CN104693069A - Improved acrylonitrile production - Google Patents
Improved acrylonitrile production Download PDFInfo
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- CN104693069A CN104693069A CN201510099427.6A CN201510099427A CN104693069A CN 104693069 A CN104693069 A CN 104693069A CN 201510099427 A CN201510099427 A CN 201510099427A CN 104693069 A CN104693069 A CN 104693069A
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
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- 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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C253/00—Preparation of carboxylic acid nitriles
- C07C253/32—Separation; Purification; Stabilisation; Use of additives
- C07C253/34—Separation; Purification
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/00902—Nozzle-type feeding elements
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00991—Disengagement zone in fluidised-bed reactors
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to improved acrylonitrile production. A method comprises the following steps: enabling ammonia, oxygen and hydrocarbon to react in the presence of a catalyst at first pressure so as to provide an acrylonitrile containing reactor effluent flow, wherein the hydrocarbon is selected from a collection consisting of propane, propene, isobutene and a combination thereof; quenching the reactor effluent flow by using a first aqueous flow so as to provide an acrylonitrile containing quenched flow; compressing the quenched flow so as to provide an acrylonitrile containing effluent compressor flow, and transferring the effluent compressor flow to an absorber at second pressure; and absorbing acrylonitrile in a second aqueous flow in the absorber so as to provide acrylonitrile containing rich water, wherein the absorbing is executed at pressure higher than the first pressure.
Description
Technical field
The present invention relates to the technique of the improvement in the manufacture of vinyl cyanide and methacrylonitrile.Specifically, the present invention relates to the technique of the improvement using effluent compressor.
Background technology
Known for the various technique of the manufacture of vinyl cyanide and methacrylonitrile and system; For example, see U.S. Patent No. 6,107,509.Typically, recovery and the purification of the vinyl cyanide/methacrylonitrile produced by the direct reaction of hydrocarbon, ammonia and the oxygen selected from the set be made up of propane, propylene or iso-butylene are in the presence of a catalyst achieved as follows, step is: the reactor effluent containing vinyl cyanide/methacrylonitrile is delivered to the first post (quenching), at this with the first aqueous flow cooling reactor effluent; The effluent of the cooling containing vinyl cyanide/methacrylonitrile is conveyed in the second post (resorber), at this effluent with the second aqueous flow contact cooling, vinyl cyanide/methacrylonitrile is absorbed in the second aqueous flow; The second aqueous flow containing vinyl cyanide/methacrylonitrile is delivered to the first distillation column (recovery post) from the second post, is separated rough vinyl cyanide/methacrylonitrile for from the second aqueous flow; With the rough vinyl cyanide/methacrylonitrile be separated is delivered to after-fractionating post (overhead distillate post (heads column)), to remove at least some impurity from rough vinyl cyanide/methacrylonitrile; The 3rd distillation column (product post) is delivered to, to obtain product acrylonitrile/methacrylonitrile with by Partial cleansing vinyl cyanide/methacrylonitrile.U.S. Pat. Nos. 4,234,510; 3,885,928; 3,352,764; 3,198,750 and 3,044,966 reclaim and purification process exemplified with the typical case for vinyl cyanide and methacrylonitrile.
In common process, reactor pressure must be retrained by resorber exhaust pressure and minimum between reactor and resorber in pressure drop.In common process, this predetermined pressure in reactor is about 8 psig, and typically causes hydrocarbon to be fed to comprising the transformation efficiency of about 80% of the reactor product effluent of vinyl cyanide.Then reactor product effluent is transported to quench vessel.In quench vessel, the quenching of reactor product effluent is made to produce the effluent of the quenching comprising acrylonitrile product.The effluent of quenching is transported to resorber via conduit.In resorber, the effluent of quenching is combined with the water of refrigeration and produces the rich water (rich water) comprising vinyl cyanide, and make the exhaust from resorber be vented burning in incinerator (AOGI) or resorber Vent Oxidation device (AOGO) at resorber.Then the rich water comprising vinyl cyanide generated in resorber be transported to from resorber and reclaim post for further process.In common process, resorber runs at atmosheric pressure, and the water of refrigeration or cooling is added into resorber mixes with the acrylonitrile product of quenching and to generate the rich water comprising vinyl cyanide.
Although the manufacture comprising the vinyl cyanide/methacrylonitrile reclaiming and purify commercially is put into practice for many years, still there is the region of improving producing remarkable benefit wherein.Be suitable for one of these regions of improving the reactor product for improving is transformed.Another improves the demand for reducing to the water refrigerated or cool in resorber.
Summary of the invention
One side of the present disclosure is for providing the safe, effectively and cost effective means and equipment of the shortcoming that overcomes or reduce common process.
A kind of technique comprises at a first pressure and in the presence of a catalyst, make ammonia, oxygen and hydrocarbon reaction carry out the reactor effluent stream of providing package containing vinyl cyanide, this hydrocarbon is selected from the set be made up of propane, propylene, Trimethylmethane and iso-butylene and their combination.This technique also comprises and utilizes the first aqueous flow quench reactor effluent stream, carrys out the quench stream of providing package containing vinyl cyanide, and compresses quench stream and carry out the effluent compressor stream of providing package containing vinyl cyanide.Effluent compressor stream is transported to resorber under being included in the second pressure by this technique, and in resorber, in the second aqueous flow, absorb vinyl cyanide carry out the rich water of providing package containing vinyl cyanide, wherein, the second pressure is greater than the first pressure.
A kind of technique comprises at a first pressure and makes ammonia, oxygen and hydrocarbon reaction be vented to provide pressurized reactor in the presence of a catalyst, and this hydrocarbon is selected from the set be made up of propane, propylene, Trimethylmethane and iso-butylene and their combination.This technique also comprises and pressure exhaust is transported to resorber and the effluent that do not absorb from this resorber is expanded.
Equipment comprises: reactor, it is configured at a first pressure and makes ammonia, oxygen and hydrocarbon reaction carry out the reactor effluent stream of providing package containing vinyl cyanide in the presence of a catalyst, and this hydrocarbon is selected from the set be made up of propane, propylene and iso-butylene and their combination; Quench vessel, it is configured to utilize the first aqueous flow quench reactor effluent stream to carry out the quench stream of providing package containing vinyl cyanide; Effluent compressor, it is configured to compress quench stream and provides the effluent compressor stream comprising vinyl cyanide under the second pressure; And resorber, it is configured to receive effluent compressor stream, and allows to absorb vinyl cyanide in the second aqueous flow, carrys out the rich water of providing package containing vinyl cyanide.
Oxidative ammonolysis technique is included in about 140kPa (absolute pressure) or less pressure and about 0.5 under the speed of about 1.2 meter per seconds, in the presence of a catalyst, make ammonia, oxygen and hydrocarbon reaction to provide reactor effluent stream, this hydrocarbon is selected from the set be made up of propane, propylene, Trimethylmethane and iso-butylene and their combination.
