CN105727582A - Evaporation system for process stream - Google Patents
Evaporation system for process stream Download PDFInfo
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- CN105727582A CN105727582A CN201610122794.8A CN201610122794A CN105727582A CN 105727582 A CN105727582 A CN 105727582A CN 201610122794 A CN201610122794 A CN 201610122794A CN 105727582 A CN105727582 A CN 105727582A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/26—Multiple-effect evaporating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/30—Accessories for evaporators ; Constructional details thereof
Abstract
The invention relates to an evaporation system for a process stream, and provides a process and a system for removing heavy organic impurities from the process stream. The process comprises the step of providing the process stream for an evaporator system from a distillation column. The evaporator system comprises one or more evaporation stages, wherein the first evaporation stage is used for receiving the process stream from the distillation tower. The process comprises the steps of providing an aqueous condensation product and liquid residues from the one or more evaporation stages and delivering the aqueous condensation product to a quenching tower and/or a light organic matter stripper.
Description
The application is the divisional application of the application for a patent for invention (China national application number is 201410511314.8, and denomination of invention is " vapo(u)rization system for process flow ") in JIUYUE in 2014 submission on the 29th.
Technical field
The one technique for removing weight organic impurities from process flow (processstream) is provided.More specifically, this technique includes providing process flow and by water and the heavy separating organic matters from process flow in vapo(u)rization system.Vapo(u)rization system is for providing aqueous condensate and liquid residue effective.
Background technology
Become known for manufacturing various techniques and the system of acrylonitrile and methacrylonitrile；For example, see U.S. Patent No. 6,107,509.nullTypically，By selected from propane、The Hydrocarbon of propylene or isobutene.、The recovery of acrylonitrile/methacrylonitrile produced by ammonia and oxygen direct reaction in the presence of a catalyst and purification are by by the reactor effluent comprising acrylonitrile/methacrylonitrile transport to the first tower (column) (being quenched (quench)) (utilizing the first aqueous stream (aqueousstream) to cool down reactor effluent there)、The cooled effluent comprising acrylonitrile/methacrylonitrile is transported to (effluent cooled there and the second aqueous stream contact to be absorbed in the second aqueous stream by acrylonitrile/methacrylonitrile) in the second tower (absorber)、By the second aqueous stream comprising acrylonitrile/methacrylonitrile from the second tower transport to being used for the first distillation column (recovery tower) of being separated from the second aqueous stream by original acrylonitrile/methacrylonitrile and (head fraction column (headscolumn) completes to the 3rd distillation column (finishing column (productcolumn)) obtaining finished product acrylonitrile/methacrylonitrile removing at least some impurity and being transported by the acrylonitrile partly purified/methacrylonitrile from original acrylonitrile/methacrylonitrile by separated original acrylonitrile/methacrylonitrile transport to after-fractionating tower.United States Patent(USP) Nos. 4,234,510,3,885,928,3,352,764,3,198,750 and 3,044,966 illustrates to be typically used for recovery and the purifying technique of acrylonitrile and methacrylonitrile.
U.S. Patent No. 4,334,965 illustrates the technique for reclaiming alkene nitrile.As, described in U.S. Patent No. 4,334,965, multi-stage evaporator is used to remove the water of the flash cold column being recirculated to acrylonitrile purification and recovery system as coolant from extractive distillation or stripping tower residue (strippertowerbottoms).This technique causes significantly reducing of the flash cold column residual waste amount produced by this system.What use that multi-effect evaporator represents compared with other technology of the water content for reducing recirculation flow is substantially energy-conservation.U.S. Patent No. 4,334,965 discloses and by 50% of the liquid in recirculation flow or more therefrom to remove with the same way shown in U.S. Patent No. 4,166,008, the recirculation flow of concentration can be stayed for use as coolant by multi-effect evaporator.U.S. Patent No. 4,334,965 discloses but because the such high energy efficiency of multi-effect evaporator, the whole energy charge of this technology is far below technology illustrated in U.S. Patent No. 4,166,008.
Although the manufacture of acrylonitrile/methacrylonitrile commercially carries out for many years, still suffer from improving wherein and will have the field of substantial benefit.One of these fields improved will be the more effective evaporator operation for recovery tower residue.
Summary of the invention
Therefore, it is an aspect of the present invention to provide a kind of safe, effective and have cost-effective technique and device, its shortcoming overcoming or reducing traditional handicraft.
A kind of technique for removing weight organic impurities from process flow includes providing and has water and about 0.5 to the process flow of the heavy organic impurities of about 1.5 percetages by weight.This technique includes Jiang Shui in the evaporator system have one or more evaporation stage and separates to provide aqueous condensate and liquid residue with weight organic impurities.Aqueous condensate has about 0.1 percetage by weight or less weight organic impurities and liquid residue has about 3 to the heavy organic impurities of about 10 percetages by weight.
A kind of for the technique that liquid residue provides to ammonia oxidation process stream is included: the process flow including water and weight organic impurities is provided；In the evaporator system have one or more evaporation stage, Jiang Shui separates to provide aqueous condensate and liquid residue with weight organic impurities；And make liquid residue contact with reactor effluent to provide ammonium sulfate in flash cold column.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 includes one or more evaporation stage, and wherein, the first evaporation stage is configured to receive the process flow from distillation column, and this one or more evaporation stage is configured to provide aqueous condensate and liquid residue；And flash cold column and/or light Organic substance detacher (lightorganicstripper), it is configured to receive aqueous condensate.
A kind of evaporation technology includes the process flow from distillation column is delivered to evaporator system, this evaporator system includes one or more evaporation stage, wherein, first evaporation stage is configured to receive the process flow from distillation column, it is provided that from aqueous condensate and the liquid residue of this one or more evaporation stage；And aqueous condensate is delivered to flash cold column and/or light Organic substance detacher.
Above-mentioned and the other side of the present invention, feature and advantage will be apparent from the detailed description below of its embodiment described (it should read in conjunction with the accompanying drawings).
Accompanying drawing explanation
Can be obtained more complete understanding and its advantage of the exemplary embodiment of the present invention when considering accompanying drawing by the ensuing explanation of reference, accompanying drawing labelling similar in the accompanying drawings indicates similar feature, wherein:
Fig. 1 shows the schematic flow chart of the technique for manufacturing acrylonitrile product,
Fig. 2 shows the schematic flow chart of the alternative technique for manufacturing acrylonitrile product.
Detailed description of the invention
Ammonia oxidation process
On the one hand, process flow is provided from ammoxidation reaction process.The example of a kind of such technique illustrates in U.S. Patent No. 4,334,965, and 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 Fig. 1, the reactor eluting gas (it includes acrylonitrile, HCN, acetonitrile, water vapour and impurity) in pipeline (conduit) 100 can be firstly transmitted to flash cold column 102.This gas can contact with the coolant in flash cold column 102.The residue stream (bottomsstream) comprising water and impurity can pass through pipeline 106 and be removed and deliver to refuse process.
Cooled reactor eluting gas can pass through circuit 108 and leaves quenching system and be sent to quenching aftercooler 107.Be quenched aftercooler 107 for quenchings effluent is cooled to lower than about 50 DEG C effective.Cooled quenching effluent is transported to absorber 110 by circuit 109.Flushing water can pass through circuit 112 and enter absorber 110 at top.Uncondensable gas can be removed from absorber by circuit 114.Aqueous solution (it comprises water, acrylonitrile, acetonitrile and impurity) can be removed and be sent to extractive distillation tower 182 as residue stream by circuit 116.
Solvent water can pass through circuit 184 and be introduced into the top of extractive distillation tower 182 to perform extractive distillation.Acrylonitrile and HCN can be removed as overhead vapours (overheadvapor) by circuit 186 and be delivered to and purify (not shown) further.The stream comprising acetonitrile and water can pass through circuit 188 and be removed and be sent to detacher 190.Heat may be added to detacher 190 to remove acetonitrile by circuit 192 as overhead vapours.The residue stream comprising water, weight Organic substance and other impurity can pass through circuit 196 and be removed from extractive distillation tower 182.The liquid stream mainly comprising water can be removed and used as the solvent water to extractive distillation tower 182 by circuit 194 by the lower half from detacher 190.
Evaporator system
According on the one hand, stripping tower residue (it is alternatively called 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 includes water, polymer, ammonia and acrylonitrile.As utilized herein, " weight organic impurities " refers to polymer.As utilized herein, polymer refers to weight organic material and a small amount of light organic mixture.Weight organic material can include the mixture (it has the nitrile sub of high level and also comprises the Hydrocarbon group of some oxidations) of different high boiling point organic compound.In this respect, process flow includes about 0.5 to the heavy organic impurities of about 1.5 percetages by weight, and on the other hand about 0.75 to about 1.25 percetages by weight.
In this respect, evaporator system can include for providing aqueous condensate and liquid residue one or more evaporation stage effective.Such as, evaporator system can include 1 to about 6 evaporation stages, 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 on the other hand 2 to about 3 evaporation stages.
In one side shown in FIG, evaporator system includes 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 tube side of heat exchanger is partially vaporized, and produces vaporous effluent and liquid efflunent.Liquid efflunent is transported to the tube side of next heat exchanger of series connection, and vaporous effluent is transported 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 detacher residue is required.In each level, the condensate produced when the steam of supply heat is condensed by heat exchange is recovered and is recycled to recycling or suffers chemistry or biology purification.
The residue stream comprising water, weight Organic substance and other impurity can pass through circuit 196 by the tube side removing and being sent to First Heat Exchanger 136 from extractive distillation tower 182, and lowpressure stream is transmitted through the shell-side of this heat exchanger.On the one hand, it is about 1 to about 3 meter per seconds by the flow of the tube side of heat exchanger, and on the other hand about 1.5 to about 2.5 meter per seconds.Heat exchange therein causes lowpressure stream condensation and evaporates with making extractive distillation tower residue fraction.Condensate can be removed for recycling from First Heat Exchanger 136 via circuit 146.
In First Heat Exchanger 136, thermally-induced its that add of extractive distillation tower residue is partially separated into liquid and vapor capacity.In in the more than one heat exchanger of use, liquid phase is removed and is delivered to the tube side of the second heat exchanger 138 via circuit 148, and a part for the liquid of taking-up is recirculated to the bottom of the tube 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 tube side of steam condensation on shell-side and liquid, thus produces into the liquid of vapour phase in the second heat exchanger 138.The condensate produced on the shell-side of the second heat exchanger 138 is discharged via circuit 154.This condensate has relatively low heavy Organic substance (such as polymer etc.) concentration.
In in use more than two heat exchanger, staying the liquid phase in the tube side of the second heat exchanger 138 and be transported to the tube side of the 3rd heat exchanger 142 via circuit 156, a part for liquid is recirculated to the tube side of the second heat exchanger 138 via circuit 158.The steam produced in the tube 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 causes again steam to condense to form condensate (it is removed via circuit 176 and is transferred in the way of identical with from the condensate of the second heat exchanger 138) on shell-side.
In the tube side of the 3rd heat exchanger 142 produce steam be removed via circuit 170, in condenser 172 condensation and be recovered in public water container and/or be combined from the condensate of circuit 146,154,162 and/or 176.Condensate from the tube side of heat exchanger 142 also can be transported to public water container via circuit 176, for instance as 135 places combine and provide.The liquid reclaimed from the tube side of the 3rd heat exchanger 142 can be removed and be recycled to via circuit 180 tube side of the 3rd heat exchanger via circuit 178.Aqueous condensate so high-purity can make it to be such as such as used in the flushing of different process equipments as traditional clear water, as being back to flash cold column (first order of such as flash cold column) and/or to light Organic substance detacher.In this respect, aqueous condensate has about 0.1 percetage by weight or less weight organic impurities, on the other hand about 0.075 weight organic impurities, on the other hand about 0.05 weight organic impurities and about 0.025 weighs organic impurities on the other hand.
On the other hand, liquid residue has about 3 to the weight organic impurities of about 10 percetages by weight, on the other hand about 4 to the weight organic impurities of about 8 percetages by weight on the other hand about 5 to the heavy organic impurities of about 7 percetages by weight.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, extremely a small amount of heavy Organic substance is comprised in the second and the 3rd aqueous condensate produced in heat exchanger.Therefore, it directly can process to produce environmentally acceptable water by traditional biological or chemistry processing mode.And, the condensate produced in the 4th heat exchanger and the condensate produced by condenser are so pure that to be enough to be used to various technique purpose, such as without the flushing water of further process.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 may be advantageous in that, because evaporator condensation thing can be reused or process, and can be incinerated from the liquid residue of the final stage of multi-stage evaporator and/or carry out other and process.
On the one hand, the evaporation percentage of the residue of extractive distillation tower can more than about 55% to about 85%.On the one hand, the evaporation percentage of the residue of extractive distillation tower can more than about 60%.On the one hand, the evaporation percentage of the residue of extractive distillation tower can more 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%.
By running with about 55 to four (4) level evaporation technologies about 60%, about 57% evaporation percentage on the one hand, liquid polymers can be about 2.2% percetage by weight at the percent from the 4th and last heat exchanger 142 vaporizer residue out.
By running four (4) the level evaporation technologies with about 60-65%, on the one hand about 63% evaporation percentage, liquid polymers can be about 3% percetage by weight at the percent from the 4th and last heat exchanger 142 vaporizer residue out.
By running four (4) the level evaporation technologies with about 80-85%, on the one hand about 83% evaporation percentage, liquid polymers can be about 6% percetage by weight at the percent from the 4th and last heat exchanger 142 vaporizer residue out.
By running four (4) the level evaporation technologies with about 73-75%, on the one hand about 74% evaporation percentage, liquid polymers can be about 5.5% percetage by weight at the percent from the 4th and last heat exchanger 142 vaporizer residue out.
On the one hand, each evaporation stage provides the evaporation rate of about 15 to about 25%.
On the one hand, the percent of evaporator condensation thing can be the evaporation percentage of the residue of extractive distillation tower 182 divided by supply percent.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% percetage 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% percetage 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% percetage by weight in liquid residue.Condensate can be supplied to light Organic substance detacher LOS (not shown) for further process via circuit 135 as aliment, or is sent to flash cold column 102 as coolant.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% percetage by weight.Condensate can be supplied to light Organic substance detacher LOS (not shown) for further process via circuit 135 as aliment, or is sent to flash cold column 102 as coolant.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 experience ratio obvious less dirt (fouling) 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% percetage by weight is to 6.0% percetage by weight under the evaporation percentage of about 83%.This is surprising result, because being originally contemplated that the percetage by weight of polymer that the amount of dirt will be linearly related in liquid residue.
Find in fourth stage vaporizer or heat exchanger 142, be likely to there is too many dirt (mainly in tube side) when evaporation percentage is more than about 83%.Find that the evaporation percentage of about 73-75% significantly reduces the amount of dirt, and the relatively high amount being simultaneously provided in liquid residue polymer weight percentage.
It would be recognized by those skilled in the art that and can make many amendments without departing from the spirit and scope of the present invention according to the present invention.Such as, any amount of level can be adopted in evaporator system.And, although lowpressure stream supply as the heat required for all evapn in the above description is illustrated, can adopt any thermal source.Typical acrylonitrile purify and recovery plant in, but lowpressure stream, namely have until 100psig, generally about 20 to 60psig pressure saturated flow can easily for and be preferably utilized.The amount of the water removed by multiple effect vaporizer in peeling off tower also can mainly change according to economy.Finally, what should be further appreciated that is that the multiple effect vaporizer of the present invention need not be limited on the stripping tower residue being used in as shown in superincumbent explanation, and can be used for concentrating any other and be recycled the process flow for use as coolant.Such as, multi-effect evaporator can be used for processing the extractive distillation tower residue of recirculation in the circuit 156 of Fig. 2 of U.S. Patent No. 4,166,008.All such modification are intended to be comprised in the scope of the present invention (it will be limited by the claims that follow).
Flash cold column operates
On the one hand, the technique for running flash cold column includes being delivered to reactor effluent flash cold column and reactor effluent and the water comprising polymer and extracts at effluent and contact the outflow logistics being extracted with offer in district.The outflow logistics that this technique also includes being extracted contacts with sulphuric acid and removes first-class to provide the first flash cold column stream with about 10 percetages by weight or less polymer in acid contact area.On the one hand, this technique includes providing at least some of of the water from evaporator system.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 in flash cold column residue stream and the amount of polymer.At related aspect, M1 is 1.5 or less and C1 is 30 or less.On the one hand, process provides there is about 10 ammonium sulfate to about 25% percetage by weight and the flash cold column residue stream less than the polymer of about 5% percetage by weight, on the other hand about 15 to the ammonium sulfate of about 21% percetage by weight and the polymer less than about 5% percetage 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 includes removing second fluid to provide the second flash cold column stream having more than the polymer of about 10 percetages by weight and the ammonium sulfate less than about 5 percetages by weight.
On the other hand, the effluent that is recirculated at least partially of the second flash cold column fluid extracts district.The outflow logistics being extracted is the adverse current relative to sulphuric acid.On the one hand, the first flash cold column stream extracts at effluent and is removed above district.Adiabatic cooling can occur to extract in district at effluent.
On the one hand, this technique can include controlling to be transported to the supplementary water of flash cold column amount and/or control are transported to the amount of the sulphuric acid of flash cold column to obtain about 10 to the concentration of the ammonium sulfate in flash cold column residue stream of about 25% percetage by weight.On the one hand, this technique can include the pH of the fluid residue of detection flash cold column residue and control the flow of the sulphuric acid to flash cold column based on the pH of the fluid residue detected and have the flash cold column residue stream of about 4.5-6.0pH to obtain.On the one hand, this technique can include the flow rate based on sulphuric acid to flash cold column and the flow rate from flash cold column or from its flash cold column residue stream out determines the concentration of ammonium sulfate flash cold column residue stream.On the one hand, this technique can include being transported to the supplementary water of flash cold column and/or the flow rate of sulphuric acid based on the concentration adjustment of ammonium sulfate determined in determining step to maintain the concentration of ammonium sulfate in the scope of about 10 to about 25% percetage by weight.By the concentration of the ammonium sulfate in flash cold column residue stream is increased to about 10 to about 25% percetage by weight from the 5-10% percetage by weight provided traditional handicraft, less water needs to be removed to obtain the even higher concentration of ammonium sulfate from flash cold column residue stream.Find by sulfate condensation device being used to about 10 effectively to condense flash cold column residue stream to about 35-40% percetage by weight to about 25% percetage by weight the increase of the concentration of the ammonium sulfate in flash cold column residue stream.
Although describing the present invention about its certain preferred embodiment in the above description and set forth many details for illustrative purposes, it will be apparent to one skilled in the art that the present invention can be subject to additional embodiment to affect and details more described herein can change considerably when not necessarily departing from the basic principle of the present invention.It it should be understood that inventive feature is easily when without departing from the spirit and scope of the present invention or can be subject to amendment when not necessarily departing from scope of the claims, change, change or replace affect.Such as, the size of all parts, quantity, size and shape can be changed to accommodate special applications.Therefore, specific embodiment being merely to illustrate property purpose that is illustrated here and that describe.
Claims (19)
1. an evaporation technology, including:
From distillation column, process flow is delivered to evaporator system, and described evaporator system includes one or more evaporation stage, and wherein, the first evaporation stage is configured to receive the process flow from described distillation column,
Aqueous condensate and liquid residue is provided from one or more evaporation stage；And
Aqueous condensate is delivered to flash cold column and/or lightweight Organic substance detacher.
2. technique according to claim 1, it is characterised in that described liquid residue is transported to waste water incineration device.
3. technique according to claim 1, it is characterised in that liquid residue is transported to the bottom of described flash cold column.
4. technique according to claim 1, it is characterised in that described evaporator system includes 1 to about 6 evaporation stage.
5. technique according to claim 1, it is characterised in that described evaporator system includes 2 to about 6 evaporation stages.
6. technique according to claim 1, it is characterised in that described evaporator system includes 2 to about 5 evaporation stages.
7. technique according to claim 1, it is characterised in that described evaporator system includes 2 to about 4 evaporation stages.
8. technique according to claim 1, it is characterised in that described evaporator system includes 2 to about 3 evaporation stages.
9. technique according to claim 1, it is characterised 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, it is characterised in that described process flow includes the heavy organic impurities of about 0.5 to about 1.5 percetage by weight.
11. technique according to claim 10, it is characterised in that described heavy organic impurities includes the polymeric material produced in ammoxidation reaction process.
12. technique according to claim 1, it is characterised in that described aqueous condensate has about 0.075 percetage by weight or less heavy organic impurities.
13. technique according to claim 12, it is characterised in that described aqueous condensate has about 0.05 percetage by weight or less heavy organic impurities.
14. technique according to claim 13, it is characterised in that described aqueous condensate has about 0.025 percetage by weight or less heavy organic impurities.
15. technique according to claim 1, it is characterised in that described liquid residue has the heavy organic impurities of about 4 to about 8 percetages by weight.
16. technique according to claim 15, it is characterised in that described liquid residue has the heavy organic impurities of about 5 to about 7 percetages by weight.
17. technique according to claim 1, it is characterised in that described evaporator system includes at least one shell and tube exchanger.
18. technique according to claim 17, it is characterised in that be about 1 to about 3 meter per second by the flow of the tube side of described heat exchanger.
19. technique according to claim 1, it is characterised in that each evaporation stage provides the evaporation rate of about 15 to about 25%.
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| CN201610122794.8A CN105727582A (en) | 2014-09-29 | 2014-09-29 | Evaporation system for process stream |
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| CN201610122794.8A CN105727582A (en) | 2014-09-29 | 2014-09-29 | Evaporation system for process stream |
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| CN201410511314.8A Division CN105521616A (en) | 2014-09-29 | 2014-09-29 | Evaporation system used for process stream |
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| CN1368983A (en) * | 1998-12-18 | 2002-09-11 | Lg化学株式会社 | Process for preparing acrylonitrile-styrene copolymer |
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| CN1802347A (en) * | 2003-03-31 | 2006-07-12 | 科学与工业研究委员会 | Process for recovery of pure acrylonitrile |
| CN102657946A (en) * | 2012-04-20 | 2012-09-12 | 中国天辰工程有限公司 | Method for recovering and preparing ammonium sulfate from acrylonitrile device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4334965A (en) * | 1980-12-31 | 1982-06-15 | Standard Oil Company | Process for recovery of olefinic nitriles |
| CN1141968A (en) * | 1995-07-28 | 1997-02-05 | 日本爱克兰工业株式会社 | Method for production of improved acrylonitrile polymer melt |
| CN1110475C (en) * | 1996-10-23 | 2003-06-04 | 索罗蒂亚公司 | Process for purifying acrylonitrile |
| CN1368983A (en) * | 1998-12-18 | 2002-09-11 | Lg化学株式会社 | Process for preparing acrylonitrile-styrene copolymer |
| CN1802347A (en) * | 2003-03-31 | 2006-07-12 | 科学与工业研究委员会 | Process for recovery of pure acrylonitrile |
| CN102657946A (en) * | 2012-04-20 | 2012-09-12 | 中国天辰工程有限公司 | Method for recovering and preparing ammonium sulfate from acrylonitrile device |
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