CN106955644A - The feed distributor of the fluidized-bed reactor reacted for ammoxidation - Google Patents
The feed distributor of the fluidized-bed reactor reacted for ammoxidation Download PDFInfo
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- CN106955644A CN106955644A CN201610011756.5A CN201610011756A CN106955644A CN 106955644 A CN106955644 A CN 106955644A CN 201610011756 A CN201610011756 A CN 201610011756A CN 106955644 A CN106955644 A CN 106955644A
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- China
- Prior art keywords
- orifice
- aperture
- supervisor
- feed distributor
- branch pipe
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- 238000006243 chemical reaction Methods 0.000 claims abstract description 47
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 15
- 239000012530 fluid Substances 0.000 claims abstract description 11
- 238000004891 communication Methods 0.000 claims abstract description 7
- 239000004744 fabric Substances 0.000 claims description 7
- GLAKNHGQBRSLIO-UHFFFAOYSA-N azane;prop-1-ene Chemical compound N.CC=C GLAKNHGQBRSLIO-UHFFFAOYSA-N 0.000 abstract description 41
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 abstract description 23
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 abstract description 23
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 abstract description 8
- 238000007086 side reaction Methods 0.000 abstract description 3
- 238000005304 joining Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 85
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 25
- 239000008246 gaseous mixture Substances 0.000 description 13
- 229910021529 ammonia Inorganic materials 0.000 description 12
- 239000003054 catalyst Substances 0.000 description 9
- HRPVXLWXLXDGHG-UHFFFAOYSA-N Acrylamide Chemical compound NC(=O)C=C HRPVXLWXLXDGHG-UHFFFAOYSA-N 0.000 description 8
- 230000000052 comparative effect Effects 0.000 description 7
- 238000000034 method Methods 0.000 description 7
- 239000007921 spray Substances 0.000 description 7
- 238000009826 distribution Methods 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- 150000001336 alkenes Chemical class 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000005299 abrasion Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 206010054949 Metaplasia Diseases 0.000 description 1
- KCTXIKYLOYGADP-UHFFFAOYSA-N [O].N.C=CC Chemical compound [O].N.C=CC KCTXIKYLOYGADP-UHFFFAOYSA-N 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000003090 exacerbative effect Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 230000015689 metaplastic ossification Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000004080 punching Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C253/00—Preparation of carboxylic acid nitriles
- C07C253/24—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
- C07C253/26—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/00911—Sparger-type feeding elements
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of fluidized-bed reactor unstripped gas feed distributor for ammoxidation reaction.A kind of fluidized-bed reactor unstripped gas feed distributor for ammoxidation reaction, including：For the branch pipe for being used to shunt unstripped gas for connecting the supervisor of unstripped gas entrance and being in fluid communication with the supervisor, there is the orifice for being used for unstripped gas charging on supervisor or branch pipe, wherein, along along unstripped gas flow direction, the aperture of supervisor or any one orifice on branch pipe be equal to or more than close to upstream side orifice aperture.The propylene ammonia feed distributor for the fluidized-bed reactor that ammoxidation of propylene reacts is used for according to the present invention, by joining with the gas temperature in conduit, pressure correlation, reasonably determine orifice aperture, it can make propylene ammonia more even into fluidized-bed reactor inside, so as to significantly improve the yield of acrylonitrile and the conversion ratio of propylene, and side reaction is significantly inhibited, reduce CO2Amount.
Description
Background technology
It is industrial to utilize fluidized-bed reactor to carry out ammoxidation reaction for a long time.In general it is this kind of anti-
Answering device includes a container, and the distributor for transmitting and disperseing to include organic unstrpped gas
With for transmit and decentralized oxygen gas distributor, wherein, distributor generally comprises conveying gas
The conduit of body, and perforate is provided with conduit in order to the discharge of unstripped gas and oxygen-containing gas.
For example, countries in the world generally produce acrylonitrile using propylene ammmoxidation process, this is an allusion quotation
The example that ammoxidation of propylene reaction is carried out using fluidized-bed reactor of type.Utilizing propylene ammonia oxygen
During metaplasia production acrylonitrile, there are certain ratio requirement, the ratio of such as ammonia and propylene to raw material
Value should be 1~1.5, and the ratio of air and propylene should be 8.5~10.5.In fact, this ratio
Also in the range of the explosion limit for being exactly in propylene ammonia.Therefore, in process of production, not will
Be re-fed into after propylene, the three kinds of unstripped gas mixing of ammonia and air in reaction bed, but by this three
Plant unstripped gas and be introduced separately bed by two distributors：Propylene mixed with ammonia after by one point
Cloth device enters bed, and air is to enter bed by another distributor, to avoid raw material air lift
Preceding reaction is exploded.
When carrying out ammoxidation reaction using fluidized-bed reactor, the mol ratio pair of reacting gas
The influence of reaction yield is very big：When empty higher than (air and propylene gas mol ratio), depth oxygen
Change ratio is improved, and therefore reaction yield declines；And when empty than (air and propylene gas mol ratio)
When low, unreacted Organic Ingredients ratio increase, reaction yield equally declines.Therefore reactor
It is necessary to have correct mol ratio for the reacting gas of interior mixing.
