CN104941523B - Feed distributor for ammonia oxidation reactor designs - Google Patents
Feed distributor for ammonia oxidation reactor designs Download PDFInfo
- Publication number
- CN104941523B CN104941523B CN201410124901.1A CN201410124901A CN104941523B CN 104941523 B CN104941523 B CN 104941523B CN 201410124901 A CN201410124901 A CN 201410124901A CN 104941523 B CN104941523 B CN 104941523B
- Authority
- CN
- China
- Prior art keywords
- distributor
- reactor
- ammonia
- pipeline
- header tube
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- 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
-
- 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
-
- 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
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/00911—Sparger-type feeding elements
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 being attached to the diameters of feed nozzle of these branch pipes in these distributor sections and being altered to be conducive to the Uniform Flow of the feed gas by these components.Distributor can be subdivided into multiple feed distributor sections of the arrangement for the control of better reactor.Finally, nozzle can be equipped with by being terminated at the end cap of the distal end of distributor branch pipes pipeline, for removing any ammoxidation catalyst that may not inadvertently reach inside distributor.
Description
Background technique
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 fluidized bed ammoxidation catalyst at high temperature with
Gas phase carries 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 in reactor 10 by air intake 22, and the mixture of propylene and ammonia passes through charging point
Cloth device 16 is filled in reactor 10.The flow of the two is 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 is wherein occurring.
The product gas generated by reaction leaves reactor 10 by reactor effluent outlet 26.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 that reaction temperature is maintained at 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 explosion can occur.Phase
Ying Di, reactor 10, which is designed and operated into, to allow in the normal operation period plant air contact propylene and ammonia uniquely
Side be in the fluidized bed of ammoxidation catalyst 24, and therefore only the temperature of catalyst be up to enough catalytic ammoxidation reaction
When.
For this purpose, the traditional approach that propylene and ammonia are fed to reactor 10 is used 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 (Fig. 2 and Fig. 3 that this two width figure is renumbered as the literature), feed distributor 16 take a series of supply pipes or
The form of pipeline comprising main collector 30 and branch pipe (lateral) 32, branch pipe 32 are attached to collector 30 and separate 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 make across the whole of reactor 10
Every square metre of about 10 to 30 feed nozzle in total is substantially evenly located in a cross-sectional area.
In general, each feed nozzle 34 is surrounded by charging shield 36, 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 for being pierced by the gas of nozzle 10
Enough significantly to slow down before exiting into catalyst bed 24, this prevent the disintegrations of original generable catalyst.
Plant air usually pass through air grid 14 after enter catalyst bed 24 (Fig. 1), air grid 14 be located at into
Expect 16 lower section of distributor.As the well-known, the form of continuous metal sheet is usually taken in air grid 14, defined therein
A series of airports or nozzle.The diameter of air nozzle, across air grid 14 plant air mass flow and pass through into
Expect that propylene/ammonia mixture mass flow of distributor 16 is chosen, so that the ammoxidation catalyst in catalyst bed 24 is just
Often fluidized completely during operation by these gases.
Air nozzle is typically provided with the protective atmosphere shield (not shown) of their own, which is usually located at air grid
14 lower sections.In addition, in many cases, feed nozzle 34 is arranged with the air nozzle in air grid 14 with one-one relationship,
Wherein each charging shield 36 is directed at its corresponding air nozzle directly to promote the gas for being pierced by both different nozzles
Quickly and adequately mix.Referring to U.S. 4,801,731.
Although the propylene of this general type/ammonia feed system works well, there are certain disadvantages in it really.For example,
Due to being constantly exposed to ammonia at high temperature, forms the metal of feed distributor 16 and undergo nitridation over time.As a result, charging
Each section of distributor 16 and sometimes entire feed distributor need to be replaced frequently.It is very high that this can be cost, especially
It is since when being replaced, reactor must dead halt.
Second Problem associated with this propylene/ammonia feed system is the inhomogeneities of operation.This is not only adversely
The productivity of influence system, and uneven nitridation is also resulted in, nitridation problem has been further aggravated in this.
Summary of the invention
According to the present invention, a kind of new feed distributor design is provided, it significantly reduces these problems, and one
Problem is substantially completely eliminated in a little situations.
According to the new distributor designs feature, main collector pipe of the accessory by distributor is quickly disconnected using air-tightness
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 to that
This, or both.Due to this feature, when replacement becomes when necessary, to replace some or all of charging distributions due to excessively nitrogenizing
Time needed for device and labour substantially reduce.
