WO2019096065A1 - 一种流体分布器、反应装置及其应用 - Google Patents

一种流体分布器、反应装置及其应用 Download PDF

Info

Publication number
WO2019096065A1
WO2019096065A1 PCT/CN2018/114771 CN2018114771W WO2019096065A1 WO 2019096065 A1 WO2019096065 A1 WO 2019096065A1 CN 2018114771 W CN2018114771 W CN 2018114771W WO 2019096065 A1 WO2019096065 A1 WO 2019096065A1
Authority
WO
WIPO (PCT)
Prior art keywords
fluid
distributor
fluid delivery
branch
groups
Prior art date
Application number
PCT/CN2018/114771
Other languages
English (en)
French (fr)
Inventor
赵乐
吴粮华
Original Assignee
中国石油化工股份有限公司
中国石油化工股份有限公司上海石油化工研究院
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 中国石油化工股份有限公司, 中国石油化工股份有限公司上海石油化工研究院 filed Critical 中国石油化工股份有限公司
Priority to AU2018369015A priority Critical patent/AU2018369015B2/en
Priority to US16/763,917 priority patent/US11571673B2/en
Priority to KR1020207017032A priority patent/KR102536047B1/ko
Priority to BR112020009630-0A priority patent/BR112020009630B1/pt
Priority to JP2020526550A priority patent/JP7216087B2/ja
Priority to EA202091142A priority patent/EA202091142A1/ru
Priority to EP18879404.4A priority patent/EP3711851A4/en
Publication of WO2019096065A1 publication Critical patent/WO2019096065A1/zh

Links

Images

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
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • 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
    • 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
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • 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
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/44—Fluidisation grids
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C255/00—Carboxylic acid nitriles
    • C07C255/01—Carboxylic acid nitriles having cyano groups bound to acyclic carbon atoms
    • C07C255/06—Carboxylic acid nitriles having cyano groups bound to acyclic carbon atoms of an acyclic and unsaturated carbon skeleton
    • C07C255/07—Mononitriles
    • C07C255/08—Acrylonitrile; Methacrylonitrile