Technique for absorbing the reactor effluent stream comprising vinyl cyanide comprises: utilize the first aqueous flow quench reactor effluent stream to carry out the quench stream of providing package containing vinyl cyanide; Compression quench stream carrys out the effluent compressor stream of providing package containing vinyl cyanide; Under the pressure (absolute pressure) of about 300kPa to about 500kPa, effluent compressor stream is transported to resorber; And in resorber, in the second aqueous flow, absorb vinyl cyanide carry out the rich water of providing package containing vinyl cyanide.
In another aspect, a kind of technique for absorbing the reactor effluent stream comprising vinyl cyanide, this technique comprises: utilize the first aqueous flow quench reactor effluent stream to carry out the quench stream of providing package containing vinyl cyanide; Compression quench stream carrys out the effluent compressor stream of providing package containing vinyl cyanide; Effluent compressor stream is transported to resorber; And in resorber, have about 4 DEG C to about 45 DEG C temperature the second aqueous flow in absorb vinyl cyanide and carry out providing package containing the rich water of vinyl cyanide.
In another aspect, oxidative ammonolysis system comprises turbine, and this turbine is for driving the single driver circuit comprising air compressor and at least one effluent compressor to be effective.
In another aspect, oxidative ammonolysis technique comprises: at about 100kPa (absolute pressure) or less pressure and about 0.5 under the speed of about 1.2 meter per seconds, in the presence of a catalyst, make ammonia, oxygen and hydrocarbon reaction to provide reactor effluent stream, this hydrocarbon is selected from the set be made up of propane, propylene, Trimethylmethane and iso-butylene and their combination.
In related fields, oxidative ammonolysis equipment comprises: reactor, it to be configured under first pressure of about 100kPa (absolute pressure) or less and to make ammonia, oxygen and hydrocarbon reaction carry out the reactor effluent stream of providing package containing vinyl cyanide in the presence of a catalyst, and this hydrocarbon is selected from the set be made up of propane, propylene and iso-butylene and their combination.
In another aspect, oxidative ammonolysis system comprises turbine, this turbine is operatively attached to the single driver of at least one air compressor and at least one effluent compressor for driving, air compressor structure is for providing air to oxidative ammonolysis reactor, effluent compressor constructions is for providing effluent compressor stream to resorber, and oxidative ammonolysis reactor and resorber are configured to allow independently pressure-controlling.
According to the following detailed description of the illustrative embodiments of the present disclosure that accompanying drawing to be combined is read, above-mentioned and other side, feature and advantage of the present disclosure will become clear.
Accompanying drawing explanation
By referring to the following explanation considering accompanying drawing, can obtain the more complete understanding of example embodiment of the present invention and advantage thereof, wherein similar label indicates similar feature, and wherein:
Fig. 1 is the block diagram according to the embodiment being applied to the disclosed aspect that vinyl cyanide manufactures.
Fig. 2 is the block diagram according to another embodiment being applied to the disclosed aspect that vinyl cyanide manufactures.
Fig. 3 illustrates the block diagram comprising the aspect of more than one reactor, quench column and effluent compressor.
Fig. 4 is the block diagram exemplifying single line driving mechanism.
Embodiment
Fig. 1 is the block diagram according to the embodiment being applied to the disclosed aspect that vinyl cyanide manufactures.With reference to accompanying drawing, equipment 100 comprises reactor 10, quench vessel 20, effluent compressor 30 and resorber 40.The stream 3 that ammonia in stream 1 and hydrocarbon (HC) charging of flowing in 2 can be used as combination is supplied to reactor 10.HC incoming flow 2 can comprise hydrocarbon, and this hydrocarbon selects from the set be made up of propane, propylene and iso-butylene and their combination.Catalyzer (not showing in FIG) can be present in reactor 10.Oxygen-containing gas can be supplied to reactor 10.Such as, air can be compressed by air compressor (not showing in FIG) and is supplied to reactor 10.
Vinyl cyanide is produced in the reactor by the reaction of hydrocarbon when being present in reactor 10 at catalyzer, ammonia and oxygen.Reactor 10 can run for 1 time at reactor or the first pressure P, and wherein, the first pressure can be characterized as the pressure at entrance (first step entrance of such as cyclonic separator 22) 17 places.According to the disclosure, cyclonic separator 22 can be the first cyclonic separator of Multicyclone system, and this Multicyclone system can be configured to the stream comprising vinyl cyanide is transported to high-tension room (not showing in FIG).The stream comprising vinyl cyanide can leave high-tension room and go to as reactor effluent stream 4 outside the top section of reactor 10.In one aspect, cyclonic separator 22 can be configured to be separated and may comprise what enter entrance 17 the catalyzer carried secretly in the stream of vinyl cyanide, and by catalyzer loopback leaching pin (dip leg) (not display in FIG), the catalyzer of separation is recycled to the catalyst bed in reactor 10.The reactor effluent stream 4 comprising vinyl cyanide produced in reactor 10 is transported to quench vessel 20 by circuit 11.In this aspect, first pressure is about 140kPa or less, be about 135kPa or less in another aspect, be about 130kPa or less in another aspect, be about 125kPa or less in another aspect, be about 101kPa to about 140kPa in another aspect, be about 110kPa to about 1400kPa in another aspect, be about 125kPa to about 145kPa in another aspect, be about 120kPa to about 140kPa in another aspect, be about 130kPa to about 140kPa in another aspect, be about 125kPa to about 140kPa in another aspect, be about 125kPa to about 135kPa in another aspect, be about 120kPa to about 137kPa in another aspect, be about 115kPa to about 125kPa in another aspect.
In quench vessel 20, reactor effluent stream 4 is cooled by contacting with quenching aqueous flow 5, and this quenching aqueous flow 5 enters quench vessel 20 via circuit 12.Quenching aqueous flow 5 can comprise acid in addition to water.The reactor effluent comprising the cooling of vinyl cyanide (comprising by product, such as acetonitrile, prussic acid and impurity) then can be used as quench stream 6, is transported to effluent compressor 30 via circuit 13.
Quench stream 6 can be compressed by effluent compressor 30, and leaves effluent compressor 30 as compressor effluent stream 7.Compressor effluent stream 7 can have second or compression pressure P2.Via circuit 14, compressor effluent stream 7 can be transported to the comparatively lower part of resorber 40.In resorber 40, vinyl cyanide can be absorbed in second or resorber aqueous flow 8, second or resorber aqueous flow 8 higher part that enters resorber 40 via circuit 15 divide.Then the aqueous flow or rich current 18 that comprise vinyl cyanide and other by product can be delivered to recovery post (not showing in FIG) for further product cleanup via circuit 19 from resorber 40.
Do not absorb effluent 9 to be left by the top of conduit 16 from resorber post 40.Do not absorb effluent 9 and can comprise exhaust, exhaust can be vented burning in incinerator (AOGI) or resorber Vent Oxidation device (AOGO) at resorber.