Prior art is disclosed being reacted for ammoxidation such as BP NO.1265770
In fluidized-bed reactor, the nozzle on the nozzle and Acrylamide distributor of dispersion plate should be one by one
Correspondence, toward each other, but the patent does not illustrate and unstripped gas is sent on Acrylamide distributor
Opening aperture.CN1172440A has described third in a kind of fluidized-bed reactor in greater detail
The ratio model of opening orifice pore-size distribution and maximum diameter of hole and minimum-value aperture on alkene ammonia distributor
Enclose, it is believed that the mass flow of the gaseous mixture flowed out at Acrylamide distributor opening depends primarily on gas
Temperature, therefore propose the big of orifice aperture that be open of the gaseous mixture discharge on Acrylamide distributor
It is small only relevant with gas temperature.But in fact, in ammoxidation of propylene course of reaction, due to third
Alkene ammonia feed distributor takes the mixture pressure in multitube form, distributor to change not only
There is the pressure loss along journey, the change of pressure caused by factor also including Variable Mass Flow etc..Especially
It is the maximization with device, supervisor/branch length of tube of feed distributor all increased, supervisor/
The pressure differential that near-end and distal nozzle on more nozzles, conduit are distributed on branch pipe just becomes apparent from
.Therefore, for large-scale propylene ammonoxidizing fluid bed reactor, if not taking in pressure
Power changes the influence to aperture, will certainly cause the problem of unstripped gas distribution is uneven, finally influence
To reaction yield.
The content of the invention
The present invention provides a kind of fluidized-bed reactor unstripped gas for ammoxidation reaction and feeds distribution
Device, including：For connecting the supervisor of unstripped gas entrance and being responsible for being used for for fluid communication with described
Shunt has for the sharp of unstripped gas charging on the branch pipe of unstripped gas, the supervisor or the branch pipe
Hole, wherein,
Along along unstripped gas flow direction, any one orifice on the supervisor or the branch pipe
Aperture be equal to or more than close to upstream side orifice aperture.
According to the feed distributor of the present invention, it is preferable that appointing on the supervisor or the branch pipe
Anticipate an orifice aperture compared to close to the aperture ratio in aperture of upstream side orifice exist
Between 1.0~1.080.
According to the feed distributor of the present invention, it is preferable that appointing on the supervisor or the branch pipe
Anticipate an orifice aperture compared to close to the aperture ratio in aperture of upstream side orifice exist
Between 1.0~1.060.
According to the feed distributor of the present invention, it is preferable that appointing on the supervisor or the branch pipe
Anticipate an orifice aperture compared to close to the aperture ratio in aperture of upstream side orifice exist
Between 1.0~1.040.
According to the feed distributor of the present invention, it is preferable that appointing on the supervisor or the branch pipe
Anticipate an orifice aperture compared to close to the aperture ratio in aperture of upstream side orifice exist
Between 1.0~1.020.
According to the feed distributor of the present invention, it is preferable that appointing on the supervisor or the branch pipe
Anticipate an orifice aperture compared to close to the aperture ratio in aperture of upstream side orifice exist
Between 1.0~1.015.
According to the feed distributor of the present invention, it is preferable that appointing on the supervisor or the branch pipe
Anticipate an orifice aperture compared to close to the aperture ratio in aperture of upstream side orifice exist
Between 1.0~1.010.
According to the feed distributor of the present invention, it is preferable that when the fluidized-bed reactor is a diameter of
At 10~15 meters, the aperture of the supervisor or the maximum orifice on the branch pipe and minimum orifice
Aperture between ratio be 1.05~1.15 between.
According to the feed distributor of the present invention, it is preferable that when the fluidized-bed reactor is a diameter of
At 10~15 meters, the aperture of the supervisor or the maximum orifice on the branch pipe and minimum orifice
Aperture between ratio be 1.08~1.12 between.
According to the feed distributor of the present invention, it is preferable that when the fluidized-bed reactor is a diameter of
At 5~10 meters, the aperture of the supervisor or the maximum orifice on the branch pipe and minimum orifice
Aperture between ratio be 1.02~1.13 between.
According to the feed distributor of the present invention, it is preferable that when the fluidized-bed reactor is a diameter of
At 5~10 meters, the aperture of the supervisor or the maximum orifice on the branch pipe and minimum orifice
Aperture between ratio be 1.05~1.11 between.
According to the feed distributor of the present invention, it is preferable that on the unstripped gas feed distributor
The aperture of the orifice is 3.0~10.0mm.
According to the feed distributor of the present invention, it is preferable that on the unstripped gas feed distributor
The aperture of the orifice is 3.5~9.0mm.
According to the feed distributor of the present invention, it is preferable that on the unstripped gas feed distributor
The aperture of the orifice is 4.0~7.5mm.
According to the feed distributor of the present invention, it is preferable that the phase on the supervisor or the branch pipe
Pitch of holes between adjacent orifice is 100~300mm.
According to the feed distributor of the present invention, it is preferable that the phase on the supervisor or the branch pipe
Pitch of holes between adjacent orifice is 125~275mm.