Definitions

  • the present invention relates to a fluid distributor, and more particularly to a fluid distributor suitable for transporting a mixture of propylene and ammonia.
  • the invention also relates to a reaction device comprising the fluid distributor and to the use of the fluid distributor in fluid delivery or acrylonitrile manufacture.
  • Acrylonitrile is an important chemical raw material for petrochemical industry. At present, the demand for acrylonitrile in the international market is increasing. This situation has prompted acrylonitrile producers to further expand their production capacity. By increasing the size of the reactor, it is possible to expand the production capacity without increasing the number of reactor equipment, and relatively, that is, to reduce the cost of equipment manufacturing, and is therefore regarded as the main means of expanding production capacity.
  • the propylene ammonia fluid distributor is in a high temperature for a long period of time, and the propylene ammonia mixture (hereinafter sometimes referred to as a mixture gas) in the fluid distributor is along the manifold/main pipe/branch of the fluid distributor (below Sometimes referred to as a conduit) the flow is constantly being heated by the bed. As the length of the mixture traveling in the conduit increases, the temperature of the mixture also rises. When the temperature of the mixture is higher than the temperature at which ammonia decomposes the reactive nitrogen atom (this temperature is sometimes referred to as the nitridation temperature).
  • US3704690A uses a nitride-resistant alloy to make a distributor.
  • CN1089596A proposes to add a layer of thermal insulation on the outer surface of each conduit such that the temperature of the ammonia-containing mixture in the conduit is lower than the temperature of the nitridation reaction.
  • the inventors of the present invention have found that even in the case of the existing reactor size, there is still a temperature at which the temperature of the propylene-ammonia mixture is too high, so that the local temperature of the fluid distributor is higher than the nitriding temperature for a long time, resulting in fluid distribution.
  • the problem of nitriding cracking of the material If the reactor diameter is further increased, it is bound to further increase the path length of the mixture traveling within the fluid distributor, thereby further aggravating the problem of nitriding of the fluid distributor.
  • the inventors of the present invention have also found that similar problems are required not only in the field of acrylonitrile production but also in the field of transport of other fluids (especially nitrogen-containing fluids, more particularly ammonia-containing fluids) (such as methacrylonitrile production). solve.
  • a special structure fluid distributor (sometimes referred to as a feed distributor) exhibits a reduced risk of nitriding brittle fracture, and on the basis of this invention.
  • the present invention relates to the following aspects.
  • CLAIMS 1.
  • One or more (preferably 1-8, more preferably 1-4 or 1-2) fluid delivery supervisors configured to extend their centerline and/or centerline extensions
  • the plurality of fluid delivery tubes are configured to form a closed shape (preferably substantially conforming to the closed shape of the outer peripheral contour of the container) when their respective centerline and/or centerline extensions are joined end to end, More preferably, a substantially planar closed shape, more preferably a substantially planar circular, elliptical or polygonal shape, more preferably the closed shape is substantially perpendicular to the centerline of the container, and each of said fluid delivery supervisors Having at least one (preferably 1-3, more preferably 1) fluid inlets,
  • each of said fluid delivery manifolds having a starting end and an end (the ends are closed, a semi-closed or open structure, preferably a closed structure), the starting end being connected and in fluid communication with the fluid delivery main pipe, and the starting end and the end defining a length L of the fluid transporting branch,
  • each of the fluid transporting branches preferably, the connecting portion is disposed closer to the starting end than the end, and more preferably, the connecting portion is a distance between the installation position and the starting end along the longitudinal direction of the fluid transport branch pipe is 1/4 or less, 1/6 or less, 1/8 or less, 1/10 or less or less of the length L of the fluid transport branch pipe)
  • the connecting portion is configured to connect (preferably fixed, more preferably airtight) the fluid delivery branch after the fluid delivery branch passes through the housing of the container into the inner cavity
  • the housing preferably the outer surface of the housing).
  • the inner tube section of at least one of the fluid delivery manifolds has a constant or varying direction along the direction from the junction to the end of the fluid delivery manifold (eg, gradually adding The inner diameter of the inner tube section, and/or the length Li of the inner tube section such that the center line of the inner tube section after the fluid delivery branch tube passes through the housing of the container into the inner chamber
  • An extension line to the end of the inner tube section and the inner end of the inner tube form two intersection points, and the length of the line segment between the two intersection points is Ld, then 0 ⁇ Li ⁇ Ld, preferably 0.25Ld ⁇ Li ⁇ 0.99 Ld, preferably 0.40 Ld ⁇ Li ⁇ 0.99 Ld, more preferably 0.40 Ld ⁇ Li ⁇ 0.50 Ld.
  • each of the plurality of fluid delivery manifolds is divided into one or more groups (multiple groups, such as two or more groups, on each of the fluid delivery mains) Especially in the group of 2-8, 2-6 or 2-4), in any group of fluid transport branches, i) the center line of any two adjacent fluid transport branches is in the same direction (called the The direction in which the group of fluid delivery manifolds extend is parallel or substantially parallel to one another, and/or ii) the inner diameters of any two adjacent fluid delivery manifolds are identical or different from each other (eg, the same), each independently being 50-150 mm (preferred) 65-125 mm), and/or, iii) the vertical distances D2 of the centerlines of any two adjacent fluid delivery branches are identical or different (for example identical), each independently being 250-750 mm (preferably 300-650 mm, more preferably 350-550 mm), and/or, iv) the D1 and the D2 satisfy the relationship:
  • each of the plurality of fluid delivery manifolds is divided into one or more groups (multiple groups, such as two or more groups, on each of the fluid delivery mains) In particular, 2-8 groups, 2-6 groups or 2-4 groups), or all fluid delivery branches of the fluid distributor are divided into one or more groups (multiple groups such as 2 groups or more, especially 2-8) Groups, groups 2-6 or groups 2-4), between the plurality of sets of fluid transport manifolds, i) the direction in which the set of fluid transport branches and the other set of fluid transport branches extend at an angle to each other (preferably parallel to each other) Or perpendicular to each other, and/or, ii) the projection of a set of fluid delivery manifolds on the closed shape does not overlap with the projection of another set of fluid delivery manifolds on the closed shape, preferably the fluid distributor comprises The sum of projected areas of the fluid transport branches of the entire group on the closed shape is smaller than the area Ac of the closed shape, preferably At
  • Fluid flow controller preferably fluid flow control valve
  • connection is configured to have a shape surrounding the fluid delivery manifold, preferably having a flange shape, or the closed shape having a diameter of 5.5- 32.0 meters (preferably 6.0-23.0 meters, more preferably 11.0-23.0 meters or 13.0-23.0 meters).
  • the vessel is a fluidized bed reactor, the reactor having a lumen diameter of 5-29 meters (preferably 5-20 meters, more preferably 10) -20 meters or 12-20 meters), and the fluid is a nitrogen-containing fluid or an ammonia-containing fluid, in particular a nitrogen-containing gas or an ammonia-containing gas, in particular an alkyne mixture, more particularly a propylene-ammonia mixture.
  • More than one distributor inlet More than one distributor inlet
  • a nozzle disposed on the branch pipe around a corresponding orifice and coaxial with the corresponding orifice to pass the propylene ammonia mixture through the distributor inlet, the branch pipe, the orifice, and the The nozzles are finally evenly distributed inside the reactor.
  • a ratio of the pitch of the holes between the adjacent orifices to a vertical distance between the adjacent branches is 1/N, wherein N is an integer of 2 or more.
  • the fluid distributor of any of the preceding or subsequent aspects further comprising more than one feed mains disposed outside the fluidized bed reactor, and the feed mains are respectively coupled to the one
  • the upper distributor inlet is coupled to the plurality of branch pipes and is in fluid communication with the one or more feed distributor inlets and the plurality of branch pipes.
  • a method of using any of the fluid dispensers of any of the preceding aspects to deliver fluid to a container lumen comprising delivering a fluid (preferably a gas, more preferably a propylene-ammonia mixture) to the at least one fluid inlet of the fluid distributor. And the step of passing the fluid through the fluid delivery main tube, the fluid delivery manifold, and the opening into the inner chamber.
  • a fluid preferably a gas, more preferably a propylene-ammonia mixture
  • a reaction apparatus comprising a reactor and the fluid distributor of any of the preceding aspects, wherein the reactor has at least a housing, a plurality of through holes disposed on the housing, and the shell a lumen defined by an inner surface of the body, the through holes having a one-to-one correspondence with the fluid delivery manifold of the fluid distributor in a number and arrangement position, thereby enabling each fluid delivery branch to pass through its corresponding A through hole enters the inner cavity, and the fluid delivery branch pipe passes through the through hole and is hermetically fixed to the outer surface of the casing through a connection portion of the fluid transfer branch.
  • a process for the manufacture of acrylonitrile comprising the use of a fluid distributor as described in any of the preceding aspects or the use of a process as described in any of the preceding aspects to deliver a mixture of propylene and ammonia to the interior of a reactor, preferably a fluidized bed reactor. And supplying an oxygen-containing gas (preferably air) to the reactor inner chamber, or a step of ammoxidizing the propylene to form acrylonitrile in the reaction apparatus according to any of the preceding aspects.
  • an oxygen-containing gas preferably air
  • Figure 1 is a schematic view showing the structure of a prior art propylene ammoxidation fluidized bed reactor.
  • FIG. 2 is a schematic block diagram of one embodiment of a prior art fluid distributor.
  • FIG. 3 is a schematic structural view of another embodiment of a prior art fluid distributor, wherein FIG. 3A is a side view and FIG. 3B is a bottom view.
  • FIG. 4 is a schematic structural view of one embodiment of a fluid distributor of the present invention.
  • Figure 5 is a schematic view showing the structure of one embodiment of the fluid distributor of the present invention.
  • Figure 6 is a schematic view showing the structure of one embodiment of the fluid distributor of the present invention.
  • Figure 7 is a schematic view showing the structure of an embodiment of the fluid distributor of the present invention.
  • Figure 8 is a schematic view showing the structure of an embodiment of the fluid distributor of the present invention.
  • Figure 9 is a schematic view showing the structure of an embodiment of the fluid distributor of the present invention.
  • Figure 10 is a partial enlarged view of Figure 4 illustrating the connection of the fluid delivery manifold to the housing.
  • Fluid Delivery Supervisor (sometimes referred to as Feed Supervisor)
  • the term "fluid" refers to any substance which behaves as a liquid or a gas at 25 ° C and a standard atmospheric pressure.
  • the fluid include a nitrogen-containing fluid or an ammonia-containing fluid, particularly a nitrogen-containing gas or an ammonia-containing gas, particularly an alkene (such as a C2-6 olefin) ammonia gas mixture, more particularly a propylene ammonia gas mixture.
  • the content of ammonia in the fluid is not particularly limited, and the skilled person can arbitrarily select it depending on the circumstances.
  • a fluid distributor is provided.
  • the fluid distributor is adapted to deliver fluid to the interior of the container.
  • the fluid is a nitrogen-containing fluid or an ammonia-containing fluid, in particular a nitrogen-containing gas or an ammonia-containing gas, in particular an alkyne mixture, more particularly a propylene-ammonia mixture.
  • the fluid distributor comprises at least one or more fluid delivery supervisors.
  • the fluid delivery mains in the presence of one of the fluid delivery mains, are configured to form a closed shape when their centerline and/or centerline extensions are joined end to end. Additionally, when there are a plurality of said fluid delivery mains, these fluid delivery mains are configured to form a closed shape when their respective centerline and/or centerline extensions are joined end to end.
  • centerline extension refers to the replacement of the centerline by its centerline extension when the fluid delivery mains is discontinuous or disconnected. Other concepts can be similarly understood.
  • the closed shape preferably a closed shape substantially conforming to the outer peripheral contour of the container, more preferably a substantially planar closed shape, more preferably a substantially planar circular, elliptical or polygonal shape .
  • the closed shape is substantially perpendicular to a centerline of the container. In other words, the closed shape is a substantially planar shape and the closed shape is substantially parallel to the cross section of the container.
  • Figures 4, 5, 7, and 8 illustrate what is the centerline, centerline extension, and closed shape (both circular) of the fluid delivery main tube, all indicated by dashed lines.
  • the invention is not limited to these specific shapes.
  • the outer peripheral contour of the container is the shape of the housing 4.
  • Figures 4 and 5 also illustrate what is the inner cavity, that is, the inner space surrounded by the housing 4.
  • the diameter of the closed shape (such as an equivalent circular diameter) is generally 5.5-32.0 meters, preferably 6.0-23.0 meters, more preferably 11.0-23.0 meters or 13.0-23.0 meters.
  • each of said fluid delivery tubes has at least one fluid inlet.
  • each of said fluid delivery hosts has 1-3 or 1 fluid inlets.
  • a plurality of fluid delivery manifolds are provided on each of the fluid delivery mains.
  • the number of fluid delivery manifolds may be 5-100 or 5-50, although the invention is not limited thereto.
  • each of the fluid delivery manifolds has a starting end and an end.
  • the end may be a closed, semi-closed or open structure, preferably a closed structure.
  • the starting end is coupled to and in fluid communication with the fluid delivery tube, and the starting end and the tip define a length L of the fluid delivery manifold.
  • Figure 4 illustrates what is the beginning and end of the fluid delivery manifold and how the length L is determined.
  • a plurality of openings are provided on each of the fluid delivery manifolds along the length of the fluid delivery manifold.
  • the number of openings may be 2-140 or 6-60, but the invention is not limited thereto.
  • a connection is provided on each of the fluid delivery branches.
  • the connecting portion is configured to connect (preferably fixed, more preferably airtight) the fluid delivery branch after the fluid delivery branch has passed through the housing of the container into the inner cavity.
  • the housing preferably the outer surface of the housing.
  • the fluid delivery manifold can be fixed (preferably airtight) to the housing, in particular to the outer surface of the housing.
  • the connecting portion is disposed closer to the starting end than the end.
  • the distance between the installation position of the connecting portion and the starting end along the longitudinal direction of the fluid transport branch is 1/4 or less, 1/6 or less, 1/8 or less of the length L of the fluid transport branch pipe. , 1/10 or less or less.
  • the fluid delivery mains are one or more, preferably 1-8, more preferably 1-4 or 1-2.
  • the inner diameters of the fluid delivery tubes are identical or different (e.g. identical) to each other when present in plurality, each independently being 150-700 mm, preferably 170-500 mm.
  • the plurality of openings are disposed along the length direction of the fluid delivery manifold from the connecting portion to the fluid delivery branch On the end of the pipe section (called the inner pipe section).
  • Figures 4 and 6 illustrate how the inner and outer pipe sections are determined.
  • the plurality of openings may be arranged at equal or unequal spacing.
  • the distance D1 between any two adjacent said openings is the same or different from each other, each independently being 125-375 mm, preferably 175-250 mm.
  • the inner tube section of at least one of the fluid delivery manifolds has a constant or varying inner diameter in a direction from the connection to the end of the fluid delivery manifold.
  • the change for example, it may be gradually thickened or tapered.
  • the length Li of the inner tube section is such that after the fluid delivery branch passes through the housing of the container into the inner chamber, the center line of the inner tube section faces the inner tube section
  • the extension line in the direction of both ends of the head and the tail creates two intersection points with the inner surface of the casing, and the length of the line segment between the two intersection points is Ld, then 0 ⁇ Li ⁇ Ld, preferably 0.25Ld ⁇ Li ⁇ 0.99Ld
  • 0.40 Ld ⁇ Li ⁇ 0.99 Ld more preferably 0.40 Ld ⁇ Li ⁇ 0.50 Ld.
  • Figure 8 illustrates how to determine the centerline, extension, Li, and Ld of the inner tube segment, and also illustrates how to determine the centerline of the manifold.
  • the plurality of fluid delivery manifolds are divided into one or more groups on each of the fluid delivery mains, such as more than two groups, particularly 2-8 groups, 2- 6 groups or 2-4 groups, in any group of fluid transport branches, the center line of any two adjacent fluid transport branches is in the same direction (in the context of the present invention, it is referred to as the group of fluid transport
  • the extension directions of the branch pipes are parallel or substantially parallel to each other.
  • Figure 7 illustrates the direction of extension (four), respectively indicated by four arrows, but the invention is not limited to the four directions of extension.
  • the plurality of fluid delivery manifolds are divided into one or more groups on each of the fluid delivery mains, such as more than two groups, particularly 2-8 groups, 2- 6 sets or 2-4 sets, in any set of fluid transport branches, the inner diameters of any two adjacent fluid transport branches are the same or different (for example the same), each independently 50-150 mm, preferably 65-125 mm.
  • the plurality of fluid delivery manifolds are divided into one or more groups on each of the fluid delivery mains, such as more than two groups, particularly 2-8 groups, 2- 6 groups or 2-4 groups, in any group of fluid transport branches, the vertical distance D2 of the center line of any two adjacent fluid transport branches is the same or different (for example, the same), each independently 250-750mm, It is preferably 300-650 mm, more preferably 350-550 mm.
  • the plurality of fluid delivery manifolds are divided into one or more groups on each of the fluid delivery mains, such as more than two groups, particularly 2-8 groups, 2- 6 sets or 2-4 sets, in any set of fluid transport branches, the D1 and the D2 satisfy the relationship: D1/D2 ⁇ 0.3, preferably D1/D2 ⁇ 0.5.
  • the plurality of fluid delivery manifolds are divided into one or more groups on each of the fluid delivery mains, such as more than two groups, particularly 2-8 groups, 2- In group 6 or group 2-4, in any group of fluid delivery branches, the ends of two adjacent fluid delivery branches are connected in pairs to form a line segment.
  • the line segments have the shape of a broken line or a straight line.
  • the height difference between the highest point and the lowest point of the fold line is H C
  • the length of the longest fluid transport branch pipe in the set of fluid transfer branches is Lmax
  • FIG. 6 illustrates the line segments of a straight line shape
  • FIG. 8 illustrates the line segments of a polygonal line shape, but the present invention is not limited to these specific shapes.
  • these figures also illustrate how to determine H C and Lmax.
  • the plurality of fluid delivery manifolds are divided into one or more groups on each of the fluid delivery mains, such as more than two groups, particularly 2-8 groups, 2- 6 sets or 2-4 sets, in any group of fluid transport branches, the length Lmax of the longest fluid transport branch in the set of fluid transport branches is 5000-29000 mm, preferably 5000-20000 mm, preferably 5000-10000 mm, more preferably 6000-10000mm.
  • the plurality of fluid delivery manifolds are divided into one or more groups on each of the fluid delivery mains, or all fluid delivery branches of the fluid distributor are grouped Or a plurality of groups, such as more than 2 groups, in particular 2-8 groups, 2-6 groups or 2-4 groups, between the plurality of sets of fluid transport branches, one set of fluid transport branches and another set of fluids
  • the extending directions of the conveying branches are at an angle to each other, preferably parallel to each other or perpendicular to each other, including substantially parallel or substantially vertical.
  • the plurality of fluid delivery manifolds are divided into one or more groups on each of the fluid delivery mains, or all fluid delivery branches of the fluid distributor are grouped Or a plurality of groups, such as more than 2 groups, in particular 2-8 groups, 2-6 groups or 2-4 groups, between the plurality of sets of fluid transport branches, a set of fluid transport branches in the closed shape
  • the projection on the top does not overlap the projection of the other set of fluid delivery branches on the closed shape.
  • the sum of the projected areas of the fluid transport branches of the entire set of fluid transporting tubes on the closed shape is smaller than the area Ac of the closed shape, preferably At/Ac is 75% or more, more preferably At /Ac is 80% or more, and more preferably At/Ac is 90% or more.
  • Figure 7 illustrates how to determine the projection.
  • the projection is actually a line segment formed by the ends of all fluid delivery branches in each set of fluid delivery manifolds, the centerline of the fluid delivery mains where it is located (and, depending on the situation, may also include a centerline) An extension line) and a projection of a pattern defined by an outer edge of the outermost two fluid delivery branches of the set of fluid delivery branches in the closed shape.
  • the graphic and the closed shape are both substantially planar shapes, and both are generally in substantially the same plane.
  • each group of fluid delivery branches may all be on the same fluid delivery main pipe, or may be in any combination or in any combination with each other.
  • the different fluid delivery mains are, in particular, separately or in any combination with one another on different fluid delivery mains.
  • the phrase "arbitrarily combined with each other" means that when the number of fluid delivery branch groups is different from the number of fluid delivery main tubes, one or more sets of fluid delivery manifolds are on the same fluid delivery main pipe, and the remaining group of fluids The delivery manifold is on the remaining one or more fluid delivery mains.
  • one of the four sets of fluid transport branch pipes is in one fluid transport main pipe, and the other three sets of fluids are arbitrarily combined with each other.
  • the delivery manifold is on another fluid delivery main, or the two fluid delivery manifolds of the four fluid delivery manifolds are on one fluid delivery main and the other two fluid delivery manifolds are on another fluid delivery main.
  • each of the fluid delivery manifolds is substantially straight. That is, each of the fluid delivery manifolds is substantially a straight tube.
  • the plurality of openings are identical or different from each other (such as the same), and each independently has a shape selected from the group consisting of a circle, an ellipse, a square, a rectangle, and a trapezoid. And the outer shape of the diamond.
  • a fluid flow controller preferably a fluid flow control, is provided on at least one of the fluid delivery manifolds on a section of the fluid delivery manifold from the connection to the starting end (referred to as an outer section) valve.
  • connection portion is configured to have a shape surrounding the fluid delivery branch, preferably having a flange shape.
  • the fluid distributor further comprises a nozzle disposed around the opening.
  • the branch pipe is in fluid communication with the corresponding nozzle through the opening, causing the transport fluid to be ejected from the opening, rectified through the nozzle, and then enter through the opening (generally circular) at the other end of the nozzle.
  • the inner cavity of the container is in fluid communication with the corresponding nozzle through the opening.
  • the openings are coaxial with their respective nozzles and are located in a radial section perpendicular to the centerline of the respective branch pipe.
  • the plurality of openings are identical or different from each other (such as the same), each independently having 3-10 mm (preferably 4.5-8.5 mm, more preferably 5.0) -7.5) diameter (generally equivalent circle diameter).
  • the diameter of the opening is smaller than the diameter of the corresponding nozzle and nozzle tip opening.
  • the diameters of the plurality of openings may be identical to each other or may be different from each other, such as the diameter gradually increasing or decreasing.
  • the nozzle extends downwards from the branch pipe.
  • the extension angle of each nozzle may be the same or different.
  • the ends of all of the nozzles are in substantially the same horizontal cross section.
  • the nozzle may be selected from the group consisting of cylindrical, conical, and/or preferably cylindrical.
  • the cross sections of the nozzles each independently have a shape selected from the group consisting of a circle, an ellipse, a square, a rectangle, a trapezoid and a diamond, preferably a circle and/or an ellipse, more preferably a circle.
  • the ratio of the column length of the nozzle to the inner diameter of the nozzle is 4 or more, preferably 6 or more, more preferably 8 or more.
  • the vertical distances of the ends of all nozzles from the underlying air distribution plate are substantially the same.
  • the vessel is a fluidized bed reactor.
  • the inner diameter of the reactor is from 5 to 29 meters, preferably from 5 to 20 meters, more preferably from 10 to 20 meters or from 12 to 20 meters.
