CN205797156U - Feed distributor for the fluidized-bed reactor of ammoxidation reaction - Google Patents
Feed distributor for the fluidized-bed reactor of ammoxidation reaction Download PDFInfo
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- CN205797156U CN205797156U CN201620016982.8U CN201620016982U CN205797156U CN 205797156 U CN205797156 U CN 205797156U CN 201620016982 U CN201620016982 U CN 201620016982U CN 205797156 U CN205797156 U CN 205797156U
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Abstract
This utility model 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 supervisor connecting unstripped gas entrance and the arm for shunting unstripped gas being in fluid communication with described supervisor, there is on supervisor or arm the orifice for unstripped gas charging, it is characterized in that, along unstripped gas flow direction, the aperture of any one orifice on supervisor or arm is equal to or more than the aperture of the upstream side orifice of next-door neighbour.Propylene ammonia feed distributor according to the fluidized-bed reactor for ammoxidation of propylene reaction of the present utility model, by joining with the gas temperature in conduit, pressure correlation, reasonably determine orifice aperture, can make propylene ammonia more even into fluidized-bed reactor inside, thus improve the yield of acrylonitrile and the conversion ratio of propylene significantly, and significantly inhibit side reaction, reduce CO2Amount.
Description
Technical field
This utility model relates to a kind of fluidized-bed reactor unstripped gas feed distributor for ammoxidation reaction.
Background technology
Industrial fluidized-bed reactor is utilized to carry out ammoxidation reaction for a long time.The most this kind of reactor includes an appearance
Device, and for transmitting and disperse the distributor comprising organic unstrpped gas and for transmitting and the gas distribution of decentralized oxygen
Device, wherein, distributor generally comprises the conduit of conveying gas, and has perforate on conduit so that unstripped gas and oxygen-containing gas
Discharge.
Such as, the commonly used propylene ammmoxidation process in countries in the world produces acrylonitrile, and this is one and typically utilizes fluid bed
Reactor carries out the example of ammoxidation of propylene reaction.During utilizing ammoxidation of propylene to produce acrylonitrile, raw material is had one
Fixed ratio requirement, as the ratio of ammonia Yu propylene should be 1～1.5, and the ratio of air and propylene should be 8.5～10.5.True
On, in the range of this ratio is also exactly in the explosion limit of propylene ammonia.Therefore, in process of production, not by propylene, ammonia with
And be re-fed in reaction bed after three kinds of unstripped gas mixing of air, but these three kinds of unstripped gas are separately led by two distributors
Entering bed: propylene enters bed by a distributor after mixing with ammonia, air is to enter bed by another distributor, with
Avoid unstripped gas antedating response or explode.
When utilizing fluidized-bed reactor to carry out ammoxidation reaction, the impact on reaction yield of the mol ratio of reacting gas
The biggest: when sky is higher than (air and propylene gas mol ratio), deep oxidation ratio improves, and therefore reaction yield declines；And when sky
Time lower than (air and propylene gas mol ratio), unreacted Organic Ingredients ratio increases, and reaction yield declines equally.The most anti-
Answer the reacting gas of mixing in device it is necessary to have correct mol ratio.
Prior art such as British patent NO.1265770 discloses in the fluidized-bed reactor that ammoxidation reacts,
The nozzle of dispersion plate answers one_to_one corresponding with the nozzle on Acrylamide distributor, and toward each other, but this patent is the most specifically
The aperture of the opening of unstripped gas is sent on bright Acrylamide distributor.CN1172440A has described a kind of fluidized-bed reaction in greater detail
The ratio range of opening orifice pore-size distribution on the Acrylamide distributor in device and maximum diameter of hole and minimum-value aperture, it is believed that propylene
The mass flow of the gaseous mixture that ammonia distributor opening part flows out depends primarily on gas temperature, it is proposed that on Acrylamide distributor
The size in opening orifice aperture discharged of gaseous mixture only relevant with gas temperature.But it is true that reacted at ammoxidation of propylene
Cheng Zhong, owing to propylene ammonia feed distributor takes multitube form, the mixture pressure in distributor changes the most only along journey
The pressure loss, also include the change of the pressure that the factors such as Variable Mass Flow cause.In particular with the maximization of device, charging point
The supervisor of a cloth device/length of tube all increased, and supervisor/arm distributed more nozzle, and on conduit, near-end sprays with far-end
The pressure differential of mouth just becomes apparent from.Therefore, for large-scale propylene ammonoxidizing fluid bed reactor, if not taking in pressure
The change impact on aperture, will certainly cause the problem that unstripped gas distribution is uneven, finally have influence on reaction yield.