According to the feed distributor of the present invention, it is preferable that the phase on the supervisor or the branch pipe
Pitch of holes between adjacent orifice is 150~225mm.
The effect of the present invention
According to the present invention propylene ammonia feed distributor, by with the gas temperature in conduit, pressure
Power is associated, and reasonably determines orifice aperture, can make propylene ammonia more even into fluidisation
Bed inside reactor, so as to significantly improve the yield of acrylonitrile and the conversion ratio of propylene, and shows
Write and suppress side reaction, reduce CO2Amount.
Brief description of the drawings
Figure 1A and Figure 1B respectively illustrate the fluidized-bed reaction for ammoxidation reaction of the present invention
The example of the propylene ammonia feed distributor of device.
Fig. 2A and Fig. 2 B respectively illustrate the nozzle signal of the propylene ammonia feed distributor of the present invention
Figure, including propylene ammonia feed distributor nozzle and orifice.
Fig. 3 is the schematic diagram of the propylene ammonia feed distributor of the present invention.
Embodiment
Hereinafter, the embodiment that the present invention is described in detail with reference to the accompanying drawings will be combined.But this
Invention is not construed to limited to these specific embodiments.
The present invention provides a kind of feed distributor for fluidized-bed reactor.The feed distributor
It is intended to improve the ammoxidation reaction device of industrial practicality, does not have to the ammoxidation reaction applied
There is special limitation.
Figure 1A shows an instantiation of the feed distributor of the present invention, and it is related to one kind third
Alkene ammonia feed distributor, the propylene ammonia feed distributor can be applied to industrialized production acrylonitrile
In fluidized-bed reactor.Figure 1B shows another specific propylene ammonia charging distribution of the present invention
Device embodiment.Fig. 2A and Fig. 2 B are the nozzle schematic diagrames of the propylene ammonia feed distributor of the present invention,
Wherein 6 be propylene ammonia feed distributor branch pipe cross section, and 7 be to connect with feed distributor branch pipe fluid
Logical nozzle, 8 be the orifice on feed distributor branch pipe.Fig. 3 is the propylene ammonia charging of the present invention
The schematic diagram of distributor.
According to the present invention, the propylene ammonia feed distributor shown in Figure 1A can include：Distributor enters
Mouthful, and the feed distributor supervisor that distributor inlet is in fluid communication, and be in fluid communication with supervisor
Branch pipe；Also, on the supervisor and branch pipe of feed distributor, or only in feed distributor
Branch pipe on, the opening equidistantly provided with referred to as orifice；The supervisor is with branch pipe and positioned at pipe
Nozzle outside line is in fluid communication by the orifice, another distal opening of nozzle so as to it is anti-
Answer device internal fluid communication.Therefore, material mixed gas enter after feed distributor from porch,
Each branch pipe is sent to along the supervisor of feed distributor, then via feed distributor supervisor and/or branch pipe
On orifice be ejected into nozzle, the reaction of reactor is finally entered by nozzle end opening again
Bed.
The propylene ammonia feed distributor that the present invention is provided can be monomer as shown in Figure 1A, may be used also
To be the complex for including many sub- distributors as shown in Figure 1B.This little distributor is respectively provided with
Similar entrance-supervisor-branch pipe-orifice-nozzle arrangements, are connected in parallel with each other, and each distributor
Temperature, pressure residing for the unstripped gas of porch are the same.Preferably, in feed distributor
Many sub- distributors be it is identical, can be with substituted for one another.When fluidized-bed reactor charging point
When cloth device contains many sub- distributors, it is preferable that two neighboring sub- distributor inlet is along reactor
Wall circumferential distance is equal.
Each part of the propylene ammonia feed distributor can be in the same level section of reactor
On, can also be on the varying level section of reactor, but identical component should be limited to instead
Answer in the same level section of device.For example, the same referred to as charging distribution in each feed distributor
The many supervisors of device supervisor should be in same level section, with referred to as feed distributor branch pipe
All branch pipes should be in the same level section, with all of referred to as feed distributor nozzle
Nozzle, its end should be divided in same level section, and with the air below reactor
The vertical range of the nozzle of cloth device should be identical.
Embodiments in accordance with the present invention, the supervisor of the propylene ammonia feed distributor is preferably straight tube.
The branch pipe is straight tube or curved pipe.The branch pipe can come the both sides or the same side of supervisor,
And all branch pipes in same sub- distributor be parallel to each other (when for straight tube) or with one heart (when
During for curved pipe).Preferably, the axis (when for straight tube) of these branch pipes or tangent line (when
During for curved pipe) intersected vertically with the supervisor being connected.When branch pipe is located at supervisor both sides, branch
Pipe be mutually aligned with supervisor's cross or wrong cross.