  • the inventors have found through extensive experiments, calculations and computer simulations that the fluid distributor can meet the requirements of an propylene ammoxidation fluidized bed reactor having the lumen diameter, that is, to ensure that the temperature of the mixture in the fluid distributor is always Below the nitriding temperature.
  • the fluid distributor is a feed distributor for uniformly distributing the propylene ammonia mixture inside the fluidized bed reactor, the feed distributor comprising:
  • More than one distributor inlet ie, the fluid inlet
  • a plurality of delivery manifolds ie, fluid delivery manifolds coupled to the distributor inlets and in fluid communication with the distributor inlets, respectively, and the plurality of delivery manifolds are directed from the distributor inlet Internal extension of the reactor;
  • a nozzle disposed on the transfer branch around a corresponding opening and coaxial with the corresponding opening to pass a propylene ammonia mixture through the distributor inlet, the delivery branch, the opening And the nozzle is finally evenly distributed inside the reactor,
  • feed mains ie, the fluid transfer mains
  • the feed mains are respectively connected to the one or more distributor inlets and the plurality One of the delivery manifolds is in fluid communication with the one or more feed distributor inlets and the plurality of delivery manifolds.
  • a fluid delivery method for delivering a fluid to a container lumen using the fluid distributor of the present invention as described above.
  • the method includes the step of delivering fluid to the at least one fluid inlet of the fluid distributor, the fluid entering the interior cavity through at least the fluid delivery manifold, the fluid delivery manifold, and the opening.
  • the fluid a gas is preferred, and a propylene-ammonia mixture is more preferred.
  • a fluidized bed reactor is preferred as the container.
  • a fluid distributor according to the invention as described above as a feed distributor for transporting a reaction feedstock to the interior of an ammoxidation reactor.
  • a reaction raw material a propylene ammonia mixed gas is preferable.
  • the reaction apparatus includes a reactor and a fluid distributor as hereinbefore described.
  • the reactor has at least a housing, a plurality of through holes provided on the housing, and a lumen defined by an inner surface of the housing.
  • the through holes have a one-to-one correspondence with the fluid delivery branches of the fluid distributor in the number and arrangement positions, thereby enabling each of the fluid delivery branches to pass through a corresponding through hole to enter the An inner cavity, and the fluid delivery branch is fixed to the outer surface of the housing by a connection portion of the fluid delivery branch after passing through the through hole.
  • a method of producing acrylonitrile comprising: using a fluid distributor as hereinbefore described, to deliver a mixture of propylene and ammonia to a lumen of a reactor (such as a fluidized bed reactor), and An oxygen-containing gas is supplied to the reactor inner chamber to cause an ammoxidation reaction of propylene to form acrylonitrile.
  • a fluid distributor as hereinbefore described
  • An oxygen-containing gas is supplied to the reactor inner chamber to cause an ammoxidation reaction of propylene to form acrylonitrile.
  • the oxygen-containing gas specifically, for example, air can be mentioned.
  • a method of producing acrylonitrile comprising: transporting a propylene-ammonia mixture into a lumen of a reactor (such as a fluidized bed reactor) using the fluid delivery method of the present invention as described above, and An oxygen-containing gas is supplied to the reactor inner chamber to cause an ammoxidation reaction of propylene to form acrylonitrile.
  • a reactor such as a fluidized bed reactor
  • An oxygen-containing gas is supplied to the reactor inner chamber to cause an ammoxidation reaction of propylene to form acrylonitrile.
  • the oxygen-containing gas specifically, for example, air can be mentioned.
  • a method for producing acrylonitrile comprising the step of subjecting propylene to an ammoxidation reaction to produce acrylonitrile in the reaction apparatus according to the present invention.
  • the length of the branch of the same form of fluid distributor is correspondingly extended, so that the temperature rise of the mixed gas stream after passing through the conduit is greater.
  • the mass flow rate of the mixture in the branch is the product of the number of nozzles and the mass flow of the mixture flowing out of a single nozzle.
  • the mass flow rate of the propylene-ammonia mixture flowing through the longest branch pipe is correspondingly increased.
  • the average heating rate in the branch pipe is slightly lowered. Therefore, the temperature rise of the mixture flowing through the same distance will decrease again.
  • ⁇ T i is the product of the mixed temperature rise rate and the length of the branch pipe.
  • the longest branch pipe is the same.
  • the change of ⁇ T i of other branch pipes is the combination of the above changes.
  • the variation factor of the branch pipe length of the long branch pipe is larger than the variation factor of the mixed temperature rise of the short branch pipe.
  • the most The temperature ⁇ T i at the end nozzle of the long branch pipe changes the most, that is, the highest temperature point of the propylene ammonia distributor nozzle. If the temperature is lower than the nitriding temperature, it can be considered as any position of the propylene ammonia distributor in the reactor. The average is lower than the nitriding temperature.
  • the main internal components of a typical propylene ammoxidation fluidized bed reactor 1 include a cyclone (not shown), a cooling coil 7, and a fluid distributor (i.e., propylene ammonia mixed gas distributor) 100. , air distribution plate 6 and process air inlet 8.
  • the fluid distributor 100 is located between the air distribution plate 6 and the cooling coil 7.
  • An propylene ammonia mixture from a feed gas mixing system enters the fluid distributor 10 from the fluid distributor fluid inlet, through the fluid distributor 10 through the reactor housing (also referred to as the reactor wall) 4,
  • the nozzle disposed on the conduit of the fluid distributor 100 enters the catalyst bed, is thoroughly mixed with the process air introduced from the process air inlet 8, and undergoes an ammoxidation reaction in the presence of the catalyst to produce a product such as acrylonitrile.
  • prior art fluid distributor 100 generally includes a fluid distributor fluid inlet 105, a main tube y (y tube), a branch tube z (branch), an opening 103, and a nozzle (not shown).
  • the manifold is an air conduit that is in direct fluid communication with the nozzle and functions primarily to deliver the mixture to the nozzle.
  • the branch pipes are usually not branched into the gas pipe and arranged in the same cross section of the reactor, on which the openings 3 are evenly distributed in a certain manner and thus communicated with the nozzles, so that a uniform distribution of the nozzle openings in the same cross section of the reactor is achieved.
  • the y tube is an air guiding tube that is in fluid communication with the branch pipe, and mainly serves to transport the mixed gas to the branch pipe.
  • the y tube is typically a straight tube that is uniformly connected to the branch tube and is in the same cross-section as the tube in the reactor to achieve a uniform distribution of the aforementioned nozzle openings in the same cross-section of the reactor.
  • the y tube is in fluid communication with the manifold in the same manner as the branch tube, and is in direct fluid communication with the nozzle through the opening 103 for achieving uniform distribution of the aforementioned nozzle opening in the same cross section of the reactor.
  • the manifold and the y tube are in the same cross section of the reactor, but they are not in the same plane as the fluid distributor fluid inlet 105, thus providing a manifold x (x tube) introduces the propylene ammonia mixture into the y tube from the distributor fluid inlet.
  • x tube typically only one of the x tubes is required and there are no branches at other locations except that the ends are in fluid communication with the y tubes.
  • the x tube is an air tube that is in direct fluid communication with the y tube, and functions primarily to deliver the mixture to the y tube.
  • the propylene ammonia mixture enters from the propylene ammonia fluid distributor fluid inlet 105 along the x-tube, the y-tube, the manifold, and ultimately through the opening 103 disposed in the y-tube and branch. Disperse evenly into the reactor bed through the nozzle.
  • the propylene ammonia mixture exchanges heat with the catalyst bed during the uniform delivery of the fluid distributor conduit to the catalyst bed, causing the temperature to rise until the maximum temperature is reached before the nozzle enters the reactor.
  • the inventors of the present invention have found through research that when a conventional fluid distributor 100 such as that shown in Figures 2 and 3 is employed, only reactors having a diameter of less than 10 meters can be satisfied.
  • the risk of the propylene ammonia mixture in the fluid distributor 100 reaching the nitriding temperature is significantly increased. Moreover, even in a reactor having a diameter of less than 10 m, there is a risk that the propylene-ammonia mixture reaches the nitriding temperature.
  • fluid distributor 10 includes a fluid inlet 15, a feed header 12, a manifold 11, an opening 13 and a connection 16, and optionally includes a nozzle (not shown).
  • the distributor fluid inlet 15 is connected in a gastight manner to the line from the feed gas mixing system to deliver the mixture to the fluid distributor.
  • the fluid distributor may include more than one distributor fluid inlet 15, each connected to a separate feed main 12 .
  • one or more feed mains 12 are coupled to and in fluid communication with more than one distributor fluid inlet 15 and are surrounded by a distributor fluid inlet 15 in accordance with one embodiment of the present invention.
  • the wall extends to both sides.
  • a plurality of branch pipes 11 are connected to the feed main pipe 12 at different positions and are in fluid communication with the feed main pipe 12 to deliver the propylene ammonia mixed gas to the branch pipe 11.
  • the shape of the feed main pipe 12 of the fluid distributor of the present invention is not particularly limited, but is preferably an annular shape (Figs. 4 and 6), a semicircular shape (Fig. 5 and 7) or an arc shape (Fig. 8). shape.
  • the pipe diameter of the feed main pipe is larger than the pipe diameter of the branch pipe 11.
  • the branch pipe 11 is a straight pipe that passes through the reactor wall 4, and the branch pipe 11 does not have any branches in the reactor interior except for the openings and nozzles provided thereon.
  • the plurality of branch pipes 11 are not connected or intersect each other in the reactor interior.
  • One end of the plurality of branch pipes 11 is connected to the feed main pipe 12, and the other end extends through the reactor wall 4 toward the inside of the reactor.
  • the specific position of the connection point of the branch pipe 11 and the feed main pipe 12 is not specifically limited, and the branch pipe 11 may be connected to the feed main pipe 12 outside the reactor, or may be connected to the feed main pipe 12 at the reactor wall.
  • connection manner of the branch pipe 11 and the reactor wall is not specifically limited, and a welding method commonly used in the art may be employed, or as shown in FIGS. 9 and 10 The airtight connection shown.
  • branches 11 are in the same cross section of the reactor. More preferably, the fluid distributor fluid inlet 15, the feed header 12, and the manifold 11 are all within the same cross section of the reactor.
  • the branch pipe 11 when the reactor diameter is small, as shown in Fig. 8, in the entire cross section of the reactor, the branch pipe 11 can be introduced from one side of the cross section of the reactor and extended to the other side. The form near the wall. At this time, the upper limit of the length of the branch pipe 11 (the extension length of the branch pipe 11 inside the reactor) is smaller than the diameter of the reactor.
  • the temperature of the mixture reaches the nitriding temperature
  • Figures 4 and 5 in the reactor cross section, a plurality of branch pipes 11 are divided into two groups, respectively passing through the reactor wall 4 from both sides of the cross section and extending to a direction perpendicular to the extending direction of the branch pipe 11. Near the central axis of the cross section.
  • the branch pipes 11 respectively arranged correspondingly on the two sides of the cross section are symmetrical to each other. At this time, the length of the branch pipe 11 is preferably smaller than the radius of the reactor.
  • the plurality of branch pipes 11 are not connected or cross-connected inside the reactor, and preferably, the plurality of branch pipes 11 are parallel to each other. More preferably, the vertical distance between the branch pipes 11 adjacent in the direction perpendicular to the extending direction of the branch pipe 11 is the same. The vertical distance is preferably from 250 to 750 mm, preferably from 300 to 650 mm, more preferably from 350 to 550 mm.
  • the cross section of the reactor inner cavity may be divided into a plurality (for example, two or more, particularly 2-8, 2-6 or 2). - 4) fan-shaped regions, and a fluid distributor form in which a plurality of branch pipes 11 are arranged in parallel in each sector region.
  • the cross section of the reactor is preferably divided into four sectoral regions (four quadrants). The vertical distance between adjacent branches in the same quadrant is the same and is preferably 250-750 mm, preferably 300-650 mm, more preferably 350-550 mm.
  • one or more openings 13 called acute holes are arranged in the axial direction thereof for injecting a mixture from the fluid distributor. reactor.
  • the vertical distance in the axial direction between the centers of the adjacent holes in the axial direction of the branch pipe 11 is referred to as a hole pitch.
  • the aperture spacing of adjacent apertures in the axial direction of either branch is the same.
  • the ratio of the hole pitch between adjacent openings to the vertical distance between the adjacent parallel branch pipes is 1/N, and N is an integer of 2 or more.
  • N is 2, i.e. the aperture spacing between adjacent apertures is one-half of the vertical distance between said adjacent parallel branches.
  • N is 3, i.e., the spacing between adjacent openings is one third of the vertical distance between adjacent adjacent branches.
  • more than one opening 13 may be arranged in the same radial section of the branch pipe 11 (this section corresponding to the center of the openings is referred to as an opening section). These openings 13 in the same radial section are also connected to the respective nozzles and are concentric with the nozzles.
  • the same radial section on the branch pipe 11 of the fluid distributor is arranged with the same number of openings, a plurality of openings in the same radial section and a plurality of openings in the other radial sections
  • the holes are in one-to-one correspondence so as to be aligned in the axial direction along the respective branch pipes, the columns being parallel to the axis of the branch pipe.
  • the apertures of the openings at different radial sections of different branches or the same branch may be the same or different.
  • the branch pipe 11 in the fluid distributor, may be equipped with a nozzle as needed, and therefore, in view of workability of the fluid distributor, the pipe diameter lower limit of the branch pipe is preferably 70 mm or more, and more preferably More than 75mm.
  • the upper limit of the pipe diameter of the branch pipe is preferably 145 mm or less, more preferably 135 mm or less.
  • all of the branches 11 inside the reactor are of the same diameter.
  • branch pipes having more than one diameter may be disposed in the same fluid distributor according to actual conditions. 11.
  • the same branch pipe 11 may have more than one different diameter in the extending direction thereof.
  • a fluid flow controller 14 may be provided at the distributor fluid inlet 15 for controlling propylene ammonia in the fluid distributor. Mixed gas flow. Furthermore, in order to make the propylene ammonia mixture more uniformly distributed throughout the reactor bed. As shown in Figure 9, a fluid flow controller 14 can be provided at each of the branches 11 at a location external to the reactor, in accordance with an embodiment of the present invention.
  • the length of the branch pipe refers to the length of the inner tube section of the branch pipe.
  • the diameter of the propylene ammoxidation fluidized bed reactor (internal cavity diameter, the same below) is 10 meters.
  • the acetylenic acid catalyst of SANC series of Sinopec Shanghai Petrochemical Research Institute is used to produce acrylonitrile.
  • the reaction unit is operated at full load and the ratio of raw material gas is used.
  • C 3 H 6 :NH 3 :air was 1 :1.2:9.3, the reaction temperature was 440 ° C, the reaction pressure was 50 KPa, and the propylene ammonia mixed gas fluid inlet temperature was controlled to 80 °C.
  • the fluid distributor adopts the form of Figure 4, the material is carbon steel, the distributor has one main pipe, the main pipe diameter is ⁇ 500mm, and there are 52 branch pipes, each connected to the main pipe.
  • the diameter of the branch pipe is ⁇ 80mm, the distance between the branch pipes is 380mm, and the branch pipe is Parallel to each other, the nozzle opening distance in the direction of the branch pipe is 190mm, the longest branch pipe length is 4.9m with 52 nozzles, the shortest branch pipe length is 1.8m with 15 nozzles, the total number of distributor nozzles is 2100, the nozzle inner diameter It is 20 mm and has a length of 200 mm; the aperture of the orifice is 6.0 mm.
  • the propylene ammonia mixture gas is passed through the fluid distributor to the nozzle end of each branch pipe (not shown in FIG.
  • the temperature at the nozzle end of the longest branch pipe of the propylene-ammonia mixture was 282 °C.
  • the propylene ammoxidation fluidized bed reactor has a diameter of 12 meters. It is produced by the Sinopec Shanghai Petrochemical Research Institute SANC series acrylonitrile catalyst for the production of acrylonitrile.
  • the reaction unit is operated at full load, and the raw material gas ratio C 3 H 6 :NH 3 :
  • the air was 1:1.2:9.5, the reaction temperature was 440 ° C, the reaction pressure was 50 KPa, and the propylene ammonia mixed gas fluid inlet temperature was controlled to 80 °C.
  • the fluid distributor adopts the form of Figure 5, the material is carbon steel, the distributor is provided with two main tubes, the main pipe diameter is ⁇ 420mm, and there are 60 branch pipes, each connected to the main pipe.
  • the diameter of the branch pipe is ⁇ 100mm, the distance between the branch pipes is 410mm, and the branch pipe Parallel to each other, the nozzle opening distance in the direction of the branch pipe is 205mm, the longest branch pipe length is 5.9 meters with 58 nozzles, the shortest branch pipe length is 1.9 meters with 15 nozzles, and the total number of distributor nozzles is 2560.
  • the inner diameter is 20 mm and the length is 180 mm; the orifice diameter is 6.2 mm.
  • the propylene-ammonia mixture is passed through the fluid distributor to the nozzle at the end of each branch pipe, and the temperature of the propylene-ammonia mixture at the nozzle end of each branch pipe is measured by a thermocouple, wherein the highest point temperature of the mixture in the fluid distributor is the length of the propylene-ammonia mixture.
  • the temperature at the end of the longest branch is 282 °C.
  • the propylene ammoxidation fluidized bed reactor has a diameter of 15 meters. It is produced by the Sinopec Shanghai Petrochemical Research Institute SANC series acrylonitrile catalyst for the production of acrylonitrile.
  • the reaction unit is operated at full load, and the raw material gas ratio C 3 H 6 :NH 3 :
  • the air was 1:1.2:9.5, the reaction temperature was 435 ° C, the reaction pressure was 55 KPa, and the propylene ammonia mixed gas fluid inlet temperature was controlled to 80 °C.
  • the fluid distributor adopts the form of Figure 6, the material is carbon steel, the distributor is provided with one main pipe, the main pipe diameter is ⁇ 650mm, and there are 44 branch pipes, each connected to the main pipe.
  • the diameter of the branch pipe is ⁇ 100mm, the distance between the branch pipes is 690mm, and the branch pipe Parallel or perpendicular to each other, the nozzle opening distance along the branch pipe is 230mm, the longest branch pipe length is 7.45 meters with 96 nozzles, the shortest branch pipe length is 2.4 meters with 45 nozzles, and the total number of distributor nozzles is 3008.
  • the inner diameter is 20 mm and the length is 150 mm; the orifice diameter is 6.5 mm.
  • the propylene-ammonia mixture is passed through the fluid distributor to the nozzle at the end of each branch pipe, and the temperature of the propylene-ammonia mixture at the nozzle end of each branch pipe is measured by a thermocouple, wherein the highest point temperature of the mixture in the fluid distributor is the length of the propylene-ammonia mixture.
  • the temperature at the end of the longest branch is 298 °C.
  • the propylene ammoxidation fluidized bed reactor has a diameter of 20 meters. It is produced by the Sinopec Shanghai Petrochemical Research Institute SANC series acrylonitrile catalyst for the production of acrylonitrile.
  • the reaction unit is operated at full load, and the raw material gas ratio C 3 H 6 :NH 3 :
  • the air was 1:1.2:9.5, the reaction temperature was 435 ° C, the reaction pressure was 55 KPa, and the propylene ammonia mixed gas fluid inlet temperature was controlled to 80 °C.
  • the fluid distributor adopts the form of Figure 7, which is made of carbon steel.
  • the distributor is equipped with two main pipes.
  • the main pipe has a diameter of ⁇ 500mm and 84 branch pipes, each connected to the main pipe.
  • the diameter of the branch pipe is ⁇ 120mm, and the distance between the pipe branches is 460mm. Parallel or perpendicular to each other, the nozzle opening distance along the branch pipe is 230mm, the longest branch pipe length is 9.8 meters with 84 nozzles, the shortest branch pipe length is 2.9 meters with 20 nozzles, the number of nozzles is 5740, and the nozzle inner diameter is 20mm, length 150mm; orifice aperture is 6.6mm.
  • the propylene-ammonia mixture passes through the fluid distributor to the nozzle at the end of each branch pipe. According to the HTFS calculation of the model and the existing experimental data, the highest point temperature of the mixture in the fluid distributor is the longest branch of the propylene-ammonia mixture in the travel length. The temperature at the end nozzle is 316 °C.
  • the propylene ammoxidation fluidized bed reactor has a diameter of 20 meters. It is produced by the Sinopec Shanghai Petrochemical Research Institute SANC series acrylonitrile catalyst for the production of acrylonitrile.
  • the reaction unit is operated at full load, and the raw material gas ratio C 3 H 6 :NH 3 : The air was 1:1.2:9.5, the reaction temperature was 435 ° C, the reaction pressure was 55 KPa, and the propylene ammonia mixed gas fluid inlet temperature was controlled to 100 °C.
  • the fluid distributor adopts the form of Figure 7, and has three openings at the same section of the branch pipe, the distance between adjacent parallel branches is 750 mm, the hole spacing between adjacent openings is 250 mm, and the material is carbon steel, the distributor There are 2 main pipes, the diameter of the main pipe is ⁇ 500mm, the diameter of the branch pipe is ⁇ 130mm, the number of branch pipes is 52, the branch pipes are parallel or perpendicular to each other, the length of the longest branch pipe is 9.8 meters with 120 nozzles, and the length of the shortest branch pipe is 4.3 meters.
  • the number of nozzles is 4,880, the inner diameter of the nozzle is 20 mm, the length is 150 mm, and the aperture of the orifice is 6.5 mm.
  • the propylene-ammonia mixture passes through the fluid distributor to the nozzle at the end of each branch pipe.
  • the highest point temperature of the mixture in the fluid distributor is the longest branch of the propylene-ammonia mixture in the travel length.
  • the temperature at the end nozzle is 305 °C.
  • the propylene ammoxidation fluidized bed reactor has a diameter of 15 meters. It is produced by the Sinopec Shanghai Petrochemical Research Institute SANC series acrylonitrile catalyst for the production of acrylonitrile.
  • the reaction unit is operated at full load, and the raw material gas ratio C 3 H 6 :NH 3 :
  • the air was 1:1.2:9.5, the reaction temperature was 435 ° C, the reaction pressure was 55 KPa, and the propylene ammonia mixed gas fluid inlet temperature was controlled to 80 °C.
  • the fluid distributor adopts the form of Figure 3 and is made of carbon steel.
  • the diameter of the x tube is ⁇ 500mm
  • the diameter of the y tube is ⁇ 250mm
  • the diameter of the branch tube is ⁇ 100mm
  • the number of branches is 66
  • the distance between the branches is 460mm
  • the distance between the nozzles is 230mm
  • the longest branch pipe length is 7.45 meters with 64 nozzles
  • the shortest branch pipe length is 2.0 meters with 18 nozzles
  • the total number of distributor nozzles is 3008, the nozzle inner diameter is 20mm, the length is 200mm; the orifice diameter is 6.5 Mm.
  • the propylene-ammonia mixture passes through the fluid distributor line to the nozzle at the end of each branch. According to the HTFS calculation of the model and the existing experimental data, the maximum temperature of the mixture in the fluid distributor is 355 °C.
  • the propylene ammoxidation fluidized bed reactor has a diameter of 15 meters. It is produced by the Sinopec Shanghai Petrochemical Research Institute SANC series acrylonitrile catalyst for the production of acrylonitrile.
  • the reaction unit is operated at full load, and the raw material gas ratio C 3 H 6 :NH 3 :
  • the air was 1:1.2:9.5, the reaction temperature was 435 ° C, the reaction pressure was 55 KPa, and the propylene ammonia mixed gas fluid inlet temperature was controlled to 80 °C.
  • the fluid distributor adopts the form of Figure 2 and is made of carbon steel.
  • the diameter of the y tube is ⁇ 250mm
  • the diameter of the branch pipe is ⁇ 100mm
  • the number of branch pipes is 66
  • the distance between the branch pipes is 460mm
  • the distance between nozzles is 230mm
  • the length of the longest branch pipe is
  • 64 nozzles for 7.45 meters 18 nozzles for the shortest branch length of 2.0 meters, a total of 3008 nozzles for the distributor, a nozzle inner diameter of 20 mm, a length of 200 mm, and an orifice diameter of 6.5 mm.
  • the propylene-ammonia mixture passes through the fluid distributor line to the nozzle at the end of each branch. According to the HTFS calculation of the model and the existing experimental data, the maximum temperature of the mixture in the fluid distributor is 348 °C.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Rigid Pipes And Flexible Pipes (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