Utility model content
This utility model provides a kind of fluidized-bed reactor unstripped gas feed distributor for ammoxidation reaction, including:
For connect unstripped gas entrance supervisor and with described supervisor fluid communication the arm for shunting unstripped gas, described supervisor or
There is on described arm the orifice for unstripped gas charging, it is characterised in that
Along unstripped gas flow direction, the aperture of any one orifice on described supervisor or described arm is equal to or big
Aperture in the upstream side orifice of next-door neighbour.
According to feed distributor of the present utility model, it is preferable that any one orifice on described supervisor or described arm
Aperture compared to the aperture ratio in aperture of the upstream side orifice of next-door neighbour between 1.0～1.080.
According to feed distributor of the present utility model, it is preferable that any one orifice on described supervisor or described arm
Aperture compared to the aperture ratio in aperture of the upstream side orifice of next-door neighbour between 1.0～1.060.
According to feed distributor of the present utility model, it is preferable that any one orifice on described supervisor or described arm
Aperture compared to the aperture ratio in aperture of the upstream side orifice of next-door neighbour between 1.0～1.040.
According to feed distributor of the present utility model, it is preferable that any one orifice on described supervisor or described arm
Aperture compared to the aperture ratio in aperture of the upstream side orifice of next-door neighbour between 1.0～1.020.
According to feed distributor of the present utility model, it is preferable that any one orifice on described supervisor or described arm
Aperture compared to the aperture ratio in aperture of the upstream side orifice of next-door neighbour between 1.0～1.015.
According to feed distributor of the present utility model, it is preferable that any one orifice on described supervisor or described arm
Aperture compared to the aperture ratio in aperture of the upstream side orifice of next-door neighbour between 1.0～1.010.
According to feed distributor of the present utility model, it is preferable that when a diameter of 10～15 meters of described fluidized-bed reactor,
Ratio between the aperture of the aperture of the maximum orifice on described supervisor or described arm and the orifice of minimum be 1.05～
Between 1.15.
According to feed distributor of the present utility model, it is preferable that when a diameter of 10～15 meters of described fluidized-bed reactor,
Ratio between the aperture of the aperture of the maximum orifice on described supervisor or described arm and the orifice of minimum be 1.08～
Between 1.12.
According to feed distributor of the present utility model, it is preferable that when a diameter of 5～10 meters of described fluidized-bed reactor,
Ratio between the aperture of the aperture of the maximum orifice on described supervisor or described arm and the orifice of minimum be 1.02～
Between 1.13.
According to feed distributor of the present utility model, it is preferable that when a diameter of 5～10 meters of described fluidized-bed reactor,
Ratio between the aperture of the aperture of the maximum orifice on described supervisor or described arm and the orifice of minimum be 1.05～
Between 1.11.
According to feed distributor of the present utility model, it is preferable that the described orifice on described unstripped gas feed distributor
Aperture is 3.0～10.0mm.
According to feed distributor of the present utility model, it is preferable that the described orifice on described unstripped gas feed distributor
Aperture is 3.5～9.0mm.
According to feed distributor of the present utility model, it is preferable that the described orifice on described unstripped gas feed distributor
Aperture is 4.0～7.5mm.
According to feed distributor of the present utility model, it is preferable that between the adjacent orifice on described supervisor or described arm
Pitch of holes be 100～300mm.
According to feed distributor of the present utility model, it is preferable that between the adjacent orifice on described supervisor or described arm
Pitch of holes be 125～275mm.
According to feed distributor of the present utility model, it is preferable that between the adjacent orifice on described supervisor or described arm
Pitch of holes be 150～225mm.
