CN104941522B - Feed distributor for ammonia oxidation reactor designs - Google Patents
Feed distributor for ammonia oxidation reactor designs Download PDFInfo
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- CN104941522B CN104941522B CN201410124814.6A CN201410124814A CN104941522B CN 104941522 B CN104941522 B CN 104941522B CN 201410124814 A CN201410124814 A CN 201410124814A CN 104941522 B CN104941522 B CN 104941522B
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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
-
- 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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- 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
-
- 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
Quickly disconnect that each section of distributor is attached to each other by accessory and the wall of reactor is convenient for changing the different sections of the feed distributor used in commercial ammonia oxidation reactor by using air-tightness.In addition, the diameter of branch pipeline and it is attached to the diameters of feed nozzle of these branch pipes in these distributor sections and is altered to be advantageous to the Uniform Flow of the feed gas by these parts.Distributor can be subdivided into multiple feed distributor sections that arrangement is used for the control of more preferable reactor.Finally, nozzle can be provided with by being terminated at the end cap of the distal end of distributor branch pipes pipeline, and any ammoxidation catalyst inside distributor may be not inadvertently reached for removal.
Description
Background technology
In the business manufacture of acrylonitrile, propylene, ammonia and oxygen react according to following reaction scheme one：
CH2=CH-CH3 + NH3 + 3/2 O2 → CH2=CH-CN+ 3 H2O
Commonly referred to as this process of ammoxidation in the presence of suitable fluid bed ammoxidation catalyst at high temperature with
Gas phase is carried out.
Fig. 1 shows the typical ammonia oxidation reactor for carrying out the process.As shown in the drawing, reactor 10 includes anti-
Answer wall 12, air grid 14, feed distributor (sparger) 16, cooling coil 18 and cyclone (cyclone) 20.Just
Often during operation, plant air is filled with reactor 10 by air intake 22, and the mixture of propylene and ammonia passes through charging point
Cloth device 16 is filled with reactor 10.Both flows are all sufficiently high, so that the bed 24 of the ammoxidation catalyst of inside reactor flows
Change, the catalytic ammoxidation of propylene and ammonia to acrylonitrile occurs wherein.
Product gas leaves reactor 10 by reactor effluent outlet 26 as caused by reaction.Before doing so,
Product gas passes through cyclone 20, and cyclone 20 removes any ammoxidation catalyst that these gases can be carried secretly, to pass through dipleg
(diplegs) 25 catalyst bed 24 is returned to.Ammoxidation is high exothermic heat, therefore is taken away using cooling coil 18 excessive
Heat, so as to which reaction temperature is maintained at into proper level.
Propylene and ammonia can form explosive mixture with oxygen.However, at normal operating temperatures, inside reactor 10 by
The ammoniation catalyst of fluidisation prevents from exploding, the catalyst preferential catalytic ammoxidation reaction before blast can occur.Phase
Ying Di, reactor 10, which is designed and operated into, to allow plant air contact propylene and ammonia in the normal operation period uniquely
Side be in the fluid bed of ammoxidation catalyst 24, and therefore only catalyst temperature be up to enough catalytic ammoxidation reaction
When.
Therefore, the traditional approach that propylene and ammonia are fed to reactor 10 uses the institute such as in U.S. 5,256,810
The feed distributor system 16 shown, the disclosure of which is incorporated herein by reference.Such as Fig. 1 and figure of ' 810 patents
Shown in 2 (this two width figure is renumbered as Fig. 2 and Fig. 3 of the literature), feed distributor 16 take a series of supply pipes or
The form of pipeline, it includes main collector 30 and branch pipe (lateral) 32, and branch pipe 32 is attached to collector 30 and separated from collector 30.
A series of feed nozzles 34 downwards are limited in collector 30 and branch pipe 34, and the mixture of propylene and ammonia is in normal reaction device
It is filled with during operation by feed nozzle 34.The number and spacing of branch pipe 32 and feed nozzle 34 cause across the whole of reactor 10
Every square metre of about 10 to 30 feed nozzle altogether is substantially evenly located in individual cross-sectional area.
Generally, each feed nozzle 34 is surrounded by charging shield 36, and charging shield 36 takes the shape of the short section of pipeline
Formula, the internal diameter of the pipeline are the several times of the diameter of nozzle 34.Charging shield 34 enables the speed of the gas for passing nozzle 10
Enough significantly to slow down before catalyst bed 24 is exited into, this prevent the disintegration of original generable catalyst.
Plant air generally through entering catalyst bed 24 (Fig. 1) after air grid 14, air grid 14 be located at into
Expect the lower section of distributor 16.As the well-known, the form of continuous metal sheet is usually taken in air grid 14, and it is limited to therein
A series of airports or nozzle.The diameter of air nozzle, through air grid 14 plant air mass flow and pass through into
Expect that the mass flow of propylene/ammonia mixture of distributor 16 is chosen so that the ammoxidation catalyst in catalyst bed 24 is just
Often fluidized completely by these gases during operation.
Air nozzle is typically provided with the protective atmosphere shield (not shown) of their own, and the shield is usually located at air grid
14 lower sections.In addition, in many cases, feed nozzle 34 is set with the air nozzle in air grid 14 with one-one relationship,
Wherein each charging shield 36 is directly directed at its corresponding air nozzle to promote to pass the gas of both different nozzles
Quick and sufficiently mixing.Referring to U.S. 4,801,731.
