CN106478457A - Improved ammoxidation of propylene technique and its reactor - Google Patents
Improved ammoxidation of propylene technique and its reactor Download PDFInfo
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- CN106478457A CN106478457A CN201510552970.7A CN201510552970A CN106478457A CN 106478457 A CN106478457 A CN 106478457A CN 201510552970 A CN201510552970 A CN 201510552970A CN 106478457 A CN106478457 A CN 106478457A
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Abstract
A kind of ammoxidation of propylene reaction process for industrialized production acrylonitrile, the operation lines speed of its fluidized-bed reactor is 0.7-1.0m/s, and wherein, the yield that propylene is converted into acrylonitrile is maintained at more than 80%.According to the ammoxidation of propylene reaction process of the present invention, high acrylonitrile yield can be kept, controls low catalyst loss simultaneously in the case of improving operation lines speed.
Description
Technical field
The present invention relates to a kind of ammoxidation of propylene technique, and anti-for ammoxidation of propylene technique
Answer device.
Background technology
Acrylonitrile is the important industrial chemicals of petrochemical industry.Countries in the world commonly used Sohio method
Produce acrylonitrile, that is, unstripped gas air, propylene, ammonia press certain proportioning, in acrylonitrile catalysis
In the presence of agent, under certain reaction condition, there is propylene ammonia Selective Oxidation, generate
Acrylonitrile by-product acetonitrile and hydrocyanic acid etc., release substantial amounts of reaction heat simultaneously.Shown in Fig. 1
For business acrylonitrile fluid bed reactor, its inner member includes：Dispersion plate, third
Alkene ammonia distributor, cooling coil, cyclone separator.
Carried out using acrylonitrile fluid bed reactor propylene ammonia oxidation reaction when, the behaviour of fluid bed
It is an important parameter as linear velocity.Document is had once to report the operation of acrylonitrile fluid bed reactor
Linear velocity is improper less than 0.4m/s, easily causes the deep oxidation of ammoxidation of propylene reaction,
Reduce acrylonitrile yield；But also there is document report to think, too high operation lines speed can make third
Alkene ammonia unstripped gas is not enough for time of contact in beds, causes ammoxidation of propylene to generate propylene
The incomplete reactions such as aldehyde, acrylic acid increased, thus affecting acrylonitrile yield.Document《Third
The research of alkene nitrile fluid reactor pressure decrease》Report, fluidized-bed reactor operation lines speed should
Control in 0.5～0.68m/s, from the table 1 of the document, according to also showing, it is anti-that it describes institute's number of cases
Device is answered to run substantially all under the conditions of the such a relatively low operation lines speed of 0.6m/s.
Powerful with the follow-up chemical products market demand with acrylonitrile as raw material, also drive city
The demand to acrylonitrile for the field.In the case, in prior art 0.6m/s low operation lines speed
Acrylonitrile process maximization, the demand of scale can not have been met.By increasing by a certain percentage
Plus the input of unstripped gas, improve ammoxidation of propylene operation linear velocity, technical staff is simultaneously
Easily reach the purpose increasing acrylonitrile production capacity.But, according to prior art, for propylene
For nitrile production firm, although the production capacity of acrylonitrile increased after the raising of operation lines speed, but
Accordingly can be reduced by the efficiency that propylene is converted into target product, such as less than 80%, even lower,
Cause propylene material consumption to increase, from an economic point of view, be not necessarily to one's profit；On the other hand,
From the perspective of environmental protection, more propylene are had to be not converted into target product and other by-product,
Remain in tail gas.With tail gas, directly discharge leads to the discharge of non-methane gas exceeded to unreacted propylene
Or entering next device for purifying and treating tail gas with tail gas, which kind of processing mode all causes raw material
The waste of gas, this is also improper.Meanwhile, after operation lines speed improves, there are more catalysis
Agent granule is suspended in the dilute phase section of reactor, in the case that cyclone separator disposal ability is limited,
Reacting gas will be carried more catalyst secretly and take reactor assembly out of, cause catalyst stack less amount
Increase, in the course of time, add catalyst additional amount constant in the case of, urge in reactor
Agent reserve constantly reduces, and catalyst loading increases, and eventually affects propylene and is transformed into target product
The yield of thing.