Effect of the present utility model
According to propylene ammonia feed distributor of the present utility model, by joining with the gas temperature in conduit, pressure correlation, come
Reasonably determine orifice aperture, it is possible to make propylene ammonia more even into fluidized-bed reactor inside, thus improve third significantly
The yield of alkene nitrile and the conversion ratio of propylene, and significantly inhibit side reaction, reduce CO2Amount.
Accompanying drawing explanation
Figure 1A and Figure 1B respectively illustrates the propylene ammonia of the fluidized-bed reactor for ammoxidation reaction of the present utility model
The example of feed distributor.
Fig. 2 A and Fig. 2 B respectively illustrates the nozzle schematic diagram of propylene ammonia feed distributor of the present utility model, including propylene
Ammonia feed distributor nozzle and orifice.
Fig. 3 is the schematic diagram of propylene ammonia feed distributor of the present utility model.
Detailed description of the invention
Hereinafter, combination is described in detail with reference to the accompanying drawings detailed description of the invention of the present utility model.But this utility model is not
Can be interpreted limited to these specific embodiments.
This utility model provides a kind of feed distributor for fluidized-bed reactor.This feed distributor is intended to improve work
Ammoxidation reaction device practical in industry, the ammoxidation reaction to being applied is not particularly limited.
Figure 1A shows an instantiation of feed distributor of the present utility model, and it relates to a kind of propylene ammonia charging point
Cloth device, this propylene ammonia feed distributor can be applicable in the fluidized-bed reactor of industrialized production acrylonitrile.Figure 1B shows this
Another concrete propylene ammonia feed distributor embodiment of utility model.Fig. 2 A and Fig. 2 B is that propylene ammonia of the present utility model enters
The nozzle schematic diagram of material distributor, wherein 6 is propylene ammonia feed distributor arm cross section, and 7 are and feed distributor Zhi Guanliu
The nozzle of body connection, 8 is the orifice on feed distributor arm.Fig. 3 is the former of propylene ammonia feed distributor of the present utility model
Reason figure.
According to this utility model, the propylene ammonia feed distributor shown in Figure 1A may include that distributor inlet, and distributor
The feed distributor supervisor of fluid communication, and and the arm of supervisor's fluid communication；Further, the supervisor of feed distributor
With on arm, or only on the arm of feed distributor, it is provided with the opening of referred to as orifice equidistantly；Described supervisor and arm
Be in fluid communication by described orifice with the nozzle being positioned at outside pipeline, another distal opening of described nozzle thus with inside reactor stream
Body connects.Therefore, material mixed gas is after porch enters feed distributor, and the supervisor along feed distributor is sent to each
Pipe, then it is ejected into nozzle via the orifice on feed distributor supervisor and/or arm, entered by nozzle end opening the most again
Reaction bed to reactor.
The propylene ammonia feed distributor that this utility model provides can be monomer as shown in Figure 1A, it is also possible to be such as Figure 1B
The shown complex comprising many sub-distributors.This little distributor is respectively provided with similar entrance-supervisor-arm-orifice-spray
Mouth structure, is connected in parallel with each other, and at each distributor inlet, temperature, pressure residing for unstripped gas is the same.Preferably, enter
Many sub-distributors in material distributor are identical, can be substituted for one another.When fluidized-bed reactor feed distributor contains
When having many sub-distributors, it is preferable that adjacent two sub-distributor inlet are equal along wall of reactor circumferential distance.
Each parts of described propylene ammonia feed distributor can be on the same level cross section of reactor, it is also possible to be in anti-
Answer on the varying level cross section of device, but identical assembly should be limited in the same level cross section of reactor.Such as, each charging
The same many supervisors being referred to as feed distributor supervisor in distributor should be in same level cross section, with being referred to as feeding distribution
All arms of device arm should be in same level cross section, with all nozzles of referred to as feed distributor nozzle, its end
Should be in same level cross section, and should be identical with the vertical dimension of nozzle of air sparger below reactor
's.
According to embodiment of the present utility model, the supervisor of described propylene ammonia feed distributor is preferably straight tube.Described arm
For straight tube or curved pipe.Described arm can come all in both sides or the same side of supervisor, and same sub-distributor
Pipe is parallel to each other (when for straight tube) or concentric (when for curved pipe).Preferably, the axis (when for straight tube) of these arms
Or tangent line (when for curved pipe) intersects vertically with the supervisor being connected.When arm is positioned at supervisor both sides, arm is mutually aligned
With with this supervisor's cross or wrong cross.