Although propylene/ammonia feed system of this general type works well, there are some shortcomings in it really.For example,
Due to being constantly exposed to ammonia at high temperature, form the metal of feed distributor 16 over time and undergo nitridation.As a result, feed
Each section of distributor 16 and sometimes whole feed distributor need to be changed frequently.It is very high that this can be cost, especially
It is due to that reactor must dead halt when being changed.
The Second Problem associated with this propylene/ammonia feed system is the inhomogeneities of operation.This is not only adversely
The productivity ratio of influence system, and uneven nitridation is also results in, this has further aggravated nitridation problem.
The content of the invention
According to the present invention, there is provided a kind of new feed distributor design, it significantly reduces these problems, and one
Problem is substantially completely eliminated in the case of a little.
According to the new distributor designs feature, accessory is quickly disconnected using air-tightness by the main collector pipe of distributor
Road is attached to the wall for the reactor that main header tube is passed through, or the various pipelines for forming feed distributor are connected into that
This, or both.Due to this feature, when replacing becomes if necessary, to change some or all of chargings and be distributed due to excessively nitrogenizing
Time and work needed for device substantially reduce.
According to another feature of the new distributor designs, with the entrance from feed distributor to each feed nozzle
Travel path increase, the relative diameter of feed nozzle 34 are slightly increased.Due to this feature, through entering containing ammonia for each feed nozzle
The mass flow of material mixture becomes between feed nozzle closer to uniformly.This causes inside reactor between zones more again
Close to uniform operation, this enables productivity ratio to maximize.This feature is also by ensuring that the gas of correct flow flows through all the time
Distributor feed nozzle minimizes catalyst reverse flow (back up), i.e. is starting, shuts down and is even being urged during normal operating
Pollution of the agent to feed distributor.
According to another feature of the new distributor designs, the diameter of branch pipe 32 (that is, connects from its near-end to its distal end from it
It is connected to the end to its end away from main header tube of main header tube) reduce.Due to this feature, containing for these branch pipes is flowed through
Whole length of the speed of ammonia incoming mixture along branch pipe and especially keep sufficiently high in its far-end, it is any by what be may be present
Ammoxidation catalyst is purged to next feed nozzle 34, will pass through the feed nozzle from branch pipe internal discharge.
According to another newly-designed feature, feed distributor 16 is subdivided into multiple feed distributor sections, each
Section has the ingress port of their own for being fed from reactor external reception containing ammonia.Due to this feature, can be achieved to anti-
Device is answered in interregional more preferable control, because individually control system can be used to that each feed distributor is individually monitored and controlled
Operation in section.
Therefore, the present invention provides a kind of improved distributor in one embodiment, for from ammonia oxidation reactor
Supply charging containing ammonia is mixed in the outside reactor wall by reactor and the fluid bed of the ammoxidation catalyst to inside reactor
Used in compound, the improved distributor includes：Main header tube；Distributor inlet, it is in fluid communication with main header tube, should
Distributor inlet is rigidly attached to reactor wall；And multiple branch road distributor pipelines, itself and main collector distributor pipeline stream
Body connects, and the branch road distributor pipeline limits feed nozzle for propylene/ammonia incoming mixture is discharged into ammoxidation catalyst
Fluid bed in, wherein distributor inlet quickly disconnects accessory by means of air-tightness and is rigidly attached to reactor wall.
In another embodiment, the invention provides a kind of improved distributor, for outside ammonia oxidation reactor
Supply is containing ammonia charging mixing in the fluid bed of reactor wall of the portion by reactor and the ammoxidation catalyst to inside reactor
Used in thing, the improved distributor includes：Main header tube；Distributor inlet, it is in fluid communication with main header tube；And
Multiple branch road distributor pipelines, itself and main collector distributor fluid communication, the branch road distributor pipeline limit feed nozzle
For incoming mixture containing ammonia is discharged into the fluid bed of ammoxidation catalyst, at least one wherein in branch road distributor pipeline
Attachment is quickly disconnected to main header tube by corresponding air-tightness a bit.
In yet another embodiment, the invention provides a kind of improved distributor, for outside ammonia oxidation reactor
Supply is containing ammonia charging mixing in the fluid bed of reactor wall of the portion by reactor and the ammoxidation catalyst to inside reactor
Used in thing, the improved distributor includes：Main header tube；Distributor inlet, it is in fluid communication with main header tube；And
Multiple branch road distributor pipelines, itself and main collector distributor fluid communication, each branch road distributor pipeline limit charging spray
Mouth is for incoming mixture containing ammonia is discharged into the fluid bed of ammoxidation catalyst, and wherein feed nozzle has at least two not
With size, wherein less feed nozzle is located closer at distributor inlet, and larger nozzle is located further away from point
Cloth device porch, depending on propylene/ammonia incoming mixture from distributor inlet is advanced through distributor to the distance of each nozzle.
In yet another embodiment, the invention provides a kind of improved distributor, for outside ammonia oxidation reactor
Ammonia incoming mixture is supplied in the fluid bed of reactor wall of the portion by reactor and the ammoxidation catalyst to inside reactor
Middle use, the improved distributor include：Main header tube；Distributor inlet, it is in fluid communication with main header tube；It is and more
Individual branch road distributor pipeline, each branch road sparger tube road have the near-end being in fluid communication with main header tube and remote main collector
The distal end of pipeline, each branch road distributor pipeline further define the fluidisation for incoming mixture containing ammonia to be discharged into ammoxidation catalyst
Feed nozzle in bed, the wherein at least some of diameter in branch road distributor pipeline reduce from its near-end to its distal end.