According to another feature of the new distributor designs, with the entrance from feed distributor to each feed nozzle
Travel path increases, and the relative diameter of feed nozzle 34 is slightly increased.Due to this feature, across each feed nozzle containing ammonia into
The mass flow of material mixture becomes between feed nozzle closer to uniformly.This leads to inside reactor between zones more again
Close to uniform operation, this enables productivity to maximize.This feature is also by ensuring that the gas of correct flow flows through always
Distributor feed nozzle minimizes catalyst reverse flow (back up), that is, in starting, shuts down and even urges 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 is from its proximal end to its distal end (that is, from its company
It is connected to the end to its end far from main header tube of main header tube) reduce.Due to this feature, containing for these branch pipes is flowed through
The speed of ammonia incoming mixture along branch pipe whole length and especially its far-end keep it is sufficiently high, 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 to feed for receiving outside reactor containing ammonia.Due to this feature, it can be achieved that anti-
Answer device 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
It is mixed that the charging containing ammonia is supplied in outside through the reactor wall of reactor and into the fluidized bed of the ammoxidation catalyst of inside reactor
It closes and is used in object, which includes: main header tube；Distributor inlet is in fluid communication with main header tube, should
Distributor inlet is rigidly attached to reactor wall；And multiple branch distributor pipelines, with main collector distributor pipeline stream
Body connection, the branch distributor pipeline limit feed nozzle for propylene/ammonia incoming mixture to be discharged into ammoxidation catalyst
Fluidized bed in, wherein distributor inlet quickly disconnects accessory by means of air-tightness and is rigidly attached to reactor wall.
In another embodiment, the present invention provides a kind of improved distributors, for outside ammonia oxidation reactor
Portion is supplied through the reactor wall of reactor and into the fluidized bed of the ammoxidation catalyst of inside reactor containing ammonia charging mixing
It is used in object, which includes: main header tube；Distributor inlet is in fluid communication with main header tube；And
Multiple branch distributor pipelines, with main collector distributor fluid communication, which limits feed nozzle
To be discharged into the fluidized bed of ammoxidation catalyst for ammonia incoming mixture will to be contained, wherein at least one in branch distributor pipeline
Attachment is quickly disconnected to main header tube by corresponding air-tightness a bit.
In yet another embodiment, the present invention provides a kind of improved distributors, for outside ammonia oxidation reactor
Portion is supplied through the reactor wall of reactor and into the fluidized bed of the ammoxidation catalyst of inside reactor containing ammonia charging mixing
It is used in object, which includes: main header tube；Distributor inlet is in fluid communication with main header tube；And
Multiple branch distributor pipelines, with main collector distributor fluid communication, each branch distributor pipeline limits charging spray
Mouth for that will contain ammonia incoming mixture to be discharged into the fluidized bed of ammoxidation catalyst, and wherein feed nozzle does not have at least two not
With size, wherein lesser feed nozzle is located closer at distributor inlet, and biggish nozzle is located further away from point
Cloth device inlet, depending on propylene/ammonia incoming mixture from distributor inlet be advanced through distributor to each nozzle distance.
In yet another embodiment, the present invention provides a kind of improved distributors, for outside ammonia oxidation reactor
Portion supplies ammonia incoming mixture through the reactor wall of reactor and into the fluidized bed of the ammoxidation catalyst of inside reactor
Middle use, the improved distributor include: main header tube；Distributor inlet is in fluid communication with main header tube；And it is more
A branch distributor pipeline, each branch sparger tube road have the proximal end being in fluid communication with main header tube and far from main collectors
The distal end of pipeline, each branch distributor pipeline further define the fluidisation for being discharged into ammoxidation catalyst for that will contain ammonia incoming mixture
Feed nozzle in bed, wherein the diameter of at least some of branch distributor pipeline reduces from its proximal end to its distal end.
In yet another embodiment, the present invention provides a kind of improved distributors, for outside ammonia oxidation reactor
Portion is supplied through the reactor wall of reactor and into the fluidized bed of the ammoxidation catalyst of inside reactor containing ammonia charging mixing
It is used in object, which includes: main header tube；Distributor inlet is in fluid communication with main header tube；And
Multiple branch distributor pipelines, with main collector distributor fluid communication, which limits feed nozzle
To be discharged into the fluidized bed of ammoxidation catalyst for ammonia incoming mixture will to be contained, wherein improved distributor is by being arranged in reaction
Multiple feed distributor sections inside device are constituted, and each feed distributor section has the distributor inlet of their own, with
In outside reactor, the system of the branch distributor pipeline of the main header tube of their own and their own receive containing ammonia feed.
