CN104587684A - Vaporization system used for process flow - Google Patents
Vaporization system used for process flow Download PDFInfo
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- CN104587684A CN104587684A CN201410811080.9A CN201410811080A CN104587684A CN 104587684 A CN104587684 A CN 104587684A CN 201410811080 A CN201410811080 A CN 201410811080A CN 104587684 A CN104587684 A CN 104587684A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0088—Cascade evaporators
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to a vaporization system used for a process flow. The invention relates to a process and a system used for removing heavy organic impurities from the process flow. According to the process, the process flow is provided for an evaporator system from a distillation column. The evaporator system comprises one or more than one evaporation stages, wherein the first evaporation stage is used for receiving the process flow from the distillation column. The process comprises the steps of providing water-containing condensate and liquid residue from one or more than one evaporation stages and transmitting the water-containing condensate to a flash cold column and/or a light organic matter stripper.
Description
Technical field
There is provided a kind of for removing the technique of heavy organic impurities from process flow (process stream).More specifically, this technique comprises provides process flow to be separated with the heavy organics from process flow by water with in vapo(u)rization system.Vapo(u)rization system for provide aqueous condensate and liquid residue effective.
Background technology
Become known for the various technique and the system that manufacture acrylonitrile and methacrylonitrile; For example, see U.S. Patent No. 6,107,509.Typically, by being selected from propane, the hydrocarbon of propylene or isobutene, the recovery of acrylonitrile/methacrylonitrile that the direct reaction in the presence of a catalyst of ammonia and oxygen produces and purification are by being transported to the first tower (column) (quenching (quench)) (utilizing the first aqueous stream (aqueous stream) to carry out cooling reactor effluent there) by the reactor effluent comprising acrylonitrile/methacrylonitrile, the cooled effluent comprising acrylonitrile/methacrylonitrile is transported to (effluent cooled there contacts to be absorbed in the second aqueous stream by acrylonitrile/methacrylonitrile with the second aqueous stream) in the second tower (absorber), the second aqueous stream comprising acrylonitrile/methacrylonitrile is transported to the first destilling tower (recovery tower) for being separated from the second aqueous stream by original acrylonitrile/methacrylonitrile from the second tower and separated original acrylonitrile/methacrylonitrile is transported to after-fractionating tower (head fraction column (headscolumn) is to remove at least some impurity from original acrylonitrile/methacrylonitrile and the acrylonitrile/methacrylonitrile partly purified to be transported to the 3rd destilling tower (finishing column (productcolumn)) to have come to obtain finished product acrylonitrile/methacrylonitrile.United States Patent(USP) Nos. 4,234,510,3,885,928,3,352,764,3,198,750 and 3,044,966 illustrate typically for recovery and the purifying technique of acrylonitrile and methacrylonitrile.
In U.S. Patent No. 4,334, the technique for reclaiming alkene nitrile is described in 965.As in U.S. Patent No. 4,334, described in 965, multi-stage evaporator is used to from extractive distillation or peels off the water that tower residue (stripper tower bottoms) removes the flash cold column being recirculated to acrylonitrile purification and recovery system as quench liquid.This technique causes the obvious minimizing of the discarded flash cold column level of residue produced by this system.What use multi-effect evaporator to represent compared with other technology of the water content for reducing recirculation flow is obviously energy-conservation.U.S. Patent No. 4,334,965 disclose by multi-effect evaporator can with in U.S. Patent No. 4,166, the same way shown in 008 therefrom removes 50% of the liquid in recirculation flow or more, leaves concentrated recirculation flow to be used as quench liquid.U.S. Patent No. 4,334,965 disclose but because multi-effect evaporator high energy efficiency like this, the whole energy charge of this technology far below in U.S. Patent No. 4,166, technology illustrated in 008.
Although being manufactured on of acrylonitrile/methacrylonitrile is commercially carried out for many years, still exist and wherein improve and will have the field of substantial benefit.One of these fields of improving will be the more effective evaporator operation for recovery tower residue.
Summary of the invention
Therefore, an aspect of of the present present invention is to provide a kind of safe, effective and have cost-effective technique and device, and it overcomes or reduces the shortcoming of common process.
A kind of technique for removing heavy organic impurities from process flow comprises the process flow providing the heavy organic impurities with water and about 0.5 to about 1.5 percetage by weight.This technique is included in the evaporator system with one or more evaporation stage and is separated to provide aqueous condensate and liquid residue with heavy organic impurities by water.Aqueous condensate has about 0.1 percetage by weight or less heavy organic impurities and liquid residue has the heavy organic impurities of about 3 to about 10 percetages by weight.
A kind of technique for liquid residue being provided to ammonia oxidation process stream comprises: provide the process flow comprising water and heavy organic impurities; In the evaporator system with one or more evaporation stage, water is separated to provide aqueous condensate and liquid residue with heavy organic impurities; And in flash cold column, make liquid residue contact to provide ammonium sulfate with reactor effluent.On the one hand, the amount of ammonium sulfate and the amount of polymer are limited by formula y=-M1x+C1, and wherein, y is the percetage by weight of ammonium sulfate, and x is the percetage by weight of polymer, and M1 is 4.6 or less and C1 is 45 or less.
A kind of evaporator system comprises one or more evaporation stage, and wherein, the first evaporation stage is configured to receive the process flow from destilling tower, and this one or more evaporation stage is configured to provide aqueous condensate and liquid residue; And flash cold column and/or lightweight organic matter stripper (lightorganic stripper), it is configured to receive aqueous condensate.
A kind of evaporation technology comprises the process flow from destilling tower is delivered to evaporator system, this evaporator system comprises one or more evaporation stage, wherein, first evaporation stage is configured to receive the process flow from destilling tower, provides the aqueous condensate from this one or more evaporation stage and liquid residue; And aqueous condensate is delivered to flash cold column and/or lightweight organic matter stripper.
Above-mentioned and other side of the present invention, feature and advantage are by apparent in the detailed description below the embodiment (it should read in conjunction with the accompanying drawings) illustrated by it.
Accompanying drawing explanation
Can obtain more complete understanding and its advantage of exemplary embodiment of the present invention when considering accompanying drawing by reference to ensuing explanation, Reference numeral similar in the accompanying drawings indicates similar feature, wherein:
Fig. 1 shows the schematic flow chart of the technique for the manufacture of acrylonitrile product.
Fig. 2 shows the schematic flow chart of the alternative technique for the manufacture of acrylonitrile product.
Detailed description of the invention
Ammonia oxidation process
On the one hand, process flow is provided from ammoxidation reaction process.A kind of example of such technique in U.S. Patent No. 4,334, illustrate in 965, it is included in wherein on the whole at it.
Fig. 1 is the schematic expression of the overall situation of various aspects.With reference to figure 1, first the reactor eluting gas (it comprises acrylonitrile, HCN, acetonitrile, water vapour and impurity) in pipeline (conduit) 100 can be transferred into flash cold column 102.This gas can contact with the quench liquid in flash cold column 102.The residue stream (bottoms stream) comprising water and impurity is removed by pipeline 106 and delivers to refuse process.
Cooled reactor eluting gas leaves quench system by circuit 108 and is sent to quenching aftercooler 107.Quenching aftercooler 107 is for quench stream effluent being cooled to lower than about 50 DEG C effectively.Cooled quench stream effluent is supplied to absorber 110 by circuit 109.Flushing water enters absorber 110 by circuit 112 at top.Uncondensable gas is removed by from absorber by circuit 114.Aqueous solution (it comprises water, acrylonitrile, acetonitrile and impurity) can be used as residue and flows through circuit 116 and be removed and be sent to extractive distillation tower 182.
Solvent water is introduced into the top of extractive distillation tower 182 to perform extractive distillation by circuit 184.Acrylonitrile and HCN be can be used as overhead vapours (overhead vapor) and are removed by circuit 186 and deliver to (not shown) of purifying further.The stream comprising acetonitrile and water is removed by circuit 188 and is sent to stripper 190.Heat can be added to stripper 190 to remove acetonitrile by circuit 192 as overhead vapours.The residue stream comprising water, heavy organics and other impurity is removed by from extractive distillation tower 182 by circuit 196.The liquid stream mainly comprising water to be removed by the Lower Half from stripper 190 by circuit 194 and is used as the solvent water to extractive distillation tower 182.
Evaporator system
According to one side, the stripping tower residue (it also can be called as process flow) in circuit 196 can be evaporated in evaporator system.In this respect, the extractive distillation tower residue (it can enter heat exchanger 136) in circuit 196 comprises water, polymer, ammonia and acrylonitrile.As utilized herein, " heavy organic impurities " refers to polymer.As utilized herein, polymer refers to heavy organic material and the organic mixture of a small amount of lightweight.Heavy organic material can comprise the mixture (it has the nitrile sub of high level and also comprises some hydrocarbon groups be oxidized) of different higher boiling organic compound.In this respect, process flow comprises the heavy organic impurities of about 0.5 to about 1.5 percetage by weight, and about 0.75 to about 1.25 percetage by weight on the other hand.
In this respect, evaporator system can comprise for providing aqueous condensate and liquid residue one or more evaporation stage effective.Such as, evaporator system can comprise 1 to about 6 evaporation stage, on the other hand 2 to about 6 evaporation stages, on the other hand 2 to about 5 evaporation stages, on the other hand 2 to about 4 evaporation stages and 2 to about 3 evaporation stages on the other hand.
In one side in FIG, evaporator system comprises the shell and tube exchanger 136,138 and 142 of arranged in series.As utilized herein, " evaporation stage " refers to mono heat exchanger.In each heat exchanger, the liquid in the pipe side of heat exchanger is partially vaporized, and produces vaporous effluent and liquid efflunent.Liquid efflunent is supplied to the pipe side of next heat exchanger of series connection, and vaporous effluent is supplied to the shell-side of same heat exchanger, causes the additional part evaporation of liquid.This technology is continuous print for so much level that the water removing desired amount from stripper residue is required.In each level, the condensate produced when the steam supplying heat is condensed by heat exchange is recovered and is recycled for recycling or suffer purification that is chemical or biology.
The residue stream comprising water, heavy organics and other impurity is removed from extractive distillation tower 182 by circuit 196 and is sent in the pipe side of First Heat Exchanger 136, and lowpressure stream is transmitted through the shell-side of this heat exchanger.On the one hand, be about 1 to about 3 meter per second by the flow of the pipe side of heat exchanger, and about 1.5 to about 2.5 meter per seconds on the other hand.Heat exchange wherein causes lowpressure stream condensation and evaporates with making extractive distillation tower residue fraction.Condensate can be removed from First Heat Exchanger 136 for recycling via circuit 146.
In First Heat Exchanger 136, the heating of extractive distillation tower residue causes its part to be separated into liquid and vapor capacity.In in the more than one heat exchanger of use, liquid phase is removed via circuit 148 and is delivered to the pipe side of the second heat exchanger 138, and a part for the liquid of taking-up is recirculated to the bottom of the pipe side of First Heat Exchanger 136 via circuit 150.The steam produced in First Heat Exchanger 136 is removed and is delivered to the shell-side of the second heat exchanger 138 via circuit 152.Heat exchange in heat exchanger 138 causes the part evaporation in pipe side of the condensation of steam on shell-side and liquid, produces into the liquid of vapour phase thus in the second heat exchanger 138.The condensate that the shell-side of the second heat exchanger 138 produces is discharged via circuit 154.This condensate has relatively low heavy organics (such as polymer etc.) concentration.
In use more than in two heat exchangers, the liquid phase stayed in the pipe side of the second heat exchanger 138 is transported to the pipe side of the 3rd heat exchanger 142 via circuit 156, a part for liquid is recirculated to the pipe side of the second heat exchanger 138 via circuit 158.The steam produced in the pipe side of the second heat exchanger 138 is transported to the shell-side of the 3rd heat exchanger 142 via circuit 160.Heat exchange in the 3rd heat exchanger 142 cause again steam on shell-side condensation to form condensate (its be removed via circuit 176 and be transferred in the mode identical with the condensate from the second heat exchanger 138).
The steam produced in the pipe side of the 3rd heat exchanger 142 is removed via circuit 170, condensation and be recovered in public water container and/or be combined with the condensate from circuit 146,154,162 and/or 176 in condenser 172.Condensate from the pipe side of heat exchanger 142 also can be transported to public water container via circuit 176, and what such as combine at 135 places and provide is such.The liquid reclaimed from the pipe side of the 3rd heat exchanger 142 can be removed via circuit 178 and be recycled to the pipe side of the 3rd heat exchanger via circuit 180.Aqueous condensate can so high-purity make it to be such as such as used in the flushing of different process equipments as the clear water of routine, as being back to flash cold column (first order of such as flash cold column) and/or to lightweight organic matter stripper.In this respect, aqueous condensate has about 0.1 percetage by weight or less heavy organic impurities, on the other hand about 0.075 heavy organic impurities, on the other hand about 0.05 heavy organic impurities and about 0.025 heavy organic impurities on the other hand.
On the other hand, liquid residue has the heavy organic impurities of heavy organic impurities, on the other hand about 4 to about 8 percetages by weight of about 3 to about 10 percetages by weight and the heavy organic impurities of about 5 to about 7 percetages by weight on the other hand.As shown in FIG. 1, liquid residue can be sent to waste water incineration device (WWI).Alternatively, as shown in FIG. 2, liquid residue can be sent to the bottom of flash cold column 102 via circuit 179.
On the one hand, the aqueous condensate produced in heat exchanger second and the 3rd comprises extremely a small amount of heavy organics.Therefore, its biology by routine or the processing mode of chemistry directly process to produce environmentally acceptable water.And, the condensate produced in the 4th heat exchanger and the condensate produced by condenser so pure that to be enough to be used to various technique object, such as without the flushing water of process further.The condensate produced by First Heat Exchanger is high purity, because it does not contact other process flow any.
Evaporation percentage
On the one hand, higher evaporation can be useful, because evaporator condensation thing can be reused or process, and can be burned and/or carry out other process from the liquid residue of the final stage of multi-stage evaporator.
On the one hand, the evaporation percentage of the residue of extractive distillation tower can be greater than about 55% to about 85%.On the one hand, the evaporation percentage of the residue of extractive distillation tower can be greater than about 60%.On the one hand, the evaporation percentage of the residue of extractive distillation tower can be greater than about 60% to about 85%.On the one hand, the evaporation percentage of the residue of extractive distillation tower can in the scope of about 73% to about 75%.
Had an appointment by operating band four (4) level evaporation technologies of 55 to about 60%, on the one hand about 57% evaporation percentage, liquid polymers can be about 2.2 percetages by weight at the percentage from the 4th and in last heat exchanger 142 evaporimeter residue out.
Had an appointment by operating band four (4) level evaporation technologies of 60-65%, on the one hand about 63% evaporation percentage, liquid polymers can be about 3 percetages by weight at the percentage from the 4th and in last heat exchanger 142 evaporimeter residue out.
Had an appointment by operating band four (4) level evaporation technologies of 80-85%, on the one hand about 83% evaporation percentage, liquid polymers can be about 6 percetages by weight at the percentage from the 4th and in last heat exchanger 142 evaporimeter residue out.
Had an appointment by operating band four (4) level evaporation technologies of 73-75%, on the one hand about 74% evaporation percentage, liquid polymers can be about 5.5 percetages by weight at the percentage from the 4th and in last heat exchanger 142 evaporimeter residue out.
On the one hand, each evaporation stage provides the evaporation rate of about 15 to about 25%.
On the one hand, the percentage of evaporator condensation thing can be the evaporation percentage of the residue of extractive distillation tower 182 divided by supply percentage.On the one hand, evaporation percentage is about 55 to about 60% on the other hand about 57%.In liquid residue, the amount of polymer is about 2.2 percetages by weight.On the one hand, evaporation percentage is about 55-60: 2.2 with the ratio of the percetage by weight of polymer.
On the other hand, the amount of polymers in liquid residue is about 3 percetages by weight.On the one hand, evaporation percentage is about 60-65: 3 with the ratio of the percetage by weight of polymer.
On the one hand, evaporation percentage is about 82 to about 83%, and the amount of polymer is about 6.0 percetages by weight in liquid residue.Condensate can via circuit 135 supply thing be supplied to lightweight organic matter stripper LOS (not shown) for further process, or be sent to flash cold column 102 as quench liquid.On the one hand, evaporation percentage is about 82-83: 6 with the ratio of the percetage by weight of polymer.
On the one hand, evaporation percentage is about 73 to about 75%, and the polymer in liquid residue is about 5.5 percetages by weight.Condensate can via circuit 135 supply thing be supplied to lightweight organic matter stripper LOS (not shown) for further process, or be sent to flash cold column 102 as quench liquid.On the one hand, evaporation percentage is about 73-75: 5.5 with the ratio of the percetage by weight of polymer.
On the one hand, find that experience is than less dirt (fouling) obvious under the evaporation percentage of about 83% when evaporation percentage is about 74%, and realize the polymer weight percentage of amount relatively high in liquid residue simultaneously, namely 5.5 percetages by weight are to 6.0 percetages by weight under the evaporation percentage of about 83%.This is surprising result, because be originally contemplated that the percetage by weight of polymer that the amount of dirt will be linearly related in liquid residue.
Find may there be too many dirt (mainly on pipe side) when evaporation percentage is greater than about 83% in fourth stage evaporimeter or heat exchanger 142.Find that the evaporation percentage of about 73-75% significantly reduces the amount of dirt, and be simultaneously provided in the relatively high amount of polymer weight percentage in liquid residue.
Those skilled in the art will recognize that and can make many amendments according to the present invention and without departing from the spirit and scope of the present invention.Such as, any amount of level can be adopted in evaporator system.And, although lowpressure stream is illustrated, can adopt any thermal source as the supply for the required heat of all evapn in the above description.To purify and in recovery plant at typical acrylonitrile, however lowpressure stream, namely have until 100psig, usual about 20 to 60psig pressure saturated flow can easily for and preferably used.Also can mainly change according to economy in the amount peeling off the water removed by multiple effect evaporimeter in tower.Finally, what should also understand is that multiple effect evaporimeter of the present invention does not need to be limited on the stripping tower residue that is used in as shown in superincumbent explanation, but can be used to concentrated any other and be recycled process flow to be used as quench liquid.Such as, multi-effect evaporator can be used to process in U.S. Patent No. 4, the extractive distillation tower residue of recirculation in the circuit 156 of Fig. 2 of 166,008.All such modification intentions are comprised in scope of the present invention (it will only be limited by claim).
Flash cold column operates
On the one hand, the technique for running flash cold column comprises and reactor effluent is delivered to flash cold column and reactor effluent and the water comprising polymer and extracts in district at effluent and contact to provide the effluent stream be extracted.This technique also comprises the effluent stream be extracted and contacts with sulfuric acid and remove first-class to provide the first flash cold column stream with about 10 percetages by weight or less polymer in sour contact zone.On the one hand, this technique comprise provide from evaporator system water at least partially.As illustrated here, this water can be aqueous condensate and/or liquid residue.
On the one hand, formula y=-M1x+C1 (wherein, y is the percetage by weight of ammonium sulfate, and x is the percetage by weight of polymer, and M1 is 4.6 or less and C1 is 45 or less) defines the amount of ammonium sulfate and the amount of polymer in flash cold column residue stream.At related aspect, M1 is 1.5 or less and C1 is 30 or less.On the one hand, the flash cold column residue stream of the ammonium sulfate that process provides the ammonium sulfate with about 10 to about 25 percetages by weight and the polymer being less than about 5 percetages by weight, on the other hand about 15 to about 21 percetages by weight and the polymer being less than about 5 percetages by weight.This flash cold column residue stream has the pH of about 4.5 to about 6.0.
On the other hand, this technique comprise remove second with provide have more than about 10 percetages by weight polymer and be less than the second flash cold column stream of ammonium sulfate of about 5 percetages by weight.
On the other hand, the effluent that is recirculated at least partially of the second flash cold column stream extracts district.The effluent stream be extracted is the adverse current relative to sulfuric acid.On the one hand, the first flash cold column stream extracts above district at effluent and is removed.Adiabatic cooling can occur in effluent and extract in district.
On the one hand, this technique can comprise and controls to be transported to the amount of the supplementing water of flash cold column and/or control is transported to the amount of the sulfuric acid of flash cold column to obtain the concentration of the ammonium sulfate in flash cold column residue stream of about 10 to about 25 percetages by weight.On the one hand, this technique can comprise the pH of the fluid residue detecting flash cold column residue and control flow to the sulfuric acid of flash cold column to obtain the flash cold column residue stream with about 4.5-6.0pH based on the pH of detected fluid residue.On the one hand, this technique can comprise based on sulfuric acid to the flow rate of flash cold column with from flash cold column or the concentration determining ammonium sulfate flash cold column residue stream from the flow rate of its flash cold column residue stream out.On the one hand, the concentration adjustment that this technique can comprise based on ammonium sulfate determined in determining step is transported to the sulfuric acid of flash cold column and/or the flow rate of supplementing water to maintain the concentration of ammonium sulfate in the scope of about 10 to about 25 percetages by weight.By the concentration of the ammonium sulfate in flash cold column residue stream is increased to about 10 to about 25 percetages by weight from the 5-10 percetage by weight provided common process, less water needs from flash cold column residue stream, removed the even higher concentration obtaining ammonium sulfate.Find can use sulfate condensation device that flash cold column residue stream is condensed to about 35-40 percetage by weight effectively by the concentration of the ammonium sulfate in flash cold column residue stream being increased to about 10 to about 25 percetages by weight.
Although describe the present invention about its certain preferred embodiment in the above description and set forth many details for illustration of object, it will be apparent to one skilled in the art that the present invention can affect by additional embodiment and some details described herein can change considerably when not departing from basic principle of the present invention.Be understood that feature of the present invention easily or can replace affecting by amendment, change, change when departing from the scope of claim without departing from the spirit and scope of the present invention or not.Such as, the size of all parts, quantity, size and shape can be changed to adapt to special applications.Therefore, illustrated and described herein specific embodiment is only for illustration of property object.
Claims (19)
1. an evaporation technology, comprising:
Process flow is delivered to evaporator system from destilling tower, and described evaporator system comprises one or more evaporation stage, and wherein, the first evaporation stage is configured to receive the process flow from described destilling tower,
Aqueous condensate and liquid residue is provided from one or more evaporation stage described; And
Aqueous condensate is delivered to flash cold column and/or lightweight organic matter stripper.
2. technique according to claim 1, is characterized in that, described liquid residue is transported to waste water incineration device.
3. technique according to claim 1, is characterized in that, liquid residue is transported to the bottom of described flash cold column.
4. technique according to claim 1, is characterized in that, described evaporator system comprises 1 to about 6 evaporation stage.
5. technique according to claim 1, is characterized in that, described evaporator system comprises 2 to about 6 evaporation stages.
6. technique according to claim 1, is characterized in that, described evaporator system comprises 2 to about 5 evaporation stages.
7. technique according to claim 1, is characterized in that, described evaporator system comprises 2 to about 4 evaporation stages.
8. technique according to claim 1, is characterized in that, described evaporator system comprises 2 to about 3 evaporation stages.
9. technique according to claim 1, is characterized in that, described aqueous condensate has about 0.1 percetage by weight or less heavy organic impurities and described liquid residue has the heavy organic impurities of about 3 to about 10 percetages by weight.
10. technique according to claim 1, is characterized in that, described process flow comprises the heavy organic impurities of about 0.5 to about 1.5 percetage by weight.
11. techniques according to claim 10, is characterized in that, described heavy organic impurities is included in the polymeric material produced in ammoxidation reaction process.
12. techniques according to claim 1, is characterized in that, described aqueous condensate has about 0.075 percetage by weight or less heavy organic impurities.
13. techniques according to claim 12, is characterized in that, described aqueous condensate has about 0.05 percetage by weight or less heavy organic impurities.
14. techniques according to claim 13, is characterized in that, described aqueous condensate has about 0.025 percetage by weight or less heavy organic impurities.
15. techniques according to claim 1, is characterized in that, described liquid residue has the heavy organic impurities of about 4 to about 8 percetages by weight.
16. techniques according to claim 15, is characterized in that, described liquid residue has the heavy organic impurities of about 5 to about 7 percetages by weight.
17. techniques according to claim 1, is characterized in that, described evaporator system comprises at least one shell and tube exchanger.
18. techniques according to claim 17, is characterized in that, are about 1 to about 3 meter per second by the flow of the pipe side of described heat exchanger.
19. techniques according to claim 1, is characterized in that, each evaporation stage provides the evaporation rate of about 15 to about 25%.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410811080.9A CN104587684A (en) | 2014-09-30 | 2014-09-30 | Vaporization system used for process flow |
| PCT/US2015/048068 WO2016053564A1 (en) | 2014-09-30 | 2015-09-02 | Evaporation system comprising a serie of evaporator for treating an ammoxidation process stream |
| TW104131281A TWI713466B (en) | 2014-09-30 | 2015-09-22 | Evaporation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410811080.9A CN104587684A (en) | 2014-09-30 | 2014-09-30 | Vaporization system used for process flow |
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| CN104587684A true CN104587684A (en) | 2015-05-06 |
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| CN201410811080.9A Pending CN104587684A (en) | 2014-09-30 | 2014-09-30 | Vaporization system used for process flow |
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| Country | Link |
|---|---|
| CN (1) | CN104587684A (en) |
| TW (1) | TWI713466B (en) |
| WO (1) | WO2016053564A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107941039A (en) * | 2016-10-12 | 2018-04-20 | 英尼奥斯欧洲股份公司 | Flash cold column aftercooler |
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| US4166008A (en) * | 1977-07-29 | 1979-08-28 | The Standard Oil Company | Process for recovery of olefinic nitriles |
| US4334965A (en) * | 1980-12-31 | 1982-06-15 | Standard Oil Company | Process for recovery of olefinic nitriles |
| CN204447371U (en) * | 2014-09-29 | 2015-07-08 | 英尼奥斯欧洲股份公司 | Evaporator system |
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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 |
| US4148865A (en) * | 1978-01-06 | 1979-04-10 | The Lummus Company | Treatment of cyanide byproduct in nitrile production |
| US6107509A (en) | 1999-03-31 | 2000-08-22 | The Standard Oil Company | Process for the recovery of acrylonitrile and methacrylontrile |
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2014
- 2014-09-30 CN CN201410811080.9A patent/CN104587684A/en active Pending
-
2015
- 2015-09-02 WO PCT/US2015/048068 patent/WO2016053564A1/en active Application Filing
- 2015-09-22 TW TW104131281A patent/TWI713466B/en active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4166008A (en) * | 1977-07-29 | 1979-08-28 | The Standard Oil Company | Process for recovery of olefinic nitriles |
| US4334965A (en) * | 1980-12-31 | 1982-06-15 | Standard Oil Company | Process for recovery of olefinic nitriles |
| CN204447371U (en) * | 2014-09-29 | 2015-07-08 | 英尼奥斯欧洲股份公司 | Evaporator system |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107941039A (en) * | 2016-10-12 | 2018-04-20 | 英尼奥斯欧洲股份公司 | Flash cold column aftercooler |
| CN107941039B (en) * | 2016-10-12 | 2020-03-03 | 英尼奥斯欧洲股份公司 | Quench tower aftercooler |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2016053564A1 (en) | 2016-04-07 |
| TW201622792A (en) | 2016-07-01 |
| TWI713466B (en) | 2020-12-21 |
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Application publication date: 20150506 |