CN100355494C - Mixing device for two-phase concurrent vessels - Google Patents
Mixing device for two-phase concurrent vessels Download PDFInfo
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- CN100355494C CN100355494C CNB2003801073442A CN200380107344A CN100355494C CN 100355494 C CN100355494 C CN 100355494C CN B2003801073442 A CNB2003801073442 A CN B2003801073442A CN 200380107344 A CN200380107344 A CN 200380107344A CN 100355494 C CN100355494 C CN 100355494C
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/16—Fractionating columns in which vapour bubbles through liquid
- B01D3/18—Fractionating columns in which vapour bubbles through liquid with horizontal bubble plates
- B01D3/20—Bubble caps; Risers for vapour; Discharge pipes for liquid
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
- B01F23/232—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles
- B01F23/2323—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles by circulating the flow in guiding constructions or conduits
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
- B01F25/40—Static mixers
- B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
- B01F25/421—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions by moving the components in a convoluted or labyrinthine path
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
- B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0492—Feeding reactive fluids
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/002—Apparatus for fixed bed hydrotreatment processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00327—Controlling the temperature by direct heat exchange
- B01J2208/00336—Controlling the temperature by direct heat exchange adding a temperature modifying medium to the reactants
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00823—Mixing elements
- B01J2208/00831—Stationary elements
- B01J2208/00849—Stationary elements outside the bed, e.g. baffles
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/00929—Provided with baffles
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
- B01J2219/332—Details relating to the flow of the phases
- B01J2219/3322—Co-current flow
Abstract
Vapor and liquid flows concurrently through a vertical vessel in a catalytic reactor (1). A horizontal flow obstructing mixing box (8) is located within the vessel and forces the vapor and liquid to pass in a vertical direction through one or more entrances to the horizontal mixing box. The mixing box consists of circular top (13) and bottom (14) walls and a cylindrical side wall (15). Inside the mixing box vertical flow baffles (18, 19, 20) are provided. These flow baffles form one or more mixing orifices (21, 22). The entire process stream is flowing through each mixing orifice at high flow velocity. Each mixing orifice is followed by a tee where the process stream is divided into two tower velocity streams. In the transition from high flow velocity in the mixing orifice to lower flow velocity in the divided streams, turbulent flow conditions are generated. In the lower velocity divided streams hold-up time is provided to allow for heat and mass transfer. The flow inside the mixing box is mainly in the horizontal plane. The outlet stream from the mixer equilibrated regarding temperature and chemical composition.
Description
Technical field
The present invention relates to a kind of in container the mixing arrangement of mist or steam and liquid, liquid and vapor capacity concurrent flow in this device.The purpose of this device is to make the temperature and the chemical composition of the outlet mixture that leaves this device reach balance.The present invention is suitable for but is not limited to, and between two contiguous beds, rich hydrogen processing gas of heat and hot hydrocarbon liquid is mixed with the cool stream thigh in a kind of hydroprocessing reactor such as hydrotreating reactor or hydrocracking reactor.The invention further relates to and a kind ofly comprise the steam of the catalytic reactor of aforementioned mixing arrangement, a kind of concurrent flow in this reactor and the mixed method of liquid, and a kind of product that adopts described method preparation.
Background technology
The mixing arrangement of a large amount of two-phases and fluid capacitance device is disclosed in existing document and the patent.Most of device belongs to a kind of in following six kinds:
The 1st kind is provided in the turbine mixer collecting column plate and have the charging chute:
United States Patent (USP) 3,541,000 has recorded and narrated an example of this mixer design.This blender is made up of the collection column plate 6 of level.This collection column plate has a plurality of skewed slots 32/34.Cross these charging chutes from whole steams and liquid process streams high velocity stream that top beds flows down.Below the collection column plate is annular blending bin 8.The outlet nozzle of groove is provided with horizontal member, can form eddy current and flow in annular blending bin.Fluid is by interior weir 12, afterwards vertically downward by centre bore 10 then.In the exit of centre bore 10, add cooling fluid by the perforated pipe distributor in many leg supports equipment 30.Be provided with one below the blender and be used for the distribution column plate 14 that liquid crude is distributed.Column plate 14 also can be as the shock plate of the high-velocity fluid that flows out from centre bore 10.Rough segmentation join column plate below be provided with one and be used for the final distribution column plate 4 that distributes of liquid.
Other examples of vortex mixer:
United States Patent (USP) 4,836,989 disclose one with United States Patent (USP) 3,541,000 in the similar vortex mixer of blender.But in order to improve cooling fluid with the steam that flows down from top beds and the mixing of liquid, quench fluid is by the upstream of collecting column plate 12 but not the perforated pipe distributor 13 in downstream adds.
United States Patent (USP) 5,837,208,5,989,502 and WO0248286 in the similar blender of blender in 989 is disclosed and United States Patent (USP) 4,836.
The 2nd kind has radially/the whirlpool performance chamber mixer of horizontal inlet flow:United States Patent (USP) 3,353 has been recorded and narrated an example of this mixer design in 924.This blender is formed by collecting column plate 6.Cooling medium adds by the porous pipe ring 11 of collecting the column plate top.Steam that flows out from the beds 3 of blender top and liquid and cooling fluid enter in the whirlpool case 7 by a plurality of imports 8.Different with aforementioned turbine mixer design, fluid mainly is to enter the whirlpool performance chamber mixer by import in the horizontal direction/radially.Import is provided with blade 9, and this blade can make the fluid in the whirlpool case 7 do eddy motion.Fluid flows out the whirlpool case by centre bore 13a.The centre bore below, porose shock plate is provided with vertical baffle 16.
Other examples of whirlpool performance chamber mixer:
United States Patent (USP) 3,787,189 disclose with United States Patent (USP) 3,353, the similar whirlpool performance chamber mixer of blender in 924.But the intake channel of this whirlpool case is different with it with the design of blade, and shock plate 23 atresias of centre bore 20 belows.Collect column plate 18 belows and be provided with blade 22, can make the fluid vortex motion flow out blender, substituted the vertical plate washer that the mixer outlet place radially is provided with.
United States Patent (USP) 5,462 discloses with United States Patent (USP) 3,353 in 719,924 similar whirlpool performance chamber mixers.Steam and liquid at first flow through the radial hole in the cylindrical blind 24, flow through blade 22 then, make it eddy motion in the whirlpool case.Fluid flows out the whirlpool case by centre bore 21, and enters second blending bin that is positioned under the collection column plate 20.In second blending bin, fluid flows out blender along flowing radially outward by the radial hole in the cylindrical wall 26.
The 3rd kind of bubble-cap blender:
United States Patent (USP) 5,152 discloses an example of this mixer design in 967.This blender is collected column plate 16 and one and downspout 17 overlapping bubble- caps 18 and 19 by one and is formed.This bubble-cap and downspout have determined that first mixes whirlpool chamber.The sidewall of bubble-cap 19 is provided with inclined open.When steam and liquid enter first whirlpool chamber by inclined open, form eddy motion.Fluid at first upwards flows through the top edge of downspout 17, flows downward by the centre bore in downspout and the column plate 6 then.This blender also is provided with second whirlpool chamber below first whirlpool chamber that inner radial flows.
Other examples of bubble-cap blender:
United States Patent (USP) 6,183,702 B1 disclose another bubble-cap blender.This blender is formed by collecting column plate 1125, and this collection column plate can remain on certain liquid level.This collection column plate is provided with vertical plate washer 1130, can promote liquid eddy motion on column plate 1125.Can further strengthen eddy motion from the cooling fluid of managing ejection 1140.Collecting on the column plate, the bubble-cap blender is formed with the overlapping elongated cylindrical cover 1150 of cylindrical downspout 1165 by one, and this bubble-cap blender is arranged on above the centre bore in the column plate 1125.Be provided with half-spiral plate washer 1155 in the annular space between bubble-cap and downspout.Steam enters into this annular space by the slit in the cylindrical wall of bubble-cap 1150.Like this, steam is being carried the liquid rising secretly and is being entered annular space, and steam and liquid upwards flow by annular space.In this annular space, form eddy motion by plate washer 1155.
Steam and liquid flow downward along the passage in downspout and the collection column plate 1125.
United States Patent (USP) 3,824,080,3,824,081 and 5,403,560 disclose other examples of bubble-cap blender.
The 4th kind: the blender that steam and liquid mix separately
European patent 716,881 discloses an example of this mixer design.This blender is made up of the collection column plate 20 that has centre bore 30.Above centre bore, be provided with the steam whirlpool case 100/55 that is used for mixed vapour.This steam whirlpool case is provided with porose 95 and swirling device 105.Collect column plate 20 and be provided with other openings 40 that are used for liquid flow.Opening links to each other with passage 65, makes the center line of flow direction reactor.In the normal running, collect column plate 20 and remain on the certain liquid height, steam enters in the steam whirlpool case blender 100/55 and by centre bore 30 and flows out, and liquid passes through from the bypass of whirlpool performance chamber mixer by parallel fluid passage 40/65.The blender below is provided with a thick distributor/shock plate 90.
United States Patent (USP) 5,935 discloses other examples of the blender of independent mixed vapour and liquid in 413
The 5th kind: the plate washer performance chamber mixer of perpendicular flow
United States Patent (USP) 4,233 discloses an example of this mixer design in 269.This blender is made up of charging aperture 12, and steam and liquid can enter blender by this charging aperture.The fluid that enters from charging aperture flows through two circular annularly flow districts of mixing mouth and being formed by disk 34 that formed by annular column plate 32 and 36.
The 6th kind: the plate washer performance chamber mixer of bottom horizontal flow sheet
United States Patent (USP) 5,690,896 disclose an example of this mixer design.This blender can be used as a part of catalyst support system.Steam and liquid are collected in the annular collection trough 24.Cooling fluid joins in the annular collection trough by cooling tube 22 and 23.Steam and liquid flow in the blending bin 30 that is arranged between brace summer 14 and 15 by annular collection trough.All process-stream enters in the blender case at import 36 places.This blender case is made up of independent flow channel, and flow direction can 360 ° of rotations.Fluid through after 360 ° of rotations, flows out by centre bore 37 in blender.