Detailed description of the invention
It is better understood the present invention by referring to the following drawings, in the accompanying drawings:
Fig. 1 is schematic diagram, and it illustrates the reactor sections for the conventional ammonia oxidation reactor for being used to prepare acrylonitrile；
Fig. 2 is plan view, and it illustrates the downsides of the conventional sparger system of the ammonia oxidation reactor of Fig. 1；
Fig. 3 is the cross-sectional view intercepted along the line 3-3 of Fig. 2, and Fig. 3 shows the feed nozzle of the conventional sparger system of Fig. 2
With associated charging shield；
Fig. 4 is cross-sectional view, and the main header tube for showing 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 the cross-sectional view of Fig. 4, shows a feature of the present invention, wherein the main collector of 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 the air-tightness of Fig. 5 quickly disconnects the side view of connector；
Fig. 7 is analogous to the cross-sectional view of Fig. 2, shows another feature of the invention, and wherein distributor branch pipes pipeline is borrowed
Help air-tightness and quickly disconnects the main header tube that connector is connected to distributor；
Fig. 8 is plan view, 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 for the distributor branch pipes pipeline that another feature according to the present invention uses, and 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 the distributor branch pipes pipeline of Fig. 9, 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 that another feature of sparger system according to the present invention uses
The vertical cross-sectional view of cloth device branch pipe end-cap；And
Figure 12 is plan view, it illustrates another feature of the invention, the wherein feed distributor of acrylonitrile reactor
It is subdivided into multiple feed distributor sections.
Specific 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 company for referring to and object being allowed to disconnect by non-destructive mode " is releasedly fixed "
It connects.For example, releasedly fixation can refer to bolt, anchor bolt, the flange being spirally connected and their combination.
As used herein, " incoming mixture containing ammonia " refers to ammonia and saturation and/or unsaturated C3 being blended to C4 hydrocarbon
Object.Saturation and/or unsaturated C3 to C4 hydrocarbon may include propane, propylene, butane, butylene and their mixture.
Quickly disconnect connector
As described above, the main problem encountered in the operation of commercial propylene nitrile reactor is feed distributor due to shape
It fails over time at the nitridation of its metal.In order to solve this problem, it has been suggested that by for example in U.S. 3,704,
690, 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 certain 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 describe it is a kind of for substantially eliminating the distributor in 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, the solution is also proved to be unsatisfactory due to cost and somewhat complex design.
This feature according to the present invention, this problem that distributor is failed over time due to nitride metal is by adopting
The distributor that entire distributor with each section for enabling distributor and as a whole is quickly and easily replaced is set
Meter is to solve.Although, compared to for conventional practice, being realized when carrying out this replacement there is still a need for shutting down acrylonitrile reactor
This replacement the time it takes 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 to the outer wall of ammonia oxidation reactor to solve.In the drawings
Shown in 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 constitutes 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 design in conjunction with shown in Fig. 4, Fig. 5 and Fig. 6 is described to this feature of the invention.
It will be appreciated, however, that this feature and its advantage are applied equally to other reactor designs, 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 to be 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 weld repairs method is used, 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
It is repaired by being welded with suitable patch, and new main header tube 30 is mounted on the reaction repaired also by welding
In wall 40.This needs the live manpower and additional material of significant quantity, this can be with high costs.
This feature according to the present invention, the problem is by using for being attached to reactor wall 40 for main header tube 30
Air-tightness disconnects connector design quickly to avoid.The example of such connector is shown in fig. 5 and fig., is shown in figure
First side of " manhole " 42 with 44 form of cylindrical sleeve, cylindrical sleeve 44 is permanently welded to be formed in a gastight manner
The periphery 46 of permanent opening 48 in reactor wall 40.The other side of cylindrical sleeve 44 or second side carry flange 50,
Flange 50 is limited in a series of through-holes for wherein receiving bolt 52.Meanwhile the hoop 54 of flat circular slab form is with airtight
Mode is permanently welded to the outside of main header tube 30.Correspond in the flange 50 of manhole 42 in addition, hoop 54 also limits
Through-hole a series of through-holes 56.
Using the structure, the flange 50 simply by the hoop 54 of main header tube 30 to be screwed to manhole 42 can be by master
Header tube 30 is releasably secured to the reactor wall 40 of reactor 10 in a gastight manner.It in an identical manner, can be simply
Main header tube 30 is separated with reactor wall 40 by that will bind round 54 and go to be spirally connected 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
It realizes.Due to not needing site welding, so the replacement 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 disconnecting connector quickly 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, this is with high costs
's.