In one aspect, effluent compressor 30 is by working through circuit 13 attracts quench stream 6.The compressible quench stream 6 of effluent compressor 30, so that its effluent compressor stream 7 as compression leaves effluent compressor 30, this effluent compressor stream 7 has the pressure (second pressure) higher than reactor pressure (the first pressure).In one aspect, pressure in the circuit 14 of the effluent compressor stream 7 of compression is about 2 of the working pressure of reactor 10 to about 11.5 times, be about 2 to about 12.5 times in another aspect, be about 2.5 to about 10 times in another aspect, be about 2.5 to about 8 times in another aspect, be about 2.5 to about 5 times in another aspect, be about 2.5 to about 4 times in another aspect, be about 2.5 to about 3.2 times in another aspect, be about 2 to about 3.5 times in another aspect, be about 2 to about 3 times in another aspect, be about 3 to about 11.25 times in another aspect, be about 5 to about 11.25 times in another aspect, in another aspect for about 7 to about 11.25 times (all comparing based on absolute pressure).In one aspect, second pressure (absolute pressure) is for about 300 to about 500kPa, be about 340kPa to about 415kPa in another aspect, be about 350kPa to about 400kPa in another aspect, be about 250kPa to about 500kPa in another aspect, be about 200kPa to about 400kPa in another aspect, be about 250kPa to about 350kPa in another aspect, be about 300kPa to about 450kPa in another aspect, and be about 360kPa to about 380kPa in another aspect.
In one aspect, when aqueous flow 8 is uncolled or do not refrigerate and/or be in 4 DEG C to about 45 DEG C, operate under aqueous flow 8 flow velocity of the vinyl cyanide final product that the second pressure makes resorber can produce about 15 to about 20kg/kg, and wherein, the rich current of resorber comprise about 5 weight percents or more organism, be about 6 weight percents or more organism in another aspect, and be about 7 weight percents or more organism in another aspect.In another aspect, the flow velocity of aqueous flow 8 can be about 15 to about 19kg/kg vinyl cyanide, is about 15 to about 18kg/kg vinyl cyanide in another aspect, and is about 16 to about 18kg/kg vinyl cyanide in another aspect.In another aspect, aqueous flow that is uncolled or that do not refrigerate is about 20 to about 45 DEG C, is about 25 to about 40 DEG C in another aspect, is about 25 to about 35 DEG C in another aspect, and is about 25 to about 30 DEG C in another aspect.
Cooling system (not showing in FIG) can be positioned on compressor 30 place or its downstream, wherein, cooling system is configured to the effluent compressor stream 7 of compression to be cooled to preset temperature before entering resorber 40, such as, and about 105 ℉ (about 40.5 DEG C).
In one aspect, resorber 40 can comprise 40 to six ten (40-60) individual dish.In one aspect, resorber 40 can comprise 50 (50) individual dishes.The effluent compressor stream 7 of compression can enter resorber 40 below the bottom plate of resorber.In one aspect, resorber 40 can operate under the variable flow rate of cold-storage water (wrapping the cold-storage water of zero content) in the second aqueous flow 8.
In one aspect, resorber 40 can in higher than the resorber in common process pressure pressure under operate.By operating resorber 40 under this elevated pressures, the resorber in comparable common process more effectively operates resorber.Due to the higher resorber efficiency realized in technique of the present disclosure, thus can realize the recovery of vinyl cyanide in the rich current 18 identical with common process, but require that less water absorbs vinyl cyanide in resorber.In this aspect, Fu Shui refers to have about 5 weight percents or more organic water, is about 6 weight percents or more organism in another aspect, and is about 7 weight percents or more organism in another aspect.In one aspect, the water for absorbing vinyl cyanide in resorber can be technique or municipal water (such as, having the temperature of about 4-45 DEG C).In this aspect, technique or municipal water are the water more than about 95 weight percents, be the water of about 97 weight percents or more in another aspect, be the water of about 99 weight percents or more in another aspect, and be the water of about 99.9 weight percents or more in another aspect.In one aspect, the temperature of the second aqueous flow 8 can, in the scope of about 4 to about 45 DEG C, be about 10 to about 43 DEG C in another aspect, and is about 27 to about 32 DEG C in another aspect.
In one aspect, aqueous flow 8 can be free of the water of cooling or refrigeration.In one aspect, aqueous flow 8 can have the temperature higher than the temperature required in the aqueous flow in common process.In one aspect, aqueous flow 8 can comprise cold-storage water, and when aqueous flow 8 comprises cold-storage water, and the flow velocity of aqueous flow 8 can be less than the flow velocity required in the aqueous flow in common process.In this aspect, the first aqueous flow has the temperature of about 20 DEG C to about 50 DEG C, is about 25 DEG C to about 45 DEG C in another aspect, and is about 30 DEG C to about 40 DEG C in another aspect.The about 25kg of vinyl cyanide that the first aqueous flow can be produced with every kg is provided to resorber to the ratio of about 35kg first aqueous flow, and be the about 27kg of vinyl cyanide extremely about 33kg first aqueous flow that every kg produces in another aspect.
In one aspect, reactor 10 can operate under the pressure that required pressure is low in than common process.In the common process without effluent compressor, reactor 10 needs to run under the pressure of about 8psig usually, obtains the transformation efficiency that hydrocarbon is fed to such as 80% of the effluent product comprising vinyl cyanide or more.In in of the present disclosure, this technique is included in and operates reactor 10 than under the pressure of about 35 to about 50% low in common process (absolute pressure basis).In of the present disclosure, this technique operates reactor 10 under being included in the pressure of about 4-5psig.Have been found that, by reducing the working pressure of reactor 10 according to the disclosure, the transformation efficiency of hydrocarbon be fed to vinyl cyanide at least about 70% or more can be realized, be about 75% or more in another aspect, be about 81% or more in another aspect, and be about 82% or more in another aspect.
Fluidized-bed reactor is in the center of vinyl cyanide factory.Fail correctly to design new reactor and can affect the efficiency of whole vinyl cyanide factory, reliability or throughput at least significantly, and cause the prolonged shutdowns produced in extreme circumstances when reactor amendment or change should be performed.The operation of fluidized-bed is extremely sensitive to the concrete operations condition selected, and industry is at the design aspect extreme caution changing operational condition and/or reactor or its inside.Due to operation window (such as pressure and fluidization rate) or fluidized-bed characteristic variations (such as, the ratio of reactor diameter, inside, bed height, bed pressure drop and grid (grid) pressure drop) and specificity of catalyst change (particle size, particle size distribution, fine particle content, rubbing characteristics), the critical cycle pattern also alterable thus in fluidized-bed.