Content of the invention
An aspect of of the present present invention provides a kind of ammoxidation of propylene for industrialized production acrylonitrile anti-
Answer technique, the operation lines speed of its fluidized-bed reactor is 0.7-1.0m/s, and wherein, propylene converts
Yield for acrylonitrile is maintained at more than 80%.
It is preferable that catalyst loss is effectively controlled in the ammoxidation of propylene reaction process of the present invention
System is in below 0.5kg/t.AN.
It is preferable that the top pressure of reactor is in the ammoxidation of propylene reaction process of the present invention
0.40-0.50kg/cm2(G).
It is preferable that the grain of catalyst used in the ammoxidation of propylene reaction process of the present invention
Degree is distributed as：Mean diameter is 40～80 μm, and calculated in weight percent, and particle diameter is more than 90
Micron account for 0-30%, particle diameter be less than 45 microns account for 30-50%, and particle diameter be less than 20 μm
Not higher than 10%.
It is preferable that regular during the course of the reaction in the ammoxidation of propylene reaction process of the present invention
Sampling analyses catalyst in reactor particle size distribution, select different grain size distribution adds catalyst,
With the particle size distribution maintaining catalyst in device it is：Mean diameter is 40～80 μm, with weight hundred
Point ratio, particle diameter be more than 90 microns account for 0-30%, particle diameter be less than 45 microns account for 30-50%,
And particle diameter is less than 20 μm not higher than 10%.
Another aspect of the present invention provides a kind of ammoxidation of propylene reaction process for the present invention
Reactor, wherein, the organic efficiency of cyclone separator used is more than 99.999%.
It is preferable that described in the present invention is for the reactor of ammoxidation of propylene reaction process
Cyclone separator is secondary cyclone.
It is preferable that described in the present invention is for the reactor of ammoxidation of propylene reaction process
Secondary cyclone is PV cyclone separator.
Another aspect of the present invention provides a kind of ammoxidation of propylene reaction process for the present invention
Reactor, wherein, cooling coil straight tube is highly not less than 7.2 meters.
It is preferable that cooling down in the present invention is for the reactor of ammoxidation of propylene reaction process
The height of coil pipe straight tube is not less than 7.5 meters.
It is preferable that cooling down in the present invention is for the reactor of ammoxidation of propylene reaction process
Coil pipe is away from dispersion plate upper surface apart from 30-150cm.
Another aspect of the present invention provides a kind of ammoxidation of propylene reaction process for the present invention
Reactor, the operation lines speed of this reactor is 0.7-1.0m/s, and propylene is converted into acrylonitrile
Yield be maintained at more than 80% it is characterised in that cyclone separator used is organic efficiency
Secondary cyclone for more than 99.999%, cooling coil straight tube is highly not less than 7.2 meters,
And described cooling coil is away from dispersion plate upper surface apart from 30-150cm.
The effect of the present invention
According to the ammoxidation of propylene reaction process of the present invention, can be in the feelings improving operation lines speed
Under condition, keep high acrylonitrile yield, control low catalyst loss simultaneously.
Brief description
Fig. 1：In prior art fluidized-bed reactor
List of reference signs
1：Acrylonitrile fluid bed reactor
2：Acrylamide distributor
3：Air intake
4：Dispersion plate
5：Cooling coil
6：Cyclone separator
Specific embodiment
(if necessary) describe being embodied as of the present invention in detail with reference to the accompanying drawings and examples
Mode.
The present invention provides a kind of improved process for production of acrylonitrile, improves the operation lines of reactor
Speed, but still keep propylene to be transformed into the efficiency of acrylonitrile more than 80.0%, and used catalyst
Loss be effectively controlled below 0.50kg/t.AN.On the other hand, the invention provides in response to changing
The acrylonitrile fluid bed reactor of the process for production of acrylonitrile entering and corresponding catalyst.This
Bright advantage is to make the yearly productive capacity of same device acrylonitrile can significantly improve, or
Person, in the case that acrylonitrile yearly productive capacity is constant, significantly decreases fluidized-bed reactor diameter,
Thus being conducive to the manufacture of equipment to process.
For reaching object defined above, inventor has carried out substantial amounts of calculating and has tested, and finds,
Under conditions of improving fluidized-bed reaction linear velocity, if simultaneously to inclusion cyclone separator, cooling
Water pipe and catalyst have carried out the improvement of each side, it is possible to achieve keep propylene to be transformed into third
The efficiency of alkene nitrile is more than 80.0%, and the loss of used catalyst is effectively controlled 0.50kg/t.AN
Goal of.