This feature according to the present invention, the problem is by using for being attached to main header tube 30 for each branch pipe 32
Air-tightness disconnects connector design quickly 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 attached 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 component that wherein cooperates (that is, when connected and together and even that air-tightness, which quickly disconnects connector 60,
Connect the component removed when being disconnected) it is designed specifically to only be joined to that by mechanical means (that is, without using welding or adhesive)
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 such reactor start-up and when shutting down
That encountered during the temperature cycles of generation.The example for being suitble to the commercially available connector of this purposes is to be available from Grayloc
Inner hole sealing clamp connector between the Grayloc metal of Products (Houston, Texas).It is suitble to the commercially available of this purposes
Another example of connector is to be available from Freudenberg Oil & Gas Technologies (Houston, Texas)
Vector group Techlok clamp connector.Another example for being suitble to the commercially available connector of this purposes is to be available from
The G-Lok of Australasian Fittings & Flanges (Osborne Park, WA, Australia)®Fixture connection
Device.Conventional flange connection is less desirable for this application, because they are due to the temperature during reactor operates
It recycles and easily leaks out.
Fig. 8 shows the structure that typical air-tightness quickly disconnects connector 60, including the connector interconnects branch pipe 30
To the mode of main header tube 30.As shown, connector 60 is by receiving and the clamp assembly that keeps together hub 64 and 66
62 form, and hub 64 and 66 is carried on the end 68 and 70 of 32 sum aggregate pipe fitting 72 of branch pipe faced.When fixed just by bolt 73
When position, clamp assembly 62 causes metallic packing ring (not shown) to be fixed between hub 64 and 66 and sealingly engages 64 He of hub
66, to be formed between branch pipe 32 and collector 30 gas-tight seal.
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 be fixed to main header tube 30 and from main header tube 30 remove.Becoming accordingly, due to excessive nitridation can not
May be replaced by of existing branch pipe 32 simply goes to be spirally connected and is spirally connected process again and simply and easily realizes.Due to not
Site welding is needed, which implements much easier and cost more compared with the weld repairs method routinely carried out
It is low.
The reactor that various aspects described herein can be used for having various sizes diameter.In a preferred aspect,
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 outer 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 increases, and the diameter of feed nozzle 34 is slightly increased.
When incoming mixture containing ammonia is advanced through distributor 16, the heat transmitting of the hot gas outside distributor is caused
The temperature of incoming mixture inside distributor increases.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.It is located at more specifically, leaving
The temperature of incoming mixture far 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
Expect that mixture passes through its specific feed nozzle for leaving distributor.
In conventional ammonia oxidation reactor, the diameter of feed nozzle 34 (Fig. 3) is all identical.As a result, by being located 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 inlet 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 by being located 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, pass through this uniformity of the mass flow of each feed nozzle
Shortage causes on the whole lower than optimal reactor performance, because of the incoming mixture containing ammonia of the bed 24 into ammoxidation catalyst
Amount (that is, gross mass of unit time) be less than in reactor area of the feed nozzle further from distributor inlet and sprayed in charging
Mouth is closer in the region of the entrance.
This feature according to the present invention, this problem are overcome by changing the size of distributor feed nozzle 34, wherein
It those of is located further away from distributor inlet feed nozzle and is greater than and those of be located closer at distributor inlet feed nozzle.
" size ", " bigger " and " smaller " refers to the cross-sectional area of nozzle opening in this context.In this respect, reactor outer 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 another 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 problem unevenly fed.On the other hand, if reactor has about 2 to about 5 meters of outer diameter, feed nozzle tool
There are about 3 to about 4 kinds of different sizes.On the other hand, it if reaction utensil has more than about 5 to about 12 meters of diameter, feeds
Nozzle has about 5 to about 8 kinds of different sizes.Thus, for example, using tool, there are three types 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, it uses
It is more suitable for that there is about 26 to 32 feet (~ 7.9 to ~ 9.7 meters) or bigger diameter with five or six kind of various sizes of nozzle
" large size " 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, that is, every square metre is anti-
Answer the number of the feed nozzle 34 of device cross section.This identical jet size design also makes in combination with this feature of the invention
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 routine 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, pass through it is any specifically into
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
There are the specific dimensions of the specific nozzle of medium size can be by referring to the estimating temperature for the incoming mixture for passing through the feed nozzle
And be readily determined, which can be readily determined again by actual measurement or by heat transfer calculations appropriate.
Using this feature, across the mass flow of the incoming mixture containing ammonia of each feed nozzle become feed nozzle it
Between closer to uniformly.This causes inside reactor between zones closer to uniform operation again, this enable productivity 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 also minimizes by ensuring that the gas of correct flow flows through distributor feed nozzle always and is starting, stopping
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 distributor pipeline or " branch pipe " 32 is close from it
Its distal end (that is, being connected to the end of collector 30 to its opposed end far from collector 30 from it) is held to reduce.