一种流体分布器、反应装置及其应用。流体分布器(10)包括：一个或多个流体输送主管(12)，一个流体输送主管(12)被构造为在将其中心线和/或中心线延长线首尾相接时，或者多个流体输送主管(12)被构造为在将其各自的中心线和/或中心线延长线首尾相接时，构成闭合形状，并且每一个流体输送主管(12)具有至少一个流体入口(15)，在每一个流体输送主管(12)上设置的多个流体输送支管(11)，在每一个流体输送支管(11)上沿着流体输送支管(11)的长度方向设置的多个开孔(13)，在每一个流体输送支管(11)上设置的连接部(16)，连接部(16)被构造为在流体输送支管(11)穿过容器的壳体而进入内腔之后，将流体输送支管(11)连接在壳体上。流体分布器至少能够表现出降低的氮化脆裂风险。

Description

一种流体分布器、反应装置及其应用 技术领域
本发明涉及一种流体分布器，特别是一种适合输送丙烯氨混合气的流体分布器。本发明还涉及包括该流体分布器的反应装置以及该流体分布器在流体输送或丙烯腈制造中的应用。
背景技术
丙烯腈是石油化工的重要化工原料，目前国际市场上对丙烯腈的需求量日益增大，这一情况促使丙烯腈生产企业希望进一步扩大产能。采用增大反应器尺寸的方式能够在不增加反应器设备数量的情况下扩大产能，相对而言，也即减少设备制造方面的成本费用，因此也被视作扩大产能的主要手段。
已知的是，在丙烯腈生产过程中，丙烯氨流体分布器长期处于高温当中，流体分布器内的丙烯氨混合气(以下有时简称混合气)沿流体分布器的总管/主管/支管(以下有时统称为导管)流动过程中不断的被床层加热。随着混合气在导管中行进的长度的增加，混合气的温度也在不断上升，当混合气的温度高于氨分解出活性氮原子的温度时(该温度以下有时简称为氮化温度)，由于混合气中游离氨的持续存在，部分氨分解出活性氮原子，并与导管中的金属原子结合，生成脆性的金属氮化物，该氮化物在工况条件下很容易发生脆裂，会造成流体分布器的破裂，致使丙烯氨分布不均，导致反应性能下降，严重时使反应器被迫停车更换分布器。
US3704690A采用抗氮化合金来制造分布器，但由于氨氧化特有的某些问题及成本原因，也在丙烯腈生产企业使用过程中，被证实是不能解决氮化脆裂问题的。CN1089596A提出在每个导管外表面加设一层隔热层，使得导管内含氨混合气的温度低于氮化反应温度。
发明内容
本发明的发明人通过研究认为，即使是在现有反应器尺寸的情况下，仍然存在丙烯氨混合气温度过高，使流体分布器局部温度长期高于氮化温度的高温下，导致流体分布器材料的氮化脆裂的问题。如果进一步增大反应器直径，则势必会进一步增加混合气在流体分布器内行进的路径长度，从而使流体分布器 氮化脆裂的问题进一步恶化。
本发明的发明人还发现，不仅是丙烯腈制造领域，在其他流体(特别是含氮流体，更特别是含氨流体)输送领域(比如甲基丙烯腈制造等)，也存在类似的问题需要解决。
本发明的发明人通过进一步的研究，发现了一种特殊结构的流体分布器(有时也称为进料分布器)，其表现出降低的氮化脆裂风险，并在此基础上完成了本发明。
具体而言，本发明涉及以下方面的内容。
1.一种流体分布器，适合向容器内腔输送流体，所述流体分布器包括：
一个或多个(优选1-8个，更优选1-4个或1-2个)流体输送主管，所述一个流体输送主管被构造为在将其中心线和/或中心线延长线首尾相接时，或者所述多个流体输送主管被构造为在将其各自的中心线和/或中心线延长线首尾相接时，构成闭合形状(优选基本上顺应所述容器外周轮廓的闭合形状，更优选基本上平面的闭合形状，更优选基本上平面的圆形、椭圆形或者多边形形状，更优选所述闭合形状与所述容器的中心线基本上垂直)，并且每一个所述流体输送主管具有至少一个(优选1-3个，更优选1个)流体入口，
在每一个所述流体输送主管上设置的多个(优选5-100个，更优选5-50个)流体输送支管，每一个所述流体输送支管具有起始端和末端(所述末端为封闭、半封闭或开放结构，优选封闭结构)，所述起始端与所述流体输送主管连接且流体连通，并且所述起始端与所述末端限定了所述流体输送支管的长度L，
在每一个所述流体输送支管上沿着所述流体输送支管的长度方向设置的多个(优选2-140个，更优选6-60个)开孔，
在每一个所述流体输送支管上设置的连接部(优选的是，所述连接部的设置位置与所述末端相比更靠近所述起始端，更优选的是，所述连接部的所述设置位置与所述起始端沿着所述流体输送支管长度方向的距离为所述流体输送支管长度L的1/4以下、1/6以下、1/8以下、1/10以下或更小)，所述连接部被构造为在所述流体输送支管穿过所述容器的壳体而进入所述内腔之后，将所述流体输送支管连接(优选固定，更优选气密性固定)在所述壳体(优选所述壳体的外表面)上。
2.前述或后述任一方面所述的流体分布器，其中所述多个流体输送主管的内径彼此相同或不同(比如相同)，各自独立地为150-700mm(优选170-500mm)。 3.前述或后述任一方面所述的流体分布器，其中在每一个所述流体输送支管上，所述多个开孔沿着所述流体输送支管的长度方向设置(比如等间距或不等间距设置，更优选任意相邻两个所述开孔之间的距离D1彼此相同或不同，各自独立地为125-375mm(优选175-250mm))在所述流体输送支管的从所述连接部至所述末端的管段(称为内管段)上。
4.前述或后述任一方面所述的流体分布器，其中至少一个所述流体输送支管的内管段沿着从所述流体输送支管的连接部至末端的方向具有恒定或变化(比如逐渐加粗或逐渐变细)的内径，和/或，所述内管段的长度Li使得在所述流体输送支管穿过所述容器的壳体而进入所述内腔之后，所述内管段的中心线向所述内管段首尾两端方向的延长线与所述壳体的内表面产生两个交点，设所述两个交点之间的线段的长度为Ld，则0＜Li＜Ld，优选0.25Ld≤Li≤0.99Ld，优选0.40Ld≤Li＜0.99Ld，更优选0.40Ld≤Li＜0.50Ld。
5.前述或后述任一方面所述的流体分布器，其中在每一个所述流体输送主管上，将所述多个流体输送支管分为一组或多组(多组比如2组以上，特别是2-8组、2-6组或2-4组)，则在任意一组流体输送支管中，i)任意相邻两个流体输送支管的中心线沿着同一个方向(称为该组流体输送支管的延伸方向)彼此相互平行或基本上平行，和/或，ii)任意相邻两个流体输送支管的内径彼此相同或不同(比如相同)，各自独立地为50-150mm(优选65-125mm)，和/或，iii)任意相邻两个流体输送支管的中心线的垂直距离D2彼此相同或不同(比如相同)，各自独立地为250-750mm(优选300-650mm，更优选350-550mm)，和/或，iv)所述D1与所述D2满足关系式：D1/D2≥0.3(优选D1/D2≥0.5)，和/或，v)相邻两个流体输送支管的末端两两相连而形成线段，该线段具有折线或直线的形状(优选设所述折线的最高点与最低点之间的高度差为H C，该组流体输送支管中最长的流体输送支管的长度为Lmax，则H C/Lmax≤44％，优选H C/Lmax≤37％，更优选H C/Lmax≤28％，更优选H C基本上为0，更优选所述直线与该组流体输送支管的延伸方向基本上垂直)，和/或，vi)该组流体输送支管中最长的流体输送支管的长度Lmax为5000-29000mm(优选5000-20000mm，优选5000-10000mm，更优选6000-10000mm)。
6.前述或后述任一方面所述的流体分布器，其中在每一个所述流体输送主管上，将所述多个流体输送支管分为一组或多组(多组比如2组以上，特别是2-8组、2-6组或2-4组)，或者将所述流体分布器的所有流体输送支管分为一组或多组(多组比如2组以上，特别是2-8组、2-6组或2-4组)，则在 所述多组流体输送支管之间，i)一组流体输送支管与另一组流体输送支管的延伸方向彼此形成角度(优选彼此相互平行或彼此相互垂直)，和/或，ii)一组流体输送支管在所述闭合形状上的投影与另一组流体输送支管在所述闭合形状上的投影不重叠，优选所述流体分布器包含的全部组的流体输送支管在所述闭合形状上的投影面积之和At小于所述闭合形状的面积Ac，优选At/Ac为75％以上，更优选At/Ac为80％以上，更优选At/Ac为90％以上。
7.前述或后述任一方面所述的流体分布器，其中每一个所述流体输送支管的中心线(基本上)是直线。
8.前述或后述任一方面所述的流体分布器，其中在每一个所述流体输送支管上，所述多个开孔彼此相同或不同(比如相同)，各自独立地具有选自圆形、椭圆形、正方形、长方形、梯形和菱形的外周形状，和/或，所述多个开孔彼此相同或不同(比如相同)，各自独立地具有3-10mm，(优选4.5-8.5mm，更优选5.0-7.5mm)的等效圆直径。
9.前述或后述任一方面所述的流体分布器，其中在至少一个所述流体输送支管上，在所述流体输送支管的从连接部至起始端的管段(称为外管段)上设置流体流量控制器(优选流体流量控制阀)。
10.前述或后述任一方面所述的流体分布器，其中所述连接部被构造为具有环绕所述流体输送支管的形状，优选具有法兰形状，或者所述闭合形状的直径为5.5-32.0米(优选6.0-23.0米，更优选11.0-23.0米或者13.0-23.0米)。
11.前述或后述任一方面所述的流体分布器，还包括环绕所述开孔设置的喷嘴。
12.前述或后述任一方面所述的流体分布器，其中所述容器为流化床反应器，所述反应器的内腔直径为5-29米(优选5-20米，更优选10-20米或者12-20米)，并且所述流体是含氮流体或含氨流体，特别是含氮气体或者含氨气体，特别是烯氨混合气，更特别是丙烯氨混合气。
13.一种流体分布器，是用于使丙烯氨混合气在流化床反应器内部均匀分布的进料分布器，该进料分布器包括：
一个以上分布器入口；
多个支管，该多个支管分别连接至所述分布器入口并分别与所述分布器入口流体连通，并且该多个支管所述分布器入口向反应器内部延伸；
锐孔，该锐孔设置在所述支管上；以及
喷嘴，该喷嘴围绕相应的锐孔设置在所述支管上，并且与所述相应的锐孔同轴，以使丙烯氨混合气经过所述分布器入口、所述支管、所述锐孔和所述喷嘴，最终在反应器内部均匀分布。
14.前述或后述任一方面所述的流体分布器，其中在延伸方向上相邻的所述支管之间相互平行。
15.前述或后述任一方面所述的流体分布器，其中相互平行的所述相邻支管间的距离是相同的。
16.前述或后述任一方面所述的流体分布器，其中在气流方向上相邻的所述锐孔间的孔间距是相同的。
17.前述或后述任一方面所述的流体分布器，其中所述相邻的锐孔间的所述孔间距与所述相邻的支管间的垂直距离的比值为1/N，其中，N为2以上的整数。
18.前述或后述任一方面所述的流体分布器，其中所述相邻的支管间的距离为250-750mm。
19.前述或后述任一方面所述的流体分布器，其中所述一个以上分布器入口和所述多个支管处于所述反应器的同一水平截面内。
20.前述或后述任一方面所述的流体分布器，其中所述支管在所述流化床反应器内部延伸的长度低于反应器的直径。
21.前述或后述任一方面所述的流体分布器，其中所述支管在所述流化床反应器内部延伸的长度低于反应器的半径。
22.前述或后述任一方面所述的流体分布器，其中所述流化床反应器的直径为5-29米。
23.前述或后述任一方面所述的流体分布器，其中所述流化床反应器的直径为5-20米。
24.前述或后述任一方面所述的流体分布器，其中所述多个支管的管径为70-145mm。
25.前述或后述任一方面所述的流体分布器，还包括一个以上进料主管，该进料主管设置在所述流化床反应器外部，并且该进料主管分别连接至所述一个以上分布器入口和所述多个支管连接并与所述一个以上进料分布器入口和所述多个支管流体连通。
26.前述或后述任一方面所述的流体分布器，其中所述进料主管为圆环状、半圆环状、或圆弧状。
27.前述任一方面所述的流体分布器，还包括流量控制器，该流量控制器用于控制所述进料分布器内的丙烯氨混合气的流量。
28.一种使用前述任一方面所述的流体分布器向容器内腔输送流体的方法，包括向所述流体分布器的所述至少一个流体入口输送流体(优选气体，更优选丙烯氨混合气)，使所述流体至少经过所述流体输送主管、所述流体输送支管和所述开孔进入所述内腔的步骤。
29.前述任一方面所述的流体分布器作为进料分布器向氨氧化反应器的内腔输送反应原料(优选丙烯氨混合气)的用途。
30.一种反应装置，包括反应器和前述任一方面所述的流体分布器，其中所述反应器至少具有壳体、设置在所述壳体上的多个通孔、以及由所述壳体的内表面限定的内腔，所述通孔在数量和设置位置上与所述流体分布器的流体输送支管具有一一对应关系，由此使得每一个流体输送支管都能够穿过与其对应的一个通孔而进入所述内腔，并且所述流体输送支管穿过所述通孔之后通过所述流体输送支管的连接部气密性固定在所述壳体的外表面上。
31.一种丙烯腈的制造方法，包括使用前述任一方面所述的流体分布器或者使用前述任一方面所述的方法向反应器(优选流化床反应器)内腔输送丙烯氨混合气，并向所述反应器内腔输送含氧气体(优选空气)，或者在前述任一方面所述的反应装置中，使丙烯发生氨氧化反应而生成丙烯腈的步骤。
技术效果
根据本发明的流体分布器，可以实现如下技术效果中的至少一个：
(1)不仅是现有尺寸的反应器，即使对于更大尺寸的反应器，也能够满足流体(特别是丙烯氨混合气)均匀分布的要求。
(2)特别是在输送含氮流体或含氨流体(比如丙烯氨混合气)的情况下，不仅是现有尺寸的反应器，即使对于更大尺寸的反应器，也能够表现出降低的氮化脆裂风险。
附图说明
图1是现有技术丙烯氨氧化流化床反应器的结构示意图。
图2是现有技术流体分布器的一个实施方式的结构示意图。
图3是现有技术流体分布器的另一个实施方式的结构示意图，其中图3A为侧视图，图3B为仰视图。
图4是本发明流体分布器的一个实施方式的结构示意图。
图5是本发明流体分布器的一个实施方式的结构示意图。
图6是本发明流体分布器的一个实施方式的结构示意图。
图7是本发明流体分布器一个实施方式的结构示意图。
图8是本发明流体分布器一个实施方式的结构示意图。
图9是本发明流体分布器一个实施方式的结构示意图。
图10是图4的局部放大示意图，举例说明了流体输送支管与壳体的连接。
附图标记说明
1       丙烯氨氧化反应器
13、103 开孔
4       壳体
15、105 流体入口
6       空气分布板
7       冷却盘管
8       工艺空气入口
10、100 流体分布器
x       总管
y       主管
z       支管
11      流体输送支管(有时简称为支管)
12      流体输送主管(有时也称为进料主管)
14      流体流量控制器
16      连接部
17      通孔
具体实施方式
下面对本发明的具体实施方式进行详细说明，但是需要指出的是，本发明的保护范围并不受这些具体实施方式的限制，而是由附录的权利要求书来确定。
本说明书提到的所有出版物、专利申请、专利和其它参考文献全都引于此供参考。除非另有定义，本说明书所用的所有技术和科学术语都具有本领域技术人员常规理解的含义。在有冲突的情况下，以本说明书的定义为准。
当本说明书以词头“本领域技术人员公知”、“现有技术”或其类似用语来导出材料、物质、方法、步骤、装置或部件等时，该词头导出的对象涵盖本申请提出时本领域常规使用的那些，但也包括目前还不常用，却将变成本领域公认为适用于类似目的的那些。
在本发明的上下文中，术语“流体”指的是在25℃和一个标准大气压下表现为液体或气体的任何物质。作为所述流体，具体比如可以举出含氮流体或含氨流体，特别是含氮气体或者含氨气体，特别是烯(比如C2-6烯烃)氨混合气，更特别是丙烯氨混合气。特别地，对于氨在所述流体中的含量没有特别的限定，技术人员可以根据情况任意选择。
在没有明确指明的情况下，本说明书内所提到的所有百分数、份数、比率等都是以摩尔为基准的，而且反应压力是表压。
在本说明书的上下文中，本发明的任何两个或多个实施方式都可以任意组合，由此而形成的技术方案属于本说明书原始公开内容的一部分，同时也落入本发明的保护范围。
根据本发明的一个实施方式，涉及一种流体分布器。该流体分布器适合向容器内腔输送流体。
根据本发明的一个实施方式，所述流体是含氮流体或含氨流体，特别是含氮气体或者含氨气体，特别是烯氨混合气，更特别是丙烯氨混合气。