As shown in Figure 2 A and 2B, according to this utility model, on the arm 23,26 of described propylene ammonia feed distributor, or
Person is according to circumstances on the supervisor and arm of described propylene ammonia feed distributor, along the axis direction arrangement of supervisor and/or arm
There is the circular open 24,28 of referred to as orifice, be used for allowing gaseous mixture spray into reactor in feed distributor.Described supervisor or arm
Connected with the nozzle 27 being correspondingly positioned at outside supervisor or arm by described orifice, gaseous mixture therefore after orifice at a high speed ejection, and
Not directly enter the reaction bed of inside reactor, but through the circular open entrance of the nozzle other end after nozzle rectification
Inside reactor.Orifice is coaxial with feed distributor nozzle, and is positioned at vertical with the central axis of feed distributor supervisor or arm
On straight radial section.According to this utility model, the aperture of described orifice is less than described nozzle and open-ended diameter thereof.
Between the orifice center of circle adjacent along the axial direction of supervisor or arm respectively on supervisor or arm vertically just
To vertical dimension be referred to as pitch of holes.According to this utility model, for arbitrary propylene ammonia feed distributor, at arbitrary arm
Axial direction on the pitch of holes of adjacent orifice be identical；Equally, the hole of adjacent orifice on the axial direction of arbitrary supervisor
Spacing is also identical.Preferably, adjacent along the axial direction of the arbitrary arm pitch of holes between orifice and along arbitrary master
The pitch of holes between orifice adjacent on the axial direction of pipe is also mutually to be equal to.According to embodiment of the present utility model, institute
The pitch of holes stating orifice can be typically 100～300mm, preferably 125～275mm, more preferably 150～225mm.
As shown in Figure 2 A and 2B, according to this utility model, can be with cloth on the same radial section of supervisor and/or arm
It is equipped with an orifice or multiple orifice (this cross section corresponding to these orifice centers of circle is referred to as orifice cross section).These are in same section
The orifice in face is respectively connected with corresponding nozzle, and concentric with nozzle equally.According to a specific embodiment of the present utility model,
Same radial section on the supervisor and/or arm of propylene ammonia feed distributor is all disposed with same amount of orifice, is in
Multiple orifices of same radial section and the multiple orifices one_to_one corresponding respectively being positioned at other radial sections, thus along corresponding main
Managing or arranged in columns on the axial direction of arm, these row are parallel with the axis of this supervisor or arm.According to of the present utility model one
Individual preferred embodiment, arranges at least one orifice on the same radial section of supervisor and/or arm.
Skilled in the art realises that, according to the difference of the operating condition of the fluidized-bed reactor applied, feed distributor
On the orifice aperture for the unstripped gas that carries mixing also need to do respective change.It is, in general, that be used for the sharp of transferring raw material gas
Hole can not be the biggest or the least.If orifice aperture is bigger than normal, easily causes catalyst and alter entrance Acrylamide distributor by orifice
In supervisor or arm；This partial catalyst is in the atmosphere of propylene ammonia gaseous mixture, and unstripped gas propylene, ammonia enter at catalyst surface
Row ammoxidation reaction, final catalyst will be lost activity by over reduction because of anoxia；It addition, enter into Acrylamide distributor master
Catalyst in pipe or arm can cause distributor local stoppages, causes unstripped gas skewness, affects the stable fortune of reactor
OK.If orifice aperture is less than normal, unstripped gas perforation hole speed will increase；Too fast perforation Kong Su exacerbates catalyst granules
Abrasion, exacerbates the abrasion to orifice simultaneously the most to some extent.
According to this utility model, coordinating the higher operating linear velocity degree of existing acrylonitrile reactor device, this utility model sets
In fixed acrylonitrile feeder, the punching rate of unstripped gas is in the range of 60～250m/s, preferably 80～230m/s, and more preferably 100
～200m/s.Setting according to this, the orifice diameter on described propylene ammonia feed distributor is advisable with 3.0～10.0mm, and preferably 3.5
～9.0mm, more preferably 4.0～7.5mm.In this case, the purpose of uniform gas distribution can i.e. be reached, it is possible to avoid catalyst
The probability altered and wear and tear catalyst and orifice is down to minimum.