As shown in Figure 2 A and 2B, according to the present invention, in the branch of the propylene ammonia feed distributor
Manage on (23,26), or the according to circumstances supervisor in the propylene ammonia feed distributor and branch
Guan Shang, along supervisor and/or branch pipe axis direction be arranged with referred to as orifice circular open (24,
28), for allowing gaseous mixture to spray into reactor out of feed distributor.The supervisor or branch pipe are logical
The nozzle (27) that the orifice is crossed with being correspondingly positioned at outside supervisor or branch pipe is connected, and gaseous mixture is therefore
After orifice sprays at a high speed, not directly into the reaction bed of inside reactor, but pass through
Circular open through the nozzle other end after nozzle rectification enters inside reactor.Orifice and charging point
Cloth device nozzle is coaxial, and positioned at the footpath with feed distributor supervisor or the central axis upright of branch pipe
To on section.According to the present invention, the aperture of the orifice is less than the nozzle and its distal opening
Diameter.
The orifice center of circle adjacent along along the axial direction of supervisor or branch pipe respectively on supervisor or branch pipe
Between vertical range in axial direction be referred to as pitch of holes.According to the present invention, for any propylene
For ammonia feed distributor, the pitch of holes of adjacent orifice is phase on the axial direction of any branch pipe
With；Equally, the pitch of holes of adjacent orifice is also identical on the axial direction of any supervisor.
Preferably, between orifice adjacent along along the axial direction of any branch pipe pitch of holes and along any
Pitch of holes on the axial direction of supervisor between adjacent orifice is also mutually equivalent.According to this
The embodiment of invention, the pitch of holes of the orifice can be typically 100~300mm, be preferably
125~275mm, more preferably 150~225mm.
As shown in Figure 2 A and 2B, according to the present invention, cut in the same radial direction of supervisor and/or branch pipe
An orifice can also be disposed with face or multiple orifices (correspond to this section in these orifice centers of circle
Face is referred to as orifice section).These orifices for being in same section are equally distinguished with corresponding nozzle
It is connected, and it is concentric with nozzle.According to the specific embodiment of the present invention, in the charging of propylene ammonia
Same radial section on the supervisor of distributor and/or branch pipe is arranged with same amount of orifice,
Multiple orifices in same radial section and multiple orifices difference one positioned at other radial sections
One correspondence, so that arranged in columns on the axial direction along corresponding supervisor or branch pipe, these row are with being somebody's turn to do
Supervisor or the diameter parallel of branch pipe.According to a preferred embodiment of the present invention, supervisor and/or
At least one orifice is set on the same radial section of branch pipe.
Skilled in the art realises that, according to the operating condition of the fluidized-bed reactor of application not
Together, the orifice aperture of the unstripped gas for being used for conveying mixing on feed distributor also needs to do mutually to strain
Change.It is, in general, that the orifice for transferring raw material gas can not be too big or too small.Orifice aperture is such as
It is really bigger than normal, easily cause catalyst and fall to alter by orifice into Acrylamide distributor supervisor or branch pipe
It is interior；This partial catalyst is in the atmosphere of propylene ammonia gaseous mixture, and unstripped gas propylene, ammonia are being urged
Agent surface carries out ammoxidation reaction, and final catalyst will be lost work by over reduction because of anoxic
Property；In addition, the catalyst entered in Acrylamide distributor supervisor or branch pipe can cause distributor
Local stoppages, cause unstripped gas skewness, influence the stable operation of reactor.Orifice aperture
If less than normal, unstripped gas perforation hole speed will increase；Too fast perforation Kong Su is exacerbated to catalysis
The abrasion of agent particle, while also exacerbating the abrasion to orifice to some extent.
According to the present invention, coordinate the higher operation lines speed of existing acrylonitrile reactor device, this
The punching rate of unstripped gas in the acrylonitrile feeder of setting is invented in the range of 60~250m/s,
It is preferred that 80~230m/s, more preferably 100~200m/s.Set according to this, the propylene ammonia charging point
Orifice diameter on cloth device is advisable with 3.0~10.0mm, preferably 3.5~9.0mm, more preferably
For 4.0~7.5mm.In this case, you can to reach the purpose of uniform gas distribution, it can also avoid
Catalyst falls to alter and the possibility that catalyst and orifice wear and tear is minimized.
In addition, the good yield in order to ensure ammoxidation of propylene reaction, those skilled in the art
Reacting gas mol ratio in solution, ammonia oxidation reactor must be well controlled：Local gas
If body mol ratio skewness, the yield of whole reactor will be significantly reduced.Therefore,
How the aperture of each orifice is designed, it is ensured that sprayed from each orifice of feeder diverse location
Gaseous mixture has identical mass flow so that the unstrpped gas blown out in feed distributor is uniform
It is distributed in reactor, is the key of feeder design.
Disclosed document and technique teaching notes, using the nozzle on Acrylamide distributor with being placed in stream
Perforate on air sparger below fluidized bed reactor is corresponded, make it that propylene ammonia is fed
The oxygen-containing air that the propylene and the mixed gas of ammonia that distributor sprays can spray with air sparger
Realize that one blows for a pair, so as to facilitate propylene, ammonia and air being uniformly distributed in reactor.In
State's patent 96191736.9 further discloses the unstripped gas outlet needs on Acrylamide distributor
Using different apertures.According to the patent application, need to close during design unstripped gas outlet aperture
What key considered is the change of gas temperature in reactor.In the fill process of unstripped gas, gas
Length, gas temperature and the bed temperature that the elevated degree of temperature is advanced in the catheter with gas it
Difference and change.The length that gas is advanced in the catheter is longer, and the heat exchanger time of experience is longer,
Gas temperature is corresponding also higher.Sometimes, the nozzle at the air inlet with branch pipe distally
The temperature difference of nozzle can 50~200 DEG C, even more high.Therefore, in ammoxidation feed distributor
It is former with the increase of stroke of the unstripped gas in reactor on the airflow direction of supervisor or branch pipe
Material gas gradually heats up, and therefore density diminish, therefore corresponding orifice diameter needs gradually to increase.