One of most sensitive parameter that can affect fluidizing performance is the increase in proportion of reactor diameter.In this aspect, reactor can have the internal diameter of about 5 to about 15 meters, is about 7 to about 12 meters in one aspect, is about 8 to about 11 meters in another aspect, and is about 9 to about 11 meters in another aspect.Reactor diameter is also cause one of parameter increasing attention at most in proportion because exist restricted can with alleviating option, excessive diameter is corrected in the reactor change of shortage increases in proportion.By a considerable amount of experiment and optimization, have been found that, when using the catalyzer of the average particulate diameter had between about 10 and 100 μ, wherein particle size distribution is that about 0 to 30 weight percent is greater than about 90 μ, and when about 30 to 50 weight percents are less than 45 μ, when operating under the reactor pressure of about 140kPa or lower, the reactor inside diameter of 11m is greater than about 9m until approximately can be combined the acceptable fluidization conditions of the production realized for vinyl cyanide and methacrylonitrile with suitable operational condition and inside reactor, be about 135kPa or lower in another aspect, be about 130kPa or lower in another aspect, be about 125kPa or lower in another aspect, be about 101Kpa to about 140kPa in another aspect, be about 110kPa to about 140kPa in another aspect, be about 125kPa to about 145kPa in another aspect, be about 120kPa to about 140kPa in another aspect, be about 130kPa to about 140kPa in another aspect, be about 125kPa to about 140kPa in another aspect, be about 125kPa to about 135kPa in another aspect, be about 120kPa to about 137kPa in another aspect, and be about 115kPa to about 125Kpa in another aspect.
Because reactor pressure reduces, so need to increase reactor diameter and/or reactor speed, to realize the given productivity of vinyl cyanide.In addition under having been found that the reactor pressure reduced at these, alternatively under larger diameter, go back the relatively high bed height of possible operation and bed diameter ratio, thus make catalyst inventory maximize the increase simultaneously reducing diametrically.In one aspect, the catalyst bed pressure drop of about 30 to 40% (minimum) when air grid design is provided in the reactor underproduction.Determine, as long as catalyzer is within the scope of above-mentioned particle characteristics, and the frictionloss preferably had between about 1 and 4%, so for the reactor of internal diameter with 9 to 11m, fluidization rate (based on effluent volume flow with except spiral coil cooling tube and the leaching extra-regional reactor cross section area of pin (" CSA ")) until operate under 1.2m/s, can be preferably between 0.55 and 1.Currently known methods can be used to determine frictionloss, the The 13th International Conference on Fluidization – New Paradigm in Fluidization Engineering of such as Hartge etc., Art.33 (2010), based on ASTM D4058 and ASTM D5757, and U.S. Patent No. 8, the method of 455,388 (they all by reference and entirety is incorporated herein).In related fields, the total catalyst loss carrying out autoreactor can be about 0.35 vinyl cyanide produced to about 0.45kg/ metric ton.
Even if until under indicated speed, also have been found that when operation has about 0.25 to about 0.45kg/cm
2the reactor of top pressure, and/or when there is the pressure drop of 15kPa or less and depart from the cyclonic separator of height higher than fluidized-bed top about 5.5 to the particulate of about 7.5m, may to operate under acceptable catalyst loss.Thus when the reactor inside diameter utilizing about 9 to about 11m according to the present invention, use there is average particulate diameter between about 10 and 100 μ catalyzer (wherein particle size distribution be about 0 to 30 weight percent be greater than about 90 μ, and about 30 to 50 weight percents are less than 45 μ) time, find, when at about 0.4m and 1.05m/s, when operating under the fluidization rate (based on effluent volume flow with except spiral coil cooling tube and the extra-regional reactor cross section area of leaching pin) preferably between 0.55 and 0.85m/s, the reactor diameter of about 0.45 to about 0.6 and the ratio of reactor cylinder height (tangent line is to tangent line) are effective.Thus this cause the possibility of the throughput of the per unit reactor volume (tangent line is to tangent line) of the increase between 0.005 and 0.015 tonne of every cubic metre of reactor volume per hour, being about 0.0075 to about 0.0125 in another aspect, is about 0.009 to about 0.01 tonne of every cubic metre of reactor volume per hour in another aspect.
Expect to guarantee to optimize the specific storage that reactor efficiency increases (comprising about agent transforms and catalyst loss) reactor simultaneously.The design of cyclonic separator is crucial to the working pressure of reactor, catalyst loss (comprise and caused by friction) and the height for reactor (tangent line is to tangent line) of requirement.Have been found that, at the first step cyclone inlet speed of about 20 to about 30 and the ratio of reactor effluent speed, and/or the ratio of the height of first step cyclonic separator is when being about 4% to about 7% of height for reactor (tangent line is to tangent line), above-mentioned gratifying reactor operation window can be realized.As shown in Figure 3, cyclonic separator height is determined according to the distance of the distal section 107 of top 101 to the cyclonic separator from cyclonic separator.
In one aspect, reactor 10 can be configured to, and for predetermined catalyzer, has the handling capacity larger than the conventional reactor with identical predetermined catalyzer and predetermined height for reactor.In one aspect, the reactor handling capacity of a kind of method for improving predetermined catalyzer and predetermined height for reactor is provided.Augmenting response device diameter while the method is included in and maintains predetermined top pressure.The method can comprise the predetermined reactor design speed of maintenance.
In one aspect, a kind of technique comprises operation or makes hydrocarbon reaction in the reactor, wherein, reactor has the predetermined reactor inside diameter of the reactor cylinder height (tangent line is to tangent line) being greater than about 40% to about 60%, and is about 45% to about 55% in another aspect.These are different from common process, and common process comprises the reactor that operation has the reactor diameter of about 40% of height for reactor.In related fields, height for reactor (tangent line is to tangent line) can be about 10 to about 25 meters, being about 10 to about 20 meters in another aspect, is about 12 to about 18 meters in another aspect, and is about 14 to about 16 meters in another aspect.
In one aspect, this technique comprises operation or makes hydrocarbon reaction in the reactor, wherein, the fluidized bed height of about 40% to about 60% of reacting appliance promising reactor cylinder height (tangent line is to tangent line), be about 42% to about 50% in another aspect, be about 45% to about 55% in another aspect, and be about 44% to about 47% in another aspect.These are different from common process, common process comprise operation have for height for reactor (tangent line is to tangent line) about 25% fluidized bed height, and therefore there is the reactor of larger disengaging height.
In one aspect, this technique comprises operation or makes hydrocarbon reaction in the reactor, wherein, the fluidized bed height of about 70% to about 110% of the promising reactor diameter of reacting appliance, being about 70% to about 100% in another aspect, is about 75% to about 90% in another aspect, is about 80% to about 90% in another aspect, be about 85% to about 95% in another aspect, and be about 85% to about 90% in another aspect.These are different from common process, common process comprise operation have for reactor diameter about 65% the reactor of fluidized bed height.
In one aspect, this technique comprises operation or makes hydrocarbon reaction in the reactor, and wherein, reactor has about 0.25 to about 0.45kg/cm
2scope in top pressure, be about 0.3 to about 0.5kg/cm in another aspect
2, be about 0.2 to about 0.4kg/cm in another aspect
2, and be about 0.2 to about 0.5kg/cm in another aspect
2.Reactor head pressure in this scope provides the benefit of the catalyst performance of the improvement being better than the reactor head pressure higher than this scope.In one aspect, the method is included in about 0.4 to about 0.45kg/cm
2scope in operant response device.