In conventional acrylonitrile reactor, the diameter of branch distributor pipeline 32 is identical along the whole length of pipeline
's.It for should designing, is substantially reduced by the flow of the incoming mixture of pipeline from its proximal end to its distal end, because entering close
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.
This feature according to the present invention, this problem by from its proximal end to its distal end reduce branch 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 invention.Such as at this
A little as shown in the figure, the diameter of branch pipe 32 is gradually reduced from its proximal 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 and urges herein
Agent will discharge together with the feeding gas for flowing through the feed nozzle.Although the mechanism for removing catalyst is also being set earlier
It is 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.This feature according to the present invention, the problem is by by the straight of branch pipe
Diameter reduces from its proximal end to its distal end to avoid.As a result, the speed of the feeding gas inside these branch pipelines keeps enough
Height will may be present in any catalyst purge of there to next available feed nozzle, or even the far-end in pipeline.Make
Making appropriate high speed even with ever-reduced diameter is also possible in the far-end of pipeline, while also being avoided in pipeline
The unacceptably high speed and/or pressure drop in proximal end.
Although Fig. 9 A, Fig. 9 B, Figure 10 A, Figure 10 B and Figure 10 C show that branch pipe 32 has three individual 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.
The reactor that various aspects described herein can be used for having various sizes diameter.It is anti-in a preferred aspect,
It answers 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 outer diameter that about 9 to about 11 meters of aspect.
Branch pipe end-cap
In the optional preferred embodiment for realizing features above of the invention, it is configured with the branch of ever-reduced diameter
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 speed that the ever-reduced feature of diameter ensures to flow through the feeding gas of branch pipe 32 at or near its distal end keeps relatively high.It is logical
It crosses 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 so that may be present in any ammoxidation catalyst at or near the distal end keeps movement, so as to its eventually by
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 reduced feed nozzle 34.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 reduced feed nozzle 34.Reduced feed nozzle configuration makes wherein that catalyst can
Become the dead space being trapped minimum, 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 to feed for receiving outside reactor containing ammonia.
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 that all branch pipes 32 of system are fed.These systems it is most of in, in Fig. 2 and Fig. 4
Further shown in, 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.
When this distributor designs for biggish acrylonitrile reactor (that is, having greater than about 6 meters (~ 20 feet) straight
The reactor of diameter) in when, by feeding gas containing ammonia between most short travel path experienced in distributor and longest travel path
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, leaving the temperature of the incoming mixture of each feed nozzle 34, density and therefore matter
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 two side of reactor performance and the uniformity of nitridation
Sizable problem in face.
In order to solve this problem, it has been suggested that distributor inlet 31 is moved into the position much higher than collector 30 and utilizes conjunction
The center of collector 30 is arrived in the engagement of distributor inlet 31 by suitable pipeline.Idea is, because feeding gas is transported in collector 30
The heart rather than only at one in its end, so the feeding gas is by collector 30 to all branch pipes 32 and passing 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 to collector 30
Center needed for additional line become to be nitrogenized over time, this is very unfavorable due to indicated above
's.
This feature according to the present invention, feed distributor 16 is divided into multiple feed distributor sections, wherein each distribution
Device sub-portion section is equipped with the distributor inlet 31 of their own to feed for receiving outside reactor containing ammonia.Each distributor section
It is additionally provided with the control system of their own, 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 no more than 10 feet, no more than
5 feet.
This feature of distributor designs of the invention is shown in FIG. 12, and the figure illustrates relative to each other with substantially simultaneously
The relationship of row is arranged in four separated and independent feed distributor sections 100,102,104 and 106 of inside reactor.Herein
In context, " side by side " should be understood to mean the height that each distributor section is arranged substantially at the same in inside reactor
Degree, without being arranged to one on top of the other.As further shown in Figure 12, distributor section 100,102,104
Distributor inlet 110,112,114 and 116 is respectively included with each of 106, 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 being 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 of reaction
Each region of device is individually controllable.This enables each region by " adjustment " to match other regions again, thus whole
Optimum performance is realized on a reactor.
The reactor that various aspects described herein can be used for having various sizes diameter.In a preferred aspect,
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 outer diameter.
Although foregoing describes only some specific examples of the invention, it is to be understood that, do not departing from spirit of the invention
With many modifications can be carried out in the case where range.All such modifications are intended to be included in the sheet being limited only by the following claims
In the range of invention.