But inventor calculates and tested by a large amount of, finds to cause what is flowed out from each orifice
Mixed material gas has identical mass flow, it is necessary to which the factor considered includes the density of gaseous mixture
And gas perforation pressure difference etc.；And mixed gas density be based primarily upon residing working condition such as temperature,
Pressure etc..Therefore, to realize and allow each nozzle there is identical mass flow, the diameter D of orifice
Need with mixed gas density (ρ) and gas perforation pressure differential deltap P1 associate together with consider, its
Correlation can be expressed as D4∝1/(ρ*ΔP1).And mixed gas density ρ with residing for gas
Temperature T it is relevant with pressure P, ρ ∝ P/T.
In fact, the ammoxidation feed distributor that modern fluid bed reactor is used is generally multitube
Air distributor, the change of gas pressure is influenceed by many wherein.As shown in figure 3,
Gas sentences certain speed flow forward along supervisor 31, when by branch pipe 33, some
Gas flows out toward the direction of side line branch pipe 33, and residual gas continues the flow forward along supervisor 32；
Equally, gas with certain speed along at branch pipe 35 to flowing at distal end branch pipe 36, by spray
During mouth, some gas flows out toward side line nozzle direction, and residual gas continues along branch pipe to remote
Hold and flowed at 36.By this way, in propylene ammonia feed distributor, propylene ammonia gaseous mixture edge
Conduit flows through each nozzle dispersion into bed, no matter in feed distributor supervisor or branch pipe,
Gas quality in flow process is constantly reduced.And propylene ammonia gaseous mixture is in flow process,
The kinetic energy of gaseous fluid is also to be continually changing.Still so that shown in Fig. 3, mixed gas is in supervisor
Kinetic energy at 31 is higher than being responsible at 32, equally, and the kinetic energy at branch pipe 35 is higher than branch pipe 36
Place.Meanwhile, gas also by along frictional resistance of the Cheng Guandao walls to it, and along journey with
The heat exchange of reacting gas etc., these aspect factors result in the change of gas pressure in conduit.
Inventor has found that the pressure of the gaseous mixture at each nozzle can pass through appropriate variable mass
Flow theory etc. is calculated and determined.So, it is distributed according to propylene ammonia charging in fluidized-bed reactor
The characteristics of device, as gas is in the Bottomhole pressure of leading of propylene ammonia feed distributor, inventor has found
The gas pressure at branch pipe end nozzle is reached to be likely to be breached with distributor inlet gas pressure difference
- 2.5Kpa~+3.0Kpa, or it is bigger.Such change of gas pressure can not only draw in conduit
The change of gas density is played, while also causing perforation pressure differential deltap P1 change.It was recognized by the inventor that
When unit scale is smaller, such as when reactor diameter is 7 meters or less, temperature is straight to orifice
The influence in footpath is the effect determined, and pressure change of the gaseous mixture in the conduit of feed distributor
Not very acutely, the influence to orifice diameter is smaller.But with the increase of unit scale,
The increase of reactor diameter, the amplitude of pressure change of the gaseous mixture in the conduit of feed distributor
It is significantly increased.Therefore, in this case, the determination of orifice diameter is needed while and gas temperature
Degree and pressure are associated could be accurate, so as to can make it that each nozzle of feed distributor sprays
The mass flow of gaseous mixture is more consistent, and gas is more evenly distributed, and reaction result is also more preferable.
Found more than, inventor provide a kind of improved propylene ammonia feed distributor, its
With it is following the characteristics of：Along feed distributor supervisor or branch pipe, the side advanced along unstripped gas
To the orifice diameter nearer from distributor inlet is smaller, and the orifice more remote from distributor inlet is straight
Footpath is bigger.Here, it should be understood to mean just from distributor inlet " nearer " or " more remote "
Unstripped gas (is responsible for or branch pipe) in distributor ducts for the length of interior course, closer to
Or further from distributor inlet, the calculating of the travel path should start from the nearly distributor inlet of conduit
Hold and spray finally at the orifice opening of unstripped gas.According to the present invention, it is responsible for along feed distributor
Or branch pipe, on the direct of travel of unstripped gas, the change ratio in the aperture of two neighboring orifice exists
Between 1.0~1.080, between preferably 1.0~1.060, between more preferably 1.0~1.040, also
Between more preferably 1.0~1.020, between most preferably 1.0~1.015.In the present invention, institute
It can be continuous change to state orifice diameter, i.e., each thereon by the travel path of unstripped gas air inlet
Do minor adjustment in individual orifice aperture；Can also be that staged changes, i.e., by unstripped gas air inlet
Travel path, if adjacent dry hole can have same aperture thereon, is then jumped to down again
One orifice aperture level, keeps identical aperture, successively class between several adjacent holes
Push away.When carrying out the adjustment of staged change, with the proviso that the unstripped gas quality stream of each orifice
Measure uniformity.