In one aspect, the method comprises operation or makes hydrocarbon reaction in the reactor, wherein, effluent volume flow has the linear velocity of about 0.5 to about 1.2m/sec (based on effluent volume flow with except spiral coil cooling tube and the leaching extra-regional reactor cross section area of pin (" CSA "), that is, the open CSA of ~ 90%).Have been found that, likely use this speed to design and operant response device system, also realize good fluidisation/catalyst performance and the rational catalyst entrainment/catalyst loss from cyclonic separator simultaneously, the speed when reactor capacity increases can be maintained in this scope about as much as possible.In an embodiment, can until about 0.75m/sec to about 0.95m/sec speed (based on 90%CSA and effluent gas) under operate reactor, and maintain about 0.25 to about 0.5kg/cm
2top pressure, and be about 0.2 to about 0.45kg/cm in another aspect
2.In one aspect, in the cyclone inlet speed of meter per second be 20 or larger in the ratio of the reactor effluent speed of meter per second, be about 20 to about 30 in another aspect, be about 22 to about 25 in another aspect, be about 23 to about 26 in another aspect, and be about 27 to about 29 in another aspect.
Because fluidization rate increases, the possibility of the thus friction of catalyzer also increases.The speed increased also causes the larger particulate above fluidized-bed to depart from height.Thus the increase of this gained of particulate aspect also can increase the solid supported on cyclonic separator.
In one aspect, have been found that by operant response device or make hydrocarbon reaction in the reactor, wherein, reactor has: predetermined reactor diameter, and it has the length in the scope of about 45% to about 60% of the length at height for reactor; The length of fluidized bed height, it is about 80% of the length of reactor diameter to about 95%; Pressure, its about 0.3 to about 0.5kg/cm
2scope in; With reactor speed (based on 90%CSA and effluent gas), it is about 0.6 to about 0.65m/sec, this technique can produce such as below fado until about 100% or more acrylonitrile product, in the method, operant response device, wherein, reactor diameter is about 40% of height for reactor, fluidized bed height is about 25% of height for reactor, and fluidized bed height is about 65% of reactor diameter.
In one aspect, wherein, reactor diameter is the internal diameter of at least 8m and uses optimizing integration of above-mentioned feature, equipment and method provide about 12.5 tonnes/hr or the reactor capacity based on the every reactor of the annual 100ktpa of 8000 hours run.Wherein, reactor diameter is 10.5m, and single reactor capacity can between 15 and 20 tonnes/hr.
For the determination of the fluidized bed height of the application
Reactor needs equipment at least 3 nozzles, for the following fluidized-bed pressure reduction of measurement:
1) first in these nozzles bottom (above air distributor) orientated as close to fluidized-bed.In this aspect, nozzle can above air distributor about 0.1 to about 0.7 meter, and is about 0.2 to about 0.4 meter in another aspect.
2) second in these nozzles top about 2 meters (still in fluidized-bed) being typically positioned at first jet.Distance must be known to calculating accurately.
3) the 3rd nozzle is positioned at the top place (higher than fluidized-bed) of reactor.
By measuring pressure reduction between the first and second nozzles and measuring at the first and the 3rd pressure reduction between nozzle, bed height can be calculated as follows:
Bed height=(distances between the first and second nozzles) x (the first-three pressure reduction)/(the first-the second pressure reduction).
Note in the equation above, assuming that fluidized bed densities approximately constant.
Unit for two pressure measurements needs for each to be identical, but can be any typical pressure unit (such as, lbs/in
2, inch of water or millimeter water column).
Unit for the distance between tap (tap) can be any typical parasang (such as foot or rice).Bed height is by the same units for selecting.
Preferably measure pressure reduction with two differential pressure transmitter, one for first-second nozzle differential pressure measurement, and one for the first-three nozzle differential pressure measurement.Usual fluidizing air purge nozzle keeps them unimpeded.In this aspect, the air speed purged for nozzle is about 2 to about 8m/sec.
In one aspect, equipment 100 can comprise water injection system 23 (as shown in Figures 1 and 2), and it is configured at least one surperficial jet water course 24 of effluent compressor 30 to reduce the dirt on this surface.In one aspect, variable-ratio turbine can use together with effluent compressor 30.
In one aspect, when top pressure operant response device 10 with about 5psig, the effluent gas of cooling must be compressed before can being further processed.In one aspect, gas leaves compressor attraction separator and flows to the first section of effluent compressor 30.Can demineralization jet of water-be injected into compressor be attracted in circuit and spray-be injected in diffuser passageway.This water injects and can be configured to maintain moisture film, so that can not accumulated deposits in rotation and static surface.This water injects and can be configured to make throughout the gas of effluent compressor minimized (and thus making polymer synthesis speed minimize).Evaporation by some in jet of water reduces gas temperature.This net benefits can be the acceptable operation factor for effluent compressor.
Gas from effluent compressor first section can travel across effluent compressor intercooler.The gas of cooling can flow to separator between compressor stage, removes condensation product wherein.Gas from separator can be transported to the second section of effluent compressor, and wherein, mode that can be identical with the first section with effluent compressor 30 utilizes jet of water.From the second section, effluent gas can be cooled in effluent compressor aftercooler or interchanger.The mixture of gas and condensation product can leave aftercooler or interchanger, and enters resorber 40 below the bottom plate of resorber 40.
Process condensate thing can remove from stage separation device, and is back to attraction separator by pressure reduction, and at this, it mixes with the condensation product of the secondary flow effluent water cooler from effluent upstream of compressor.In conjunction with process condensate thing can be recycled to the technique side entrance of secondary flow effluent water cooler and compression stage interstage cooler.Clean condensation product can deliver to the entrance of aftercooler.To provide washing liq above the tube sheet that condensation product can be injected in these interchanger, contribute to the cleaning inside keeping Tube Sheet of Heat Exchanger.
In one aspect, effluent compressor 30 can have shell and wheel, and this wheel construction injects attraction and wheel passage, to maintain the moisture film throughout compressor for allowing demineralization make up water with predetermined amount.These washing water can be provided by controller and control.Can be the be added to professional etiquette of inhibitor to washing water to determine.
In one aspect, effluent compressor 30 can be set in quenching and be cooled to about 105 ℉ (40.5 DEG C) control response device effluent gas afterwards in size.Gas velocity and composition can be derived from predetermined output and speed.A part for resorber exhaust can be used as eluent gas (stripping gas) for quench bottom elutriator.This eluent gas can be recycled to resorber 40 via effluent compressor 30, and effluent compressor 30 can be set to the stream for this increase in size.
In one aspect, effluent compressor frame size configurations can be the excess load (overcapacity) allowing about 5%.If in identical frame dimensions, so in another aspect, altogether can provide until about 35% additional overcapacity, being about 25% in another aspect, is about 15% in another aspect, and is about 10% in another aspect.For each in these two sections, the maximum exhaust temperature maintained by jet of water can be 200 Fahrenheit degrees (93.3 DEG C).
In one aspect, when compressive flow effluent compressor stream 7 enters resorber 40, process condensate thing can be transported to resorber storage tank or be used in other technique mutually, and the katabatic drainage of gas and absorption water or the second aqueous flow 8 upwards flows through resorber dish (valve type dish) on the contrary.Can extract out, cool and deliver to the top disc of resorber from reclaim post for the poor-water that absorbs.In one aspect, do not provide refrigeration to poor-water, and not to any other part supplies refrigeration of resorber.