Claims (26)
1. a kind of distributor, effective for outside ammonia oxidation reactor by the reactor wall of the reactor and to described
Incoming mixture containing ammonia is supplied in the fluidized bed of the ammoxidation catalyst of inside reactor, the distributor includes: main collector pipe
Road；Distributor inlet is in fluid communication with the main header tube, and the distributor inlet is rigidly attached to the reactor
Wall；And multiple branch distributor pipelines, be in fluid communication with the main header tube, the branch distributor pipeline limit into
Expect nozzle to be discharged into the fluidized bed of ammoxidation catalyst for ammonia incoming mixture will to be contained, wherein the distributor inlet is borrowed
Help air-tightness and quickly disconnect accessory to be rigidly attached to the reactor wall, and the distal end of the branch distributor pipeline
It is connected to the end cap penetrated by feed nozzle.
2. distributor according to claim 1, which is characterized in that the reactor wall, which limits, to be permanently open, and into
One step wherein, it includes the column with the first side and second side opposite with first side that the air-tightness, which quickly disconnects accessory,
Shape sleeve, wherein the first side of the cylindrical sleeve is permanently welded to the periphery being permanently open in a gastight manner,
It further includes the hoop for being permanently welded to the outside of the main header tube in a gastight manner that the air-tightness, which quickly disconnects accessory,
Wherein, described to bind round the second side for being releasably secured to the cylindrical sleeve.
3. distributor according to claim 1, which is characterized in that the incoming mixture containing ammonia be ammonia and saturation and/or
Unsaturated C3 to C4 hydrocarbon blend.
4. distributor according to claim 3, which is characterized in that the institute of ammonia and saturation and/or unsaturated C3 to C4 hydrocarbon
It states blend and is selected from the group being made of propane, propylene, butane, butylene and their mixture.
5. distributor according to claim 1, which is characterized in that the reactor outer diameter is 2 to 12 meters.
6. distributor according to claim 1, which is characterized in that the reactor outer diameter is 8 to 12 meters.
7. distributor according to claim 1, which is characterized in that the reactor outer diameter is 9 to 11 meters.
8. a kind of distributor, effective for outside ammonia oxidation reactor by the reactor wall of the reactor and to described
Incoming mixture containing ammonia is supplied in the fluidized bed of the ammoxidation catalyst of inside reactor, the distributor includes: main collector pipe
Road；Distributor inlet is in fluid communication with the main header tube；And multiple branch distributor pipelines, with the main collection
Pipeline is in fluid communication, and the branch distributor pipeline limits feed nozzle for the incoming mixture containing ammonia to be discharged into ammonia
In the fluidized bed of oxidation catalyst, wherein at least some of described branch distributor pipeline is quick by corresponding air-tightness
Attachment is disconnected to the main header tube, the main header tube includes for being attached to corresponding branch distributor pipeline
Multiple collection pipe fittings, and further, wherein it includes metallic packing ring and clamping group that each air-tightness, which quickly disconnects accessory,
Part, the clamping component are configured to for the metallic packing ring to be fixed on corresponding collection pipe fitting and branch point in a gastight manner
Between the end faced in air manifold tube road, the distal end of the branch distributor pipeline is terminated with the end cap penetrated by feed nozzle.
9. distributor according to claim 8, which is characterized in that the ammonia incoming mixture is for ammonia and saturation and/or not
The blend of C3 to the C4 hydrocarbon of saturation.
10. distributor according to claim 9, which is characterized in that the institute of ammonia and saturation and/or unsaturated C3 to C4 hydrocarbon
It states blend and is selected from the group being made of propane, propylene, butane, butylene and their mixture.
11. distributor according to claim 8, which is characterized in that the reactor outer diameter is 2 to 12 meters.
12. distributor according to claim 8, which is characterized in that the reactor outer diameter is 8 to 12 meters.
13. distributor according to claim 8, which is characterized in that the reactor outer diameter is 9 to 11 meters.
14. a kind of method for being supplied to ammonia oxidation reactor for ammonia incoming mixture will to be contained, which comprises
By distributor by the reactor wall of the reactor and to the inside reactor outside the ammonia oxidation reactor
The fluidized bed of ammoxidation catalyst supplies incoming mixture containing ammonia,
Wherein, the distributor includes: main header tube；Distributor inlet is in fluid communication with the main header tube, described
Distributor inlet is rigidly attached to the reactor wall；And multiple branch distributor pipelines, with the main header tube
It is in fluid communication, the branch distributor pipeline limits feed nozzle to be discharged into ammoxidation catalyst for that will contain ammonia incoming mixture
Fluidized bed, wherein the distributor inlet quickly disconnects accessory by means of air-tightness and is rigidly attached to the reactor wall,
And the distal end of the branch distributor pipeline is terminated with the end cap penetrated by feed nozzle.