Additionally, in order to ensure the good yield that ammoxidation of propylene reacts, skilled in the art realises that, ammonia oxidation reactor
Interior reacting gas mol ratio must be well controlled: if local gas mol ratio skewness, the most whole reaction
The productivity of device will significantly reduce.Therefore, the aperture of each orifice how is designed, it is ensured that each sharp from feeder diverse location
The gaseous mixture of hole ejection has identical mass flow so that from feed distributor, the unstrpped gas of blowout is evenly distributed on reaction
In device, it it is the key of feeder design.
Disclosed document and technique teaching notes, utilize nozzle on Acrylamide distributor and be placed in below fluidized-bed reactor
Air sparger on perforate one_to_one corresponding so that propylene ammonia feed distributor ejection propylene and the gaseous mixture physical ability of ammonia
The oxygen-containing air that enough and air sparger sprays realizes 1 and blows for a pair, thus facilitates equal in reactor of propylene, ammonia and air
Even distribution.Chinese patent 96191736.9 further discloses the unstripped gas outlet on Acrylamide distributor to be needed to use difference
Aperture.According to this patent application, need crucial it is considered that gas temperature in reactor during design unstripped gas outlet aperture
Change.In the fill process of unstripped gas, gas temperature raise degree advance in the catheter with gas length, gas temperature
Spend the difference with bed temperature and change.The length that gas is advanced in the catheter is the longest, and the heat exchanger time of experience is the longest, gas temperature
Degree is the highest.Sometimes, the temperature difference of the nozzle at the air inlet and the nozzle of arm far-end can 50～200 DEG C,
The highest.Therefore, on the supervisor of ammoxidation feed distributor or the airflow direction of arm, along with unstripped gas is in reactor
The increase of stroke, unstripped gas gradually heats up, and therefore density diminish, and therefore corresponding orifice diameter needs to be gradually increased.
But inventor calculates and experiment through a large amount of, find so that the mixing unstripped gas flowed out from each orifice has
Identical mass flow, needs the factor considered to include density and the gas perforation pressure reduction etc. of gaseous mixture；And mixed gas density
It is based primarily upon residing working condition such as temperature, pressure etc..Therefore, realize allowing each nozzle have identical mass flow,
The diameter D needs of orifice consider together with associating with mixed gas density (ρ) and gas perforation pressure differential deltap P1, and its correlation is permissible
It is expressed as D4∝1/(ρ*ΔP1).And mixed gas density ρ is relevant with pressure P with temperature T residing for gas, ρ ∝ P/T.
It is true that the ammoxidation feed distributor that modern fluid bed reactor uses mostly is multitube air distributor, gas
The change of body pressure is affected by many wherein.As it is shown on figure 3, gas sentences certain speed flow forward along supervisor 31,
When through arm 33, some gas flows out toward side line arm 33 direction, and residual gas continues to flow forward at supervisor 32
Dynamic；Equally, gas flows along at arm 35 with certain speed at far-end arm 36, through nozzle, and some gas
Flowing out toward side line nozzle direction, residual gas continues to flow at far-end 36 along arm.By this way, in the charging point of propylene ammonia
In cloth device, propylene ammonia gaseous mixture along pipe flow by each nozzle dispersion to bed, no matter feed distributor supervisor or
Arm, gas quality in flow process is constantly to reduce.And propylene ammonia gaseous mixture is in flow process, moving of gaseous fluid
Can also be continually changing.Still with shown in Fig. 3, mixed gas kinetic energy at supervisor 31 is higher than being responsible at 32, equally,
Kinetic energy at arm 35 is higher than at arm 36.Meanwhile, gas is also by along the Cheng Guandao wall frictional resistance to it, Yi Jiyan
The heat exchange of journey and reacting gas etc., these aspect factors result in the change of gas pressure in conduit.
Inventor finds, the pressure of the gaseous mixture at each nozzle can be calculated by suitable mass variable flow theory etc.