Leave the gas of absorber overhead in fact not containing vinyl cyanide and other organism, but carbon monoxide and unconverted hydrocarbon (such as propane) can be comprised.Environmental requirement can make to be necessary to eliminate these compounds before will being discharged to air.The elimination of these compounds can utilize incinerator or oxidizer system (such as AOGO 21) to realize.
Absorber bottom water or rich water comprise vinyl cyanide and other organism of recovery, and these rich current can deliver to vinyl cyanide recovery post.
As shown in Figure 3, equipment 300 comprises the feature identical with equipment 100, and comprises expander 302.Expander 302 can be configured to make from the unabsorbed effluent 9 of resorber 40 pressure expansion or be reduced to lower pressure.In one aspect, expander 302 can be configured to the Pressure Drop not absorbing effluent 9 to be low to moderate about 1/17.5 to 1/22.5.In one aspect, expander 302 can be configured to reduce the pressure not absorbing effluent 9, and it can be identical with the pressure in resorber.Such as, expander 302 can be configured to reduce the pressure of the about 35-45psig not absorbing effluent 9, and what provide expansion does not absorb effluent 25, and it has the lower pressure of about 2psig or less.In this aspect, this expansion causes the reduction of the pressure (absolute pressure) from about 300kPa to about 500kPa to the pressure (absolute pressure) of about 115kPa or less not absorbing effluent pressure from resorber.What expand does not absorb effluent 25 and can be transported to AOGO 21 via circuit 26 from expander 302.
Equipment 300 can comprise preheater 303.Preheater 303 can be configured to not absorb effluent 9 from the preheating temperature of about 25 DEG C to about 40 DEG C to about 350 DEG C or higher temperature, and is the temperature of about 37.7 DEG C to about 371.1 DEG C in another aspect.By carrying out preheating to it not absorbing before effluent 9 enters expander 302, can avoid or reduce the condensation in expander 302.In one aspect, when not absorbing effluent 9 and expanding in expander 302, its temperature is reduced to the temperature of about 200 DEG C to about 260 DEG C from the temperature of about 300 DEG C to about 400 DEG C.
In one aspect, in resorber exhaust incinerator (AOGI) or resorber Vent Oxidation device (AOGO) 21, the fuel gas do not absorbed required by effluent 25 of burning expansion can be less than the still unexpanded fuel gas do not absorbed required by effluent 9 of burning.Have been found that the expander pressure drop by improving in expander 302, in AOGO 21, burning expansion does not absorb effluent 25 and can require less fuel gas.Such as, have been found that the pressure drop by improving in expander 302, temperature T3 can be about 500 ℉ (about 260 DEG C), instead of about 400 ℉ (about 204.4 DEG C).The temperature T3 that effluent 25 has about 500 ℉ (about 260 DEG C) is not absorbed when what expand, instead of during the temperature of about 400 ℉ (about 204.4 DEG C), in AOGO 21, the effluent 25 that do not absorb of burning expansion requires less fuel gas, and requires that less water to absorb vinyl cyanide to produce rich current 18 in resorber 40.Have been found that deliberately a small amount of acrylonitrile product of loss is more cost-efficient to the fuel gas reduced needed for the burning in AOGO 21 in some applications.
As shown in Figure 3, equipment 500 can comprise First Series 501 and second series 502.Each series can be similar or identical with the equipment 100 or 300 described before.As shown in Figure 3, each series can comprise himself reactor 10, quench vessel 20, effluent compressor 30 and resorber 40, and can operation series concurrently.In one aspect, each series can comprise the AOGO 21 of himself.In one aspect, each resorber of each series can be configured to second or the resorber aqueous flow 8 that receive himself, this second or resorber aqueous flow 8 supply in the circuit 15 separated with another series.Each circuit 15 of each series can receive resorber aqueous flow 8, and wherein, stream 8 reclaims in the operation of post 503 for vinyl cyanide or reclaims at vinyl cyanide in the operation of post 503 and generates.Rich current 18 from each resorber of each series can be transported to vinyl cyanide and reclaim post 503.These rich current can combine before further processing.
In one aspect, oxidative ammonolysis system comprises turbine, and this turbine is for driving the single driver circuit comprising air compressor and at least one effluent compressor to be effective.This turbine can be selected from the set be made up of steam turbine, gas turbine, electric turbine and variable-ratio electricity turbine.As shown in Figure 4, high pressure steam is provided to steam turbine 412.In this aspect, the steam being provided to steam turbine 412 has the pressure of about 600psig or larger, and is about 600 to about 700psig in another aspect.Steam turbine 412 is for driving the single driver circuit 417 comprising one or more air compressor 402, one or more effluent compressor 30 and at least one expander 302 to be effective.Air compressor 402 is configured to provide air to reactor 10, and effluent compressor 30 is configured to provide effluent stream to resorber 40.
In another aspect, reactor 10 and resorber 40 can comprise valve (not shown) separately.Valve constitution is allow the independence of reactor 10 and resorber 40 to control.Such as, when starting, the valve on reactor 10 can lead to air to stop vacuum formation in reactor 10.
In one aspect, method and apparatus of the present disclosure provides the handiness than ordinary method and the large operating aspect of equipment.Such as, method and apparatus of the present disclosure provides the handiness of larger underproduction aspect or uses lower speed in demand than when ordinary method and the few vinyl cyanide output of equipment.
Effluent compressor is typically cheap than chiller arrangement, in common process, needs this refrigerator device to provide cold-storage water to resorber.For this reason, equipment of the present disclosure and method can have than conventional equipment and the low capital outlay of method.
In one aspect, found that aforesaid method can realize transforming than reactor product high in common process, this common process is not included in the 3rd pressure contracting quench stream and the absorption being greater than the first pressure.In one aspect, have been found that, by operating resorber under the pressure higher than the pressure in the resorber in common process, using less cold-storage water and/or than when being used as the water of refrigeration hydro-thermal of absorption aqueous flow in common process, the rich water comprising vinyl cyanide can generated in resorber.
In another aspect, oxidative ammonolysis technique comprises: at about 100kPa (absolute pressure) or less pressure and about 0.5 under the speed of about 1.2 meter per seconds, makes ammonia, oxygen and hydrocarbon (it selects from the set be made up of propane, propylene, Trimethylmethane and iso-butylene and their combination) react in the presence of a catalyst and provides reactor effluent stream.Reaction can be carried out under the pressure of about 5kPa (absolute pressure) to about 100kPa (absolute pressure), be about 10kPa (absolute pressure) to about 90kPa (absolute pressure) in another aspect, be about 20kPa (absolute pressure) to about 80kPa (absolute pressure) in another aspect, be about 30kPa (absolute pressure) to about 70kPa (absolute pressure) in another aspect, and be about 40kPa (absolute pressure) to about 60kPa (absolute pressure) in another aspect.Have been found that, by reducing the working pressure of reactor 10 as noted, the transformation efficiency of hydrocarbon be fed to the effluent comprising vinyl cyanide at least about 70% or more can be realized, be about 75% or more in another aspect, be about 81% or more in another aspect, and be about 82% or more in another aspect.