In yet another embodiment, the invention provides a kind of improved distributor, for outside ammonia oxidation reactor
Supply is containing ammonia charging mixing in the fluid bed of reactor wall of the portion by reactor and the ammoxidation catalyst to inside reactor
Used in thing, the improved distributor includes：Main header tube；Distributor inlet, it is in fluid communication with main header tube；And
Multiple branch road distributor pipelines, itself and main collector distributor fluid communication, the branch road distributor pipeline limit feed nozzle
For incoming mixture containing ammonia is discharged into the fluid bed of ammoxidation catalyst, wherein improved distributor is by being arranged in reaction
Multiple feed distributor sections inside device are formed, and each feed distributor section has the distributor inlet of their own, with
In outside reactor, the system of the branch road distributor pipeline of the main header tube and their own of their own receives and fed containing ammonia.
Brief description of the drawings
The present invention is better understood by referring to the following drawings, in the accompanying drawings：
Fig. 1 is schematic diagram, and it illustrates the reactor section of the conventional ammonia oxidation reactor for preparing acrylonitrile；
Fig. 2 is plan, and it illustrates the downside of the conventional sparger system of Fig. 1 ammonia oxidation reactor；
Fig. 3 is to show the feed nozzle of Fig. 2 conventional sparger system along the sectional view of Fig. 2 line 3-3 interceptions, Fig. 3
With associated charging shield；
Fig. 4 is sectional view, shows that the main header tube of the feed distributor of commercial ammonia oxidation reactor is penetrated and connected
To the mode of the side wall of reactor；
Fig. 5 is analogous to Fig. 4 sectional view, shows the main collector of a feature of the present invention, wherein feed distributor
Duct penetration and the side wall that connector is connected to reactor is quickly disconnected by means of air-tightness；
Fig. 6 is that Fig. 5 air-tightness quickly disconnects the side view of connector；
Fig. 7 is analogous to Fig. 2 sectional view, shows another feature of the invention, and wherein distributor branch pipes pipeline is borrowed
Help air-tightness and quickly disconnect the main header tube that connector is connected to distributor；
Fig. 8 is plan, and the air-tightness for illustrating in greater detail Fig. 7 quickly disconnects connector；
Fig. 9 A and Fig. 9 B are the sectional views of the distributor branch pipes pipeline used according to another feature of the invention, are shown
How the diameter of the branch pipe reduces as the distance away from distributor header tube increases；
Figure 10 A, Figure 10 B and Figure 10 C are the sectional elevations of Fig. 9 distributor branch pipes pipeline, further illustrate the branch pipe
Diameter how with away from distributor header tube distance increase and reduce；
Figure 11 A, Figure 11 B, Figure 11 C and Figure 11 D are points used according to another feature of the sparger system of the present invention
The vertical sectional view of cloth device branch pipe end-cap；And
Figure 12 is plan, and it illustrates the feed distributor of another feature of the invention, wherein acrylonitrile reactor
It is subdivided into multiple feed distributor sections.
Embodiment
Definition
As used herein, " fluid communication " refers to effective for allowing identical liquid or steam to be sent to separately from a region
The connection in one region or pipeline.
As used herein, the non-solder for referring to allow object to disconnect by non-destructive mode " is releasedly fixed " to connect
Connect.For example, releasedly fixation can refer to bolt, crab-bolt, the flange being spirally connected and combinations thereof.
As used herein, " incoming mixture containing ammonia " refers to blendings of ammonia and saturation the and/or undersaturated C3 to C4 hydrocarbon
Thing.Saturation and/or undersaturated C3 may include propane, propylene, butane, butylene and their mixture to C4 hydrocarbon.
It is quick to disconnect connector
As described above, the subject matter run into the operation of commercial propylene nitrile reactor is feed distributor due to shape
Failed over time into the nitridation of its metal.In order to solve this problem, it has been suggested that by for example in U.S. 3,704,
690th, the anti-nitro-alloy shown in U.S. 4,401,153, U.S. 5,110,584 and EP 0 113 524 is distributed to manufacture
Device.Unfortunately, due to the distinctive some problems of fluid catalyst ammoxidation reaction and its cost reason, it has therefore proved that the solution
Certainly scheme in commercial propylene nitrile reactor using being unsuccessful.
Meanwhile U.S. 5,256,810 describes a kind of distributor being used in substantially elimination commercial propylene nitrile reactor
The method of nitridation, this method make the temperature of the ammonia inside distributor keep sufficiently low by using the blanket insulation specially designed,
To prevent to nitrogenize.However, due to cost and somewhat complex design, the solution is also proved to be unsatisfactory.
According to this feature of the present invention, this problem that distributor is failed over time due to nitride metal is by adopting
The distributor quickly and easily changed by the use of each section for enabling distributor and as overall whole distributor is set
Count to solve.Although stilling need to shut down acrylonitrile reactor when carrying out this replacing, for comparing conventional practice, realize
This replacing the spent time greatly shortens.As a result, for losing both production time and human cost, for continuous
On the basis of solve the problems, such as this nitridation totle drilling cost significantly reduce.