United States Patent (USP) 3,705,016 discloses a blender of being made up of the screen 11/12 that is arranged on collection column plate and the catalyst support column plate 8.This screen is covered by inert support material 7.Cooling fluid injects the beds of column plate 8 tops.Steam and liquid can pass through screen 11/12, but inert material can not pass through.Steam and liquid are by after shielding, and vertical current is crossed the centre bore of collecting in the column plate 8.Below collecting column plate a horizontal blending bin is set, this blending bin is made up of with vertical plate washer 20,21,22 and 23 base plate 16.The fluid that goes out from the center orifice flow is divided into two horizontal flows earlier.Each stream thigh is divided into two streams again afterwards, finally forms four streams.In the exit of blender, two bursts of sides that are mixed into reactor cross section once more in four plumes, and two remaining stream thighs also are mixed into the opposite side of reactor cross section once more.At last, by porous plate 25 distribution steam and fluids.
United States Patent (USP) 3,977,834 have provided another example of the plate washer performance chamber mixer of bottom horizontal flow sheet.The blender of being made up of a plurality of parallel mixing casees 13 is disclosed.Blending bin is arranged between the catalyst brace summer 7, in the upstream of blending bin, adds cooling fluid by pipe 11 between this beam.
The blender performance is discussed in the background technology
Pressure drop is the combined drive power in all mixer design of mentioning.But for example in hydrotreatment and hydrocracking unit operations, the pressure drop meeting that increases blender causes cost to increase.As: the initial cost of recycle gas compressor increases, and the required additional shaft power of recycle gas compressor increases running cost.In the two-phase blender, can realize that the standard of evenly mixing and formation balance outlet mixture is as follows in given blender pressure drop:
A) blender need have flow restriction district or high flow rate mixing mouth.High flow rate can make liquid dispersion enter in the steam, perhaps makes steam disperse to enter in the liquid.Dispersion flows has increased interfacial area and has helped conducting heat and mass transfer.High flow rate has also increased the degree of turbulent flow, and turbulent flow also produces good mixing in addition.High flow rate further produces higher mass transfer and heat transfer coefficient, helps heat transfer and mass transfer between the liquid and gas.
B) all process-stream compiles and is mixing a mouthful contact.Owing to can't contact between the concurrent flow, and can not realize the temperature and the Compositional balance of concurrent flow thus, the parallel channels that therefore passes blender is unsuitable.
C) blender has low flow velocity zone in a mixing mouthful downstream, makes steam and liquid keep certain time of staying, creates turbulent-flow conditions for changing from high flow rate to low flow velocity.Heat transfer and mass transfer need the time of staying.Mix mutually and need turbulent-flow conditions.
D), must reach the reasonable distribution and the diffusion of the fluid that passes reactor cross section at the mixer outlet place.Even blender below is provided with the distribution column plate, still need distribute at the mixer outlet place, with excessive gradient of liquid level on the column plate that prevents to distribute along the particular fluid of reactor cross section.As, all liquid is just inapplicable in the mixer design that reactor one effluent goes out.
In addition, the height of whole blender is also very important.Blender is compact as much as possible to reduce the height requirement of reactor/vessel.In hydrotreatment or hydrocracking reactor, the space that blender occupies can not be had active catalyst utilization.For reactant being changed into the expection product, need the total measurement (volume) of given catalyst.So the space that blender occupies has increased the size of required reactor/highly.Hydrocracking reactor is designed to have the high partial pressures of hydrogen and hydrogen sulfide simultaneously in 200 crust and 450 ℃ of operations.Reactor is usually designed to the internal diameter that has up to 5 meters.Based on the strict design condition, hydrocracking reactor will have a very thick shell, and this shell is usually by the 1.0 molybdenum steel manufacturings of 2.25 chromium and have the austenite stainless steel lining, as 347SS.The cost of every meter reactor straight flange is up to megabuck (2002).Therefore, if adopt compacter mixer design, there is bigger potential saving space.
First kind of blender has the turbine mixer of charging chute, is the mixer design that the most generally adopts during present industrial hydrotreatment and hydrocracking are used.The major part of blender pressure drop is used for the charging chute.But these grooves show as parallel flow channels.Therefore do not arrive the requirement of standard B.In addition, owing to irregular collection column plate or other fabrication tolerance reason, the steam of each inlet channel and liquid distribution situation may be relatively poor.Most of liquid is by some grooves, and most of steam is then by other grooves.In this case, steam just can not contact in the charging chute effectively with liquid.The time of staying of fluid in donought can't make fluid carry out the whole process rotation of one 360 degree usually, and therefore the fluid that flows out from different slots, different reactor side can't thoroughly mix forever.Flow velocity in the charging chute is too high usually, and can't resemble the fluid separation applications that makes the initial requirement in the donought.All process-stream contacts in the centre bore of blender, and fluid immediately distributes along reactor cross section then.The unqualified volume in centre bore downstream is used to produce the time of mass transfer and heat transfer.So standard C does not satisfy yet.First kind of blender is the blender of relative compact.
Second kind of blender has radially/the whirlpool performance chamber mixer of horizontal inlet flow, and the major part of pressure drop is being born in the import of vortex chamber.These imports show as parallel flow channels.Therefore can't reach the requirement of standard B.The same with first kind of blender, all process-stream contacts at centre bore.But afterwards, fluid all distributes along reactor cross section immediately.The unqualified volume in centre bore downstream is used to produce the time of mass transfer and heat transfer.So standard C does not satisfy yet.
With first kind the same with second kind of blender, the third blender, bubble-cap blender do not reach the requirement of standard B and C yet.
In the 4th kind of blender, the independent blender that mixes of steam and liquid, the blender pressure drop partly is used for premixer, the steam and the liquid that are used for the premixed separation and also flow.Each single-phase premixer itself also comprises the concurrent flow passage, as parallel feed chute or blade.Therefore this kind blender does not satisfy the requirement of standard B yet.In the European patent 716,881, just there is not two-phase to mix mouth, so do not satisfy the requirement of standard A at all yet.
The 5th kind, the plate washer performance chamber mixer of perpendicular flow, United States Patent (USP) 4,223,269 disclose the fabulous design of mixed performance and can satisfy the requirement of aforementioned A to all standards of D., the height of the 5th kind of blender is too high, has occupied a lot of volumes of reactor/vessel.
The 6th kind of blender, the plate washer performance chamber mixer of bottom horizontal flow sheet, United States Patent (USP) 3,705,016 and 3,977,834 disclose the mixer design that has a plurality of parallel flow channels, do not satisfy the requirement of standard B.Because all process-stream can't mix contact in the mouth at one, United States Patent (USP) 3,977,834 do not reach the requirement of standard A yet.In addition, because liquid flows out blender with inhomogeneous pattern, United States Patent (USP) 3,705,016 does not satisfy the requirement of standard D.For the 6th kind of blender, United States Patent (USP) 5,690,896 disclose a reasonably blender preferably.But this blender does not satisfy the requirement of standard C.After a whole process-stream was introduced the mixing mouth together, the downstream of mixing mouth did not have enough time of staying to be used for mass transfer and heat transfer.Because fluid only enters centre gangway from a side, does not also satisfy the requirement of standard D.The fluid skewness at final mixer outlet place.
Summary of the invention
The present invention relates to a kind of in the container of steam and liquid concurrent flow the mixing arrangement of mist or steam and liquid.The invention belongs to aforesaid the 6th kind of blender, the plate washer performance chamber mixer of bottom horizontal flow sheet.
Main purpose of the present invention provides this mixing, makes it have the loss of less relatively reactor volume and has relatively low energy requirement.
According to the present invention, above and other objects of the present invention and beneficial effect of the present invention is following obtains:
A kind of mixing arrangement that is used for catalytic reactor is provided, this mixing arrangement is arranged between upper catalyst bed layer and the lower catalyst bed layer, be used for mixing gas or steam and the liquid of described reactor vessel by the beds concurrent flow of described mutual superposition, described mixing arrangement forms the flow channel by described mixing arrangement, be used for described steam and liquid and flow to described subordinate beds from described upper catalyst bed layer, vice versa, and described flow channel comprises:
The import of at least one described mixing arrangement;
The outlet of at least one described mixing arrangement;
Along described flow channel continuously arranged first and at least one second mixing mouth or passage, described first and described at least one second mix mouthful be provided with and can make basically all that liquid and vapor mixing stream flow through each described mixings mouth, this circulation area of mixing mouth is relevant with the flow velocity of described mixed flow, so that in mixing mouthful the fricton-tight two-phase flow velocity of described mixed flow be 3m/s to 15m/s, preferably be enough to make liquid dispersion in steam and/or steam be distributed in the liquid;
The flow channel part of a basic horizontal, extend and be arranged between described at least one import and described at least one outlet, so that the vertical dimension of mixing arrangement is as much as possible little, described basic horizontal flow channel part preferably extends to nearest described outlet from nearest described import.
Therefore, lose the effective interaction that has obtained under the minimum situation between liquid and steam at reactor volume.
The invention provides a kind of mixing arrangement that is used for catalytic reactor, this mixing arrangement is arranged between upper catalyst bed layer and the lower catalyst bed layer, be used for mixing gas or steam and the liquid of the vertical substantially container of described reactor by the beds concurrent flow of described mutual superposition, described mixing arrangement forms the flow channel by described mixing arrangement, be used for described steam and liquid and flow to described subordinate beds from described upper catalyst bed layer, vice versa, and described mixing arrangement comprises:
Be provided with at least one import top wall;
Be provided with at least one outlet base wall;
Between described top wall outer rim and base wall outer rim, extend the lateral wall that is provided with, be used between described top wall and described base wall, constituting an enclosure space;
The inner compartment wall, extend and be arranged between described top wall and the base wall, with described top wall, base wall and lateral wall constitute described flow channel together, and described partition walls along described flow channel formed in succession first and at least one second mix mouthful or passage, described first and described at least one second setting that mixes mouthful make basically all that the mixed flow of liquid and steam flows through each described mixings mouth, this circulation area of mixing mouth is relevant with the flow velocity of described mixed flow, so that in mixing mouthful the fricton-tight two-phase flow velocity of described mixed flow be 3m/s to 15m/s, preferably be enough to make liquid dispersion in steam and/or steam be distributed in the liquid;
The flow channel part of basic horizontal, constitute together with described top wall and base wall by described inner compartment wall, extend and be arranged between described at least one import and described at least one outlet, so that the vertical dimension of described mixing arrangement is as far as possible little, described basic horizontal flow channel part preferably extends to nearest described outlet from nearest described import.