Although describe the disclosure in conjunction with its some preferred embodiment in the foregoing specification, and set forth many details for illustration object, but what it will be appreciated by one of skill in the art that is, the embodiment that disclosure tolerable is extra, and some in details as herein described can change significantly when not departing from ultimate principle of the present invention.Should understand, when not departing from the scope of spirit and scope of the present disclosure or claim, feature of the present disclosure is allowed amendment, change, change or is substituted.Such as, the size of various component, quantity, size and shape can change to mate specific application.Therefore, shown and described in this article specific embodiment is only for illustrating object.
Claims (50)
1. a technique, comprising:
At the first pressure and when there is catalyzer in the reactor, make ammonia, oxygen and hydrocarbon reaction carry out the reactor effluent stream of providing package containing vinyl cyanide, described hydrocarbon is selected from the set be made up of propane, propylene, Trimethylmethane and iso-butylene and their combination;
The quench stream of providing package containing vinyl cyanide is carried out with reactor effluent stream described in the first aqueous flow quenching;
Compress described quench stream and carry out the effluent compressor stream of providing package containing vinyl cyanide;
Under the second pressure, described effluent compressor stream is transported to resorber; And
In described resorber, the vinyl cyanide be absorbed in the second aqueous flow carrys out the rich water of providing package containing vinyl cyanide,
Wherein, described second pressure is greater than described first pressure,
Wherein, described reactor has about 0.5 to the linear velocity of about 1.2 meter per seconds.
2. technique according to claim 1, is characterized in that, described second pressure (absolute pressure) is about 2 times to about 12 times of described first pressure.
3. technique according to claim 1, is characterized in that, described second pressure is about 300kPa (absolute pressure) to about 500kPa (absolute pressure).
4. technique according to claim 1, is characterized in that, described first pressure is about 140kPa (absolute pressure) or less.
5. technique according to claim 1, is characterized in that, described first pressure is the pressure of the ingress of cyclonic separator at described reactor.
6. technique according to claim 5, is characterized in that, described entrance is the entrance of the first step cyclonic separator of Multicyclone system.
7. technique according to claim 1, is characterized in that, described technique is effective for the transformation efficiency providing the hydrocarbon of about 70% or more to be fed to vinyl cyanide.
8. technique according to claim 1, is characterized in that, described second aqueous flow has the temperature of about 4 DEG C to about 45 DEG C.
9. technique according to claim 8, is characterized in that, described second aqueous flow has the temperature of about 20 DEG C to about 45 DEG C.
10. technique according to claim 9, is characterized in that, described second aqueous flow has the flow velocity of the vinyl cyanide final product that about 15 to about 20kg/kg produce.
11. techniques according to claim 1, is characterized in that, also comprise make from described resorber do not absorb effluent expand reduce described in do not absorb the pressure of effluent.
12. techniques according to claim 11, it is characterized in that, described expansion cause from the pressure not absorbing effluent described in described resorber from about 300kPa (absolute pressure) to 500kPa the pressure of (absolute pressure) to the reduction of about 150kPa (absolute pressure) or less pressure.
13. techniques according to claim 11, is characterized in that, before being also included in the step of described expansion, preheating does not absorb effluent described in described resorber.
14. techniques according to claim 13, is characterized in that, the described temperature not absorbing effluent is increased to about 350 DEG C or higher temperature from the temperature of about 25 DEG C to about 40 DEG C by described preheating.
15. techniques according to claim 11, is characterized in that, during the step of described expansion, the described temperature not absorbing effluent is reduced to the temperature of about 200 DEG C to about 260 DEG C from the temperature of about 300 DEG C to about 400 DEG C.
16. techniques according to claim 1, is characterized in that, described reactor has about 0.5 to the linear velocity of about 1.2 meter per seconds.
17. techniques according to claim 1, is characterized in that, described reactor has the internal diameter of about 5 to about 15 meters.
18. techniques according to claim 1, is characterized in that, described reactor has the internal diameter of about 9 to about 12 meters.
19. techniques according to claim 1, is characterized in that, described reactor has the height (tangent line is to tangent line) of about 10 to about 25 meters.
20. 1 kinds of techniques, comprising:
At a first pressure and in the presence of a catalyst, ammonia, oxygen and hydrocarbon reaction are vented to provide the reactor of compression, described hydrocarbon is selected from the set be made up of propane, propylene, Trimethylmethane and iso-butylene and their combination, wherein, described reaction is carried out having about 0.5 to the reactor of the linear velocity of about 1.2 meter per seconds;
The exhaust of described compression is transported to resorber; And
The effluent that do not absorb from described resorber is expanded.
21. techniques according to claim 20, is characterized in that, described expansion causes the pressure of described exhaust to the reduction of about 150kPa (absolute pressure) or less pressure.
22. techniques according to claim 20, is characterized in that, described expansion causes the pressure of described exhaust to the reduction of about 115kPa (absolute pressure) or less pressure.
23. techniques according to claim 20, is characterized in that, also comprise and being vented described in preheating before inflation.
24. techniques according to claim 23, is characterized in that, the temperature of described exhaust is increased to about 350 DEG C or higher temperature from the temperature of about 25 DEG C to about 40 DEG C by described preheating.
25. techniques according to claim 20, is characterized in that, during the step of described expansion, the temperature of described exhaust is reduced to the temperature of about 200 DEG C to about 260 DEG C from the temperature of about 300 DEG C to about 400 DEG C.
26. techniques according to claim 20, it is characterized in that, process comprises:
The quench stream of providing package containing vinyl cyanide is carried out with reactor exhaust described in the first aqueous flow quenching;
Compress described quench stream and carry out the effluent compressor stream of providing package containing vinyl cyanide;
Under the second pressure, described effluent compressor stream is transported to resorber; And
In described resorber, the vinyl cyanide be absorbed in the second aqueous flow carrys out the rich water of providing package containing vinyl cyanide,
Wherein, described second pressure is greater than described first pressure.
27. techniques according to claim 26, is characterized in that, about 2 times to about 12 times that described second pressure (absolute pressure) is described first pressure.
28. techniques according to claim 26, is characterized in that, described second pressure is about 300kPa (absolute pressure) to about 500kPa (absolute pressure).
29. techniques according to claim 26, is characterized in that, described first pressure is the pressure of the ingress of cyclonic separator at described reactor.
30. techniques according to claim 29, is characterized in that, described entrance is the entrance of the first step cyclonic separator of Multicyclone system.
31. techniques according to claim 26, is characterized in that, described technique is effective for the transformation efficiency providing the hydrocarbon of about 70% or more to be fed to vinyl cyanide.
32. techniques according to claim 26, is characterized in that, described second aqueous flow has the temperature of about 4 DEG C to about 45 DEG C.
33. techniques according to claim 32, is characterized in that, described second aqueous flow has the temperature of about 20 DEG C to about 45 DEG C.