And determine.So, according to the feature of propylene ammonia feed distributor in fluidized-bed reactor, along with gas is in the charging distribution of propylene ammonia
Device lead Bottomhole pressure, inventor finds to arrive the gas pressure at arm end nozzle can with distributor inlet gas pressure difference
-2.5Kpa～+3.0Kpa can be reached, or bigger.In conduit, such change of gas pressure not only can cause gas density
Change, the change of pressure differential deltap P1 that simultaneously the most also causes boring a hole.It was recognized by the inventor that when unit scale is less, such as reactor
When a diameter of 7 meters or less, temperature is the effect determined on the impact of orifice diameter, and gaseous mixture is at the conduit of feed distributor
Interior pressure change is the most violent, and the impact on orifice diameter is smaller.But along with the increase of unit scale, reactor is straight
The increase in footpath, the amplitude of gaseous mixture pressure change in the conduit of feed distributor is significantly increased.Therefore, in this situation
Under, the determination of orifice diameter needs to be associated with gas temperature and pressure accurately, thus could to make charging distribution simultaneously
The mass flow of the gaseous mixture of device each nozzle ejection is more consistent, and gas is more evenly distributed, and reaction result is more preferable.
Finding according to above, inventor provide the propylene ammonia feed distributor of a kind of improvement, it has a following feature:
Along feed distributor supervisor or arm, along unstripped gas advance direction, from distributor inlet more close to orifice diameter the least,
From distributor inlet more away from orifice diameter the biggest.Here, should be understood to mean from distributor inlet " close to more " or " the most remote "
With regard to unstripped gas for the length of course in distributor ducts (supervisor or arm), closer to or enter further from distributor
Mouthful, the calculating of this travel path should start from the nearly distributor inlet end of conduit and finally spray the orifice opening part of unstripped gas.Root
According to this utility model, along feed distributor supervisor or arm, on the direct of travel of unstripped gas, the aperture of adjacent two orifices
Change ratio is between 1.0～1.080, between preferably 1.0～1.060, between more preferably 1.0～1.040, even more preferably from
It is between 1.0～1.020, between most preferably 1.0～1.015.In this utility model, described orifice diameter can be continuous
Changing, i.e. press the travel path of unstripped gas air inlet, on it, small adjustment is all done in each orifice aperture；Can also be that staged changes
Become, i.e. press the travel path of unstripped gas air inlet, if dry hole adjacent on it can have same aperture, jump to down the most again
One orifice aperture level, keeps identical aperture between several adjacent holes, the like.Carrying out staged change
Adjustment time, its premise is the unstripped gas mass flow uniformity of each orifice.
Skilled in the art realises that, on aforementioned propylene ammonia feed distributor, the adjustment in orifice aperture is in order to make
On feed distributor, the mass flow through the unstripped gas of each orifice becomes evenly consistent, thus it is anti-to improve ammoxidation of propylene
The productivity answered.According to an embodiment of the present utility model, the propylene ammonia feed distributor of improvement provided by the utility model,
It is by the mass flow of the material mixed gas of any one orifice and by the quality of the material mixed gas of any other orifice
Flow is compared, and difference can control within 3%；Preferably, described difference can control within 1.5%；It is highly preferred that institute
State difference can control within 1%.
According to this utility model, described propylene ammonia feed distributor, the varying aperture amplitude of its orifice is by reactor
The restriction of diameter.In general, reactor diameter is the biggest, and the amplitude of variation in the orifice aperture of described propylene ammonia feed distributor is more
Greatly.According to an embodiment of the present utility model, when reactor diameter is 10～15 meters, its maximum diameter of hole and minimum-value aperture it
Ratio can be in the range of 1.05～1.15；Preferably, this ratio can be in the range of 1.08～1.12.And when reactor diameter is 5
～when 10 meters, the ratio of its maximum diameter of hole and minimum-value aperture can be in the range of 1.02～1.13；Preferably, this ratio can be 1.05
～in the range of 1.11.
According to this utility model, the reaction temperature of described propylene ammonia fluidized-bed reactor, at 420～460 degrees Celsius, is reacted
Pressure is 0.4～0.8kg/cm2, in reaction, the mol ratio of propylene, ammonia and air is 1:1.1～1.3:9.0～10.5.This area
Personnel understand, in addition to this specification clearly states, in known document about ammoxidation reaction other process conditions also
All can use.The catalyst of any of ammoxidation reaction all can make catalyst of the present utility model.