Fig. 4, Fig. 5 and Fig. 6 show a feature of the present invention, wherein this distributor nitrogenizes problem by using airtight
Property quickly disconnects connector and the entrance of sparger system is connected into the outer wall of ammonia oxidation reactor to solve.In the drawings
In shown specific embodiment, the end of main collector 30 is directly attached to the wall 40 of reactor 10.Therefore, in this design, should
Collect the entrance 31 that tube end forms distributor section 16.In other designs, intermediate duct can be used to connect distributor inlet 31
It is connected to collector 30.For convenience, the reactor combined shown in Fig. 4, Fig. 5 and Fig. 6 is designed to describe this feature of the present invention.
It will be appreciated, however, that this feature and its advantage are applied equally to the design of other reactors, such as wherein distributor inlet
31 designs separated with main collector 30 by intermediate duct.
As shown in figure 4, the distributor inlet 31 of feed distributor 16 is attached to the usual manner of the wall 40 of reactor 10
It is to pass through welding.Correspondingly, when main header tube 30 needs to be replaced, it is necessary to using weld repairs method, wherein tightly enclosing
Part reactor wall 40 around main header tube 30 is cut off by welding, the opening being consequently formed in shell of reactor 12
By being welded with suitable patch to repair, and new main header tube 30 is also by welding and installed in the reaction repaired
In wall 40.This needs the live manpower of significant quantity and additional material, and this can be with high costs.
According to this feature of the present invention, the problem by main header tube 30 by using for being attached to reactor wall 40
Air-tightness quickly disconnects connector design to avoid.The example of such connector is shown in fig. 5 and fig., is shown in figure
" manhole " 42 with the form of cylindrical sleeve 44, the first side of cylindrical sleeve 44 are permanently welded to be formed in a gastight manner
The periphery 46 of permanent opening 48 in reactor wall 40.The opposite side of cylindrical sleeve 44 or the second side carrying flange 50,
Flange 50 limits a series of through holes for receiving bolt 52 wherein.Meanwhile the hoop 54 of flat circular slab form is with airtight
Mode is permanently welded to the outside of main header tube 30.In addition, hoop 54 is also limited in the flange 50 corresponding to manhole 42
Through hole a series of through holes 56.
, can be by master simply by the flange 50 that the hoop 54 of main header tube 30 is screwed to manhole 42 using the structure
Header tube 30 is releasably secured to the reactor wall 40 of reactor 10 in a gastight manner.In an identical manner, can be simply
By the way that hoop 54 is gone to be spirally connected to make main header tube 30 separate with reactor wall 40 from flange 50.Accordingly, due to excessive nitridation
And the existing main collector 30 become unavailable may be replaced by simply go to be spirally connected and be spirally connected process again and simply and readily
Realize.Due to not needing Site Welding, so the replacing program implements appearance compared with the weld repairs method routinely carried out
The more and cost that is easy to get is lower.
Fig. 2, Fig. 7 and Fig. 8 show another feature of the invention, wherein quickly disconnecting connector using air-tightness to solve
The problem of certainly distributor branch pipes nitrogenize.As shown in Figure 2, by branch pipeline (or " branch pipe ") 32 be attached to main header tube (or
" collector ") 30 usual manner is to pass through welding.Correspondingly, when each branch pipe 32 needs to be replaced due to excessively nitrogenizing,
Using weld repairs method, wherein old branch pipe is separated by welding or other suitable cutting techniques with main header tube 30,
And new branch pipe is passed through into weld attachment to main header tube 30.This is also required to the live manpower of significant quantity, and this is with high costs
's.
According to this feature of the present invention, the problem by each branch pipe 32 by using for being attached to main header tube 30
Air-tightness quickly disconnects connector design to avoid.This shows in figures 7 and 8, is shown in figure for by each branch pipe 32
The air-tightness for being connected to the main header tube 30 of sparger system 16 quickly disconnects connector 60.Although these accompanying drawings are shown each
Branch pipe is directly connected to main header tube 30, it is to be understood that, one or more of these branch pipes can be for example by means of centre
Pipeline (not shown) is connected indirectly to main header tube 30.
It is the part wherein coordinated (i.e., when connected and together and even that air-tightness, which quickly disconnects connector 60,
Connect the part removed when being disconnected) it is designed specifically to only be joined to that (that is, without using welding or adhesive) by mechanical means
This connector.Air-tightness quickly disconnects connector and is also designed to keep tight seal under the high temperature conditions, the hot conditions
For for example during the normal operating of typical commercial ammonia oxidation reactor and when when such reactor start-up and shutdown
That run into during the temperature cycles of generation.The example for being adapted to the commercially available connector of this purposes is to be available from Grayloc
Endoporus sealing clamp connector between Products (Houston, Texas) Grayloc metals.It is adapted to the commercially available of this purposes
Another example of connector is to be available from Freudenberg Oil ＆ Gas Technologies (Houston, Texas)
Vector groups Techlok clamp connectors.Another example for being adapted to the commercially available connector of this purposes is to be available from
Australasian Fittings ＆ Flanges (Osborne Park, WA, Australia) G-Lok®Fixture connects
Device.Conventional flange connection is less desirable for this application, because they are due to the temperature during reactor operates
Circulate and easily leak out.