Specifically, inventor passes through substantial amounts of calculating and experiment, there is provided a kind of improved use
In the ammoxidation of propylene reaction process of industrialized production acrylonitrile, wherein carry out ammoxidation of propylene anti-
The operation lines speed of the fluidized-bed reactor answered is 0.70-1.0m/s.Under this operation lines speed,
Catalyst has more preferable fluidization quality, and granule even suspension, in catalyst concentrated phase section, owns
Catalyst granules and reacting gas have the touch opportunity of equalization, and all reacting gas similarly flow through
The layer of catalyst particles of same thickness, reacting gas has in catalyst particle surface and uniformly stops
Stay the time sufficiently to be contacted and react it is ensured that mass transfer and heat transfer efficiency.
Reactor operation lines speed can be calculated by following equation：
Wherein：
(a)Q：Enter the flow summation of the air, hydro carbons and ammonia of reactor, Nm3/s
(b)S：Reactor net sectional area, m2
(c)Tr：Reaction temperature, K
(d)Tn：273.15K
(e)Pr：Reactor head pressure, Pa
(f)Pn：Normal atmosphere
(g)1.05：Reacting gas expansion ratio
(h)V：Reactor operation lines speed, m/s.
Understand that operation lines speed is directly proportional to unstripped gas input amount, reaction temperature from formula (1), with
Reactor diameter, reaction pressure are inversely proportional to.For the production device for acrylic nitrile of industry park plan, instead
Device diameter is answered to be to determine, reaction temperature change is less on the impact of operation lines speed, does not generally make
For regulating measure.Operation lines speed is adjusted can be by unstripped gas input amount and reaction pressure adjustment
To realize.In the case that unstripped gas input amount is constant, adjust behaviour by controlling reaction pressure
It is simple to operation as linear velocity.
Further, since ammoxidation of propylene reaction is the reaction that volume increases, so low reaction pressure
Power is conducive to the generation of acrylonitrile, but too low reaction pressure can make reaction contact time shorten,
The reduction of propylene conversion, leads to propylene consumption to rise.Therefore, the reaction pressure of the present invention is excellent
Elect 0.40-0.50kg/cm as2(G).
Inventor also finds during invention, the ammoxidation of propylene reaction process pair of aforementioned improved
It is also proposed new requirement in the catalyst being used.According to the present invention, for this improved third
The catalyst that alkene nitrile production technology provides can be Mo-Bi series familiar to the person skilled in the art
Acrylonitrile catalyst, as described by CN101767014A, CN103418405 patent, this
Being integrally incorporated this patent and be incorporated in this of a little patents.The grain to these catalyst granules for the present invention
Degree distribution proposes special requirement.
Fluidization theory think the apparent density of the granularity of gas-solid fluidized bed middle granule and granule with
The difference convection current compound of gas density has a significant impact.Catalyst granules mean diameter should be
Between 30～100 μm and apparent particle density be less than 1400kg/m3.Broaden with distribution of particles or
Particle mean size reduces, and mass-transfer efficiency increases.According to the requirement of prior art, acrylonitrile is urged
Agent mean diameter is 30～100 μm, calculated in weight percent, and particle diameter is more than 90 microns
Account for 0-30%, particle diameter be less than 45 microns account for 30-50%.Such catalyst has in bed
Good fluidizing performance, and under prior art conditions, the such particle size distribution of catalyst
Meet the requirement of acrylonitrile process, the additional amount of catalyst and catalyst stack less amount can reach one
Individual dynamic balance.