根据本发明的一个实施方式，所述流体分布器至少包括一个或多个流体输送主管。
根据本发明的一个实施方式，在存在一个所述流体输送主管时，所述流体输送主管被构造为在将其中心线和/或中心线延长线首尾相接时构成闭合形状。另外，在存在多个所述流体输送主管时，这些流体输送主管被构造为在将其各自的中心线和/或中心线延长线首尾相接时，构成闭合形状。
在本发明的上下文中，所谓“中心线延长线”指的是在所述流体输送主管不连续或断开时，以其中心线延长线代替中心线。其他概念也可类似理解。
根据本发明的一个实施方式，作为所述闭合形状，优选基本上顺应所述容器外周轮廓的闭合形状，更优选基本上平面的闭合形状，更优选基本上平面的圆形、椭圆形或者多边形形状。根据本发明的一个实施方式，所述闭合形状与所述容器的中心线基本上垂直。换句话说，所述闭合形状为基本上平面形状，而且所述闭合形状基本上平行于所述容器的横截面。
为了更清楚说明起见，图4、图5、图7、图8举例说明了什么是所述流体输送主管的中心线、中心线延长线和闭合形状(均为圆形)，全部用虚线表示，但本发明并不限于这些特定的形状。而且，所述容器的外周轮廓即为壳体4的形状。图4和图5还举例说明了什么是内腔，也就是由壳体4包围的内部空间。
在本发明的上下文中，所谓“基本上”指的是允许存在对于本领域技术人 员而言可以接受或认为合理的偏差。
根据本发明的一个实施方式，所述闭合形状的直径(比如等效圆直径)一般为5.5-32.0米，优选6.0-23.0米，更优选11.0-23.0米或者13.0-23.0米。
根据本发明的一个实施方式，每一个所述流体输送主管具有至少一个流体入口。优选的是，每一个所述流体输送主管具有1-3个或者1个流体入口。
根据本发明的一个实施方式，在每一个所述流体输送主管上设置多个流体输送支管。作为举例而言，所述流体输送支管的数量可以是5-100个或者5-50个，但本发明并不限于此。
根据本发明的一个实施方式，每一个所述流体输送支管具有起始端和末端。作为举例而言，所述末端可以是封闭、半封闭或开放结构，优选封闭结构。另外，所述起始端与所述流体输送主管连接且流体连通，并且所述起始端与所述末端限定了所述流体输送支管的长度L。
为了更清楚说明起见，图4举例说明了什么是所述流体输送支管的起始端和末端，以及如何确定所述长度L。
根据本发明的一个实施方式，在每一个所述流体输送支管上沿着所述流体输送支管的长度方向设置多个开孔(也称为锐孔)。作为举例而言，所述开孔的数量可以是2-140个或者6-60个，但本发明并不限于此。
根据本发明的一个实施方式，在每一个所述流体输送支管上设置连接部。而且，所述连接部被构造为在所述流体输送支管穿过所述容器的壳体而进入所述内腔之后，将所述流体输送支管连接(优选固定，更优选气密性固定)在所述壳体(优选所述壳体的外表面)上。举例而言，可以将所述流体输送支管固定(优选气密性固定)在所述壳体上，特别是固定在所述壳体的外表面上。
根据本发明的一个实施方式，所述连接部的设置位置与所述末端相比更靠近所述起始端。或者，所述连接部的所述设置位置与所述起始端沿着所述流体输送支管长度方向的距离为所述流体输送支管长度L的1/4以下、1/6以下、1/8以下、1/10以下或更小。
根据本发明的一个实施方式，所述流体输送主管为一个或多个，优选1-8个，更优选1-4个或1-2个。
根据本发明的一个实施方式，在存在多个时，这些流体输送主管的内径彼此相同或不同(比如相同)，各自独立地为150-700mm，优选170-500mm。
根据本发明的一个实施方式，在每一个所述流体输送支管上，所述多个开孔沿着所述流体输送支管的长度方向设置在所述流体输送支管的从所述连接 部至所述末端的管段(称为内管段)上。
为了更清楚说明起见，图4和图6举例说明了如何确定内管段和外管段。
根据本发明的一个实施方式，所述多个开孔可以等间距或不等间距设置。优选的是，任意相邻两个所述开孔之间的距离D1彼此相同或不同，各自独立地为125-375mm，优选175-250mm。
根据本发明的一个实施方式，至少一个所述流体输送支管的内管段沿着从所述流体输送支管的连接部至末端的方向具有恒定或变化的内径。作为所述变化，比如可以举出逐渐加粗或逐渐变细。
根据本发明的一个实施方式，所述内管段的长度Li使得在所述流体输送支管穿过所述容器的壳体而进入所述内腔之后，所述内管段的中心线向所述内管段首尾两端方向的延长线与所述壳体的内表面产生两个交点，设所述两个交点之间的线段的长度为Ld，则0＜Li＜Ld，优选0.25Ld≤Li≤0.99Ld，优选0.40Ld≤Li＜0.99Ld，更优选0.40Ld≤Li＜0.50Ld。
为了更清楚说明起见，图8举例说明了如何确定所述内管段的中心线、延长线、Li和Ld，而且还举例说明了如何确定支管的中心线。
根据本发明的一个实施方式，在每一个所述流体输送主管上，将所述多个流体输送支管分为一组或多组，多组比如2组以上，特别是2-8组、2-6组或2-4组，则在任意一组流体输送支管中，任意相邻两个流体输送支管的中心线沿着同一个方向(在本发明的上下文中，将其称为该组流体输送支管的延伸方向)彼此相互平行或基本上平行。为了更清楚说明起见，图7举例说明了所述延伸方向(四个)，分别由四个箭头表示，但本发明并不限于所述四个延伸方向。
根据本发明的一个实施方式，在每一个所述流体输送主管上，将所述多个流体输送支管分为一组或多组，多组比如2组以上，特别是2-8组、2-6组或2-4组，则在任意一组流体输送支管中，任意相邻两个流体输送支管的内径彼此相同或不同(比如相同)，各自独立地为50-150mm，优选65-125mm。
根据本发明的一个实施方式，在每一个所述流体输送主管上，将所述多个流体输送支管分为一组或多组，多组比如2组以上，特别是2-8组、2-6组或2-4组，则在任意一组流体输送支管中，任意相邻两个流体输送支管的中心线的垂直距离D2彼此相同或不同(比如相同)，各自独立地为250-750mm，优选300-650mm，更优选350-550mm。
根据本发明的一个实施方式，在每一个所述流体输送主管上，将所述多个 流体输送支管分为一组或多组，多组比如2组以上，特别是2-8组、2-6组或2-4组，则在任意一组流体输送支管中，所述D1与所述D2满足关系式：D1/D2≥0.3，优选D1/D2≥0.5。
根据本发明的一个实施方式，在每一个所述流体输送主管上，将所述多个流体输送支管分为一组或多组，多组比如2组以上，特别是2-8组、2-6组或2-4组，则在任意一组流体输送支管中，相邻两个流体输送支管的末端两两相连而形成线段。一般而言，所述线段具有折线或直线的形状。
根据本发明的一个实施方式，设所述折线的最高点与最低点之间的高度差为H C，该组流体输送支管中最长的流体输送支管的长度为Lmax，则H C/Lmax≤44％，优选H C/Lmax≤37％，更优选H C/Lmax≤28％，更优选H C基本上为0，更优选所述直线与该组流体输送支管的延伸方向基本上垂直。
为了更清楚说明起见，图6举例说明了直线形状的所述线段，图8举例说明了折线形状的所述线段，但本发明并不限于这些特定的形状。另外，这些图还举例说明了如何确定H C和Lmax。
根据本发明的一个实施方式，在每一个所述流体输送主管上，将所述多个流体输送支管分为一组或多组，多组比如2组以上，特别是2-8组、2-6组或2-4组，则在任意一组流体输送支管中，该组流体输送支管中最长的流体输送支管的长度Lmax为5000-29000mm，优选5000-20000mm，优选5000-10000mm，更优选6000-10000mm。
根据本发明的一个实施方式，在每一个所述流体输送主管上，将所述多个流体输送支管分为一组或多组，或者将所述流体分布器的所有流体输送支管分为一组或多组，多组比如2组以上，特别是2-8组、2-6组或2-4组，则在所述多组流体输送支管之间，一组流体输送支管与另一组流体输送支管的延伸方向彼此形成角度，优选彼此相互平行或彼此相互垂直，包括基本上平行或基本上垂直的情况。
根据本发明的一个实施方式，在每一个所述流体输送主管上，将所述多个流体输送支管分为一组或多组，或者将所述流体分布器的所有流体输送支管分为一组或多组，多组比如2组以上，特别是2-8组、2-6组或2-4组，则在所述多组流体输送支管之间，一组流体输送支管在所述闭合形状上的投影与另一组流体输送支管在所述闭合形状上的投影不重叠。优选的是，所述流体分布器包含的全部组的流体输送支管在所述闭合形状上的投影面积之和At小于所述闭合形状的面积Ac，优选At/Ac为75％以上，更优选At/Ac为80％以上，更优 选At/Ac为90％以上。
为了更清楚说明起见，图7举例说明了如何确定所述投影。在图7中，举例说明了2个投影，分别由2块阴影面积表示，但本发明并不限于所述2个投影。如图所例示，所述投影实际上是由每组流体输送支管中全部流体输送支管的末端两两相连而形成的线段、其所在的流体输送主管的中心线(根据情况，可能还包括中心线延长线)、以及该组流体输送支管中最外侧两个流体输送支管长度方向的外缘限定而成的图形在所述闭合形状上的投影。一般而言，所述图形和所述闭合形状都是基本上平面的形状，而且二者通常处于基本上同一平面之内。
根据本发明的一个实施方式，在将所述流体分布器的所有流体输送支管分为多组时，各组流体输送支管可以全部处于同一个流体输送主管上，也可以分别或彼此任意组合而处于不同的流体输送主管上，特别是分别或彼此任意组合而处于不同的流体输送主管上。在此，所谓“彼此任意组合”指的是当流体输送支管的组数与流体输送主管的数量不同时，1组或更多组的流体输送支管处于同一个流体输送主管上，剩余组的流体输送支管处于其余的一个或多个流体输送主管上。具体举例而言，假设有4组流体输送支管和2个流体输送主管，则作为彼此任意组合，所述4组流体输送支管中的1组流体输送支管处于一个流体输送主管上，另外3组流体输送支管处于另一个流体输送主管上，或者所述4组流体输送支管中的2组流体输送支管处于一个流体输送主管上，另外2组流体输送支管处于另一个流体输送主管上。
根据本发明的一个实施方式，每一个所述流体输送支管的中心线基本上是直线。也就是说，每一个所述流体输送支管基本上是直管。
根据本发明的一个实施方式，在每一个所述流体输送支管上，所述多个开孔彼此相同或不同(比如相同)，各自独立地具有选自圆形、椭圆形、正方形、长方形、梯形和菱形的外周形状。
根据本发明的一个实施方式，在至少一个所述流体输送支管上，在所述流体输送支管的从连接部至起始端的管段(称为外管段)上设置流体流量控制器，优选流体流量控制阀。
根据本发明的一个实施方式，所述连接部被构造为具有环绕所述流体输送支管的形状，优选具有法兰形状。
根据本发明的一个实施方式，所述流体分布器还包括环绕所述开孔设置的喷嘴。通过这种设置，支管通过所述开孔与相应的喷嘴流体连通，导致输送流 体从所述开孔喷出后，经过该喷嘴整流后经该喷嘴另一端的开口(一般是圆形)进入所述容器的内腔。
根据本发明的一个实施方式，所述开孔与其相应的喷嘴同轴，且位于与相应支管中心线垂直的径向截面上。
根据本发明的一个实施方式，在每一个所述流体输送支管上，所述多个开孔彼此相同或不同(比如相同)，各自独立地具有3-10mm(优选4.5-8.5mm，更优选5.0-7.5)的直径(一般是等效圆直径)。优选的是，所述开孔的直径小于相应的喷嘴及喷嘴末端开口的直径。另外，沿着所述流体输送支管的长度方向，所述多个开孔的直径可以彼此相同也可以彼此不同，比如所述直径逐渐增大或逐渐减小。
根据本发明的一个实施方式，喷嘴由支管向下方延伸。而且，各喷嘴的延伸角度可以相同也可以不同。优选的是，全部喷嘴的末端处于基本上同一水平截面内。
根据本发明的一个实施方式，所述喷嘴可以选自柱形、锥形，和/或，优选为柱形。另外，所述喷嘴的横截面各自独立地具有选自圆形、椭圆形、正方形、长方形、梯形和菱形，优选为圆形和/或椭圆形，更优选为圆形。
根据本发明的一个实施方式，所述喷嘴的柱长与所述喷嘴的内径之比大于等于4，优选为大于等于6，更优选为大于等于8。
根据本发明的一个实施方式，在丙烯氨氧化流化床反应器的情况下，全部喷嘴的末端与下方的空气分布板的垂直距离是基本上相同的。
根据本发明的一个实施方式，所述容器为流化床反应器。一般而言，所述反应器的内腔直径为5-29米，优选5-20米，更优选10-20米或者12-20米。本发明人经过大量实验、计算和计算机模拟发现，所述流体分布器能够满足具有所述内腔直径的丙烯氨氧化流化床反应器的要求，即确保流体分布器内的混合气温度总是低于氮化温度。
根据本发明的一个实施方式，所述流体分布器是用于使丙烯氨混合气在流化床反应器内部均匀分布的进料分布器，该进料分布器包括：
一个以上分布器入口(即所述流体入口)；
多个输送支管(即所述流体输送支管)，该多个输送支管分别连接至所述分布器入口并分别与所述分布器入口流体连通，并且该多个输送支管从所述分布器入口向反应器内部延伸；
开孔，所述开孔设置在所述输送支管上；以及
喷嘴，该喷嘴围绕相应的开孔设置在所述输送支管上，并且与所述相应的开孔同轴，以使丙烯氨混合气经过所述分布器入口、所述输送支管、所述开孔和所述喷嘴，最终在反应器内部均匀分布，
还包括一个以上进料主管(即所述流体输送主管)，该进料主管设置在所述流化床反应器外部，并且该进料主管分别连接至所述一个以上分布器入口和所述多个输送支管，并与所述一个以上进料分布器入口和所述多个输送支管流体连通。
根据本发明的一个实施方式，还涉及使用本发明如前所述的流体分布器向容器内腔输送流体的方法(以下称为流体输送方法)。所述方法包括向所述流体分布器的所述至少一个流体入口输送流体，使所述流体至少经过所述流体输送主管、所述流体输送支管和所述开孔进入所述内腔的步骤。在此，作为所述流体，优选气体，更优选丙烯氨混合气。另外，作为所述容器，优选流化床反应器。
根据本发明的一个实施方式，还涉及本发明如前所述的流体分布器作为进料分布器向氨氧化反应器的内腔输送反应原料的用途。在此，作为所述反应原料，优选丙烯氨混合气。
根据本发明的一个实施方式，还涉及一种反应装置。该反应装置包括反应器和本发明如前所述的流体分布器。
根据本发明的一个实施方式，所述反应器至少具有壳体、设置在所述壳体上的多个通孔、以及由所述壳体的内表面限定的内腔。而且，所述通孔在数量和设置位置上与所述流体分布器的流体输送支管具有一一对应关系，由此使得每一个流体输送支管都能够穿过与其对应的一个通孔而进入所述内腔，并且所述流体输送支管穿过所述通孔之后通过所述流体输送支管的连接部气密性固定在所述壳体的外表面上。
根据本发明的一个实施方式，还涉及一种丙烯腈的制造方法，包括使用本发明如前所述的流体分布器向反应器(比如流化床反应器)内腔输送丙烯氨混合气，并向所述反应器内腔输送含氧气体，使丙烯发生氨氧化反应而生成丙烯腈的步骤。在此，作为所述含氧气体，具体比如可以举出空气。
根据本发明的一个实施方式，还涉及一种丙烯腈的制造方法，包括使用本发明如前所述的流体输送方法向反应器(比如流化床反应器)内腔输送丙烯氨混合气，并向所述反应器内腔输送含氧气体，使丙烯发生氨氧化反应而生成丙烯腈的步骤。在此，作为所述含氧气体，具体比如可以举出空气。
根据本发明的一个实施方式，还涉及一种丙烯腈的制造方法，包括在本发明如前所述的反应装置中，使丙烯发生氨氧化反应而生成丙烯腈的步骤。
根据本发明的一个实施方式，当反应器直径增大时，同一形式流体分布器的支管的长度相应延长，因此混合气流经导管后的温升更大。在存在喷嘴时，支管内混合气质量流量是喷嘴数和单个喷嘴流出的混合气质量流量的乘积。在假定喷嘴间距及单个喷嘴混合气质量流量相同时，流过最长的支管中丙烯氨混合气的质量流量也会相应增加。在支管的管径相对固定的情况下，会导致支管中的平均升温率略有降低。因此，流经同样距离的混合气的温升幅度又将减小。而ΔT i是混合气温升幅度与支管长度的乘积。最长的支管是如此，其它支管的ΔT i的变化均是前述变化的综合，相对于短支管，长支管的支管长度的变化因子大于短支管内混合气温升的变化因子，通常情况下，最长支管的末端喷嘴处的温度ΔT i的变化最大，也即是丙烯氨分布器喷嘴的最高温度点，该点温度若低于氮化温度，则可认为反应器内丙烯氨分布器任一位置处均低于氮化温度。
以下将参考附图并结合丙烯腈制造技术举例描述本发明，但本发明并不限于这些附图或者丙烯腈制造技术。