Fig. 8 shows that typical air-tightness quickly disconnects the structure of connector 60, including the connector interconnects branch pipe 30
To the mode of main header tube 30.As illustrated, connector 60 is by hub 64 and 66 is received and the clamp assembly that keeps together
62 are formed, and hub 64 and 66 is carried on branch pipe 32 and the end 68 and 70 faced for collecting pipe joint 72.Fixed just when by bolt 73
During position, clamp assembly 62 causes metallic packing ring (not shown) to be fixed between hub 64 and 66 and sealingly engages the He of hub 64
66, it is gas-tight seal so as to be formed between branch pipe 32 and collector 30.
Connector 60 is quickly disconnected by using air-tightness, each branch pipe 32 can be simply by being spirally connected or going the fixture that is spirally connected
Component 62 and fixed to main header tube 30 and being removed from main header tube 30.Becoming accordingly, due to excessive nitridation can not
May be replaced by of existing branch pipe 32 is simply gone to be spirally connected and is spirally connected process again and simply and easily realizes.Due to not
Site Welding is needed, the replacing program implements much easier and cost more compared with the weld repairs method routinely carried out
It is low.
Various aspects specifically described herein can be used for the reactor with various sizes diameter.In terms of one is preferable,
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 another
On the one hand about 9 to about 11 meters of external diameter.
Variable feed nozzle size
According to another feature of the new distributor designs, with the entrance from feed distributor to each feed nozzle
Travel path increase, the diameter of feed nozzle 34 are slightly increased.
When incoming mixture containing ammonia is advanced through distributor 16, the heat transfer of the hot gas outside distributor causes
The temperature increase of incoming mixture inside distributor.As a result, the temperature for leaving the incoming mixture of each feed nozzle is not
With, be specifically dependent upon time of the incoming mixture before leaving in distributor have how long.Specifically, leave positioned at more
The temperature of incoming mixture away from the feed nozzle at distributor inlet is hotter to be located closer to distributor inlet in leaving
The temperature of the incoming mixture of feed nozzle.In this context, " further from " and " closer to " should be understood to mean just
For the length of inbound path further from closer to distributor inlet, the travel path start from distributor inlet and terminate at into
Material mixture leaves the specific feed nozzle of distributor by it.
In the ammonia oxidation reactor of routine, the diameter of feed nozzle 34 (Fig. 3) is all identical.As a result, by positioned at
The density of the incoming mixture left further from the feed nozzle 34 at distributor inlet is less than by being located closer to distributor
The density for the incoming mixture that the feed nozzle 34 of porch leaves, because density is inversely proportional with temperature.This causes to pass through position again
It is less than in the mass flow of the incoming mixture containing ammonia left further from the feed nozzle 34 at distributor inlet and passes through positioned at more
The mass flow for the incoming mixture that feed nozzle 34 at distributor inlet leaves, precondition is other condition phases
Together, because mass flow is directly proportional to density.Regrettably, this uniformity of the mass flow of each feed nozzle is passed through
Shortage causes to be less than optimal reactor performance on the whole, because the incoming mixture containing ammonia of the bed 24 into ammoxidation catalyst
Amount (that is, the gross mass of unit interval) in reactor area of the feed nozzle further from distributor inlet be less than charging spray
Mouth is closer in the region of the entrance.
According to this feature of the present invention, this problem is overcome by changing the size of distributor feed nozzle 34, wherein
It is located further away from those feed nozzles at distributor inlet and is more than those feed nozzles being located closer at distributor inlet.
" size ", " bigger " and " smaller " refers to the cross-sectional area of nozzle opening in this context.In this respect, reactor external diameter with
The ratio of the number of various sizes of feed nozzle is about 0.5 to about 2.5, on the other hand about 1 to about 2 and in the opposing party
Face about 1.5 to about 2.
Although can be used in specific acrylonitrile reactor has various sizes of nozzle, it has been found that, make
With with from about 2 to about 10 kinds of different sizes, on the other hand about 2 to about 8 kinds of different sizes, about 2 to about 6 kinds on the other hand
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 and on the other hand about 5 to
About 8 kinds of various sizes of nozzles (diameter for being specifically dependent upon reactor) are enough to overcome to be had in most of acrylonitrile reactors
The above mentioned problem of uneven charging.On the other hand, if reactor has about 2 to about 5 meters of external diameter, then feed nozzle has
There are about 3 to about 4 kinds of different sizes.On the other hand, if reaction utensil has more than about 5 to about 12 meters of diameter, then charging
Nozzle has about 5 to about 8 kinds of different sizes.Thus, for example, use with three kinds of various sizes of nozzles generally for big
It is enough for " small-sized " acrylonitrile reactor of the diameter of about 8 to 12 feet (~ 2.4 to ~ 3.7 meters).On the other hand, use
It is more suitable for five or six kind of various sizes of nozzle with about 26 to 32 feet (~ 7.9 to ~ 9.7 meters) or bigger diameter
" large-scale " acrylonitrile reactor.
In general, the size (cross-sectional area) of feed nozzle 34 is 15 to 80mm in commercial propylene nitrile reactor2, more
Typically 20 to 60mm2In the range of, it is specifically dependent upon the size of reactor and the density of feed nozzle, i.e. every square metre is anti-
Answer the number of the feed nozzle 34 of device cross section.This feature that this identical jet size design can also combine the present invention makes
With.In other words, the average nozzle size of all feed nozzles will correspond to these values in given acrylonitrile reactor.