In a specific embodiment, the invention provides a kind of horizontal blending bin of choked flow that is arranged between cylindrical reactor wall.This blending bin has one or more passages, makes the fluid of basic perpendicular flow flow to blender.This blending bin comprises the circular top wall of a level, the circular base wall of level, and a vertical cylinder wall, and this cylindrical wall can be used as the part of reactor wall.In order to make the height minimum of blending bin, the diameter of blending bin preferably approaches the internal diameter of reactor, or consistent with the internal diameter of reactor.In horizontal blending bin, be provided with the perpendicular flow plate washer.This perpendicular flow plate washer has formed and has mixed mouth, flows through this mixing mouth at these whole process-stream high flow rates.Be provided with a threeway behind this mixing mouth, process-stream can be divided into the effluent of two low flow velocitys.Horizontal blending bin is made up of the mixing mouth that a series of back are provided with threeway, and at first fluid mixes with high flow rate in the first mobile restricted area, is divided into two low flow velocitys stream thighs by first threeway then, mix once more with high flow rate in the second flow restriction district afterwards, or the like.In mixing mouth, liquid is dispersed in the steam, for mass transfer provides bigger interfacial area with conducting heat.High flow rate in mixing mouthful has also produced higher heat transfer and mass tranfer coefficient, and has formed and mix required turbulence state.Therefore satisfied the requirement of standard A.Because all process-stream flows through from each mixing mouth, so also satisfied the requirement of standard B.In two low flow velocity districts of mixing between the mouth, provide the holdup time that is used for mass transfer and heat transfer.Therefore, also satisfied the requirement of standard C.After by a series of mixing mouth and threeway, fluid flows out in vertical direction by one or more passages of circular horizontal bottom wall.Preferably be provided with an opening on the center line of reactor, the fluid of symmetry can enter this opening, for the below of blender provides uniform liquid distribution.Therefore, standard D also is met.Be provided with a shock plate below the passage in circular horizontal bottom wall, can reduce the high flow rate of two-phase injection stream, liquid is distributed on reactor cross section.
Cooling fluid can mix a mouthful upstream at first, adds between the top of horizontal top wall or horizontal top wall and the base wall.Cooling fluid also can mix between the mouth at two and add.
Yet existing the 6th kind of blender can't satisfy the requirement of correct all standards of mixed performance A-D, but the present invention can accomplish.Compare with prior art, the present invention has improved mixed performance, makes the temperature and the composition that flow from the outlet of blender outflow reach balance.And different with most of blenders in the prior art, the present invention has made full use of the reactor cross section of blending bin.Compare with prior art, the major diameter of blending bin has reduced the requirement of the present invention to height.Table 1 be in 12 kinds of industrial hydrogenation are used computed altitude of the present invention with United States Patent (USP) 4,836, the comparison of the computed altitude of the turbine mixer in 989.In 12 kinds of commercial Application, the overall presure drop that two kinds of blenders are set in every kind of application is identical.If replace turbine mixer, highly can reduce 35mm to 440mm or reduce by 15% to 55% with blender of the present invention.This is the height that blender itself can reduce.In addition, if inject cooling fluid, a cooling fluid distributor can be set so as a part of the present invention, and an independent cooling fluid distributor will be set above blender for turbine mixer.Referring to United States Patent (USP) 4,836,989.Independent cooling fluid distributor will take certain extra height.
Table 1: aspect ratio for the same turbine mixer of blender height of the present invention (United States Patent (USP) 4.836.989)
The blender aspect ratio
The present invention with the turbine mixer among the United States Patent (USP) 4.836.989 relatively
Description of drawings
Fig. 1 is catalyst and internals exemplary configurations schematic diagram in having the hydroprocessing reactor of two solid catalyst particle beds, and Fig. 1 has also represented the exemplary position of the mixer apparatus between the beds of two vicinities in the reactor;
Fig. 2 is the axle cutaway views such as perspective of an embodiment of mixing arrangement of the present invention;
Fig. 3 A is the vertical view of Fig. 2 blender embodiment;
The side sectional view of Fig. 3 B for obtaining along A-A among Fig. 3 A;
Fig. 3 C is the side sectional view that obtains along B-B among Fig. 3 A;
Fig. 4 A, 5A, 6A, 7A, 8A, 9A and 10A are the vertical view of the available embodiment of the present invention;
Fig. 4 B, 5B, 6B, 7B, 8B, 9B and 10B corresponding side sectional view for obtaining along A-A;
Fig. 4 C, 5C, 6C, 7C, 8C, 9C and 10C corresponding side sectional view for obtaining along B-B;
The side sectional view of Fig. 7 D for obtaining along C-C among Fig. 7 A;
Available embodiment of the present invention includes but not limited to the design shown in the figure.
The specific embodiment
The reaction that takes place in the hydroprocessing reactor is heat release.Therefore, under the pressurized conditions of heating, when reactant changes into product in the presence of the hydroprocessing catalyst, can emit heat in the course of reaction and elevate the temperature.
In industrial hydroprocessing reactor, the two-phase mixture of reactant flows by the solid catalyst particle bed.The ideal flow mode is a plug flow in this reactor, and promptly liquid flows downward with same flow velocity (based on empty reactor) have a few of reactor cross section.Under the resonable plug flow situation that would like to live, vapor phase also is same: steam flows downward with same flow velocity (based on empty reactor) have a few of reactor cross section.
In industrial reactor, because sedimental existence in the space of nonideal distribution column plate, the filling of uneven catalyst and/or catalyst particles intergranular, plug flow is in the cards never.Therefore, in some zones of beds, flow rate of liquid will be higher than mean flow rate, and steam flow rate will be lower than mean flow rate.Because the thermal capacitance height of the heat capacity ratio steam of liquid, in these zones the temperature rise of every meter flow channel lower, temperature rise in ℃.Equally, in other zone of beds, the flow velocity of liquid is lower than mean flow rate, and the flow velocity of steam is higher than mean flow rate.Because the thermal capacitance height of the heat capacity ratio steam of liquid, in these zones the temperature rise of every meter flow channel higher, temperature rise in ℃.
So even reactant mixture is identical in the temperature at reactor inlet place, but when fluid flow through beds, some zone of beds was hotter than other zones.And owing to reaction rate is that rising along with temperature increases, understand the carrying out of accelerated reaction like this: the thermal region reaction rate of beds is higher, so these thermal regions will be emitted more heat than cool region.
Because the reaction rate of beds thermal region and cool region is different, makes the chemical composition of fluid also inequality.
Temperature on a horizontal plane and chemical composition are inhomogeneous can to produce several negative effects:
All hydroprocessing catalyst can inactivation in operating process.Reduce in order to remedy catalyst activity, in running, will improve the mean temperature of bed.At certain time point, during end of run, the maximum temperature of beds reaches maximum permissible value.At this moment, the whole operation unit needs to stop, and catalyst need regenerate or replace.If the non-uniform temperature on the horizontal plane so will be in early stage and out of service than the harmonic(-)mean bed temperature time.Because the high-frequency that non-uniform temperature causes is stopped and is being caused producer's cost's raising aspect production loss, catalyst consumption and the additional labour.
Inhomogeneous another influence that causes is that the chemical conversion degree is inhomogeneous.Part reaction-ure conversion-age is higher, and remaining reaction-ure conversion-age is lower.The result can reduce the overall product quality.First example is the diesel engine hydrotreating reactor, and hydrocarbon component and hydrogen with sulfur-bearing in this reactor change into hydrocarbon component and the H that does not conform to sulphur
2S.If non-uniform temperature, a part of feed oil is reacted under higher temperature, because aforesaid flow rate of liquid is lower, also can react under lower air speed.Another part feed oil is reacted at a lower temperature, because flow rate of liquid is higher, also can react under higher space velocity.Organic sulfur often passes through beds from the zone bypass of low temperature high-speed as a result.This bypass by serious increase the content of organic sulfur in all over products.In order to meet product specification aspect the organic sulfur content, the producer need reduce feed rate, or the operating temperature that improves reactor inhomogeneous with compensation temperature and composition.Reduce feed rate and aspect product loss, can increase cost.Improve temperature of reactor and can cause energy consumption to increase, the regeneration/replacing of catalyst increases the parking frequency, has reduced service cycle.The increase of parking frequency increases aforesaid cost.
Second example is hydrocracking reactor, in this reactor heavy hydrocarbon component and hydrogen changed into light hydrocarbon component.If non-uniform temperature, so a part of feed oil is at high temperature reacted, because flow rate of liquid is lower, also can react under low-speed.Another part feed oil is reacted at low temperatures, because flow rate of liquid is higher, also can react under high-speed.The result causes the heavy feed oil overcracking of a part, makes unwanted C
1-C
4Gaseous product and light naphthar component seriously increase, and the conversion ratio of the heavy feed oil of another part is very low.Thereby reduced the selectivity of hydrocracking unit, also reduced the total conversion that heavy feed component is converted into the light product component expected product.Two kinds of influences have all increased the producer's cost.
In industrial hydroprocessing reactor, temperature in the beds horizontal plane and chemical composition are inhomogeneous to be unavoidable.But suitable reactor internal components is installed makes this inhomogeneous minimum that reaches.
For first beds, charging/reactant enters at first thus, need provide a good import distributor evenly to distribute on reactor cross section to guarantee liquid and steam.The fluid that enters distributor need suitably mix to guarantee component balanced and thermal balance in the upstream of distributor.Well-mixed fluid is provided in reactant usually in the pipeline of reactor.
For any beds subsequently, need good import distributor on reactor cross section, evenly to distribute too to guarantee liquid and steam.Yet the import of beds subsequently stream promptly is the outlet stream of upstream catalyst bed, and the outlet temperature and the chemical composition of this upstream catalyst bed are inhomogeneous.Therefore be necessary between upstream catalyst bed and distributor, to be provided with a mixing arrangement.Otherwise the inhomogeneous of this temperature and chemical composition will be passed to next bed from a bed, becomes more serious.The purpose that mixing arrangement is set obtains temperature exactly and forms outlet stream uniformly.
Usually, a kind of cooling fluid lower than inside reactor fluid temperature (F.T.) is injected between the beds of two vicinities in the hydroprocessing reactor, before this fluid enters next bed, makes the fluid cooling of flowing out from a beds.Can make reactor operation near isothermy like this, it has many-sided effect aspect product quality increasing service cycle and improve.In this case, this mixing arrangement further purpose is that the cool stream thigh is mixed with the effluent that flows out from a beds, so that the stream thigh reached thermal balance and component balanced before entering next beds.