By finding to the research of acrylonitrile Fluidization Engineering, the catalytic amount carried secretly by gas with
Operation lines speed also has certain relation, increases with operation lines speed, the catalysis carried secretly by gas
Agent also can accordingly increase.Wherein, increase with operation lines speed, the granule of small particle in catalyst
It is easier to be entrained to the higher bed height of fluidized-bed reactor by gas or be more readily pulled from being catalyzed
Agent bed is suspended in the more high position of the dilute phase section of reactor.Increase with operation lines speed, have
More small particle catalyst granules are suspended in cyclone separator one cyclonic porch, when exceeding
During cyclone separator disposal ability, easily causing catalyst stack less increases, and limiting case may be made
The blocking of forming apparatus causes the shut-down of production.Meanwhile, cyclone separator is difficult to for particle diameter to be less than 20 μm
Catalyst granules separate with reacting gas, this partial catalyst can leave reaction with reacting gas
Device.In the case that operation lines speed increases, when the catalyst granules being less than 20 μm in bed is many
When 10%, the catalyst granules being less than 20 μm in cyclone separator one cyclonic porch also can
Increase, cause the increase further of catalyst stack less.Therefore, under conditions of improving linear velocity,
It is necessary to restriction fluid bed is anti-in addition to being satisfied with catalyst fluidised form particle size distribution of good performance
Fine grained particularly particle diameter in the acrylonitrile catalyst granule being used in device is answered to be less than 20 μm little
The concentration distribution of particles requires.
Inventor passes through substantial amounts of calculating and experiment discovery, in order to be suitable for carrying out acrylonitrile work
Industry metaplasia is produced, after the fluidized-bed reaction linear velocity of ammoxidation of propylene reactor improves, the third of use
Alkene nitrile catalyst mean diameter should be 40～80 μm, calculated in weight percent should meet following will
Ask：Particle diameter be more than 90 microns account for 0-30%, particle diameter be less than 45 microns account for 30-50%, and
And particle diameter is less than 20 μm not higher than 10%, preferably not higher than 8%.From of the present invention special
The catalyst of element combinations described in sharp CN101767014A and from heretofore described
Cyclone separator, when operation lines speed is 0.7～1.0m/s, reaction pressure exists
0.40-0.50kg/cm2(G), under the conditions of, the yield that propylene is converted into acrylonitrile is maintained at more than 80%,
Effectively catalyst stack less rate can be controlled in below 0.50kg/t.AN simultaneously.It is highly preferred that control
Make in below 0.45kg/t.AN, it is more preferred still that controlling in below 0.40kg/t.AN,
Preferably, control in below 0.35kg/t.AN.
Further, modified technique provided by the present invention is divided for the grain graininess adding catalyst
Cloth it is also proposed special requirement.
It is known that in ammoxidation of propylene course of reaction, because effective group of acrylonitrile catalyst
The loss dividing leads to the particularity of activity decrease, needs to mend by the how much quantitative of acrylonitrile process amount
Plus catalyst.Adding one of catalyst action is to supplement the active component running off, and keeps propylene to turn
The efficiency changed to acrylonitrile remains at more than 80.0%；Adding another effect of catalyst is to remain anti-
Answer catalyst inventory in device, bed height relatively stable so that additional amount and catalyst stack less
Amount reaches a dynamic balance.
During plant running, many reasons can lead to original catalyst particle size distribution to have
Changed, such as catalyst ruptures because of reasons such as abrasion, collisions, finely grained catalyst is by whirlwind
Separator takes reactor assembly, the addition adding catalyst of different grain size distribution out of.Suitably
Particle size distribution is the second best in quality basic demand of catalyst fluidization.In prior art, generally add
Catalyst mean diameter is 40～80 μm just can meet the requirement of acrylonitrile process.
But inventor is found by many experiments, after fluidized-bed reaction linear velocity improves, such as linear speed
When spending for 0.7～1.0m/s, the particle size distribution of catalyst in reactor is not unalterable, because
This, is for the suitable particle size distribution of catalyst in reactor maintenance, to adding catalyst grain size,
Need to be adjusted according to the particle size distribution situation of catalyst in reactor.Catalyst in reactor
When particle size distribution coarse granule is on the high side, add fine grain in catalyst just should point on the high side；Conversely,
When catalyst in reactor particle size distribution fine grained is on the high side, adding coarse granule in catalyst just should be partially
Multiple spot.Catalyst grain size distribution in periodic sampling analysis reactor, selects different grain size distribution
Add catalyst, maintain catalyst mean diameter in device to be 40～80 μm, maintain in device and urge
Agent particle size distribution is, calculated in weight percent：Particle diameter be more than 90 microns account for 0-30%,
Particle diameter be less than 45 microns account for 30-50%, and particle diameter is less than 20 μm not higher than 10%, preferably
For being not higher than 8%.Carry out adding of corresponding catalyst according to such standard, from the present invention
The adding catalyst and select the present invention of element combinations described in described patent CN103418405
Described in cyclone separator, when operation lines speed be 0.7～1.0m/s when, reaction pressure exists
0.40-0.50kg/cm2(G), under the conditions of, the yield that propylene is converted into acrylonitrile is maintained at more than 80%,
Catalyst stack less can be satisfied with simultaneously and be effectively controlled below 0.50kg/t.AN, even lower.