Skilled in the art realises that, the adjustment in orifice aperture on foregoing propylene ammonia feed distributor,
Purpose is in order that the mass flow of the unstripped gas on feed distributor through each orifice becomes more
Uniformity, so as to improve the yield of ammoxidation of propylene reaction.According to one of present invention implementation
Example, improved propylene ammonia feed distributor provided by the present invention, it passes through any one orifice
Material mixed gas mass flow and the quality stream by the material mixed gas of any other orifice
Amount is compared, and difference can be controlled within 3%；Preferably, the difference can be controlled 1.5%
Within；It is highly preferred that the difference can be controlled within 1%.
According to the present invention, described propylene ammonia feed distributor, the varying aperture amplitude of its orifice
Limited by the diameter of reactor.In general, reactor diameter is bigger, and the propylene ammonia enters
Expect that the amplitude of variation in the orifice aperture of distributor is bigger.According to one embodiment of present invention, when
When reactor diameter is 10~15 meters, the ratio between its maximum diameter of hole and minimum-value aperture can be 1.05~1.15
In the range of；Preferably, the ratio can be in the range of 1.08~1.12.And when reactor diameter is
At 5~10 meters, the ratio between its maximum diameter of hole and minimum-value aperture can be in the range of 1.02~1.13；It is preferred that
Ground, the ratio can be in the range of 1.05~1.11.
According to the present invention, the reaction temperature of the propylene ammonia fluidized-bed reactor is taken the photograph 420~460
Family name's degree, reaction pressure is in 0.4~0.8kg/cm2, the mol ratio of propylene, ammonia and air is in reaction
1:1.1~1.3:9.0~10.5.Those skilled in the art understand, in addition to this specification is clearly stated,
Other process conditions in known document on ammoxidation reaction also can be used.It is any of
The catalyst of ammoxidation reaction can make the catalyst of the present invention.
Embodiment
The present invention, but this are further illustrated referring to the specific embodiment and comparative example of the present invention
Invention can not be construed to be limited.It is not anti-in reacting gas in embodiment and comparative example
Answer olefine gas chromatography analysis.The component and reaction condition of reactor are except special instruction
Outer be in typically uses scope, does not influence reaction result.
Comparative example 1：Reaction process condition：440 DEG C of reaction temperature, reaction pressure 60KPa,
C3:NH3:Air is 1：1.2：9.5, catalyst loading：0.08h~1.7 meters of reactor diameter,
Air feed distributor to use and set 4 altogether on identical orifice diameter, propylene ammonia feed distributor
Various sizes of orifice is planted, corresponding aperture is respectively 4.3mm, 4.6mm, 4.9mm and 5.2
mm.Reaction result is shown in Table 1.
Embodiment 1：With the identical reaction process condition of comparative example 1.7 meters of reactor diameter,
Air feed distributor to use and set 5 altogether on identical orifice diameter, propylene ammonia feed distributor
Various sizes of orifice is planted, corresponding aperture is respectively 4.5mm, 4.6mm, 4.7mm, 4.8
Mm and 4.9mm.Reaction result is shown in Table 1.
Embodiment 2：With the identical reaction process condition of comparative example 1.9 meters of reactor diameter,
Air feed distributor to use and set 6 altogether on identical orifice diameter, propylene ammonia feed distributor
Various sizes of orifice is planted, corresponding aperture is respectively 6.5mm, 6.6mm, 6.7mm, 6.8
Mm, 6.9mm and 7.0mm.Reaction result is shown in Table 1.
Embodiment 3：With the identical reaction process condition of comparative example 1.12 meters of reactor diameter,
Air feed distributor to use and set 8 altogether on identical orifice diameter, propylene ammonia feed distributor
Various sizes of orifice is planted, corresponding aperture is respectively 5.8mm, 5.9mm, 6.0mm, 6.1
Mm, 6.2mm, 6.3mm, 6.4mm and 6.5mm.Reaction result is shown in Table 1.
Table 1：
| AN% | Propylene conversion % | CO2% | |
| Comparative example 1 | 79.3 | 97.0 | 5.8 |
| Embodiment 2 | 80.2 | 99.1 | 4.9 |
| Embodiment 3 | 80.8 | 99.2 | 4.8 |
| Embodiment 4 | 80.6 | 98.9 | 5.0 |
As shown in Table 1, the fluidized-bed reaction reacted for ammoxidation of propylene of the invention
The propylene ammonia feed distributor of device, by joining with the gas temperature in conduit, pressure correlation, comes
It is rational to determine orifice aperture, it can make propylene ammonia more even into fluidized-bed reactor inside,
So as to significantly improve the yield of acrylonitrile and the conversion ratio of propylene, and significantly inhibit side reaction,
Reduce CO2Amount.