Referring now to accompanying drawing, Fig. 1 represents to have the schematic diagram of the typical hydroprocessing reactor of two catalyst granules beds 2 and 3.Fig. 1 has represented the exemplary position of mixing arrangement with respect to beds and other reactor internal components.Reactant enters reactor by inlet nozzle 4.Fluid enters the distribution column plate 5 at top, and before fluid entered beds 2, distribution column plate 5 can make steam and liquid evenly distribute on reactor cross section.Beds 2 is actionless on a web plate or catalyst supports screen 6.Because the weight of catalyst is big and fluid flows through the caused power of beds, catalyst web plate or screen 6 will bear bigger power usually.Therefore need brace summer 7 to bear these power usually.Below catalyst carrier system 6 and 7, be provided with mixing arrangement 8.Cooling fluid can add by a cooling pipe orifice 9.Below blender, a percussion mechanism 10 is set, liquid and make the high flow rate of the injection stream that flows out from mixing arrangement retarded is used for distributing.Below blender, also be provided with the second distribution column plate 11, before fluid entered next beds 3, this distribution column plate 11 can make steam and liquid evenly distribute on the cross section of reactor.Product in the reactor leaves by outlet nozzle 12.
Can use two above beds.The quantity of mixing arrangement 8 is generally N-1, and wherein N is the quantity of catalyst reactor bed.
Fig. 2-Figure 9 shows that alternative structure of mixing arrangement of the present invention.These figure have only showed the feature of the present invention and alternatives.These figure do not limit the scope of thought disclosed herein, are as the work accompanying drawing at this.These figure should not be considered as the restriction to the inventive concept scope.Relative dimensions shown in the drawings should not be considered as with the specific embodiment of industry equal or proportional.
Fig. 2 is axle cutaway views such as the perspective of blending bin 8, and this blending bin 8 is made up of a circular top 13, a rounded bottom dish 14 and a cylindrical side wall 15.This cylindrical side wall 15 can be the part of reactor wall, also can be an independent wall littler than reactor diameter.The diameter of cylindrical wall 15 preferably approaches the diameter of reactor, so that the height of blender reaches minimum.The opening 16 in top disc 13, this blending bin forms the flow obstacle of a basic sealing in reactor 1.Under the situation of diameter less than the internal diameter of reactor of this cylindrical wall, a column plate or other device need be set to guarantee between the inwall of blending bin 8 and reactor 1, realizing basic sealing.
Cooling fluid is injected in the blending bin 8 by a perforation cooling distributor 17.In blending bin, be provided with the plate washer 18,19 and 20 that flows and formed a series of mixing openings 21 and 22 that are used for high flow rate and mixed flow, also formed a series of flow openings 23 and 24 that are used for low flow velocity and diverted flow.Except opening 21,22 and 24, these mobile plate washers have formed a basic sealing device, force fluid to flow out from these openings like this.Base plate 14 is provided with the round exit hole 25 concentric with reactor center line.。This circular open also is that last mixes mouth as the 3rd in the blender.
Fig. 3 A is the vertical view of the blender among Fig. 2.The cutaway view of Fig. 3 B for obtaining along A-A among Fig. 3 A.The cutaway view of Fig. 3 C for obtaining along B-B among Fig. 3 A.Shown in Fig. 3 A and Fig. 3 B, circular impact plate 26 is concentric with circular open 25, and is arranged at the below of circular open 25.
Fluid is flowing shown in arrow among Fig. 3 A, 3B and the 3C in the device.In the operating process, the steam and the liquid that flow out from beds 2 pass through passage 16, flow in the blending bin.Cooling fluid adds through distributor 17.This moment, all process-stream flow through mixing mouth 21, was mixing mouthful 21 places, and fluid is that high flow rate flows, and liquid is dispersed in the steam.Afterwards, this logistics is divided into two low flow velocity logistics by mobile plate washer 19.Two logistics flow to the next mouth 22 that mixes in the passage 23 of two symmetries, be mixed into the high flow rate logistics once more in mixing mouthful two logistics in 22 places.After mixing mouth 22, logistics is divided into two low flow velocity logistics by mobile plate washer 20 again, and this moment, two logistics flow to centre bore 25 by the passage 24 of two symmetries, and logistics also is that last mixing mouthful place is mixed into the high flow rate logistics once more at this in the 3rd.Last shock plate 26 can guarantee that the fluid outward radial flows out blender.This shock plate can prevent that blender from directly delivering to the injection stream of high flow rate on the distributing disc 11.Liquid level on this injection stream meeting interference profile column plate is taken away liquid.In addition, before fluid entered distribution column plate 11, shock plate 26 can make liquid evenly distribute on reactor cross-section.
Because the high flow rate of blending bin inner fluid is compared with the viscous force between the liquid and vapor capacity, gravity can be ignored.Therefore, even blending bin 8 approaches level, any tangible PHASE SEPARATION can not take place in the blending bin yet.
Mobile plate washer in the blending bin can have a lot of different shapes.It can be straight, crooked, angle or the like.Plate washer also needn't be strict vertical, as long as there is vertical part just enough.Intake channel 16 also can have different shapes with exit passageway 25, part as shown in Figures 2 and 3, ellipse, circle, rectangle, triangle or the like.The quantity of intake channel and exit passageway is respectively more than one and one.The cross section of blending bin itself can be Any shape.For the blender shown in Fig. 2,3A, 3B and 3C, it can be circle, also can be triangle, rectangle or polygon.Be preferably circle or polygon, this be since this moment blender cross-sectional area approach the cross-sectional area of container.
Fig. 4 A, 4B and 4C have provided alternative mixer design embodiment.Glide path by blender as shown by arrows.Fig. 4 A is the vertical view of an available blending bin 8.Fig. 4 B is along the cutaway view of A-A among Fig. 4 A.Fig. 4 C is along the cutaway view of B-B among Fig. 4 A.This blending bin is by polygon top wall 13 ' and polygonal bottom wall 14 ' and sidewall 15 ' form.Top wall be provided with two circular opens 16 ', be used to make fluid flow to blending bin 8 '.Cooling fluid passage 16 ' downstream and top disc 13 ' and bottom plate 14 ' between and by cooling fluid distributor 17 a with holes ' adding.Be provided with in the blending bin the crooked plate washer 18 that flows ', having formed first mixes mouthfuls 21 '.Be provided with in the blending bin plate washer 19 that flows ', earlier from mix mouthfuls 21 ' logistics that flows out be divided into two logistics enter two passages 23 ', mix mouthfuls 22 at second afterwards ' locate again two logistics to be mixed into a logistics again.Near mix mouthfuls 21 ' mobile plate washer 19 ' the turning be crooked, and near mix mouthfuls 22 ' mobile plate washer 19 ' the turning be angled.Mixing mouthfuls 22 ' the downstream be provided with a shelves stream plate 20 that becomes the angle '.Shelves stream plate 20 ' from second mix mouthfuls 22 ' logistics that flows out be divided into two logistics enter two flow channels 24 ', all stream strand also is that last mixes a mouthful place and mixes once more at the 3rd afterwards, last mix mouth be square orifice 25 '.Outlet opening 25 ' below, be provided with a shock plate 26 '.
Fig. 2,3A, 3B, 3C, 4A, the blender shown in 4B and the 4C have three mixes mouthfuls 21,22 and 25 (or 21 ', 22 ' and 25 ').Yet this blender can be provided with two or more mixing mouths.Fig. 5 A,, 5B and 5C represent to have the embodiment of four blending bins 8 that mix mouthful.Glide path by this blender as shown by arrows.Fig. 5 A is the vertical view of blending bin 8.The cutaway view of Fig. 5 B for obtaining along A-A among Fig. 5 A.The cutaway view of Fig. 5 C for obtaining along B-B among Fig. 5 A.This blending bin " is made up of circular top wall 13 ", rounded bottom wall 14 " and circular side wall 15.This top wall is provided with a rectangular opening 16 ", be used for the import that fluid flows to blending bin 8, and mix mouth as first.Cooling fluid does not add in blender 8, but can mix mouthfuls 16 " the upstream add.In blending bin, be provided with the plate washer 27 that flows ", in mixing mouth 16 " logistics that flows out is divided into two logistics and enters two flow channels 28 ".Be provided with a grade stream plate 18 in the blending bin ", formed second and mixed mouth 21 ", " locating whole process-streams mixes once more mixing mouth 21.Be provided with shelves stream plate 19 in the blending bin ", from mixing mouthful 21 " logistics that flows out is divided into two logistics and enters two passages 23 ", mix mouth 22 at the 3rd afterwards and " locate two logistics are mixed into a logistics more earlier.Mixing mouthfuls 22 " downstream be provided with a shelves stream plate 20 ".The logistics that shelves stream plate 20 " mixing mouth 22 from the 3rd " flows out is divided into two logistics admission passages 24 ", all logistics also is that last circular mouth 25 that mixes " is located to mix once more at the 4th afterwards.Mixing mouthfuls 25 " below, be provided with a circular impact plate 26 ".
The exit passageway that is used for fluid is guided in the blending bin 8 space between blending bin 8 and the distribution column plate 11 can adopt aforesaid any amount, position and shape.Fig. 6 A, 6B and 6C represent to have the embodiment of the blending bin 8 of two off-centered outlet opening 25 .Glide path by blender as shown by arrows.Fig. 6 A is the vertical view of blending bin 8.The cutaway view of Fig. 6 B for obtaining along A-A among Fig. 6 A.The cutaway view of Fig. 6 C for obtaining along B-B among Fig. 6 A.This blending bin is made up of circular top wall 13 , rounded bottom wall 14 and cylindrical side wall 15 .This top wall is provided with circular open 16 , is used for the import that fluid flows to blending bin 8, and mixes mouth as first.Cooling fluid adds by perforate cooling fluid distributor 17 between top wall 13 and base wall 14 in the downstream that first mixes mouthful 16 .Be provided with plate washer 27 that flow in the blending bin, enter in flow channel 28 being divided into two logistics from a logistics that mixes mouth 16 outflow.Be provided with shelves stream plate 18 in the blending bin, formed second and mixed mouthful 21 , mix once more at the mixing mouthful whole process-streams in 21 places.Be provided with shelves stream plate 20 in the blending bin, enter in two flow channel 24 being divided into two logistics from a logistics that mixes mouth 21 outflow.Be provided with shelves stream plate 19 in the blending bin, formed the 3rd and mixed mouthful 22 , be in the stream thigh that flows among passage 24 at mixing mouthful 22 and mix once more.Be noted that by mixing mouthful 22 flow direction with by the mixing mouth 22,22 among Fig. 2,3A, 4A and the 5A ' and 22 " direction opposite.Mix mouthful whole process-streams of 22 outflow from the 3rd and be divided into two passage 23 that lead to outlet opening 25 .In order to improve the liquid distribution of distribution column plate 11, can also use optional separation plate washer 29 , to obtain entering the more uniform shunting of logistics among each passage 23 .Logistics flows out blending bin by two rectangular aperture 25 .The below of each exit opening 25 all is provided with shock plate 26 .Embodiment with the front compares, and the defective of this blender is that the distribution situation of liquid on distribution column plate 11 is relatively poor.This is because liquid is only from entering into each exit opening 25 on one side, exit opening is not arranged on the center of reactor, and owing to the inhomogeneous shunting at the exit liquid that mixes mouthful 22 makes flow rate of liquid difference by each exit opening 25 .