Embodiment
Further illustrate this utility model referring to specific embodiment of the utility model and comparative example, but this practicality is new
Type can not be construed to be limited.In embodiment and comparative example, unreacted olefine gas chromatography in reacting gas
Analyze.Component and the reaction condition of reactor are in, in addition to special instruction, the scope of generally using, and do not affect reaction result.
Comparative example 1: reaction process condition: reaction temperature 440 DEG C, reaction pressure 60KPa, C3:NH3: air is 1:1.2:
9.5, catalyst loading: 0.08h～1.Reactor diameter 7 meters, air feed distributor uses identical orifice diameter, propylene ammonia
4 kinds of various sizes of orifices are set on feed distributor altogether, corresponding aperture be respectively 4.3mm, 4.6mm, 4.9mm and
5.2mm.Reaction result is shown in Table 1.
Embodiment 1: the reaction process condition identical with comparative example.Reactor diameter 7 meters, air feed distributor uses
Identical orifice diameter, propylene ammonia feed distributor arranges 5 kinds of various sizes of orifices altogether, and corresponding aperture is respectively
4.5mm, 4.6mm, 4.7mm, 4.8mm and 4.9mm.Reaction result is shown in Table 1.
Embodiment 2: the reaction process condition identical with comparative example 1.Reactor diameter 9 meters, air feed distributor uses
Identical orifice diameter, propylene ammonia feed distributor arranges 6 kinds of various sizes of orifices altogether, and corresponding aperture is respectively
6.5mm, 6.6mm, 6.7mm, 6.8mm, 6.9mm and 7.0mm.Reaction result is shown in Table 1.
Embodiment 3: the reaction process condition identical with comparative example 1.Reactor diameter 12 meters, air feed distributor uses
Identical orifice diameter, propylene ammonia feed distributor arranges 8 kinds of various sizes of orifices altogether, and corresponding aperture is respectively
5.8mm, 5.9mm, 6.0mm, 6.1mm, 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 propylene ammonia of the fluidized-bed reactor for ammoxidation of propylene reaction of the present utility model
Feed distributor, by joining with the gas temperature in conduit, pressure correlation, reasonably determines orifice aperture, it is possible to make propylene
Ammonia is more even into fluidized-bed reactor inside, thus improves the yield of acrylonitrile and the conversion ratio of propylene significantly, and shows
Write suppression side reaction, reduce CO2Amount.
Claims (16)
1. for a fluidized-bed reactor unstripped gas feed distributor for ammoxidation reaction, including: it is used for connecting unstripped gas and enters
Mouthful supervisor and with described supervisor's fluid communication for shunting the arm of unstripped gas, described supervisor or described arm have use
Orifice in unstripped gas charging, it is characterised in that
Along unstripped gas flow direction, the aperture of any one orifice on described supervisor or described arm is equal to or more than tight
The aperture of adjacent upstream side orifice, and
The aperture of any one orifice on described supervisor or described arm is compared to the hole in the aperture of the upstream side orifice of next-door neighbour
Footpath ratio is between 1.0～1.080.
2. feed distributor as claimed in claim 1, it is characterised in that any one on described supervisor or described arm is sharp
The aperture in hole compared to the aperture ratio in aperture of the upstream side orifice of next-door neighbour between 1.0～1.060.
3. feed distributor as claimed in claim 1, it is characterised in that any one on described supervisor or described arm is sharp
The aperture in hole compared to the aperture ratio in aperture of the upstream side orifice of next-door neighbour between 1.0～1.040.
4. feed distributor as claimed in claim 1, it is characterised in that any one on described supervisor or described arm is sharp
The aperture in hole compared to the aperture ratio in aperture of the upstream side orifice of next-door neighbour between 1.0～1.020.
5. feed distributor as claimed in claim 1, it is characterised in that any one on described supervisor or described arm is sharp
The aperture in hole compared to the aperture ratio in aperture of the upstream side orifice of next-door neighbour between 1.0～1.015.