34. techniques according to claim 33, is characterized in that, described second aqueous flow has the flow velocity of the vinyl cyanide final product that about 15 to about 20kg/kg produce.
35. 1 kinds of equipment, comprising:
Reactor, it is configured at a first pressure and in the presence of a catalyst, make ammonia, oxygen and hydrocarbon reaction carry out the reactor effluent stream of providing package containing vinyl cyanide, described hydrocarbon is selected from the set be made up of propane, propylene and iso-butylene and their combination;
Quench vessel, it is configured to carry out the quench stream of providing package containing vinyl cyanide with the first aqueous flow quench reactor effluent stream;
Effluent compressor, it is configured to carry out providing package containing the effluent compressor stream of vinyl cyanide in the second pressure described quench stream that contracts; And
Resorber, it is configured to receive described effluent compressor stream, and allows the absorption of the vinyl cyanide in the second aqueous flow, carrys out the rich water of providing package containing vinyl cyanide,
Wherein, reactor, effluent compressor described in one or more, and be configured to allow independently pressure-controlling.
36. equipment according to claim 35, is characterized in that, described second pressure (absolute pressure) is about 2 to 12 times of described first pressure.
37. equipment according to claim 35, is characterized in that, described second pressure is about 300kPa (absolute pressure) to about 500kPa (absolute pressure).
38. equipment according to claim 35, is characterized in that, described first pressure is about 140kPa (absolute pressure) or less.
39. equipment according to claim 35, is characterized in that, described first pressure is the pressure of the ingress of cyclonic separator at described reactor.
40. equipment according to claim 35, is characterized in that, described second aqueous flow has the temperature of about 4 DEG C to about 45 DEG C.
41. equipment according to claim 40, is characterized in that, described second aqueous flow has the temperature of about 20 DEG C to about 45 DEG C.
42. equipment according to claim 41, is characterized in that, described second aqueous flow has the flow velocity of the vinyl cyanide final product that about 15 to about 20kg/kg produce.
43. equipment according to claim 35, is characterized in that, also comprise expander, and described expander is configured to make expand from the effluent that do not absorb of described resorber, not absorb the pressure of effluent described in reducing.
44. equipment according to claim 35, is characterized in that, described expander is configured to be low to moderate about 150kPa (absolute pressure) or less pressure by from the Pressure Drop not absorbing effluent described in described resorber.
45. equipment according to claim 35, is characterized in that, also comprise preheater, and described preheater is configured to carrying out preheating from not absorbing described in described resorber before effluent expands in described expander to it.
46. equipment according to claim 45, is characterized in that, described preheater is configured to the described temperature not absorbing effluent to be increased to about 350 DEG C or higher temperature from the temperature of about 25 DEG C to about 40 DEG C.
47. equipment according to claim 43, is characterized in that, described expander is configured to the described temperature not absorbing effluent to be reduced to the temperature the scope of about 200 DEG C to about 260 DEG C from the temperature of about 300 DEG C to about 400 DEG C.
48. equipment according to claim 35, is characterized in that, described reactor has about 0.5 to the linear velocity of about 1.2 meter per seconds.
49. equipment according to claim 35, is characterized in that, described reactor has the internal diameter of about 5 to about 15 meters.
50. equipment according to claim 35, is characterized in that, described reactor has the height (tangent line is to tangent line) of about 10 to about 25 meters.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510099427.6A CN104693069A (en) | 2015-03-06 | 2015-03-06 | Improved acrylonitrile production |
| RU2017134470A RU2017134470A (en) | 2015-03-06 | 2016-03-03 | IMPROVED ACRYLONITRIL PRODUCTION |
| PCT/US2016/020565 WO2016144667A2 (en) | 2015-03-06 | 2016-03-03 | Improved acrylonitrile manufacture |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510099427.6A CN104693069A (en) | 2015-03-06 | 2015-03-06 | Improved acrylonitrile production |
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| CN104693069A (en) * | 2015-03-06 | 2015-06-10 | 英尼奥斯欧洲股份公司 | Improved acrylonitrile production |
| CN113336669A (en) * | 2015-03-06 | 2021-09-03 | 英尼奥斯欧洲股份公司 | Improved acrylonitrile manufacture |
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| CN1832910A (en) * | 2003-08-06 | 2006-09-13 | 巴斯福股份公司 | Operation of a continuous heterogeneously catalyzed gas phase partial oxidation of at least one organic compound |
| CN102659625A (en) * | 2012-04-20 | 2012-09-12 | 中国天辰工程有限公司 | Industrial production method of acrylonitrile |
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| US3044966A (en) | 1959-08-05 | 1962-07-17 | Standard Oil Co | Attrition resistant oxidation catalysts |
| US3198750A (en) | 1962-12-26 | 1965-08-03 | Standard Oil Co | Mixed antimony oxide-uranium oxide oxidation catalyst |
| US3352764A (en) | 1966-05-02 | 1967-11-14 | Standard Oil Co | Absorption and distillation process for separating crude unsaturated nitriles from acetonitrile with selective solvent recycle |
| US4234510A (en) | 1973-06-07 | 1980-11-18 | Standard Oil Company | Recovery of acrylonitrile or methacrylonitrile by condensation |
| US3885928A (en) | 1973-06-18 | 1975-05-27 | Standard Oil Co Ohio | Acrylonitrile and methacrylonitrile recovery and purification system |
| US4246191A (en) * | 1979-08-13 | 1981-01-20 | Uop Inc. | Ammoxidation process |
| US4868330A (en) * | 1988-04-06 | 1989-09-19 | The Boc Group, Inc. | Process for the production of nitriles |
| US6107509A (en) * | 1999-03-31 | 2000-08-22 | The Standard Oil Company | Process for the recovery of acrylonitrile and methacrylontrile |
| US8455388B2 (en) | 2010-03-23 | 2013-06-04 | Ineos Usa Llc | Attrition resistant mixed metal oxide ammoxidation catalysts |
| KR101528986B1 (en) * | 2010-12-27 | 2015-06-15 | 아사히 가세이 케미칼즈 가부시키가이샤 | Method for purifying acrylonitrile |
| CN104693069A (en) * | 2015-03-06 | 2015-06-10 | 英尼奥斯欧洲股份公司 | Improved acrylonitrile production |
-
2015
- 2015-03-06 CN CN201510099427.6A patent/CN104693069A/en active Pending
-
2016
- 2016-03-03 RU RU2017134470A patent/RU2017134470A/en unknown
- 2016-03-03 WO PCT/US2016/020565 patent/WO2016144667A2/en active Application Filing
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1832910A (en) * | 2003-08-06 | 2006-09-13 | 巴斯福股份公司 | Operation of a continuous heterogeneously catalyzed gas phase partial oxidation of at least one organic compound |
| CN102659625A (en) * | 2012-04-20 | 2012-09-12 | 中国天辰工程有限公司 | Industrial production method of acrylonitrile |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2016144667A2 (en) | 2016-09-15 |
| WO2016144667A3 (en) | 2016-12-22 |
| RU2017134470A (en) | 2019-04-09 |
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