Inventor passes through substantial amounts of calculating and experiment, for fluidized-bed reactor in the discovery present invention
Cyclone separator separation efficiency need more than 99.999%.Those skilled in the art are permissible
Solution, for reaching aforementioned efficiency, this cyclone separator can be three-level separator or two
Level separator.Preferably, this cyclone separator can be secondary cyclone.It is highly preferred that
This cyclone separator is PV cyclone separator, the whirlwind as described in CN1138599 patent
Separator, being integrally incorporated in this patent and be incorporated in this of this cyclone separator patent.
Inventor is also found by many experiments, the present invention to be realized, and needs to used by reactor
Cooling water pipe improve.
Generally it is disposed with the cooling water pipe for removing reaction heat in fluidized-bed reactor.Described cold
But water pipe is made up of a series of cooling water pipe assemblies being vertically fixed in reactor, each cooling
Straight tube that conduit assembly comprises vertical orientation and be used for connecting the U of adjacent straight tube at straight tube two ends
Shape bend pipe, these cooling water pipes are pressed ad hoc fashion and are formed cooling water pipe group, and each cooling water pipe group
It is evenly arranged in the cooling water pipe of whole reactor in conjunction with composition.During fluidized reaction,
The fluidized reaction bed being formed after unstripped gas, catalyst and product mixing needs by cooling down
Water pipe is cooling down.
Fluidization theory thinks, the granularity of the clearance rate between granule and granule and granule close
The factors such as degree, gas density, fluid linear velocity are relevant.In turbulent area, with operating linear velocity
The increase of degree, clearance rate also increased, clearance rate be impact catalyst fluidization height parameter it
One.For ripe ammoxidation of propylene reaction process, its density of catalyst, granularity, reaction gas
The change of body density is simultaneously little, so catalyst in reactor loadings, intergranular clearance rate
It is the principal element of impact catalyst fluidization height with reactor diameter size.For certain scale
Production device for acrylic nitrile, reactor diameter and loaded catalyst can calculate determination, because
This is according to this feature of ammoxidation of propylene Fluidization Engineering, linear velocity and catalyst fluidization height
Between relation by general formula (2) determine：
H=a+b*V1/2(2)
H represents catalyst fluidization height, and V represents fluid linear velocity, and a span is 2.5～3.5；
B span is 3.5～4.8.
In ammoxidation of propylene reaction running, if catalyst fluidization height h is higher than cooling coil
The upper end of straight length, partial reaction heat can not remove response system in time and cause dilute phase section temperature high,
Deep oxidation increases, and has influence on acrylonitrile yield, therefore cooling water pipe highly should be higher than that catalyst
Fluid height h；If it is larger that beds fluid height is less than cooling coil straight length upper end, hold
Easily cause the heat transfer area utilization rate that cooling coil contacted with beds not high, on the other hand
The lift that will also result in pump increases, and energy loss increases.
According to above-mentioned formula and the substantial amounts of experiment of inventor, inventor finds, when reaction linear speed
When degree is more than 0.6m/s, cooling coil straight length height H should be not less than 5.6 meters；Reaction linear speed
When degree is more than 0.7m/s, cooling coil straight length height H should be not less than 6.5 meters；Reaction linear speed
When degree is more than 0.8m/s, cooling coil straight length height H is not less than 7.2 meters.In general,
Cooling coil assembly includes cooling coil entrance, straight tube, cooling coil outlet, between two straight tubes
Connected with U-shaped bend pipe.Cooling coil can be by a U pipe or multiple identical U pipe concatenation
Become.Minimum point in cooling coil assembly, usually descends the minimum point of U, away from dispersion plate
Distance controlling is between 30～150cm, preferably 50～100cm.Ammoxidation of propylene reaction is adjoint
The generation of big calorimetric, in cooling coil minimum point to this section of interval of dispersion plate, reaction
The heat producing cannot be quickly moved out system, and the heat that the reaction of this region produces leads to this area
Domain temperature is higher compared with reaction temperature, for reaction, deep oxidation reaction aggravation, and, urge meanwhile
In agent active constituent, molybdenum is easier loss, in theory, cooling coil minimum point phase
To dispersion plate can not too high it should more low better, as far as possible near dispersion plate.But
It is to consider to remove expanding with heat and contract with cold, removing whether hot-water line can collide with other inner members of hot-water line itself
Deng the reason in engineering design, cooling coil should be not less than 30cm from dispersion plate.In cooling
In coil pack U pipe minimum point away from dispersion plate distance in 30～150cm, preferably
When between 50～100cm, in time beds bottom reaction heat can be removed reaction system,
Avoid and occur near the too high phenomenon of dispersion plate temperature, in reaction bed, axial temperature divides
Cloth is evenly.