6. feed distributor as claimed in claim 1, it is characterised in that any one on described supervisor or described arm is sharp
The aperture in hole compared to the aperture ratio in aperture of the upstream side orifice of next-door neighbour between 1.0～1.010.
7. feed distributor as claimed in claim 1, it is characterised in that a diameter of 10～15 meters when described fluidized-bed reactor
Time, the ratio between the aperture of the aperture of the maximum orifice on described supervisor or described arm and the orifice of minimum be 1.05～
Between 1.15.
8. feed distributor as claimed in claim 7, it is characterised in that the maximum orifice on described supervisor or described arm
Aperture and minimum orifice aperture between ratio be between 1.08～1.12.
9. feed distributor as claimed in claim 1, it is characterised in that a diameter of 5～10 meters when described fluidized-bed reactor
Time, the ratio between the aperture of the aperture of the maximum orifice on described supervisor or described arm and the orifice of minimum be 1.02～
Between 1.13.
10. feed distributor as claimed in claim 9, it is characterised in that maximum sharp on described supervisor or described arm
Ratio between the aperture of the aperture in hole and the orifice of minimum is between 1.05～1.11.
11. feed distributors as described in claim 1～10 any one, it is characterised in that described unstripped gas charging distribution
The aperture of the described orifice on device is 3.0～10.0mm.
12. feed distributors as claimed in claim 11, it is characterised in that described sharp on described unstripped gas feed distributor
The aperture in hole is 3.5～9.0mm.
13. feed distributors as claimed in claim 11, it is characterised in that described sharp on described unstripped gas feed distributor
The aperture in hole is 4.0～7.5mm.
14. feed distributors as described in claim 1～10 any one, it is characterised in that described supervisor or described arm
On adjacent orifice between pitch of holes be 100～300mm.
15. feed distributors as claimed in claim 14, it is characterised in that adjacent on described supervisor or described arm
Pitch of holes between orifice is 125～275mm.
16. feed distributors as claimed in claim 14, it is characterised in that adjacent sharp on described supervisor or described arm
Pitch of holes between hole is 150～225mm.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620016982.8U CN205797156U (en) | 2016-01-08 | 2016-01-08 | Feed distributor for the fluidized-bed reactor of ammoxidation reaction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620016982.8U CN205797156U (en) | 2016-01-08 | 2016-01-08 | Feed distributor for the fluidized-bed reactor of ammoxidation reaction |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205797156U true CN205797156U (en) | 2016-12-14 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201620016982.8U Active CN205797156U (en) | 2016-01-08 | 2016-01-08 | Feed distributor for the fluidized-bed reactor of ammoxidation reaction |
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| CN106955644A (en) * | 2016-01-08 | 2017-07-18 | 中国石油化工股份有限公司 | The feed distributor of the fluidized-bed reactor reacted for ammoxidation |
| CN107673360A (en) * | 2017-11-13 | 2018-02-09 | 浙江工业大学上虞研究院有限公司 | For preparing the chemical industry equipment of trichlorosilane |
| 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 |
| WO2018113417A1 (en) * | 2016-12-23 | 2018-06-28 | 中国石油化工股份有限公司 | Pressure drop control system and control method of feed distributor of a fluidized bed reactor |
| 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 |
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2016
- 2016-01-08 CN CN201620016982.8U patent/CN205797156U/en active Active
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106955644A (en) * | 2016-01-08 | 2017-07-18 | 中国石油化工股份有限公司 | The feed distributor of the fluidized-bed reactor reacted for ammoxidation |
| WO2018113417A1 (en) * | 2016-12-23 | 2018-06-28 | 中国石油化工股份有限公司 | Pressure drop control system and control method of feed distributor of a fluidized bed reactor |
| EA037190B1 (en) * | 2016-12-23 | 2021-02-17 | Чайна Петролеум Енд Кемикал Корпорейшн | Pressure drop control system and method for feed distributor in fluidized bed reactor |
| CN107673360A (en) * | 2017-11-13 | 2018-02-09 | 浙江工业大学上虞研究院有限公司 | For preparing the chemical industry equipment of trichlorosilane |
| 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 |
| CN110201610B (en) * | 2018-02-28 | 2021-11-05 | 国家能源投资集团有限责任公司 | Gas distributor and reactor |
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