 | 2024-01-05 | 中国石油化工股份有限公司 | Feed gas feed system for propylene ammoxidation reactor |
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| CN1033508C (en) * | 1992-10-14 | 1996-12-11 | 标准石油公司 | A method for eliminating nitriding during acrylonitrile production |
| WO2008017817A1 (en) * | 2006-08-08 | 2008-02-14 | The Boc Group Limited | Improvements in or relating to reaction vessels |
| CN203291710U (en) * | 2013-06-19 | 2013-11-20 | 山东润银生物化工股份有限公司 | Spray distributing device |
| CN203916613U (en) * | 2014-03-31 | 2014-11-05 | 英尼奥斯欧洲股份公司 | For the feed distributor of ammonia oxidation reactor |
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| DE2707478A1 (en) * | 1976-03-01 | 1977-09-08 | Pullman Inc | METHOD AND DEVICE FOR REGENERATING CRACK CATALYSTS |
| DE3022480A1 (en) | 1980-06-14 | 1982-01-07 | Uhde Gmbh, 4600 Dortmund | DEVICE FOR EXCHANGING HEAT BETWEEN AN NH (DOWN ARROW) 3 (DOWN ARROW) CONVERTER LEAVING CYCLE GAS AND WATER |
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| US4801731A (en) | 1987-12-14 | 1989-01-31 | E. I. Du Pont De Nemours And Company | Preparation of acrylonitrile |
| US5110584A (en) | 1990-10-22 | 1992-05-05 | Consumer Products Corporation | Scented nail enamels containing essential oils |
| KR0130715B1 (en) * | 1995-02-01 | 1998-04-08 | 유미꾸라 레이이찌 | Process for using fluidized bed and reactor |
| JPH08208583A (en) * | 1995-02-01 | 1996-08-13 | Asahi Chem Ind Co Ltd | Apparatus for producing alpha, beta-unsaturated nitrile |
| US6358483B1 (en) * | 1999-07-13 | 2002-03-19 | The Standard Oil Company | Sparger for oxygen injection into a fluid bed reactor |
| CN101396647B (en) * | 2007-09-29 | 2011-03-16 | 中科合成油技术有限公司 | Gas-liquid-solid three-phase suspended bed reactor for f-t synthesis and use thereof |
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2014
- 2014-03-31 CN CN201410124814.6A patent/CN104941522B/en active Active
-
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- 2015-03-24 WO PCT/US2015/022216 patent/WO2015153196A1/en active Application Filing
- 2015-03-24 EA EA201691968A patent/EA032715B1/en not_active IP Right Cessation
-
2016
- 2016-09-29 SA SA516371960A patent/SA516371960B1/en unknown
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| CN1033508A (en) * | 1987-12-15 | 1989-06-28 | 包头钢铁公司环境保护研究所 | Dry cleaning contains the method and apparatus that mixes the harmful components flue gas |
| CN1033508C (en) * | 1992-10-14 | 1996-12-11 | 标准石油公司 | A method for eliminating nitriding during acrylonitrile production |
| WO2008017817A1 (en) * | 2006-08-08 | 2008-02-14 | The Boc Group Limited | Improvements in or relating to reaction vessels |
| CN203291710U (en) * | 2013-06-19 | 2013-11-20 | 山东润银生物化工股份有限公司 | Spray distributing device |
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| CN108472615A (en) * | 2015-12-14 | 2018-08-31 | 特殊设计和工程局卡塔利扎托尔股份公司 | For to С3To С5The system that paraffin hydrocarbon carries out dehydrogenation |
Also Published As
| Publication number | Publication date |
|---|---|
| SA516371960B1 (en) | 2020-09-06 |
| EA032715B1 (en) | 2019-07-31 |
| WO2015153196A1 (en) | 2015-10-08 |
| EA201691968A1 (en) | 2017-02-28 |
| CN104941522B (en) | 2018-03-30 |
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