After fluidized-bed reaction linear velocity improves, correspondingly need to increase cooling coil straight tube height.
As fluidized-bed reaction linear velocity improves to 0.8m/s, Theoretical Calculation go out catalyst fluidization height up to
7.7 meters, improve cooling coil straight tube height and should be not less than 7.2 meters, preferably not less than 7.5 meters,
Avoid leading to the efficiency that propylene is transformed into acrylonitrile to reduce because of deep oxidation.From of the present invention
Catalyst after, acrylonitrile yield remains at more than 80%.
Embodiment
Embodiment 1：Reactor operation lines speed is 0.75m/s, from propylene of the present invention
Nitrile catalyst and add catalyst and cyclone separator, catalyst grain size distribution is：Mean diameter
55 μm, calculated in weight percent, particle diameter be more than 90 microns account for 20%, particle diameter be less than 45
Micron account for 40%, particle diameter be less than 20 μm be 9%, cooling water pipe straight length be 7.0 meters, mend
Plus catalyst added with 0.4kg/t.AN, and add catalyst grain size distribution and urge according in reactor
Agent particle size distribution situation is adjusted.Run 1 year, propylene is transformed into acrylonitrile efficiency and is
80.8%, catalyst bed layer height and catalyst inventory have no significant change.
Embodiment 2：Reactor operation lines speed is 0.85m/s, from propylene of the present invention
Nitrile catalyst and add catalyst and cyclone separator, catalyst grain size distribution is：Mean diameter
55 μm, calculated in weight percent, particle diameter be more than 90 microns account for 22%, particle diameter be less than 45
Micron account for 36%, particle diameter be less than 20 μm be 6%, cooling water pipe straight length be 7.5 meters, mend
Plus catalyst added with 0.4kg/t.AN, and add catalyst grain size distribution and urge according in reactor
Agent particle size distribution situation is adjusted.Run 1 year, propylene is transformed into acrylonitrile efficiency and is
81.5%, catalyst bed layer height and catalyst inventory have no significant change.
Comparative example 1：Reactor operation lines speed is 0.55m/s, from propylene of the present invention
Nitrile catalyst and add catalyst and cyclone separator, catalyst grain size distribution is：Mean diameter
55 μm, calculated in weight percent, particle diameter be more than 90 microns account for 20%, particle diameter be less than 45
Micron account for 40%, particle diameter be less than 20 μm be 16%, cooling water pipe straight length be 5.5 meters, mend
Plus catalyst added with 0.4kg/t.AN.Run 1 year, propylene is transformed into acrylonitrile efficiency and is
79.7%, catalyst bed layer height and catalyst inventory have no significant change.
Comparative example 2：Reactor operation lines speed is 0.68m/s, from propylene of the present invention
Nitrile catalyst and add catalyst and cyclone separator, catalyst grain size distribution is：Mean diameter
55 μm, calculated in weight percent, particle diameter be more than 90 microns account for 20%, particle diameter be less than 45
Micron account for 40%, particle diameter be less than 20 μm be 16%, cooling water pipe straight length be 5.5 meters, mend
Plus catalyst added with 0.4kg/t.AN.Run 1 year, propylene is transformed into acrylonitrile efficiency and is
79.3%, catalyst inventory shows and has reduced, and catalyst stack less is more than catalyst additional amount.
Claims (12)
1. a kind of ammoxidation of propylene reaction process for industrialized production acrylonitrile, its fluid bed
The operation lines speed of reactor is 0.7-1.0m/s, and wherein, the yield that propylene is converted into acrylonitrile is protected
Hold more than 80%.