For the difference of jet size, maximum nozzle and minimum in the set of nozzles for specific ammonia oxidation reactor
Ratio of the nozzle on cross-sectional area can be as small as 1.02 and greatly to 1.35.The size of feed nozzle with medium size can pass through
Calculate and/or normal experiment and be readily determined.
In this regard, be using the purpose with various sizes of feed nozzle 34 in order to realize feed nozzle it
Between as close possible to uniform incoming mixture mass flow.In given sparger system, specifically enter through any
Expect that the mass flow of the incoming mixture of nozzle is based primarily upon its density, density is based primarily upon its temperature again.Correspondingly, for having
The specific dimensions for having the specific nozzle of medium size can be by referring to the estimating temperature of the incoming mixture through the feed nozzle
And be readily determined, the estimating temperature can be readily determined by actual measurement or by appropriate heat transfer calculations again.
Using this feature, through the incoming mixture containing ammonia of each feed nozzle mass flow become feed nozzle it
Between closer to uniformly.This causes inside reactor between zones closer to uniform operation again, and this enables productivity ratio most
Bigization.In this respect, by the mass flow of any one feed nozzle in about the 5% of the mass flow of any other nozzle,
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 is also starting, stopped to minimize by ensuring that the gas of correct flow flows through distributor feed nozzle all the time
Pollution (catalyst reverse flow) of the catalyst to feed distributor during machine and even normal operating.
Branch pipe with ever-reduced diameter
According to another feature of the new distributor designs, the diameter of branch road distributor pipeline or " branch pipe " 32 is near from its
Its distal end (that is, being connected to the end of collector 30 to its opposed end away from collector 30 from it) is held to reduce.
In the acrylonitrile reactor of routine, the whole length of the diameter of branch road distributor pipeline 32 along pipeline is identical
's.For should designing, it is substantially reduced by the flow of the incoming mixture of pipeline from its near-end to its distal end, because entering near
Many incoming mixtures at end leave pipeline by the feed nozzle 34 of the length positioning along pipeline.As a result, in these pipelines
The speed of internal incoming mixture is too slow at or near pipeline distal end, so that any ammoxidation to may be present in there
Catalyst, which does not have, to be significantly affected.
According to the present invention this feature, this problem by from its near-end to its distal end reduce branch road distributor pipeline or
The diameter of " branch pipe " 32 avoids.Fig. 9 A, Fig. 9 B, Figure 10 A, Figure 10 B and Figure 10 C show this feature of the present invention.Such as at this
Shown in a little figures, the diameter of branch pipe 32 progressively reduces from its near-end 37 to its distal end 39.
Using this feature, the speed of the incoming mixture containing ammonia can keep sufficiently high along the whole length of pipeline, so that can be non-
Any ammoxidation catalyst inside intentional ground contamination sparger system 16 is purged to next feed nozzle 34, herein, urges
Agent will discharge together with the feeding gas for flowing through the feed nozzle.Although also set earlier for the mechanism for removing catalyst
Used in meter, but the speed of the feeding gas at or near the distal end of branch pipe is too slow in the designs, so that it cannot by that
In existing any catalyst purge to next feed nozzle.According to this feature of the present invention, the problem is by by the straight of branch pipe
Footpath reduces to avoid from its near-end to its distal end.As a result, the speed of the feeding gas inside these branch pipelines keeps enough
Height, any catalyst purge of there will be may be present in next available feed nozzle, or even the far-end in pipeline.Make
Cause appropriate high speed even in the far-end of pipeline to be also possible with ever-reduced diameter, while also avoid in pipeline
The unacceptably high speed in proximal end and/or pressure drop.
Although Fig. 9 A, Fig. 9 B, Figure 10 A, Figure 10 B and Figure 10 C show that branch pipe 32 has three single portions of different-diameter
Section, it is to be understood that, any different-diameter for facilitating number can be used according to the present invention.In general, the size of different-diameter
With number be selected as keeping in all distributor pipelines (that is, collector 30 and all branch pipes 32) about 10 to 30, preferably 15 to
The gas velocity of 25 meter per seconds.
Various aspects specifically described herein can be used for the reactor with various sizes diameter.In terms of one preferable, instead
Answer device and 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 another
The external diameter that about 9 to about 11 meters of aspect.
Branch pipe end-cap
In the optional preferred embodiment of features above of the present invention is realized, the branch of ever-reduced diameter is configured with
The distal end 39 of pipeline 32 is terminated with the end cap penetrated by one or more feed nozzles 34 (referring to Figure 11).As described above, should
The ever-reduced feature of diameter ensures that the speed that the feeding gas of branch pipe 32 are flowed through at or near its distal end keeps of a relatively high.It is logical
Cross with branch pipe 32 of the termination of end cap 90 with smaller distal end 39 for including one or more feed nozzles, it can be ensured that the speed is kept
It is sufficiently high, keep movement may be present in any ammoxidation catalyst at or near the distal end, so as to its eventually through
Feed nozzle 34 blows out branch pipe.Figure 11 A and Figure 11 B show circular in configuration, and a figure has the feed nozzle 34 being centered about,
And another figure has the feed nozzle 34 reduced.Figure 11 C and Figure 11 D show flat configuration, and a figure, which has, to be centered about
Feed nozzle 34, and another figure have reduce feed nozzle 34.The feed nozzle configuration of reduction makes wherein catalyst can
The dead space for becoming to be trapped minimizes, but possible manufacturing cost is higher.