Claims (17)
1. a kind of fluidized-bed reactor unstripped gas feed distributor for ammoxidation reaction, bag
Include：For connecting the supervisor of unstripped gas entrance and with supervisor's fluid communication for shunting original
Expect that there is the orifice for being used for unstripped gas charging on the branch pipe of gas, the supervisor or the branch pipe, its
In,
Along along unstripped gas flow direction, any one orifice on the supervisor or the branch pipe
Aperture be equal to or more than close to upstream side orifice aperture.
2. feed distributor as claimed in claim 1, wherein, the supervisor or the branch pipe
On any one orifice aperture compared to close to the aperture ratio in aperture of upstream side orifice exist
Between 1.0~1.080.
3. feed distributor as claimed in claim 1, wherein, the supervisor or the branch pipe
On any one orifice aperture compared to close to the aperture ratio in aperture of upstream side orifice exist
Between 1.0~1.060.
4. feed distributor as claimed in claim 1, wherein, the supervisor or the branch pipe
On any one orifice aperture compared to close to the aperture ratio in aperture of upstream side orifice exist
Between 1.0~1.040.
5. feed distributor as claimed in claim 1, wherein, the supervisor or the branch pipe
On any one orifice aperture compared to close to the aperture ratio in aperture of upstream side orifice exist
Between 1.0~1.020.
6. feed distributor as claimed in claim 1, wherein, the supervisor or the branch pipe
On any one orifice aperture compared to close to the aperture ratio in aperture of upstream side orifice exist
Between 1.0~1.015.
7. feed distributor as claimed in claim 1, wherein, the supervisor or the branch pipe
On any one orifice aperture compared to close to the aperture ratio in aperture of upstream side orifice exist
Between 1.0~1.010.
8. feed distributor as claimed in claim 1, wherein, when the fluidized-bed reactor
At a diameter of 10~15 meters, the aperture of the supervisor or the maximum orifice on the branch pipe with most
Ratio between the aperture of small orifice is between 1.05~1.15.
9. feed distributor as claimed in claim 8, wherein, the supervisor or the branch pipe
On the aperture of maximum orifice and the aperture of minimum orifice between ratio for 1.08~1.12 it
Between.
10. feed distributor as claimed in claim 1, wherein, when the fluidized-bed reaction
When device is a diameter of 5~10 meters, the aperture of the supervisor or the maximum orifice on the branch pipe with most
Ratio between the aperture of small orifice is between 1.02~1.13.
11. feed distributor as claimed in claim 10, wherein, the supervisor or the branch
Ratio between the aperture of maximum orifice on pipe and the aperture of minimum orifice is 1.05~1.11
Between.
12. the feed distributor as described in claim 1~11 any one, wherein, the original
The aperture for expecting the orifice on gas feed distributor is 3.0~10.0mm.
13. feed distributor as claimed in claim 12, wherein, the unstripped gas charging point
The aperture of the orifice on cloth device is 3.5~9.0mm.
14. feed distributor as claimed in claim 12, wherein, the unstripped gas charging point
The aperture of the orifice on cloth device is 4.0~7.5mm.
15. the feed distributor as described in claim 1~11 any one, wherein, the master
The pitch of holes between adjacent orifice on pipe or the branch pipe is 100~300mm.
16. feed distributor as claimed in claim 15, wherein, the supervisor or the branch
The pitch of holes between adjacent orifice on pipe is 125~275mm.
17. feed distributor as claimed in claim 15, wherein, the supervisor or the branch
The pitch of holes between adjacent orifice on pipe is 150~225mm.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610011756.5A CN106955644A (en) | 2016-01-08 | 2016-01-08 | The feed distributor of the fluidized-bed reactor reacted for ammoxidation |
| TW105128517A TWI803448B (en) | 2015-09-02 | 2016-09-02 | Reactor and method for producing acrylonitrile |
| KR1020160113191A KR102271764B1 (en) | 2015-09-02 | 2016-09-02 | Reactor for producing acrylonitrile and method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610011756.5A CN106955644A (en) | 2016-01-08 | 2016-01-08 | The feed distributor of the fluidized-bed reactor reacted for ammoxidation |
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|---|---|
| CN106955644A true CN106955644A (en) | 2017-07-18 |
Family
ID=59481267
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610011756.5A Pending CN106955644A (en) | 2015-09-02 | 2016-01-08 | The feed distributor of the fluidized-bed reactor reacted for ammoxidation |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107720758A (en) * | 2017-11-13 | 2018-02-23 | 浙江工业大学上虞研究院有限公司 | Chemical industry production system |