As previously mentioned, this mixing arrangement can be provided with two or more mixing mouths.Under given blender overall presure drop, the quantity of mixing mouth is many more, and the vertical height of required blending bin is just high more.Fig. 7 A, 7B, 7C and 7D represent to have two and mix mouth 21
*With 22
*The embodiment of blending bin 8.Fig. 7 A is the vertical view of this blender 8.The cutaway view of Fig. 7 B for obtaining along A-A among Fig. 7 A.The cutaway view of Fig. 7 C for obtaining along B-B among Fig. 7 A.The cutaway view of Fig. 7 D for obtaining along C-C among Fig. 7 A.Glide path by this blender as shown by arrows.This blending bin is by circular top wall 13
*, rounded bottom wall 14
*With cylinder side wall 15
*Form.This top wall is provided with two circular inlet holes 16
*, be used for the passage that steam and liquid flow to blending bin 8.In each inlet openings 16
*The top or by each inlet openings 16
*Be equipped with a top and bottom the cylinder 30 of opening is all arranged
*, at top wall 13
*With cylinder 30
*Between formed the connection of a basic sealing.Cylindrical top edge is provided with V-shaped groove.In the operation, top wall 13
*Can hold certain liquid level, and because the existence of V-shaped groove, liquid can be stable flows to inlet openings 16
*So just avoided the fluctuation of liquid-inlet flow velocity in the blender.The cylinder 30 that has V-shaped groove
*Also can be used for each inlet openings 16
*Liquid distribution so that the flow rate of liquid of each inlet openings is near consistent.Passage 30 shown in the figure is a cylinder, but also can have any other cross section, as ellipse, rectangle, triangle or polygon.Cylinder 30
*Top edge be V-shaped groove, but cylinder 30
*In be used for liquid flow opening also can take other shape, as slot or circular hole.Cooling fluid does not add in blending bin 8, but can be in circular inlet openings 16
*The upstream add, do not show in the drawings.Be provided with two shelves stream plates 18 in the blending bin
*, formed the first mixing mouth 21 that flows through whole process-streams
*Be provided with shelves stream plate 20 in the blending bin
*, from mixing mouthfuls 21
*The logistics that flows out is divided into two logistics and enters two flow channels 24
*Be provided with shelves stream plate 19 in the blending bin
*, formed second and mixed mouth 22
*, at this passage 24
*In the fluid that flows mix once more.Mix mouth 22 from second
*The whole process-streams that flow out are divided into two passages 23
*, each logistics afterwards is introduced into a rectangle exit opening 25
*In.In order to improve the liquid distribution situation of distribution column plate 11, can also use optional separation plate washer 29
*, to obtain entering each passage 23
*The more uniform shunting of middle logistics.The stream thigh is by two rectangular apertures 25
*Flow out blending bin.Each exit opening 25
*The below all be provided with a shock plate 26
*The same with the blender shown in the 6C with front Fig. 6 A, 6B, this blender also has liquid distribution situation defect of bad on distribution column plate 11.This is because fluid is only from entering into each exit opening 25 on one side
*, exit opening is not arranged on the center of reactor, and owing to mixes mouth 22 at second
*Exit liquid inhomogeneous shunting and make by each opening 25
*The flow rate of liquid difference.Compare with previous embodiment, a defective of this blender is owing to have only two to mix mouthful, rather than three or more mixed mouthful, makes mixed performance that slight reduction be arranged.This blender also has some advantages: because this blender has only two to mix mouthful, under the constant pressure drop, the flow velocity by blender will be higher than and have three or more the blenders that mix mouthful.Therefore, the cross section of flow channel can be littler in mixing mouth and the blender.Mix mouthful and the required small cross section of flow channel is lower than the height of blender to have three or more the blender height that mix mouths.Have two off-centered exit openings 25
*With by mixing mouthfuls 21
*With 22
*The identical design of flow direction also further reduced the blender height.Therefore this blender has embodied a very compact low clearance design, and this kind blender can be applied in mixing arrangement and take in the minor diameter reactor of little room.For the minor diameter reactor, it is not very strict that liquid distribution on the distribution column plate requires, and this mainly is because compare with the major diameter reactor, and the fluid that blender the flows out bad caused horizontal gradient that distributes on distributing disc 11 is not very important.
The cross section of the mixing mouth that the previous embodiment flow baffles forms all is a rectangle.But as long as all process-streams can mix with high flow rate at the mixing mouth, the cross section that mixes mouth can be Any shape.Fig. 8 A, 8B and 8C represent to have two circular cross-sections and mix mouth 16
*With 22
*The embodiment of blender 8.Fig. 8 A is the vertical view of blender 8.The cutaway view of Fig. 8 B for obtaining along A-A among Fig. 8 A.The cutaway view of Fig. 8 C for obtaining along B-B among Fig. 8 A.Glide path by this blender as shown by arrows.This blending bin is by circular top wall 13
*, rounded bottom wall 14
*With circular side wall 15
*Form.This top wall 13
*Be provided with circular import 16
*, it mixes mouth and is used for the passage that fluid flows to blending bin 8 as first.Cooling fluid does not add in blending bin 8, but can be in circular inlet port passage 16
*The upstream add, do not show among the figure.Be provided with the plate washer 27 that flows in the blending bin
*, from mixing mouthfuls 16
*The logistics that flows out is divided into two logistics and enters two flow channels 28
*In.Also be provided with another mobile plate washer 19 in the blending bin
*Mix mouth 22 to form second
*, passage 28
*In two logistics flowing mix at this.Mix mouth 22 from second
*The whole process-streams that flow out are divided into two logistics and enter two passages 23
*In, each stream thigh is introduced in a square orifice 25 afterwards
*In.In order to improve the liquid distribution situation of distribution column plate 11, can also be provided with one and separate plate washer 29
*, so that liquid is at each passage 23
*In can more uniform dispersion.Logistics is by two rectangle outlet openings 25
*Leave blending bin.At each outlet opening 25
*The below is provided with shock plate 26
*The same with the blender shown in the 7D with aforementioned Fig. 7 A, 7B, 7C, this blender has the liquid defect of bad that distributes on distribution column plate 11, compares with having three or more mixer design of mixing mouthful, also has the slight defective that descends of mixed performance.But the same with aforementioned blender, this blender has also embodied a very compact low clearance design, and this blender can be applied in mixing arrangement and take in the minor diameter reactor of little room.
Fig. 9 A, 9B represent similar three embodiment that mix the blender of mouth that have with the blender among Fig. 2,3A, 3B and the 3C with 9C.Yet improved inlet hole 16
* *, flow baffles 19
* *With 20
* *And cool stream distributor 17
* *Glide path by this blender as shown by arrows.Fig. 9 A is the vertical view of blender 8.The cutaway view of Fig. 9 B for obtaining along A-A among Fig. 9 A.The cutaway view of Fig. 9 C for obtaining along B-B among Fig. 9 A.This blending bin is by circular top wall 13
* *, rounded bottom wall 14
* *With circular side wall 15
* *Form.On this top wall opening is arranged, formed intake channel 16
* *, be used for fluid and flow to blending bin 8.Cooling fluid is at intake channel 16
* *The downstream by being arranged on top wall 13
* *With base wall 14
* *Between cooling fluid distributor 17
* *Add.This cooling fluid distributor can be for dissimilar, and cooling fluid can flow out from distributor with any direction.In this case, use "T"-shaped porose distributor with downward injection stream.Be provided with two mobile plate washers 18 in the blending bin
* *, formed first and mixed mouth 21
* *, all process-stream is crossed this mixing mouth 21 with high velocity stream
* *Be provided with the crooked plate washer 19 that flows in the blending bin
* *, first from mixing mouth 21
* *The logistics that flows out is divided into two logistics and enters two passages 23
* *, latter two logistics mix mouthfuls 22 at second
* *Be mixed into a logistics once more.Mixing mouth 22
* *The downstream be provided with the staged plate washer 20 that flows
* *Plate washer 20 flows
* *Mixing mouth 22 from second
* *The stream stock that flows out becomes two stream thighs to enter two passages 24
* *, whole then stream thighs are that last circular mixing mouth also is that exit passageway 25 places are mixed once more at the 3rd.Below exit passageway 25, be provided with a shock plate 26
* *
Below again with reference to figure 1.For all embodiment of this mixing arrangement, blending bin 8 preferred orientation settings so that the mixing mouth by bottom horizontal flow sheet, as the flow direction of the mixing mouth 21 of Fig. 2, be arranged on the catalyst web plate or support the brace summer 7 of screen 6 belows parallel.Can make fluid reach minimum like this from the pressure drop that the outlet of beds 2 flows to the intake channel 16 of blending bin.In this zone, do not wish to produce tangible pressure drop, because this can cause mobile inhomogeneous by beds 2.
The import 16 of previous blender embodiment all is provided with near mixer sidewall 15.This set of import can increase aforementioned steam and liquid flow to the blender intake channel from upstream catalyst bed 2 pressure drop.In order to reduce pressure drop, be with the center line setting of import near reactor.Figure 10 A, 10B and 10C represent an embodiment of blending bin 8, the intake channel 16 of this blending bin
XCenter line setting near blender and reactor.Figure 10 A is the vertical view of blending bin 8.The cutaway view that obtains along A-A among Figure 10 B Figure 10 A.The cutaway view of Figure 10 C for obtaining along B-B among Figure 10 A.Glide path by blending bin as shown by arrows.This blending bin has two to mix mouth.This blending bin is by circular top wall 13
X, rounded bottom wall 14
XWith cylinder side wall 15
XForm.Top wall 13
XBe provided with intake channel 16
X, flow to the intake channel of blending bin 8 as fluid.Cooling fluid does not add in blending bin 8, but can be at intake channel 16
XThe upstream add, do not show among the figure.Be provided with the mobile plate washer 18 of two semicircles in the blending bin
X, formed first and mixed mouth 21
XWith the second mixing mouth 22
XThe all processes logistics is by intake channel 16
XFlow to first and mix mouth 21
XMix mouth 21 from first
XThe process-stream that flows out is divided into the logistics of two stream and advances two passages 23
XAt passage 23
XIn, steam and liquid are along cylindrical side wall 15
XFlow to second and mix mouth 22
X, mix mouthful whole process-streams in 22 places to mix once more at a high speed at this.Can also be provided with the plate washer 20 that flows
XBe divided into two low flow velocity logistics mixing a mouthful logistics that flows out from second, this fluid is by square exit passageway 25 afterwards
XFlow out blender.In order to obtain the compact more design of a low clearance blender 8, the plate washer 20 that flows can be set
X, and replace plate washer 20
XCan be chosen in exit passageway 25
XIn the plate washer 31 that flows is set
XPlate washer 31 flows
XEffect be when stream strand from exit passageway 25
XDuring outflow, prevent that mixing mouthful high velocity stream thigh that flows out from second only penetrates towards one side of reactor.The result causes the distribution grid liquid distribution of below bad.Exit passageway 25
XWith intake channel 16
XAs mixing mouth, this is not because lower by the velocity ratio of these passages.At this exit passageway 25
XThe below be provided with a shock plate 26
X
Refer again to Fig. 1 below.The catalyst support system is made up of catalyst web plate 6 and brace summer 7.As shown in Figure 1, catalyst support system and mixing arrangement 8 are absolute construction.But mixing arrangement of the present invention can be designed to the part of catalyst support system.