Multiple feed distributor sections
According to another feature of the new distributor designs, feed distributor 16 is subdivided into multiple feed distributor portions
Section, each section have the ingress port of their own for from reactor external reception containing ammonia charging.
In all typical commercial ammonia oxidation reactors as shown in Figure 2, using single feed distributor system 16, wherein
The collector 30 of single horizontal orientation is fed for all branch pipes 32 of system.These systems it is most of in, in Fig. 2 and Fig. 4
Ground is further illustrated, the entrance 31 of distributor 16 is located at the side wall of reactor 10 in the horizontal plane substantially the same with collector 30
In.
(that is, there is the straight of greater than about 6 meters (~ 20 feet) when this distributor designs are used for larger acrylonitrile reactor
The reactor in footpath) in when, between the most short travel path and most long travel path that are undergone by feeding gas containing ammonia in distributor
Difference can become very big because unstripped gas enters the only one end of collector 30 and therefore must march to the other end always
To reach attached branch pipe thereunto.As a result, the temperature of the incoming mixture of each feed nozzle 34, density and therefore matter are left
Measure flow can between feed nozzle significant changes, be specifically dependent upon feed nozzle the location of in sparger system.Such as
Upper described, this deviation in temperature, density and mass flow can be caused in reactor performance and the side of the uniformity of nitridation two
Sizable problem in face.
In order to solve the problem, it has been suggested that distributor inlet 31 is moved into the position far above collector 30 and utilizes conjunction
Suitable pipeline engages distributor inlet 31 at the center of collector 30.Idea is, because feeding gas are transported in collector 30
At one in the heart rather than only its end, so the feeding gas are by collector 30 to all branch pipes 32 and pass through all branch pipes 32
Flowing will than original situation closer to uniformly.However, the problem of this method is that distributor inlet 31 is connected into collector 30
Center needed for additional line become to be nitrogenized over time, this is very unfavorable due to indicated above
's.
According to this feature of the present invention, feed distributor 16 is divided into multiple feed distributor sections, wherein each distribution
Device sub-portion section be provided with their own distributor inlet 31 for from reactor external reception containing ammonia charging.Each distributor section
The control system of their own is additionally provided with, in order to the stream for the incoming mixture containing ammonia being individually controlled in each distributor section
It is dynamic.In addition, the distributor inlet 31 of each distributor section is located at or near the horizontal plane limited by collector 30.Preferably,
The distributor inlet 31 of each distributor section and the horizontal plane be vertically spaced from being no more than 10 feet, no more than
5 feet.
Figure 12 illustrates the figure illustrates relative to each other with substantially simultaneously for this feature of the distributor designs of the present invention
The relation of row is arranged in four separated and independent feed distributor sections 100,102,104 and 106 of inside reactor.Herein
In context, the height that each distributor section is arranged substantially at the same in inside reactor is should be understood to mean " side by side "
Degree, without being arranged to one on top of the other.As further shown in Figure 12, distributor section 100,102,104
With 106 in each include distributor inlet 110,112,114 and 116 respectively, all distributor inlets, which are all connected to, to be located at
Common feed header tube (not shown) outside reactor 10.Further it is provided that it is connected to the list of control system (not shown)
Only control valve 120,122,124 and 126.
Using this feature, each individually distributor section is individually controllable to be fed with adjustment by the distributor section
The incoming mixture containing ammonia amount (mass flow).This allows on the whole even preferably to control reactor, because reaction
Each region of device is individually controllable.This enables each region by " adjustment " to match other regions again, so as to whole
Optimum performance is realized on individual reactor.
Various aspects specifically described herein can be used for the reactor with various sizes diameter.In terms of one is preferable,
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 another
On the one hand about 9 to about 11 meters of external diameter.
Although foregoing describes only some specific examples of the present invention, it is to be understood that, do not departing from the spirit of the present invention
With many modifications can be carried out in the case of scope.All such modifications are intended to be included in the sheet being limited only by the following claims
In the range of invention.
Claims (17)
1. a kind of distributor, its effective for outside ammonia oxidation reactor by the reactor wall of the reactor and to described
Supply ammonia feed gas mixtures, the distributor include in the fluid bed of the ammoxidation catalyst of inside reactor：Main collector
Pipeline；Distributor inlet, it is in fluid communication with the main header tube；And multiple branch road distributor pipelines, each branch road point
Air manifold tube road has the near-end being in fluid communication with the main header tube and the distal end away from the main header tube, each branch road
Distributor pipeline further defines the feed nozzle for feed gas mixtures containing ammonia to be discharged into the fluid bed of ammoxidation catalyst,
Wherein, at least some of diameter in the branch road distributor pipeline reduces from its near-end to its distal end so that in the branch road
Whole length of the speed of ammonia feed gas mixtures in distributor pipeline along branch road distributor pipeline is kept, so as to promote
Pollute any ammoxidation catalyst inside the distributor and be discharged together with the ammonia feed gas mixtures and pass through charging
Nozzle.
2. distributor according to claim 1, it is characterised in that at least some in the branch road distributor pipeline are divided
Into at least three sections, wherein, the section in the proximal end of the branch road distributor pipeline has major diameter, in the branch road point
The section of the far-end in air manifold tube road has minor diameter, and the section among these described sections is described big straight with being less than
Footpath and the mid diameter for being more than the minor diameter.
3. distributor according to claim 1 or 2, it is characterised in that the size and number of diameter are effective for all
The gas velocity of 10 to 30 meter per seconds is kept in distributor pipeline.