2. the ammoxidation of propylene reaction process described in claim 1, wherein, catalyst loss has
Effect controls in below 0.5kg/t.AN.
3. the ammoxidation of propylene reaction process described in claim 1-2, wherein, the top of reactor
Press as 0.40-0.50kg/cm2(G).
4. the ammoxidation of propylene reaction process described in claim 1-2, wherein, catalysis used
The particle size distribution of agent is：Mean diameter is 40～80 μm, and calculated in weight percent, particle diameter
The 0-30% that accounts for more than 90 microns, particle diameter be less than 45 microns account for 30-50%, and particle diameter is little
In 20 μm not higher than 10%.
5. the ammoxidation of propylene reaction process described in claim 4, wherein, during the course of the reaction
Catalyst grain size distribution in periodic sampling analysis reactor, selects adding of different grain size distribution to urge
Agent, with the particle size distribution maintaining catalyst in device be：Mean diameter is 40～80 μm, with
Percentage by weight, particle diameter be more than 90 microns account for 0-30%, particle diameter is less than 45 microns accounting for
30-50%, and particle diameter is less than 20 μm not higher than 10%.
6. a kind of reactor for ammoxidation of propylene reaction process as claimed in claim 1,
Wherein, the organic efficiency of cyclone separator used is more than 99.999%.
7. the reactor for ammoxidation of propylene reaction described in claim 6, wherein, described
Cyclone separator is secondary cyclone.
8. the reactor for ammoxidation of propylene reaction described in claim 6, wherein, described
Secondary cyclone is PV cyclone separator.
9. a kind of reactor for ammoxidation of propylene reaction process as claimed in claim 1,
Wherein, cooling coil straight tube is highly not less than 7.2 meters.
10. the reactor for ammoxidation of propylene reaction described in claim 9, wherein, cold
But the height of coil pipe straight tube is not less than 7.5 meters.
Cooling coil described in 11. claim 9 or 10 is away from dispersion plate upper surface distance
30-150cm.
A kind of 12. reactors for ammoxidation of propylene reaction process, the operation lines of this reactor
Speed is 0.7-1.0m/s, and propylene is converted into the yield of acrylonitrile and is maintained at more than 80%, its
It is characterised by, cyclone separator used is that two grades of whirlwind that organic efficiency is more than 99.999% divide
From device, cooling coil straight tube is highly not less than 7.2 meters, and described cooling coil is distributed away from air
Plate upper surface is apart from 30-150cm.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510552970.7A CN106478457A (en) | 2015-09-02 | 2015-09-02 | Improved ammoxidation of propylene technique and its reactor |
| 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 |
|---|---|---|---|
| CN201510552970.7A CN106478457A (en) | 2015-09-02 | 2015-09-02 | Improved ammoxidation of propylene technique and its reactor |
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| CN106478457A true CN106478457A (en) | 2017-03-08 |
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| CN201510552970.7A Pending CN106478457A (en) | 2015-09-02 | 2015-09-02 | Improved ammoxidation of propylene technique and its reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112584929A (en) * | 2018-08-23 | 2021-03-30 | 旭化成株式会社 | Method for producing catalyst for ammoxidation and method for producing acrylonitrile |
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| CN1188105A (en) * | 1996-11-06 | 1998-07-22 | 日东化学工业株式会社 | Process for producing acrylonitrile |
| CN104136412A (en) * | 2012-02-29 | 2014-11-05 | 三菱丽阳株式会社 | Method for producing acrylonitrile |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1188105A (en) * | 1996-11-06 | 1998-07-22 | 日东化学工业株式会社 | Process for producing acrylonitrile |
| CN104136412A (en) * | 2012-02-29 | 2014-11-05 | 三菱丽阳株式会社 | Method for producing acrylonitrile |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112584929A (en) * | 2018-08-23 | 2021-03-30 | 旭化成株式会社 | Method for producing catalyst for ammoxidation and method for producing acrylonitrile |
| US11701648B2 (en) | 2018-08-23 | 2023-07-18 | Asahi Kasei Kabushiki Kaisha | Method for producing catalyst for ammoxidation, and method for producing acrylonitrile |
| CN112584929B (en) * | 2018-08-23 | 2023-08-15 | 旭化成株式会社 | Method for producing catalyst for ammoxidation and method for producing acrylonitrile |
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