Blending bin itself needs brace summer or other structures to bear the power that is caused by the pressure drop by blending bin.Do not express these brace summers or structure in the accompanying drawing, but they can be arranged on blending bin above or below, perhaps as the part of blending bin and mobile plate washer.
For any one embodiment of the present invention, be provided with the low capacity outage.The dish of forming blender can be a slice or be formed by several set.Usually in blender, be provided with several moveable portion be convenient to check and cleaning process in the passage that provides a people to enter by blending bin is provided.
The fricton-tight flow velocity of two-phase in the flow channel (no-slip flow velocity) is defined as the flow velocity when fricton-tight between liquid phase and vapour phase, also is that liquid phase flow rate equals the vapour phase flow velocity.Therefore fricton-tight flow velocity is:
Q wherein
1Be the liquid volume flow velocity by passage, Q
vBe the gas volume flow velocity by passage, A is the cross-sectional area of this passage.
Blending bin 8 preferably approaches level, that is to say from reactor 1 one side very little to the whole inclination of the blending bin of another side.The diameter of blending bin 8 is preferably the 50%-100% of reactor inside diameter.Each mixes the cross-sectional area of mouth for can make fricton-tight flow velocity preferably reach 3-15m/s.The cross-sectional area that mixes the branched bottom in mouthful downstream preferably reaches corresponding 0.25 to 1 times of mixing mouthful flow velocity for making fricton-tight flow velocity.The height of blender from the top disc to the impact disc for from the 100mm that is used for the minor diameter reactor to be used for the major diameter reactor greater than 500mm.The horizontal diameter of plate washer 20 and 27 of flowing is preferably 1 to 3 times of Breadth Maximum of combined upstream mouth.
Table 1 is three mixer design embodiment in the different commercial Application.All embodiment in the table 1 are the blender among Fig. 2,3A, 3B and the 3C.
Table 1: mixer design embodiment
| Example 1 | Example 2 | Example 3 | |
| Type of reactor | Hydrocracking | Hydroprocessing | Hydroprocessing |
| Reactor inside diameter, mm | 5000 | 3300 | 1600 |
| Liquid flow and character | |||
| Blender actual volume flow velocity, m 3/h | 630 | 170 | 32 |
| Density, kg/m 3 | 460 | 620 | 500 |
| Viscosity, cP | 0.15 | 0.13 | 0.10 |
| Surface tension, dynes per centimeter | 7.5 | 4.9 | 2.4 |
| The steam flow rate and the character that comprise cooling fluid | |||
| The actual volume flow velocity of blender, m 3/h | 6200 | 2300 | 420 |
| Density, kg/m 3 | 18.5 | 21.9 | 53 |
| Viscosity, cP | 0.021 | 0.022 | 0.019 |
| Mix a mouthful interior fricton-tight two-phase flow velocity, m/s | 8.1 | 7.8 | 6.8 |
Generally, below the present invention will note:
On the one hand, the present invention relates to a kind of mixing arrangement, be used for being blended in the steam and the liquid of vertical container concurrent flow, the blending bin meeting of a basic horizontal hinders steam liquid flow then in this vertical container, and horizontal blending bin meeting forces steam and liquid continuously by a plurality of mixed sequences.One of them mixed sequence is defined as one and mixes mouth, is provided with a threeway thereafter.One of them mixes mouth and is defined as a mixed process stream strand passage that passes through at a high speed, and the high flow rate logistics during threeway is defined as mixed mouthful is divided into two low flow velocity logistics and enters two flow channels.
In this mixing arrangement, the basic horizontal blending bin is defined as: blending bin is lower than to the whole gradient of another side on one side from container that angle is 20% of 11.5 ° of angles to the maximum the same level face.The independent sector of blending bin can have high any gradient, as long as be lower than 11.5 ° 20% just passable to the whole gradient of another side on one side from container.
And, be the 25%-100% of cross-sectional area in this container at cross-sectional area perpendicular to the basic horizontal blending bin in the plane of chamber wall.When the cross-sectional area of blending bin during less than the cross-sectional area of reactor, the zone between blending bin and the chamber wall is coiled or other device sealings, can realize that between blending bin and chamber wall basic fluid is tightly connected.
Cold cooling fluid can pass through to mix at first the pipeline or distributor adding of mouthful upstream, perhaps mixes between the mouth at two to add with the process for cooling logistics.
Blending bin comprises that at least two are mixed mouth.
Fricton-tight two-phase flow velocity is that 3m/s is to 15m/s in the mixing mouth.
In the diverted flow passage in threeway downstream maximum fricton-tight two-phase flow velocity be during combined upstream flow to be mixed mouthful fricton-tight two-phase flow velocity 25%.
Minimum fricton-tight two-phase flow velocity flows less than combined upstream and mixes fricton-tight two-phase flow velocity in the mouth in the diverted flow passage in threeway downstream.
Reactor vessel can be a vertical hydroprocessing reactor, and steam and liquid also flow to current downflow, and in this reactor, hydrocarbon reacts with the gas that is rich in hydrogen in the presence of the hydroprocessing catalyst.
The present invention records and narrates and has explained the relation of its different embodiment.But, the multiple variation that the present invention is made and revise the scope that does not all exceed claim of the present invention.
Therefore, for example, a mixing mouth or passage are being subdivided into the mixing mouth or the passage of two or more vicinities with common wall.But the best result that it has been generally acknowledged that mixed performance and resistive connection dirt character is not realize in the mixing mouth of segmentation or the passage by any way.
Turbulent flow initiating device such as blade, plate washer, lattice plate or the like can be arranged on the upstream of mixing mouth or passage.
Claims (40)
1. mixing arrangement that is used for catalytic reactor, this mixing arrangement is arranged between upper catalyst bed layer and the lower catalyst bed layer, be used for mixing gas or steam and the liquid of described reactor vessel by the beds concurrent flow of described mutual superposition, described mixing arrangement forms the flow channel by described mixing arrangement, be used for described steam and liquid and flow to described lower catalyst bed layer from described upper catalyst bed layer, vice versa, and described flow channel comprises:
The import of at least one described mixing arrangement;
The outlet of at least one described mixing arrangement;
Along described flow channel continuously arranged first and at least one second mixing mouth or passage, described first and described at least one second mix mouthful be provided with and can make basically all that liquid and vapor mixing stream flow through each described mixings mouth, this circulation area of mixing mouth is relevant with the flow velocity of described mixed flow, so that at least one described reactor mixes in the operational phase mouthful the fricton-tight two-phase flow velocity of described mixed flow be 3m/s to 15m/s, more preferably be enough to make liquid dispersion in steam and/or steam be distributed in the liquid;
The flow channel part of a basic horizontal, extend and be arranged between described at least one import and described at least one outlet, so that the vertical dimension of mixing arrangement is as much as possible little, described basic horizontal flow channel part extends to nearest described outlet from nearest described import;
Be positioned at the described flow channel that mixes mouthful downstream, comprise an elongated area flow channel part, this elongated area flow channel partly comprises at least two flow channels, be used for described whole mixed flows are divided at least two independent two phase flows or logistics, all described logistics sizes are the same, the mixing cross-sectional area of described at least two passages can make the fricton-tight two phase flow speed ratio of each logistics at least two independent two-phase logistics much lower by the fricton-tight two-phase flow velocity of corresponding mixing mouth, so just can increase the time of staying of described fluid in described passage, help heat and transmit and the quality transmission.
2. mixing arrangement according to claim 1, wherein, at least one operational phase of described reactor, one is mixed mouthful described fricton-tight two-phase flow velocity of interior described mixed flow is that 3.5m/s is to 14.5m/s.
3. mixing arrangement according to claim 1 and 2, wherein, at least one operational phase of described reactor, one mix mouthful in the described fricton-tight two-phase flow velocity of described mixed flow be 3.5m/s to 14m/s, for example, 3.5m/s is to 4m/s, 4m/s is to 5m/s, and 5m/s is to 6m/s, and 6m/s is to 7m/s, 7m/s is to 8m/s, and 8m/s is to 9m/s, and 9m/s is to 10m/s, 10m/s is to 11m/s, and 11m/s is to 12m/s, and 12m/s is to 13m/s, 13m/s is to 14m/s, and 3.5m/s is to 13m/s, and 3.5m/s is to 12m/s, 3.5m/s to 11m/s, 3.5m/s is to 10m/s, 5m/s is to 9m/s, 3.5m/s to 8m/s, 3.5m/s is to 7m/s, 3.5m/s is to 6m/s, 3.5m/s to 5m/s, 6m/s is to 14m/s, and 6m/s is to 13m/s, and 6m/s is to 12m/s, 6m/s is to 11m/s, 6m/s is to 10m/s, and 6m/s is to 9m/s, and perhaps 6m/s is to 8m/s.
4. according to the described mixing arrangement of aforementioned any one claim, wherein, described first mixes mouth is made of described import, and/or described second mixes mouth by described export mixes.
5. described and comprise independent second mixing arrangement that mixes mouthful according to aforementioned any one claim, wherein at least one operational phase of described reactor, one is mixed a mouthful interior described fricton-tight two-phase flow velocity, two mix mouthful in a described fricton-tight two-phase flow velocity be 4.0m/s to 12.5m/s, be preferably 8.1m/s to 12.3m/s.
6. described and comprise the mixing arrangements that two second of being provided with in succession mix mouthful according to each claim among the claim 1-4, wherein at least one operational phase of described reactor, one is mixed a mouthful interior described fricton-tight two-phase flow velocity, three mix mouthful in a described fricton-tight two-phase flow velocity be 3.5m/s to 10.5m/s, be preferably 6.5m/s to 10.1m/s.
7. according to the described mixing arrangement of aforementioned any one claim, wherein, angle is 20% of 11.5 ° of angles to the maximum to described mixing arrangement the same level face from being lower than to the whole gradient of another side on one side, an independent sector of this mixing arrangement has a higher gradient, and described whole gradient is no more than 20% of described 11.5 ° of angles.
8. mixing arrangement according to claim 1, wherein, total cross-sectional area of described elongated area flow channel part or total cross-sectional area of described diverted flow passage are to make maximum fricton-tight two-phase flow velocity greater than 25% of the fricton-tight two-phase flow velocity in the mobile mixing mouth of combined upstream, for example, greater than 30% of described approximately flow velocity, greater than 35% of described approximately flow velocity, greater than 40% of described approximately flow velocity, greater than 45% of described approximately flow velocity, greater than 45% of described approximately flow velocity, greater than 50% of described approximately flow velocity, greater than 55% of described approximately flow velocity, greater than 60% of described approximately flow velocity, perhaps greater than 65% of described approximately flow velocity.
9. according to the described mixing arrangement of each claim in claim 1 or 8, wherein, total cross-sectional area of described elongated area flow channel part or total cross-sectional area of described diverted flow passage are to make minimum fricton-tight two-phase flow velocity less than the mobile fricton-tight two-phase flow velocity that mixes in the mouth of combined upstream, for example, less than 95% of described approximately flow velocity, less than 90% of described approximately flow velocity, less than 85% of described approximately flow velocity, less than 80% of described approximately flow velocity, less than 75% of described approximately flow velocity, less than 70% of described approximately flow velocity, perhaps less than 65% of described approximately flow velocity.
10. according to the described mixing arrangement of aforementioned each claim, wherein, described catalytic reactor is the vertical hydroprocessing reactor that has steam and liquid and flow to current downflow, in this reactor hydrocarbon under the situation that the hydroprocessing catalyst exists with the gas reaction of being rich in hydrogen.
11. mixing arrangement that is used for catalytic reactor, this mixing arrangement is arranged between upper catalyst bed layer and the lower catalyst bed layer, be used for mixing gas or steam and the liquid of the vertical container of described reactor by the beds concurrent flow of described mutual superposition, described mixing arrangement forms the flow channel by described mixing arrangement, be used for described steam and liquid and flow to described subordinate beds from described upper catalyst bed layer, vice versa, and described mixing arrangement comprises:
A top wall is provided with at least one import;
A base wall is provided with at least one outlet;
One is extended the lateral wall that is provided with between described top wall outer rim and base wall outer rim, be used for constituting between described top wall and described base wall an enclosure space;
The inner compartment wall, extend and be arranged between described top wall and the base wall, be used for described top wall, base wall and lateral wall constitute described flow channel together, and described partition walls has formed one first and at least one second mixing mouth or passage in succession along described flow channel, described first and described at least one second setting that mixes mouthful make the mixed flow of whole liquid and steam flow through each described mixings mouth, this circulation area of mixing mouth is corresponding with the flow velocity of described mixed flow, so that at least one described reactor mixes in the operational phase mouthful the fricton-tight two-phase flow velocity of described mixed flow be 3m/s to 15m/s, preferably being enough to make liquid dispersion in steam and/or steam be distributed in the liquid;
The flow channel part of a basic horizontal, constitute together with described top wall, base wall and lateral wall by described inner compartment wall, extend and be arranged between described at least one import and described at least one outlet, so that the vertical dimension of described mixing arrangement is as far as possible little, described basic horizontal flow channel part extends to nearest described outlet from nearest described import;
The described partition walls that is provided with can make the described flow channel that is positioned at mixing mouthful downstream comprise an elongated area flow channel part, this elongated area flow channel partly comprises at least two flow channels, be used for described whole mixed flows are divided at least two independent two phase flows or logistics, more preferably all described logistics sizes are the same, the mixing cross-sectional area of described at least two passages can make the fricton-tight two phase flow speed ratio of each logistics at least two independent two-phase logistics much lower by the fricton-tight two-phase flow velocity of corresponding mixing mouth, so just can increase the time of staying of described fluid in described passage, help heat and transmit and the quality transmission.
12. mixing arrangement according to claim 11, wherein, described mixing arrangement is from a plurality of at least first whole gradient to described top wall or base wall outer rim respective point of described top wall or base wall outer rim, from the maximum deviation of first point separately be lower than respectively angle maximum angle with horizontal plane be 11.5 ° 20%.
13. according to claim 11 or 12 described mixing arrangements, wherein, described top and described base wall are essentially the plane, more preferably are parallel to each other, more preferably basic horizontal.
14. according to the described mixing arrangement of each claim among the claim 11-13, wherein, at least one operational phase of described reactor, one is mixed mouthful described fricton-tight two-phase flow velocity of interior described mixed flow is that 3.5m/s is to 14.5m/s.
15. according to the described mixing arrangement of each claim among the claim 11-14, wherein, at least one operational phase of described reactor, one mix mouthful in the described fricton-tight two-phase flow velocity of described mixed flow be 3.5m/s to 14m/s, for example, 3.5m/s is to 4m/s, 4m/s is to 5m/s, and 5m/s is to 6m/s, and 6m/s is to 7m/s, 7m/s is to 8m/s, and 8m/s is to 9m/s, and 9m/s is to 10m/s, 10m/s is to 11m/s, and 11m/s is to 12m/s, and 12m/s is to 13m/s, 13m/s is to 14m/s, and 3.5m/s is to 13m/s, and 3.5m/s is to 12m/s, 3.5m/s to 11m/s, 3.5m/s is to 10m/s, 5m/s is to 9m/s, 3.5m/s to 8m/s, 3.5m/s is to 7m/s, 3.5m/s is to 6m/s, 3.5m/s to 5m/s, 6m/s is to 14m/s, and 6m/s is to 13m/s, and 6m/s is to 12m/s, 6m/s is to 11m/s, 6m/s is to 10m/s, and 6m/s is to 9m/s, and perhaps 6m/s is to 8m/s.
16. according to the described mixing arrangement of each claim among the claim 11-15, wherein, described first mixes mouth is made of described import, and/or described second is mixed mouth by described export mixes.
17. according to the described mixing arrangement of each claim among the claim 11-16, comprise second an independent mixing mouth, wherein, in at least one operational phase of described reactor, one is mixed a mouthful interior described fricton-tight two-phase flow velocity, preferably two mix mouthful in described fricton-tight two-phase flow velocitys be 4.0m/s to 12.5m/s, arrive 12.3m/s for 8.1m/s preferablyly.
18. according to the described mixing arrangement of each claim among the claim 11-16, comprise two second mixing mouths that are provided with in succession, wherein, in at least one operational phase of described reactor, one is mixed a mouthful interior described fricton-tight two-phase flow velocity, preferably three mix mouthful in described fricton-tight two-phase flow velocitys be 3.5m/s to 10.5m/s, arrive 10.1m/s for 6.5m/s preferablyly.
19. mixing arrangement according to claim 11, wherein, total cross-sectional area of described elongated area flow channel part or total cross-sectional area of described diverted flow passage are to make maximum fricton-tight two-phase flow velocity greater than 25% of the fricton-tight two-phase flow velocity in the mobile mixing mouth of combined upstream, for example, greater than 30% of described approximately flow velocity, greater than 35% of described approximately flow velocity, greater than 40% of described approximately flow velocity, greater than 45% of described approximately flow velocity, greater than 45% of described approximately flow velocity, greater than 50% of described approximately flow velocity, greater than 55% of described approximately flow velocity, greater than 60% of described approximately flow velocity, perhaps greater than 65% of described approximately flow velocity.
20. according to the described mixing arrangement of each claim in claim 11 or 19, wherein, total cross-sectional area of described elongated area flow channel part or total cross-sectional area of described diverted flow passage are to make minimum fricton-tight two-phase flow velocity less than the mobile fricton-tight two-phase flow velocity that mixes in the mouth of combined upstream, for example, less than 95% of described approximately flow velocity, less than 90% of described approximately flow velocity, less than 85% of described approximately flow velocity, less than 80% of described approximately flow velocity, less than 75% of described approximately flow velocity, less than 70% of described approximately flow velocity, perhaps less than 65% of described approximately flow velocity.
21. according to the described mixing arrangement of each claim among the claim 11-20, wherein, described catalytic reactor is the vertical hydroprocessing reactor that has steam and liquid and flow to current downflow, and hydrocarbon is left with the gas reaction of being rich in hydrogen at the hydroprocessing catalyst in this reactor.
22. a catalytic reactor comprises the upper catalyst bed layer, the described mixing arrangement of each claim among subordinate's beds and the claim 1-21.
23. catalytic reactor, comprise the upper catalyst bed layer, the described mixing arrangement of each claim among subordinate's beds and the claim 11-21, wherein, described mixing arrangement is from a plurality of at least first whole gradient to described top wall or base wall outer rim respective point of described top wall or base wall outer rim, from the maximum deviation of first point separately be lower than respectively angle maximum angle with horizontal plane be 11.5 ° 20%.
24. reactor according to claim 23, wherein, described top and described base wall are essentially the plane, preferablyly for being parallel to each other, and basic horizontal more preferably.
25. according to the described reactor of each claim of claim 23-24, wherein, lateral wall extends to the periphery of described base wall from the outer rim of described top wall, and is consistent with the shape and the size of the inner surface of the outer wall of described reactor vessel.
26. according to the described reactor of each claim of claim 23-25, wherein, described lateral wall is made of the outer wall of described reactor vessel.
27. according to the described reactor of each claim of claim 23-24, wherein, space between the outer wall of described lateral wall and described reactor vessel is intercepted or sealing by panel assembly or other blocking devices, mixing arrangement and reactor are held form a basic fluid-tight connection between the wall, force whole steam and liquid communication to cross described mixing arrangement.
28. according to the described reactor of each claim of claim 23-24, wherein, the cross-sectional area of the mixing arrangement of basic horizontal on the plane vertical with reactor wall be in the described reactor vessel cross-sectional area 25% to 100%.
29., wherein, be provided with flow device according to the described reactor of each claim of claim 22-28, be used between the first mixing mouthful upstream or two mixing mouths, introducing cooling fluid, make it to flow in the reactor vessel to cool off described process stream thigh.
30. between the inherent upper catalyst bed layer of a catalytic reactor and the subordinate's beds and flow the method for mist or steam and liquid, said method comprising the steps of:
The cross-sectional area of whole liquid and vapor mixing stream is compressed for the first time, so that the fricton-tight two-phase flow velocity of the described mixed flow at least one operational phase of described reactor be 3m/s to 15m/s, more preferably be enough to make liquid dispersion in steam and/or steam be distributed in the liquid;
Afterwards described cross-sectional area is enlarged for the first time;
Then described cross-sectional area is compressed for the second time, the fricton-tight two-phase flow velocity that makes described mixed flow be 3 m/s to 15m/s, more preferably be enough to make liquid dispersion in steam and/or steam be distributed in the liquid;
Described mixed flow is flowed along a flow channel, and this flow channel comprises the flow channel part that the physical length along whole flow channel of at least one basic horizontal is provided with.
31. method according to claim 30, wherein, described physical length is at least 50% of described whole flow channel, it is 55% of described whole flow channel preferablyly, it is 60% of described whole flow channel preferablyly, it is 65% of described whole flow channel preferablyly, it is 70% of described whole flow channel preferablyly, it is 75% of described whole flow channel preferablyly, it is 80% of described whole flow channel preferablyly, be 85% of described whole flow channel, be 90% of described whole flow channel preferablyly preferablyly.
32. according to claim 30 or 31 described methods, wherein after compression for the second time, described method also comprises the step that described cross-sectional area is enlarged once more.
33. according to the described method of each claim of claim 30-32, wherein, the step that enlarges described cross-sectional area comprise described mixed flow be divided at least two independent, equal-sized preferablyly two phase flow or logistics.
34. according to the described method of each claim of claim 30-33, wherein, at least one operational phase, the described fricton-tight two-phase flow velocity of described mixed flow is 3.5m/s to 14.5 during compression at described reactor.
35. according to the described method of each claim of claim 30-34, wherein, at described reactor at least one operational phase, the described fricton-tight two-phase flow velocity of described mixed flow is 3.5m/s to 14 during compression, and for example, 3.5m/s is to 4m/s, 4m/s is to 5m/s, and 5m/s is to 6m/s, and 6m/s is to 7m/s, 7m/s is to 8m/s, and 8m/s is to 9m/s, and 9m/s is to 10m/s, 10m/s is to 11m/s, and 11m/s is to 12m/s, and 12m/s is to 13m/s, 13m/s is to 14m/s, and 3.5m/s is to 13m/s, and 3.5m/s is to 12m/s, 3.5m/s to 11m/s, 3.5m/s is to 10m/s, 5m/s is to 9m/s, 3.5m/s to 8m/s, 3.5m/s is to 7m/s, 3.5m/s is to 6m/s, 3.5m/s to 5m/s, 6m/s is to 14m/s, and 6m/s is to 13m/s, and 6m/s is to 12m/s, 6m/s is to 11m/s, 6m/s is to 10m/s, and 6m/s is to 9m/s, and perhaps 6m/s is to 8m/s.
36. according to the described method of each claim of claim 30-34, wherein, at least one operational phase, the described fricton-tight two-phase flow velocity of described mixed flow is 4.0m/s to 12.5 during compression at described reactor, more preferably 8.1m/s is to 12.3m/s.
37. according to the described method of each claim of claim 31-34, also comprise a step, described cross-sectional area is compressed for the third time after the enlarged-area in the second time, so that the fricton-tight two-phase flow velocity of described mixed flow be enough to make liquid dispersion in gas and/or steam be distributed in the liquid, wherein, in at least one operational phase, the described fricton-tight two-phase flow velocity of described mixed flow is 3.5m/s to 10.5 during compression at described reactor, and more preferably 6.5m/s is to 10.1m/s.
38. according to the described method of each claim of claim 30-37, wherein this method also comprises a step, between the first mixing mouthful upstream or two mixing mouths, introduce a kind of cold cooling fluid, make it to flow in the reactor vessel to cool off described process-stream.
39. according to the described method of each claim of claim 30-38, wherein said catalytic reactor is the vertical hydroprocessing reactor that has steam and liquid and flow to current downflow, and hydrocarbon is left with the gas reaction of being rich in hydrogen at the hydroprocessing catalyst in this reactor.
40. product according to the described method preparation of claim 30-38.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DKPA200201718 | 2002-11-08 | ||
| DKPA200201718 | 2002-11-08 |
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| Publication Number | Publication Date |
|---|---|
| CN1732040A CN1732040A (en) | 2006-02-08 |
| CN100355494C true CN100355494C (en) | 2007-12-19 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2003801073442A Expired - Lifetime CN100355494C (en) | 2002-11-08 | 2003-11-05 | Mixing device for two-phase concurrent vessels |
Country Status (6)
| Country | Link |
|---|---|
| EP (1) | EP1562697A1 (en) |
| JP (1) | JP4741237B2 (en) |
| CN (1) | CN100355494C (en) |
| AU (1) | AU2003277837A1 (en) |
| EA (1) | EA007052B1 (en) |
| WO (1) | WO2004041426A1 (en) |
Families Citing this family (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102007034715A1 (en) * | 2007-07-23 | 2009-01-29 | Evonik Röhm Gmbh | Reactor for the production of hydrogen cyanide by the Andrussow method |
| FR2952835B1 (en) * | 2009-11-20 | 2011-12-09 | Inst Francais Du Petrole | COMPACT DEVICE FOR MIXING FLUIDS IN A DOWNFLOW REACTOR |
| ES2479465T3 (en) * | 2010-04-23 | 2014-07-24 | Neste Oil Oyj | Power distribution device for a separation column |
| US8841495B2 (en) * | 2011-04-18 | 2014-09-23 | Gas Technology Institute | Bubbling bed catalytic hydropyrolysis process utilizing larger catalyst particles and smaller biomass particles featuring an anti-slugging reactor |
| FR2989006B1 (en) * | 2012-04-04 | 2016-11-18 | Ifp Energies Now | CATALYTIC REACTOR WITH TEMPERATURE DEVICE PROVIDED WITH TANGENTIAL INJECTION OF A TEMPERED FLUID |
| JP6367831B2 (en) * | 2013-02-05 | 2018-08-01 | ハルドール・トプサー・アクチエゼルスカベット | Mixing device for reactor |
| US9359563B2 (en) | 2013-04-15 | 2016-06-07 | Uop Llc | Hydroprocessing initializing process and apparatus relating thereto |
| FR3034325B1 (en) * | 2015-04-01 | 2017-03-17 | Ifp Energies Now | COMPACT DISPOSITION OF MIXING AND COMBINED DISTRIBUTION |
| FR3034324B1 (en) * | 2015-04-01 | 2017-03-17 | Ifp Energies Now | MIXING AND DISPENSING DEVICE COMPRISING A DISPENSING TRAY WITH PERIPHERAL OPENINGS |
| FR3034323B1 (en) * | 2015-04-01 | 2017-03-17 | Ifp Energies Now | MIXING AND DISPENSING DEVICE WITH MIXING AND EXCHANGE ZONES |
| US9828897B2 (en) * | 2015-04-30 | 2017-11-28 | Faurecia Emissions Control Technologies Usa, Llc | Mixer for a vehicle exhaust system |
| FR3050658B1 (en) * | 2016-04-29 | 2018-04-20 | IFP Energies Nouvelles | DEVICE FOR MIXING AND DISPENSING WITH MIXING AND EXCHANGE ZONES AND DEFLECTORS. |
| FR3078636B1 (en) * | 2018-03-07 | 2020-03-13 | IFP Energies Nouvelles | MIXING DEVICE LOCATED ABOVE THE DISTRIBUTION AREA |
| CN111013495B (en) * | 2018-10-10 | 2022-03-11 | 中国石油化工股份有限公司 | Intersegment feeding structure of multi-section fixed bed reactor, multi-section fixed bed reactor and application of intersegment feeding structure |
| US10589244B1 (en) * | 2019-02-07 | 2020-03-17 | Uop Llc | Hydroprocessing reactor internals having reduced height |
| CN111659320B (en) * | 2020-06-15 | 2022-08-05 | 中国石油化工股份有限公司 | Hydrogen cooling box for hydrogenation reactor |
| US11207650B1 (en) * | 2020-09-30 | 2021-12-28 | Uop Llc | Hydroprocessing reactor internals having reduced height |
| CN112691568A (en) * | 2021-01-12 | 2021-04-23 | 陕西青叶生物科技有限公司 | Mixing stirrer for preparing hypochlorous acid solution |
| CN113636683B (en) * | 2021-08-18 | 2023-03-21 | 塔里木大学 | Inorganic chemistry experiment sewage treatment plant |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3592612A (en) * | 1966-11-02 | 1971-07-13 | John H Ballard | Two-stage apparatus for mixing fluids in concurrent downflow relationship |
| US3705016A (en) * | 1970-11-20 | 1972-12-05 | Universal Oil Prod Co | Fluid-solids contacting chamber |
| US4233269A (en) * | 1978-11-09 | 1980-11-11 | Exxon Research & Engineering Co. | Gas liquid distributor |
| US4669890A (en) * | 1985-03-25 | 1987-06-02 | Uop Inc. | Mixing device for vertical flow fluid-solid contacting |
| US5690896A (en) * | 1995-05-05 | 1997-11-25 | Chevron U.S.A. Inc. | Distributor assembly for multi-bed down-flow catalytic reactors |
| JP3676437B2 (en) * | 1995-07-10 | 2005-07-27 | 新日本石油株式会社 | Reaction tower |
-
2003
- 2003-11-05 CN CNB2003801073442A patent/CN100355494C/en not_active Expired - Lifetime
- 2003-11-05 JP JP2004548687A patent/JP4741237B2/en not_active Expired - Lifetime
- 2003-11-05 EP EP03769259A patent/EP1562697A1/en not_active Ceased
- 2003-11-05 EA EA200500791A patent/EA007052B1/en unknown
- 2003-11-05 WO PCT/DK2003/000757 patent/WO2004041426A1/en active Application Filing
- 2003-11-05 AU AU2003277837A patent/AU2003277837A1/en not_active Abandoned
Also Published As
| Publication number | Publication date |
|---|---|
| EA007052B1 (en) | 2006-06-30 |
| EA200500791A1 (en) | 2005-12-29 |
| WO2004041426A1 (en) | 2004-05-21 |
| EP1562697A1 (en) | 2005-08-17 |
| JP4741237B2 (en) | 2011-08-03 |
| AU2003277837A1 (en) | 2004-06-07 |
| CN1732040A (en) | 2006-02-08 |
| JP2006505388A (en) | 2006-02-16 |
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