如图1所示，典型的丙烯氨氧化流化床反应器1的主要内构件包括：旋风分离器(未示出)、冷却盘管7、流体分布器(即丙烯氨混合气分布器)100、空气分布板6和工艺空气入口8。流体分布器100位于空气分布板6与冷却盘管7之间。来自原料气混合系统(未示出)的丙烯氨混合气由流体分布器流体入口进入流体分布器10，经流体分布器10穿过反应器的壳体(也称为反应器壁)4，由设置于流体分布器100导管上的喷嘴进入催化剂床层，与由工艺空气入口8导入的工艺空气充分混合，在催化剂存在的情况下发生氨氧化反应生成丙烯腈等产物。
如图2所示，现有技术的流体分布器100一般包括：流体分布器流体入口105、主管y(y管)、支管z(支管)、开孔103和喷嘴(未示出)。支管为直接和喷嘴流体连通的导气管，其主要起到将混合气输送到喷嘴的作用。支管通常为不分支导气管且排布于反应器的同一横截面内，其上按一定方式均匀分布开孔3并因此连通喷嘴，从而实现喷嘴口在反应器的同一横截面的均匀分布。y管为直接与支管流体连通的导气管，其主要起到将混合气输送到支管的作用。y管通常为直管，其上均匀连通支管且与支管处于反应器的同一横截面内，以实现前述喷嘴口在反应器的同一横截面的均匀分布。在某些流体分布器中，y管除了与支管流体连通，还和支管一样直接通过开孔103与喷嘴流体连通，以 用于实现前述喷嘴口在反应器的同一横截面的均匀分布。
如图3A和3B所示，在现有技术的某些流体分布器中，支管与y管处于反应器的同一横截面内，但其与流体分布器流体入口105不在同一平面上，因此设置总管x(x管)将丙烯氨混合气由分布器流体入口引入y管。根据本发明的一个实施方式，通常情况下，x管只需要一根，且除了在末端与y管流体连通以外，在其他位置处不具有任何分支。x管为直接与y管流体连通的导气管，其主要起到将混合气输送到y管的作用。
在现有技术的这些流体分布器中，丙烯氨混合气从丙烯氨流体分布器流体入口105进入，沿着x管、y管、支管、并最终通过设置在y管和支管上的开孔103经喷嘴，均匀分散至反应器床层中。丙烯氨混合气在沿着流体分布器导管被均匀送至催化剂床层的过程中与催化剂床层发生热交换，致使温度不断上升，直至经喷嘴进入反应器前达到最高温度。本发明的发明人通过研究发现，当采用诸如图2和图3所示的现有流体分布器100时，只能够满足直径小于10米的反应器。当反应器直径进一步增大时，流体分布器100中的丙烯氨混合气达到氮化温度的风险显著提高。而且，即便是直径小于10米的反应器，也存在丙烯氨混合气达到氮化温度的风险。
根据本发明的一个实施方式，如图4所示，流体分布器10包括流体入口15、进料主管12、支管11、开孔13和连接部16，并任选包括喷嘴(未示出)。在本发明的流体分布器中，分布器流体入口15与来自于原料气混合系统的管路以气密性方式连接，以将混合气输送至流体分布器中。根据本发明的一个实施方式，流体分布器可以包括一个以上的分布器流体入口15，每个分布器流体入口15与独立的进料主管12相连接。
如图4至8所示，根据本发明的一个实施方式，一个以上进料主管12分别连接于一个以上的分布器流体入口15并与之流体连通，并且由分布器流体入口15围绕着反应器壁向两侧延伸。多个支管11在不同的位置连接至进料主管12，并与进料主管12流体连通，以将丙烯氨混合气输送至支管11中。对本发明的流体分布器的进料主管12的形状没有具体限制，但优选地，采用圆环状(图4和6)、半圆环状(图5和7)或圆弧状(图8)的形状。对进料主管的管径没有具体限制，但考虑到与支管11连接时的可加工型，优选地，进料主管12的管径大于支管11的管径。
根据本发明的一个实施方式，支管11为穿过反应器壁4的直管，并且除了在其上设置开孔和喷嘴之外，支管11在反应器内腔没有任何的分支。并且， 多个支管11在反应器内腔不互相连接或交叉。多个支管11的一端连接至进料主管12，另一端则穿过反应器壁4向反应器内部延伸。对于支管11与进料主管12的连接点的具体位置没有具体限定，支管11可以在反应器外部与进料主管12连接，也可以在反应器壁处与进料主管12连接。在支管11与进料主管12在反应器外部相连接的情况下，对于支管11与反应器壁的连接方式没有具体限定，可以采用本领域常用的焊接方式，也可以采用如图9和10所示的气密性连接方式。
根据本发明的一个实施方式，优选地，所有支管11均处于反应器的同一横截面内。更优选地，流体分布器流体入口15、进料主管12以及支管11均处于反应器的同一横截面内。
根据本发明的一个实施方式，当反应器直径较小时，如图8所示，在反应器的整个横截面内，支管11可以采用由反应器横截面的一侧进入并延伸至另一侧反应器壁附近的形式。此时，支管11的长度(支管11在反应器内部的延伸长度)上限小于反应器的直径。
根据本发明的一个实施方式，特别是在反应器直径较大时，为了避免由于支管长度过长导致混合气在支管内行进的路径长度过长而导致混合气温度达到氮化温度，可以采用如图4或图5所示的布置方式。在图4和5中，在反应器横截面内，多个支管11分为两组，分别从该横截面的两侧穿过反应器壁4，并且延伸至与支管11的延伸方向垂直的该横截面的中轴线附近。根据本发明的一个实施方式，优选地，分别在该横截面的上述两侧对应布置的支管11彼此对称。此时，支管11的长度优选地小于反应器的半径。
如图4、5和8所示，根据本发明的一个实施方式，多个支管11在反应器内部不互相连接或交叉，并且，优选地，多个支管11相互平行。更优选地，在与支管11的延伸方向垂直的方向上相邻的支管11之间的垂直距离是相同的。该垂直距离以250-750mm为宜，优选300-650mm，更优选350-550mm。
根据本发明的一个实施方式，还可以如图6或图7所示，将反应器内腔的横截面分为多个(比如2个以上，特别是2-8个、2-6个或2-4个)扇形区域，并在每个扇形区域内平行布置多个支管11的流体分布器形式。根据本发明的一个实施方式，优选将反应器的横截面分为4个扇形区域(四象限)。同一个象限中的相邻的支管间的垂直距离是相同的，并以250-750mm为宜，优选300-650mm，更优选350-550mm。
如图4至8所示，根据本发明的一个实施方式，在支管11上，沿其轴线 方向排列有一个以上称为锐孔的开孔13，用于使混合气从流体分布器内喷入反应器。
根据本发明的一个实施方式，在支管11上，沿支管11的轴向方向上相邻的开孔圆心之间沿轴向方向的垂直距离称作孔间距。根据本发明的一个实施方式，对于任一流体分布器来说，在任一支管的轴向方向上相邻开孔的孔间距是相同的。相邻开孔间的孔间距与前述相邻的平行支管之间垂直距离的比值为1/N，N为2以上的整数。根据本发明的一个实施方式，优选地，N为2，即相邻开孔间的孔间距为前述相邻的平行支管之间垂直距离的二分之一。在本发明另一些实施方式中，优选地，N为3，即相邻开孔间的孔间距为前述相邻的平行支管之间垂直距离的三分之一。
根据本发明的一个实施方式，在支管11的同一径向截面上可以布置有一个以上的开孔13(对应于这些开孔圆心的该截面称为开孔截面)。这些处于同一径向截面的开孔13同样与对应的喷嘴分别相连，且与喷嘴同心。根据本发明的一个实施方式，在流体分布器的支管11上的同一径向截面均布置有同样数量的开孔，处于同一径向截面的多个开孔与位于其他径向截面的多个开孔分别一一对应，从而在沿相应支管的轴向方向上排成列，这些列与该支管的轴线平行。
根据本发明的一个实施方式，在图4至8所示的流体分布器中，位于不同支管或相同支管的不同径向截面处的开孔的孔径可以相同也可以不同。
根据本发明的一个实施方式，在所述流体分布器中，所述支管11可以根据需要安装喷嘴，因此考虑到流体分布器的可加工性，支管的管径下限优选为70mm以上，更优选为75mm以上。当低于此管径时，支管加工性能变差，很难安装喷嘴。同时，考虑到不能影响流化效果，支管管径的上限优选为145mm以下，更优选135mm以下。
根据本发明的一个实施方式，反应器内部的所有支管11的直径都是相同的。另一方面，为了使丙烯氨混合气在整个反应器床层中被更加均匀地分布，根据本发明的一个实施方式，可以根据实际情况，在同一流体分布器中设置具有一种以上直径的支管11。此外，根据本发明的一个实施方式，可以使同一根支管11在其延伸方向上具有一种以上的不同直径。
根据本发明的一个实施方式，为了控制丙烯氨混合气在反应器内催化剂床层中的分布，可以在分布器流体入口15处设置流体流量控制器14，用以控制流体分布器内的丙烯氨混合气流量。此外，为了使丙烯氨混合气在整个反应器 床层中被更加均匀地分布。如图9所示，根据本发明的一个实施方式可以在每一根支管11的位于反应器外部的位置处均设置流体流量控制器14。
实施例
以下将通过实施例和比较例对本发明进行进一步的详细描述，但本发明不限于以下实施例。
以下所有实施例数据均是在实验室中分别模拟不同直径的氨氧化流化床反应器中的条件，以碳钢为材质根据说明书附图中各种流体分布器的形式模拟实际流体分布器，并在重要节点处设置温度变送器，来测量流体分布器温度。在以下实施例和比较例中，所有数据均经多次测量后取平均值。
在以下实施例中，支管长度指的是支管的内管段长度。
实施例1
丙烯氨氧化流化床反应器直径(内腔直径，以下同)为10米，采用中国石化上海石油化工研究院SANC系列丙烯腈催化剂用于生产丙烯腈，反应装置满负荷运行，原料气配比C 3H 6∶NH 3∶空气为1∶1.2∶9.3，反应温度440℃，反应压力为50KPa，丙烯氨混合气流体入口温度控制为80℃。流体分布器采用图4的形式，材质为碳钢，分布器有1根主管，主管直径为φ500mm，设有52根支管，各自与主管相连，支管直径为φ80mm，支管间距离为380mm，支管之间相互平行，沿支管方向的喷嘴开孔距离为190mm，最长支管长度为4.9m设有52个喷嘴，最短支管长度为1.8m设有15个喷嘴，分布器喷嘴总数为2100个，喷嘴内径为20mm，长度为200mm；锐孔孔径为6.0mm。丙烯氨混合气通过流体分布器到达每根支管尾端喷嘴(图4中未示出)处，用热电偶测量各支管末端喷嘴处丙烯氨混合气温度，其中流体分布器内混合气最高点温度为丙烯氨混合气在行进长度最长支管的尾端喷嘴处的温度为282℃。
实施例2
丙烯氨氧化流化床反应器直径为12米，采用中国石化上海石油化工研究院SANC系列丙烯腈催化剂用于生产丙烯腈，反应装置满负荷运行，原料气配比C 3H 6∶NH 3∶空气为1∶1.2∶9.5，反应温度440℃，反应压力为50KPa，丙烯氨混合气流体入口温度控制为80℃。流体分布器采用图5的形式，材质为碳钢，分布器设有2根主管，主管直径为φ420mm，设有60根支管，各自与主管相连，支管直径为φ100mm，支管间距离为410mm，支管之间相互平行，沿支管方向的喷嘴开孔距离为205mm，最长支管长度为5.9米设有58个喷嘴，最短支管长度为1.9米设有15个喷嘴，分布器喷嘴总数为2560个，喷嘴内径为20mm，长度 为180mm；锐孔孔径为6.2mm。丙烯氨混合气通过流体分布器到达每根支管尾端喷嘴处，用热电偶测量各支管末端喷嘴处丙烯氨混合气温度，其中流体分布器内混合气最高点温度为丙烯氨混合气在行进长度最长支管的尾端喷嘴处的温度为282℃。
实施例3
丙烯氨氧化流化床反应器直径为15米，采用中国石化上海石油化工研究院SANC系列丙烯腈催化剂用于生产丙烯腈，反应装置满负荷运行，原料气配比C 3H 6∶NH 3∶空气为1∶1.2∶9.5，反应温度435℃，反应压力为55KPa，丙烯氨混合气流体入口温度控制为80℃。流体分布器采用图6的形式，材质为碳钢，分布器设有1根主管，主管直径为φ650mm，设有44根支管，各自与主管相连，支管直径为φ100mm，支管间距离为690mm，支管相互平行或垂直，沿支管方向的喷嘴开孔距离为230mm，最长支管长度为7.45米设有96个喷嘴，最短支管长度为2.4米设有45个喷嘴，分布器喷嘴总数为3008个，喷嘴内径为20mm，长度为150mm；锐孔孔径为6.5mm。丙烯氨混合气通过流体分布器到达每根支管尾端喷嘴处，用热电偶测量各支管末端喷嘴处丙烯氨混合气温度，其中流体分布器内混合气最高点温度为丙烯氨混合气在行进长度最长支管的尾端喷嘴处的温度为298℃。
实施例4
丙烯氨氧化流化床反应器直径为20米，采用中国石化上海石油化工研究院SANC系列丙烯腈催化剂用于生产丙烯腈，反应装置满负荷运行，原料气配比C 3H 6∶NH 3∶空气为1∶1.2∶9.5，反应温度435℃，反应压力为55KPa，丙烯氨混合气流体入口温度控制为80℃。流体分布器采用图7的形式，材质为碳钢，分布器设有2根主管，主管直径为φ500mm，设有84根支管，各自与主管相连，支管直径为φ120mm，支管间距离为460mm，支管相互平行或垂直，沿支管方向的喷嘴开孔距离为230mm，最长支管长度为9.8米设有84个喷嘴，最短支管长度为2.9米设有20个喷嘴，喷嘴数为5740个，喷嘴内径为20mm，长度为150mm；锐孔孔径为6.6mm。丙烯氨混合气通过流体分布器到达每根支管尾端喷嘴处，根据模型的HTFS计算及现有的实验数据，其中流体分布器内混合气最高点温度为丙烯氨混合气在行进长度最长支管的尾端喷嘴处的温度为316℃。
实施例5
丙烯氨氧化流化床反应器直径为20米，采用中国石化上海石油化工研究院SANC系列丙烯腈催化剂用于生产丙烯腈，反应装置满负荷运行，原料气配 比C 3H 6∶NH 3∶空气为1∶1.2∶9.5，反应温度435℃，反应压力为55KPa，丙烯氨混合气流体入口温度控制为100℃。流体分布器采用图7的形式，且在支管同一截面处设有3个开孔，相邻平行支管之间的距离为750mm，相邻开孔间的孔间距250mm，材质为碳钢，分布器设有2根主管，主管直径为φ500mm，支管直径为φ130mm，支管数为52根，支管相互平行或垂直，最长支管长度为9.8米设有120个喷嘴，最短支管长度为4.3米设有43个喷嘴，喷嘴数为4880个，喷嘴内径为20mm，长度为150mm；锐孔孔径为6.5mm。丙烯氨混合气通过流体分布器到达每根支管尾端喷嘴处，根据模型的HTFS计算及现有的实验数据，其中流体分布器内混合气最高点温度为丙烯氨混合气在行进长度最长支管的尾端喷嘴处的温度为305℃。
比较例1
丙烯氨氧化流化床反应器直径为15米，采用中国石化上海石油化工研究院SANC系列丙烯腈催化剂用于生产丙烯腈，反应装置满负荷运行，原料气配比C 3H 6∶NH 3∶空气为1∶1.2∶9.5，反应温度435℃，反应压力为55KPa，丙烯氨混合气流体入口温度控制为80℃。流体分布器采用图3的形式，材质为碳钢，所示x管直径为φ500mm，y管直径为φ250mm，支管直径为φ100mm，支管数为66根，支管间距离为460mm，喷嘴开孔距离为230mm，；最长支管长度为7.45米设有64个喷嘴，最短支管长度为2.0米设有18个喷嘴，分布器喷嘴总数为3008个，喷嘴内径为20mm，长度为200mm；锐孔孔径为6.5mm。丙烯氨混合气通过流体分布器管线到达每根支管尾端喷嘴处，根据模型的HTFS计算及现有的实验数据，流体分布器内混合气最高温度为355℃。
比较例2
丙烯氨氧化流化床反应器直径为15米，采用中国石化上海石油化工研究院SANC系列丙烯腈催化剂用于生产丙烯腈，反应装置满负荷运行，原料气配比C 3H 6∶NH 3∶空气为1∶1.2∶9.5，反应温度435℃，反应压力为55KPa，丙烯氨混合气流体入口温度控制为80℃。流体分布器采用图2的形式，材质为碳钢，所示y管直径为φ250mm，支管直径为φ100mm，支管数为66根，支管间距离为460mm，喷嘴开孔距离为230mm，最长支管长度为7.45米设有64个喷嘴，最短支管长度为2.0米设有18个喷嘴，分布器喷嘴总数为3008个，喷嘴内径为20mm，长度为200mm；锐孔孔径为6.5mm。丙烯氨混合气通过流体分布器管线到达每根支管尾端喷嘴处，根据模型的HTFS计算及现有的实验数据，流体分布器内混合气最高温度为348℃。
在应用本发明的丙烯氨流体分布器的实施例1至4中，即使反应器直径远大于常规丙烯氨氧化反应器的直径时，流体分布器任意一处的丙烯氨混合气的温度T i也低于350℃，即低于氨分解出活性氮原子的温度。相比之下，在比较例1和2中，使用现有技术流体分布器形式时，流体分布器内丙烯氨温度达到了氮化温度，使流体分布器存在氮化脆裂的风险。