| CN110201610A (en) * | 2018-02-28 | 2019-09-06 | 国家能源投资集团有限责任公司 | Gas distributor and reactor |
| CN111676056A (en) * | 2020-06-19 | 2020-09-18 | 中耐工程科技有限公司 | Residual oil hydrogenation reactor with three-dimensional grid feeding structure, residual oil hydrogenation system containing reactor and residual oil hydrogenation process |
| JP2021502895A (en) * | 2017-11-14 | 2021-02-04 | 中国石油化工股▲ふん▼有限公司 | Fluid distributors, reactors and their applications |
| CN112439363A (en) * | 2019-09-05 | 2021-03-05 | 中石油吉林化工工程有限公司 | Propylene ammonia distributor |
| CN112439368A (en) * | 2019-09-05 | 2021-03-05 | 中石油吉林化工工程有限公司 | Reactor for preparing acrylonitrile |
| EP3711849A4 (en) * | 2017-11-14 | 2021-08-25 | China Petroleum & Chemical Corporation | Feed gas feeding system for propylene ammoxidation reactor |
| CN115055124A (en) * | 2022-06-22 | 2022-09-16 | 上海蓝科石化环保科技股份有限公司 | Acrylonitrile fluidized bed reaction device and process |
| CN117832052A (en) * | 2022-12-30 | 2024-04-05 | 江苏微镀新能源科技有限公司 | A gas release mechanism for vacuum coating ion source |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08208583A (en) * | 1995-02-01 | 1996-08-13 | Asahi Chem Ind Co Ltd | Apparatus for producing alpha, beta-unsaturated nitrile |
| CN1172440A (en) * | 1995-02-01 | 1998-02-04 | 旭化成工业株式会社 | Fluidized-bed reactor and reaction process using the same |
| CN1181063A (en) * | 1995-04-07 | 1998-05-06 | 旭化成工业株式会社 | Process for producing 'alpha', 'bela'-unsaturated nitrile |
| CN101985093A (en) * | 2009-07-29 | 2011-03-16 | 江苏新河农用化工有限公司 | Distribution plate for fluid bed reactor in ammoxidation |
| WO2015153193A1 (en) * | 2014-03-31 | 2015-10-08 | Ineos Europe Ag | Feed sparger design for an ammoxidation reactor |
| CN205797156U (en) * | 2016-01-08 | 2016-12-14 | 中国石油化工股份有限公司 | Feed distributor for the fluidized-bed reactor of ammoxidation reaction |
-
2016
- 2016-01-08 CN CN201610011756.5A patent/CN106955644A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08208583A (en) * | 1995-02-01 | 1996-08-13 | Asahi Chem Ind Co Ltd | Apparatus for producing alpha, beta-unsaturated nitrile |
| CN1172440A (en) * | 1995-02-01 | 1998-02-04 | 旭化成工业株式会社 | Fluidized-bed reactor and reaction process using the same |
| CN1181063A (en) * | 1995-04-07 | 1998-05-06 | 旭化成工业株式会社 | Process for producing 'alpha', 'bela'-unsaturated nitrile |
| CN101985093A (en) * | 2009-07-29 | 2011-03-16 | 江苏新河农用化工有限公司 | Distribution plate for fluid bed reactor in ammoxidation |
| WO2015153193A1 (en) * | 2014-03-31 | 2015-10-08 | Ineos Europe Ag | Feed sparger design for an ammoxidation reactor |
| CN205797156U (en) * | 2016-01-08 | 2016-12-14 | 中国石油化工股份有限公司 | Feed distributor for the fluidized-bed reactor of ammoxidation reaction |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107720758A (en) * | 2017-11-13 | 2018-02-23 | 浙江工业大学上虞研究院有限公司 | Chemical industry production system |
| EP3711849A4 (en) * | 2017-11-14 | 2021-08-25 | China Petroleum & Chemical Corporation | Feed gas feeding system for propylene ammoxidation reactor |
| JP2021502895A (en) * | 2017-11-14 | 2021-02-04 | 中国石油化工股▲ふん▼有限公司 | Fluid distributors, reactors and their applications |
| JP7216087B2 (en) | 2017-11-14 | 2023-01-31 | 中国石油化工股▲ふん▼有限公司 | Fluid distributor, reactor and its application |
| CN110201610A (en) * | 2018-02-28 | 2019-09-06 | 国家能源投资集团有限责任公司 | Gas distributor and reactor |
| CN110201610B (en) * | 2018-02-28 | 2021-11-05 | 国家能源投资集团有限责任公司 | Gas distributors and reactors |
| CN112439363A (en) * | 2019-09-05 | 2021-03-05 | 中石油吉林化工工程有限公司 | Propylene ammonia distributor |
| CN112439368A (en) * | 2019-09-05 | 2021-03-05 | 中石油吉林化工工程有限公司 | Reactor for preparing acrylonitrile |
| CN112439368B (en) * | 2019-09-05 | 2023-11-10 | 中石油吉林化工工程有限公司 | Reactor for preparing acrylonitrile |
| CN111676056A (en) * | 2020-06-19 | 2020-09-18 | 中耐工程科技有限公司 | Residual oil hydrogenation reactor with three-dimensional grid feeding structure, residual oil hydrogenation system containing reactor and residual oil hydrogenation process |
| CN115055124A (en) * | 2022-06-22 | 2022-09-16 | 上海蓝科石化环保科技股份有限公司 | Acrylonitrile fluidized bed reaction device and process |
| CN115055124B (en) * | 2022-06-22 | 2023-12-29 | 上海盛蓝汇科技有限责任公司 | Acrylonitrile fluidized bed reaction device and process |
| CN117832052A (en) * | 2022-12-30 | 2024-04-05 | 江苏微镀新能源科技有限公司 | A gas release mechanism for vacuum coating ion source |
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