4. distributor according to claim 1 or 2, it is characterised in that the entrance of each distributor section is located at by institute
State at the height in 10 feet of the plane of the main header tube restriction of distributor section.
5. distributor according to claim 1, it is characterised in that there is the branch road distributor pipeline of ever-reduced diameter
Distal end be terminated with the end cap penetrated by one or more feed nozzles.
6. distributor according to claim 1, it is characterised in that the reactor external diameter is 2 to 12 meters.
7. distributor according to claim 1, it is characterised in that the reactor external diameter is 8 to 12 meters.
8. distributor according to claim 1, it is characterised in that the reactor external diameter is 9 to 11 meters.
9. a kind of method for being used to for feed gas mixtures containing ammonia to be supplied to ammonia oxidation reactor, methods described include：
By distributor outside ammonia oxidation reactor by the reactor wall of the reactor and to the inside reactor
The fluid bed supply ammonia feed gas mixtures of ammoxidation catalyst,
Wherein, the distributor includes：Main header tube；Distributor inlet, it is in fluid communication with the main header tube；And
Multiple branch road distributor pipelines, each branch road sparger tube road have the near-end that is in fluid communication with the main header tube and remote
The distal end of the main header tube, each branch road distributor pipeline further defines is discharged into ammonia oxygen for that will contain ammonia feed gas mixtures
Change the feed nozzle in the fluid bed of catalyst, wherein, at least some of diameter in the branch road distributor pipeline is near from its
Its distal end is held to reduce so that the speed of the ammonia feed gas mixtures in the branch road distributor pipeline is along branch road distributor
The whole length of pipeline is kept, and is fed so as to promote to pollute any ammoxidation catalyst inside the distributor with the ammonia
Admixture of gas is discharged together passes through feed nozzle.
10. according to the method for claim 9, it is characterised in that at least some in the branch road distributor pipeline are divided
Into at least three sections, wherein, the section in the proximal end of the branch road distributor pipeline has major diameter, in the branch road point
The section of the far-end in air manifold tube road has a minor diameter, and the section among these sections have less than the major diameter and
More than the mid diameter of the minor diameter.
11. the method according to claim 9 or 10, it is characterised in that the size and number of diameter are effective for maintaining
Effectiveness is in catalyst purge to be gone out to the gas velocity outside the branch road distributor pipeline.
12. the method according to claim 9 or 10, it is characterised in that the size and number of diameter are efficiently used in institute
It is distributed the gas velocity that 10 to 30 meter per seconds are kept in device pipeline.
13. the method according to claim 9 or 10, it is characterised in that the entrance of each distributor section is located at by institute
State at the height in 10 feet of the plane of the main header tube restriction of distributor section.
14. according to the method for claim 9, it is characterised in that there is the branch road distributor of ever-reduced diameter
The distal end of pipeline is terminated with the end cap penetrated by one or more feed nozzles.
15. according to the method for claim 9, it is characterised in that the reactor external diameter is 2 to 12 meters.
16. according to the method for claim 9, it is characterised in that the reactor external diameter is 8 to 12 meters.
17. according to the method for claim 9, it is characterised in that the reactor external diameter is 9 to 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 CN104941522A (en) | 2015-09-30 |
| CN104941522B true 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) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2617397C1 (en) * | 2015-12-14 | 2017-04-24 | Акционерное общество "Специальное конструкторско-технологическое бюро "Катализатор" | System of dehydration of paraffinic hydrocarbons c3-c5 |
| 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 |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1033508C (en) * | 1992-10-14 | 1996-12-11 | 标准石油公司 | A method for eliminating nitriding during acrylonitrile production |
| 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 |
Family Cites Families (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2007528C3 (en) | 1970-02-19 | 1973-10-25 | Friedrich Uhde Gmbh, 4600 Dortmund | Device for heat exchange in ammonia synthesis plants |
| 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 |
| US4554135A (en) | 1982-11-26 | 1985-11-19 | C F Braun & Co. | Ammonia converter |
| US4801731A (en) | 1987-12-14 | 1989-01-31 | E. I. Du Pont De Nemours And Company | Preparation of acrylonitrile |
| CN1012136B (en) * | 1987-12-15 | 1991-03-27 | 包头钢铁公司环境保护研究所 | Dry method and apparatus for cleaning smoke containing combined harmful components |
| 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 |
| GB0615759D0 (en) * | 2006-08-08 | 2006-09-20 | Boc Group Plc | Improvements in and relating to reaction vessels |
| 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 |
| 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 |
-
2014
- 2014-03-31 CN CN201410124814.6A patent/CN104941522B/en active Active
-
2015
- 2015-03-24 EA EA201691968A patent/EA032715B1/en not_active IP Right Cessation
- 2015-03-24 WO PCT/US2015/022216 patent/WO2015153196A1/en active Application Filing
-
2016
- 2016-09-29 SA SA516371960A patent/SA516371960B1/en unknown
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1033508C (en) * | 1992-10-14 | 1996-12-11 | 标准石油公司 | A method for eliminating nitriding during acrylonitrile production |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2015153196A1 (en) | 2015-10-08 |
| EA032715B1 (en) | 2019-07-31 |
| EA201691968A1 (en) | 2017-02-28 |
| CN104941522A (en) | 2015-09-30 |
| SA516371960B1 (en) | 2020-09-06 |
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