Claims (17)

  1. 一种流体分布器，适合向容器内腔输送流体，所述流体分布器包括：
    一个或多个(优选1-8个，更优选1-4个或1-2个)流体输送主管，所述一个流体输送主管被构造为在将其中心线和/或中心线延长线首尾相接时，或者所述多个流体输送主管被构造为在将其各自的中心线和/或中心线延长线首尾相接时，构成闭合形状(优选基本上顺应所述容器外周轮廓的闭合形状，更优选基本上平面的闭合形状，更优选基本上平面的圆形、椭圆形或者多边形形状，更优选所述闭合形状与所述容器的中心线基本上垂直)，并且每一个所述流体输送主管具有至少一个(优选1-3个，更优选1个)流体入口，
    在每一个所述流体输送主管上设置的多个(优选5-100个，更优选5-50个)流体输送支管，每一个所述流体输送支管具有起始端和末端(所述末端为封闭、半封闭或开放结构，优选封闭结构)，所述起始端与所述流体输送主管连接且流体连通，并且所述起始端与所述末端限定了所述流体输送支管的长度L，
    在每一个所述流体输送支管上沿着所述流体输送支管的长度方向设置的多个(优选2-140个，更优选6-60个)开孔，
    在每一个所述流体输送支管上设置的连接部(优选的是，所述连接部的设置位置与所述末端相比更靠近所述起始端，更优选的是，所述连接部的所述设置位置与所述起始端沿着所述流体输送支管长度方向的距离为所述流体输送支管长度L的1/4以下、1/6以下、1/8以下、1/10以下或更小)，所述连接部被构造为在所述流体输送支管穿过所述容器的壳体而进入所述内腔之后，将所述流体输送支管连接(优选固定，更优选气密性固定)在所述壳体(优选所述壳体的外表面)上。
  2. 权利要求1所述的流体分布器，其中所述多个流体输送主管的内径彼此相同或不同(比如相同)，各自独立地为150-700mm(优选170-500mm)。
  3. 权利要求1所述的流体分布器，其中在每一个所述流体输送支管上，所述多个开孔沿着所述流体输送支管的长度方向设置(比如等间距或不等间距设置，更优选任意相邻两个所述开孔之间的距离D1彼此相同或不同，各自独立地为125-375mm(优选175-250mm))在所述流体输送支管的从所述连接部至所述末端的管段(称为内管段)上。
  4. 权利要求1所述的流体分布器，其中至少一个所述流体输送支管的内 管段沿着从所述流体输送支管的连接部至末端的方向具有恒定或变化(比如逐渐加粗或逐渐变细)的内径，和/或，所述内管段的长度Li使得在所述流体输送支管穿过所述容器的壳体而进入所述内腔之后，所述内管段的中心线向所述内管段首尾两端方向的延长线与所述壳体的内表面产生两个交点，设所述两个交点之间的线段的长度为Ld，则0＜Li＜Ld，优选0.25Ld≤Li≤0.99Ld，优选0.40Ld≤Li＜0.99Ld，更优选0.40Ld≤Li＜0.50Ld。
  5. 权利要求1所述的流体分布器，其中在每一个所述流体输送主管上，将所述多个流体输送支管分为一组或多组(多组比如2组以上，特别是2-8组、2-6组或2-4组)，则在任意一组流体输送支管中，i)任意相邻两个流体输送支管的中心线沿着同一个方向(称为该组流体输送支管的延伸方向)彼此相互平行或基本上平行，和/或，ii)任意相邻两个流体输送支管的内径彼此相同或不同(比如相同)，各自独立地为50-150mm(优选65-125mm)，和/或，iii)任意相邻两个流体输送支管的中心线的垂直距离D2彼此相同或不同(比如相同)，各自独立地为250-750mm(优选300-650mm，更优选350-550mm)，和/或，iv)所述D1与所述D2满足关系式：D1/D2≥0.3(优选D1/D2≥0.5)，和/或，v)相邻两个流体输送支管的末端两两相连而形成线段，该线段具有折线或直线的形状(优选设所述折线的最高点与最低点之间的高度差为H C，该组流体输送支管中最长的流体输送支管的长度为Lmax，则H C/Lmax≤44％，优选H C/Lmax≤37％，更优选H C/Lmax≤28％，更优选H C基本上为0，更优选所述直线与该组流体输送支管的延伸方向基本上垂直)，和/或，vi)该组流体输送支管中最长的流体输送支管的长度Lmax为5000-29000mm(优选5000-20000mm，优选5000-10000mm，更优选6000-10000mm)。
  6. 权利要求1所述的流体分布器，其中在每一个所述流体输送主管上，将所述多个流体输送支管分为一组或多组(多组比如2组以上，特别是2-8组、2-6组或2-4组)，或者将所述流体分布器的所有流体输送支管分为一组或多组(多组比如2组以上，特别是2-8组、2-6组或2-4组)，则在所述多组流体输送支管之间，i)一组流体输送支管与另一组流体输送支管的延伸方向彼此形成角度(优选彼此相互平行或彼此相互垂直)，和/或，ii)一组流体输送支管在所述闭合形状上的投影与另一组流体输送支管在所述闭合形状上的投影不重叠，优选所述流体分布器包含的全部组的流体输送支管在所述闭合形状上的投影面积之和At小于所述闭合形状的面积Ac，优选At/Ac为75％以上，更优选At/Ac为80％以上，更优选At/Ac为90％以上。
  7. 权利要求1所述的流体分布器，其中每一个所述流体输送支管的中心线(基本上)是直线。
  8. 权利要求1所述的流体分布器，其中在每一个所述流体输送支管上，所述多个开孔彼此相同或不同(比如相同)，各自独立地具有选自圆形、椭圆形、正方形、长方形、梯形和菱形的外周形状，和/或，所述多个开孔彼此相同或不同(比如相同)，各自独立地具有3-10mm，(优选4.5-8.5mm，更优选5.0-7.5mm)的等效圆直径。
  9. 权利要求1所述的流体分布器，其中在至少一个所述流体输送支管上，在所述流体输送支管的从连接部至起始端的管段(称为外管段)上设置流体流量控制器(优选流体流量控制阀)。
  10. 权利要求1所述的流体分布器，其中所述连接部被构造为具有环绕所述流体输送支管的形状，优选具有法兰形状，或者所述闭合形状的直径为5.5-32.0米(优选6.0-23.0米，更优选11.0-23.0米或者13.0-23.0米)。
  11. 权利要求1所述的流体分布器，还包括环绕所述开孔设置的喷嘴。
  12. 权利要求1所述的流体分布器，其中所述容器为流化床反应器，所述反应器的内腔直径为5-29米(优选5-20米，更优选10-20米或者12-20米)，并且所述流体是含氮流体或含氨流体，特别是含氮气体或者含氨气体，特别是烯氨混合气，更特别是丙烯氨混合气。
  13. 一种流体分布器，是用于使丙烯氨混合气在流化床反应器内部均匀分布的进料分布器，该进料分布器包括：
    一个以上分布器入口；
    多个输送支管，该多个输送支管分别连接至所述分布器入口并分别与所述分布器入口流体连通，并且该多个输送支管从所述分布器入口向反应器内部延伸；
    开孔，所述开孔设置在所述输送支管上；以及
    喷嘴，该喷嘴围绕相应的开孔设置在所述输送支管上，并且与所述相应的开孔同轴，以使丙烯氨混合气经过所述分布器入口、所述输送支管、所述开孔和所述喷嘴，最终在反应器内部均匀分布，
    还包括一个以上进料主管，该进料主管设置在所述流化床反应器外部，并且该进料主管分别连接至所述一个以上分布器入口和所述多个输送支管，并与所述一个以上进料分布器入口和所述多个输送支管流体连通。
  14. 一种使用权利要求1所述的流体分布器向容器内腔输送流体的方法， 包括向所述流体分布器的所述至少一个流体入口输送流体(优选气体，更优选丙烯氨混合气)，使所述流体至少经过所述流体输送主管、所述流体输送支管和所述开孔进入所述内腔的步骤。
  15. 权利要求1或13所述的流体分布器作为进料分布器向氨氧化反应器的内腔输送反应原料(优选丙烯氨混合气)的用途。
  16. 一种反应装置，包括反应器和权利要求1或13所述的流体分布器，其中所述反应器至少具有壳体、设置在所述壳体上的多个通孔、以及由所述壳体的内表面限定的内腔，所述通孔在数量和设置位置上与所述流体分布器的流体输送支管具有一一对应关系，由此使得每一个流体输送支管都能够穿过与其对应的一个通孔而进入所述内腔，并且所述流体输送支管穿过所述通孔之后通过所述流体输送支管的连接部气密性固定在所述壳体的外表面上。
  17. 一种丙烯腈的制造方法，包括使用权利要求1或13所述的流体分布器或者使用权利要求14所述的方法向反应器(优选流化床反应器)内腔输送丙烯氨混合气，并向所述反应器内腔输送含氧气体(优选空气)，或者在权利要求16所述的反应装置中，使丙烯发生氨氧化反应而生成丙烯腈的步骤。
PCT/CN2018/114771 2017-11-14 2018-11-09 一种流体分布器、反应装置及其应用 WO2019096065A1 (zh)

Priority Applications (7)

Application Number Priority Date Filing Date Title
AU2018369015A AU2018369015B2 (en) 2017-11-14 2018-11-09 Fluid distributor, reaction device, and application thereof
US16/763,917 US11571673B2 (en) 2017-11-14 2018-11-09 Fluid distributor, reaction device and application thereof
KR1020207017032A KR102536047B1 (ko) 2017-11-14 2018-11-09 유체 분배기, 반응 장치 및 이의 적용
BR112020009630-0A BR112020009630B1 (pt) 2017-11-14 2018-11-09 Distribuidor de fluido adaptado para transportar um fluido para uma cavidade interna de recipiente, método de uso do distribuidor de fluido, uso de um distribuidor de fluido, aparelho de reação compreendendo um reator e o distribuidor de fluido e processo para produção de acrilonitrila
JP2020526550A JP7216087B2 (ja) 2017-11-14 2018-11-09 流体分配器、反応装置及びその適用
EA202091142A EA202091142A1 (ru) 2017-11-14 2018-11-09 Распределитель текучей среды, реакционное устройство и их применение
EP18879404.4A EP3711851A4 (en) 2017-11-14 2018-11-09 FLUID DISPENSER, REACTION DEVICE AND THEIR APPLICATION

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201711128526 2017-11-14
CN201711128526.8 2017-11-14

Publications (1)

Publication Number Publication Date
WO2019096065A1 true WO2019096065A1 (zh) 2019-05-23

Family

ID=66496352

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2018/114771 WO2019096065A1 (zh) 2017-11-14 2018-11-09 一种流体分布器、反应装置及其应用

Country Status (9)

Country Link
US (1) US11571673B2 (zh)
EP (1) EP3711851A4 (zh)
JP (1) JP7216087B2 (zh)
KR (1) KR102536047B1 (zh)
CN (1) CN109772236B (zh)
AU (1) AU2018369015B2 (zh)
EA (1) EA202091142A1 (zh)
TW (1) TWI800556B (zh)
WO (1) WO2019096065A1 (zh)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102019115174A1 (de) * 2019-06-05 2020-12-10 Lübbers Anlagen- und Umwelttechnik GmbH Verfahren zum Herstellen eines Lochbleches, Lochblech, Formteil und Aufbereitungsvorrichtung
CN115337872B (zh) * 2021-04-09 2023-09-29 中国石油化工股份有限公司 一种撤热水管、流化床反应器及其在丙烯腈制造中的应用
CN113731301A (zh) * 2021-08-05 2021-12-03 中石化宁波工程有限公司 一种环管可拆卸两级分布器
CN113634198A (zh) * 2021-10-19 2021-11-12 凯莱英医药集团（天津）股份有限公司 多位点流体分布装置和连续流硝化反应装置
CN115161062A (zh) * 2022-03-23 2022-10-11 中国石油化工股份有限公司 一种气液混合分布器
CN115161063A (zh) * 2022-03-23 2022-10-11 中国石油化工股份有限公司 一种分布设备
CN114602560A (zh) * 2022-03-23 2022-06-10 中国石油化工股份有限公司 一种分布系统
CN115161061A (zh) * 2022-03-23 2022-10-11 中国石油化工股份有限公司 一种分布装置

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3704690A (en) 1970-02-19 1972-12-05 Uhde Gmbh Friedrich High pressure heat exchanger for ammonia gas synthesis plants
CN1089596A (zh) 1992-10-14 1994-07-20 标准石油公司 制丙烯腈过程中清除氮化的方法
US5605654A (en) * 1993-08-04 1997-02-25 Koch Engineering Company, Inc. Method and apparatus to improve vapor distribution in mass transfer and heat exchange columns
CN202387443U (zh) * 2011-11-04 2012-08-22 联化科技股份有限公司 卤代芳烃氨氧化流化床反应器中的分布器
CN203955188U (zh) * 2014-03-31 2014-11-26 英尼奥斯欧洲股份公司 用于氨氧化反应器的进料分布器
CN205182739U (zh) * 2015-12-04 2016-04-27 抚顺东科精细化工有限公司 一种反应釜进料分布器
CN106315526A (zh) * 2016-08-23 2017-01-11 福建梭罗复合材料研究有限公司 具有双重循环加气装置的氨氧化炉分布器
CN207576359U (zh) * 2017-11-14 2018-07-06 中国石油化工股份有限公司 用于丙烯氨氧化反应器的进料分布器

Family Cites Families (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1382991A (en) * 1971-01-12 1975-02-05 Ucb Sa Process for carrying out chemical reactions in a fluidised bed
CH667704A5 (de) * 1986-02-07 1988-10-31 Sulzer Ag Verfahren und vorrichtung zur gleichmaessigen verteilung einer fluessigkeit auf eine querschnittsflaeche.
US4875996A (en) * 1986-02-28 1989-10-24 Chevron Research Company Method for liquid feed dispersion in fluid catalytic cracking systems
JPH07155536A (ja) * 1993-12-01 1995-06-20 Babcock Hitachi Kk 湿式排煙脱硫装置
KR101363824B1 (ko) 2004-09-02 2014-02-17 그루포 페트로테멕스 에스.에이. 데 씨.브이. 최적화된 액상 산화를 위한 기포탑 반응기
US7393973B2 (en) * 2006-03-01 2008-07-01 Eastman Chemical Company Polycarboxylic acid production system with enhanced residence time distribution for oxidative digestion
US20080193340A1 (en) 2007-02-09 2008-08-14 Cocco Raymond A Fluidized bed sparger
CN201154303Y (zh) * 2008-02-01 2008-11-26 中国石化集团洛阳石油化工工程公司 一种气体进料分布器
US8092755B2 (en) * 2009-04-06 2012-01-10 Lummus Technology Inc. Devices for injection of gaseous streams into a bed of fluidized solids
EP2822678B1 (en) * 2012-03-07 2017-07-19 GE Healthcare Bio-Sciences Corp. Disposable valve and flexible containers for pressurized bioreactors
JP6272867B2 (ja) 2012-08-29 2018-01-31 ヘムロック・セミコンダクター・オペレーションズ・エルエルシー 先細り流動床反応器及びその使用のためのプロセス
DE102013208071A1 (de) 2013-05-02 2014-11-06 Wacker Chemie Ag Wirbelschichtreaktor und Verfahren zur Herstellung von granularem Polysilicium
CN104941521A (zh) * 2014-03-31 2015-09-30 英尼奥斯欧洲股份公司 用于氨氧化反应器的进料分布器设计
CN104941523B (zh) * 2014-03-31 2019-04-02 英尼奥斯欧洲股份公司 用于氨氧化反应器的进料分布器设计
CN204208540U (zh) * 2014-10-09 2015-03-18 青海宜化化工有限责任公司 一种PVC生产过程中基于电石气的C2H3Cl合成装置
CN106955644A (zh) 2016-01-08 2017-07-18 中国石油化工股份有限公司 用于氨化氧化反应的流化床反应器的进料分布器
CN106492712A (zh) 2015-09-06 2017-03-15 中国石油化工股份有限公司 进料分布器
TWI803448B (zh) 2015-09-02 2023-06-01 大陸商中國石油化工科技開發有限公司 生產丙烯腈的反應器和方法
CN205868196U (zh) 2015-09-06 2017-01-11 中国石油化工股份有限公司 进料分布器

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3704690A (en) 1970-02-19 1972-12-05 Uhde Gmbh Friedrich High pressure heat exchanger for ammonia gas synthesis plants
CN1089596A (zh) 1992-10-14 1994-07-20 标准石油公司 制丙烯腈过程中清除氮化的方法
US5605654A (en) * 1993-08-04 1997-02-25 Koch Engineering Company, Inc. Method and apparatus to improve vapor distribution in mass transfer and heat exchange columns
CN202387443U (zh) * 2011-11-04 2012-08-22 联化科技股份有限公司 卤代芳烃氨氧化流化床反应器中的分布器
CN203955188U (zh) * 2014-03-31 2014-11-26 英尼奥斯欧洲股份公司 用于氨氧化反应器的进料分布器
CN205182739U (zh) * 2015-12-04 2016-04-27 抚顺东科精细化工有限公司 一种反应釜进料分布器
CN106315526A (zh) * 2016-08-23 2017-01-11 福建梭罗复合材料研究有限公司 具有双重循环加气装置的氨氧化炉分布器
CN207576359U (zh) * 2017-11-14 2018-07-06 中国石油化工股份有限公司 用于丙烯氨氧化反应器的进料分布器

Also Published As

Publication number Publication date
CN109772236B (zh) 2022-08-12
EP3711851A4 (en) 2021-09-22
KR20200085863A (ko) 2020-07-15
AU2018369015A1 (en) 2020-06-18
TWI800556B (zh) 2023-05-01
JP7216087B2 (ja) 2023-01-31
EP3711851A1 (en) 2020-09-23
CN109772236A (zh) 2019-05-21
AU2018369015B2 (en) 2023-10-19
EA202091142A1 (ru) 2020-10-09
BR112020009630A2 (pt) 2021-01-12
US11571673B2 (en) 2023-02-07
TW201925672A (zh) 2019-07-01
KR102536047B1 (ko) 2023-05-23
JP2021502895A (ja) 2021-02-04
US20200368707A1 (en) 2020-11-26

Similar Documents

Publication Publication Date Title
WO2019096065A1 (zh) 一种流体分布器、反应装置及其应用
TWI676613B (zh) 用於氨氧化反應器的進料分佈器設計
BR112012008022B1 (pt) Dispositivo de distribuição de fluxo, e, bandeja de distribuição
CN106955644A (zh) 用于氨化氧化反应的流化床反应器的进料分布器
TWI824691B (zh) 半導體熱處理設備的氣體噴射裝置及半導體熱處理設備
TWI451909B (zh) Gas phase reaction method
CN205797156U (zh) 用于氨化氧化反应的流化床反应器的进料分布器
CN207463190U (zh) 气体分布器以及三相浆态床反应器
WO2019095531A1 (zh) 用于丙烯氨氧化反应器的原料气进料系统
CN104084065A (zh) 乙烯和氧气混合的方法
TWI803448B (zh) 生產丙烯腈的反應器和方法
CN207576359U (zh) 用于丙烯氨氧化反应器的进料分布器
CN204952862U (zh) 一种浆态床反应器进料分布器
WO2014148546A1 (ja) 燃焼バーナ、バーナ装置、及び原料粉体加熱方法
BR112020009630B1 (pt) Distribuidor de fluido adaptado para transportar um fluido para uma cavidade interna de recipiente, método de uso do distribuidor de fluido, uso de um distribuidor de fluido, aparelho de reação compreendendo um reator e o distribuidor de fluido e processo para produção de acrilonitrila
CN208554114U (zh) 一种板式反应管及板式反应器
JP2023503117A (ja) ガス分配板、流動化装置及び反応方法
EA044032B1 (ru) Распределитель текучей среды, реакционное устройство и их применение
CN217940128U (zh) 抽吸式旋流混合分布器及气液混合分布装置
US20230364575A1 (en) Chemical feed distributors and methods of using the same
CN204583145U (zh) 一种用于冷激型反应器的多流体防堵喷射冷激装置
JP2023544694A (ja) 化学原料分配器及びそれを使用する方法
CN101922611A (zh) 气体输送装置以及干法刻蚀装置
CN103305255A (zh) 一种内凸扰流管

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 18879404

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: 2020526550

Country of ref document: JP

Kind code of ref document: A

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 20207017032

Country of ref document: KR

Kind code of ref document: A

WWE Wipo information: entry into national phase

Ref document number: 139950140003002519

Country of ref document: IR

ENP Entry into the national phase

Ref document number: 2018369015

Country of ref document: AU

Date of ref document: 20181109

Kind code of ref document: A

ENP Entry into the national phase

Ref document number: 2018879404

Country of ref document: EP

Effective date: 20200615

REG Reference to national code

Ref country code: BR

Ref legal event code: B01A

Ref document number: 112020009630

Country of ref document: BR

REG Reference to national code

Ref country code: BR

Ref legal event code: B01E

Ref document number: 112020009630

Country of ref document: BR

Free format text: APRESENTE, NO PRAZO DE 60 (SESSENTA) DIAS, NOVAS FOLHAS DE DESENHOS COM O TEXTO TRADUZIDO PARA O PORTUGUES, ADAPTADO A NORMA VIGENTE, CONFORME DETERMINA O ART. 7O DA RESOLUCAO INPI PR NO 77/2013 DE 18/03/2013.

ENP Entry into the national phase

Ref document number: 112020009630

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20200514

WWE Wipo information: entry into national phase

Ref document number: 520411980

Country of ref document: SA

WWE Wipo information: entry into national phase

Ref document number: 520411980

Country of ref document: SA