15. according to the method for claim 14, which is characterized in that the reactor wall, which limits, to be permanently open, and into
One step, wherein it includes having the first side and second side opposite with first side that the air-tightness, which quickly disconnects accessory,
Cylindrical sleeve, wherein the first side of the cylindrical sleeve is permanently welded to the week being permanently open in a gastight manner
Side, it further includes the outside for being permanently welded to the main header tube in a gastight manner that the air-tightness, which quickly disconnects accessory,
Hoop, wherein described to bind round the second side for being releasably secured to the cylindrical sleeve.
16. according to the method for claim 14, which is characterized in that the ammonia incoming mixture is for ammonia and saturation and/or not
The blend of C3 to the C4 hydrocarbon of saturation.
17. according to the method for claim 16, which is characterized in that the institute of ammonia and saturation and/or unsaturated C3 to C4 hydrocarbon
It states blend and is selected from the group being made of propane, propylene, butane, butylene and their mixture.
18. according to the method for claim 14, which is characterized in that the reactor outer diameter is 2 to 12 meters.
19. according to the method for claim 14, which is characterized in that the reactor outer diameter is 8 to 12 meters.
20. according to the method for claim 14, which is characterized in that the reactor outer diameter is 9 to 11 meters.
21. a kind of method for being supplied to ammonia oxidation reactor for ammonia incoming mixture will to be contained, which comprises
By distributor by the reactor wall of the reactor and to the inside reactor outside the ammonia oxidation reactor
The fluidized bed of ammoxidation catalyst supplies incoming mixture containing ammonia,
Wherein, the distributor includes: main header tube；Distributor inlet is in fluid communication with the main header tube；And
Multiple branch distributor pipelines are in fluid communication with the main header tube, and the branch distributor pipeline limits feed nozzle
For the incoming mixture containing ammonia to be discharged into the fluidized bed of ammoxidation catalyst, wherein the branch distributor pipeline
At least some of attachment is quickly disconnected to the main header tube, the main header tube packet by corresponding air-tightness
Multiple collection pipe fittings for being attached to corresponding branch distributor pipeline are included, and further, wherein each air-tightness is fast
It includes metallic packing ring and clamping component that accessory is opened in quick-break, and the clamping component is configured to the metallic packing ring with airtight side
Formula is fixed between corresponding collection pipe fitting and the end of branch distributor pipeline faced, the branch distributor pipeline it is remote
It is terminated with the end cap penetrated by feed nozzle.
22. according to the method for claim 21, which is characterized in that the ammonia incoming mixture is for ammonia and saturation and/or not
The blend of C3 to the C4 hydrocarbon of saturation.
23. according to the method for claim 22, which is characterized in that the institute of ammonia and saturation and/or unsaturated C3 to C4 hydrocarbon
It states blend and is selected from the group being made of propane, propylene, butane, butylene and their mixture.
24. according to the method for claim 21, which is characterized in that the reactor outer diameter is 2 to 12 meters.
25. according to the method for claim 21, which is characterized in that the reactor outer diameter is 8 to 12 meters.
26. according to the method for claim 21, which is characterized in that the reactor outer diameter is 9 to 11 meters.
Priority Applications (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410124901.1A CN104941523B (en) | 2014-03-31 | 2014-03-31 | Feed distributor for ammonia oxidation reactor designs |
| EA202090252A EA039268B1 (en) | 2014-03-31 | 2015-03-24 | Feed sparger design for an ammoxidation reactor |
| EA201691865A EA037139B1 (en) | 2014-03-31 | 2015-03-24 | Feed sparger design for an ammoxidation reactor |
| PCT/US2015/022224 WO2015153197A2 (en) | 2014-03-31 | 2015-03-24 | Feed sparger design for an ammoxidation reactor |
| SA516371964A SA516371964B1 (en) | 2014-03-31 | 2016-09-29 | Feed Sparger Design for an Ammoxidation Reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410124901.1A CN104941523B (en) | 2014-03-31 | 2014-03-31 | Feed distributor for ammonia oxidation reactor designs |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104941523A CN104941523A (en) | 2015-09-30 |
| CN104941523B true CN104941523B (en) | 2019-04-02 |
Family
ID=54145977
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410124901.1A Active CN104941523B (en) | 2014-03-31 | 2014-03-31 | Feed distributor for ammonia oxidation reactor designs |
Country Status (4)
| Country | Link |
|---|---|
| CN (1) | CN104941523B (en) |
| EA (2) | EA037139B1 (en) |
| SA (1) | SA516371964B1 (en) |
| WO (1) | WO2015153197A2 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109772236B (en) | 2017-11-14 | 2022-08-12 | 中国石油化工股份有限公司 | Fluid distributor, reaction device and application thereof |
| CN109772235B (en) * | 2017-11-14 | 2023-10-31 | 中国石油化工股份有限公司 | Feed gas feed system for propylene ammoxidation reactor |
| CN110451108A (en) * | 2019-08-21 | 2019-11-15 | 中冶焦耐(大连)工程技术有限公司 | A kind of feeding device of inner floating roof benzene class storage tank |
| CN112495307A (en) * | 2020-10-27 | 2021-03-16 | 中国船舶重工集团公司第七0三研究所 | Feeding distributor for waste alkali oxidation reactor |
Family Cites Families (11)
| 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 |
| 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 |
| US4698211A (en) * | 1985-08-19 | 1987-10-06 | Exxon Chemical Patents Inc. | Catalyst injection for Ziegler polymerization |
| 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 |
| US5256810A (en) * | 1992-10-14 | 1993-10-26 | The Standard Oil Company | Method for eliminating nitriding during acrylonitrile production |
| DE10155565B4 (en) * | 2001-11-12 | 2006-09-14 | InfraServ GmbH & Co. Höchst KG | Container with injection and / or degassing device and its use |
| GB0615759D0 (en) * | 2006-08-08 | 2006-09-20 | Boc Group Plc | Improvements in and relating to reaction vessels |
| MX362330B (en) * | 2012-04-30 | 2019-01-11 | Curtiss Wright Flow Control Corp | Center feed system employing removable inserts in a retractable injection nozzle. |
| CN203955188U (en) * | 2014-03-31 | 2014-11-26 | 英尼奥斯欧洲股份公司 | For the feed distributor of ammonia oxidation reactor |
-
2014
- 2014-03-31 CN CN201410124901.1A patent/CN104941523B/en active Active
-
2015
- 2015-03-24 EA EA201691865A patent/EA037139B1/en not_active IP Right Cessation
- 2015-03-24 EA EA202090252A patent/EA039268B1/en unknown
- 2015-03-24 WO PCT/US2015/022224 patent/WO2015153197A2/en active Application Filing
-
2016
- 2016-09-29 SA SA516371964A patent/SA516371964B1/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| SA516371964B1 (en) | 2021-08-26 |
| WO2015153197A3 (en) | 2015-12-30 |
| EA201691865A1 (en) | 2017-01-30 |
| EA039268B1 (en) | 2021-12-24 |
| WO2015153197A2 (en) | 2015-10-08 |
| EA037139B1 (en) | 2021-02-10 |
| EA202090252A1 (en) | 2020-05-31 |
| CN104941523A (en) | 2015-09-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104941521A (en) | Feeding distributor designed for ammonia oxidation reactor | |
| CN104941523B (en) | Feed distributor for ammonia oxidation reactor designs | |
| CN204017797U (en) | Feed distributor for ammonia oxidation reactor | |
| CN109772236B (en) | Fluid distributor, reaction device and application thereof | |
| CN107532494A (en) | For introducing fluid into the device of air-flow | |
| CN106488800A (en) | Grid nozzle assembly, the fluidized-bed reactor with grid nozzle assembly and the method using grid nozzle assembly | |
| CN104941522B (en) | Feed distributor for ammonia oxidation reactor designs | |
| CN208771380U (en) | For being distributed the system and reaction chamber of gas phase and/or liquid phase in the reaction chamber | |
| CN100482766C (en) | Feed nozzle assembly | |
| TWI666053B (en) | Feed sparger design for an ammoxidation reactor | |
| CN203916613U (en) | For the feed distributor of ammonia oxidation reactor | |
| CN203955188U (en) | For the feed distributor of ammonia oxidation reactor | |
| KR101594310B1 (en) | Remote plasma source block | |
| CN204017798U (en) | For the feed distributor of ammonia oxidation reactor | |
| CN113088928A (en) | Inner cylinder wall blowing device | |
| KR20160071334A (en) | Quench-cooling system | |
| JPS6312907B2 (en) | ||
| JP6006777B2 (en) | Flexible molded cover plate configuration for pressure confinement | |
| CN205868042U (en) | Still crude gas and tail gas blender | |
| US4418049A (en) | Changing oil tubes in a carbon black reactor | |
| US4500491A (en) | Changing oil tubes in a carbon black reactor | |
| US10589246B2 (en) | High temperature inlet distributor | |
| CN217351624U (en) | Diffusion furnace tube and diffusion furnace | |
| CN202220158U (en) | Quenching pipe | |
| CN106076209A (en) | Synthesis reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |