CN204233802U - For alleviating the equipment of the pollution in acetonitrile fractionating column in acrylonitrile recovery - Google Patents
For alleviating the equipment of the pollution in acetonitrile fractionating column in acrylonitrile recovery Download PDFInfo
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- CN204233802U CN204233802U CN201420310033.1U CN201420310033U CN204233802U CN 204233802 U CN204233802 U CN 204233802U CN 201420310033 U CN201420310033 U CN 201420310033U CN 204233802 U CN204233802 U CN 204233802U
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Abstract
There is provided a kind of equipment for alleviating the pollution in acetonitrile fractionating column in acrylonitrile recovery, it comprises: acetonitrile fractionator, and it is configured to produce the tower top comprising acetonitrile and distillates stream; Reflux pipeline, it is configured to reflux stream to be transported to acetonitrile fractionator; And pipeline is added in acid, it is configured to add acid to reflux stream; It is characterized in that, described acetonitrile fractionator comprises top tray and the multiple tower trays below described top tray, and described reflux pipeline is configured to described reflux stream to be transported to described top tray, and wherein acid alleviates the pollution in acetonitrile fractionator.
Description
Technical field
The disclosure is directed to process and the system of the improvement for manufacturing acrylonitrile or methacrylonitrile.Especially, the disclosure is directed to the acetonitrile that acrylonitrile reclaims and removes the pollution improved in step and alleviate.
Background technology
The various process and the system that are used for manufacturing acrylonitrile and methacrylonitrile are known; Referring to such as U.S. Patent No. 3,936,360, No.3,433,822, No.3,399,120 and No.3,535,849.Propylene, ammonia and oxygen (as constituent of air) are fed to acrylonitrile reactor, and acrylonitrile reactor comprises catalyst and runs as fluid bed.Conventional way carrys out operant response device relative to the propylene amount being fed into reactor with excess of ammonia in charging.Some in extra ammonia is burnt in the reactor, and this can be combined with propylene with the extreme condition formed before acrylonitrile owing at it.All the other extra ammonia, are commonly referred to as " excess ammonia " and leave reactor in eluting gas.Then this gas usually pass cooler and then arrive quencher to remove excess ammonia.Referring to such as U.S. Patent No. 3,936,360, No.4,166,008, No. 4,334,965, No.4,341,535, No.5,895,635 and No.6,793,776.
Conventional process is usually directed to comprise propane by being selected from, hydrocarbon in the group of propylene or isobutene, the recovery of acrylonitrile/methacrylonitrile that the direct reaction under catalyst exists situation of ammonia and oxygen produces and purifying, realized by following steps: the reactor effluent comprising acrylonitrile/methacrylonitrile is transported to the first tower (chilling), in the first tower, utilize the first aqueous stream cooling reactor effluent, the effluent of the cooling comprising acrylonitrile/methacrylonitrile is transported in the second tower (absorber), in the second tower, the effluent of cooling contacts to absorb in the second aqueous stream by acrylonitrile/methacrylonitrile with the second aqueous stream, the second aqueous stream comprising acrylonitrile/methacrylonitrile is transported to the first destilling tower (recovery tower) for separation crude acetonitrile/methacrylonitrile and the second aqueous stream from the second tower, and, crude acetonitrile/the methacrylonitrile of separation is transported to after-fractionating tower (head fraction column) to remove at least some impurity from crude acetonitrile/methacrylonitrile, and, partially purified acrylonitrile/methacrylonitrile is transported to the 3rd destilling tower (product tower) to obtain product acrylonitrile/methacrylonitrile.Referring to such as, U.S. Patent No. 4,334,295 and No.4,238,295, it discloses conventional process, in single extraction distillation column, wherein perform being separated of acetonitrile and acrylonitrile.In this conventional process, distillate stream at the bottom of the tower of acetonitrile fractionator and be sent to recovery tower or extraction distillation column.
The problem run in conventional process and system is hydrogen cyanide gathering in higher-boiling compound, the temperature decomposition that higher-boiling compound is required in acetonitrile fractionator.The hydrogen cyanide of decomposition release in radical form of higher-boiling compound, hydrogen cyanide is polymerized and pollutes in acetonitrile fractionator.The operation that pollution may cause acetonitrile fractionator poor, and cause unit shut down with clean acetonitrile fractionating column and remove pollution.In addition, a small amount of ammonia is through quencher, because chilling reaction is not 100% efficient.This ammonia tends to gather.
Utility model content
Therefore, one side of the present disclosure is to provide a kind of and alleviates and/or remove pollute in acetonitrile fractionating column safe, effectively and have cost-benefit process and equipment.
On the one hand, provide a kind of process, it comprises: add acid to reflux stream; And reflux stream is transported to acetonitrile fractionator.
On the other hand, a kind of process comprises and is transported to quench tower by distillating stream at the bottom of the tower of acetonitrile fractionating column.In this regard, distillate stream at the bottom of tower and comprise at least some acid.
On the other hand, a kind of equipment of the pollution for alleviating in acetonitrile fractionating column in acrylonitrile recovery comprises: acetonitrile fractionator, and it is configured to produce the tower top comprising acetonitrile and distillates stream; Reflux pipeline, it is configured to reflux stream to be transported to acetonitrile fractionator; And pipeline is added in acid, and it is configured to add acid to reflux stream; Wherein, described acetonitrile fractionator comprises top tray and the multiple tower trays below described top tray, and described reflux pipeline is configured to described reflux stream to be transported to described top tray.
Read by reference to the accompanying drawings, by the detailed description of the hereafter illustrated embodiment of the application, above-mentioned and other side, feature and advantage of the present disclosure will be apparent.
Accompanying drawing explanation
In consideration of the drawings by reference to the following description, can obtain the understanding more comprehensively of exemplary embodiment to the application and its advantage, in the accompanying drawings, similar Reference numeral indicates similar feature and in the accompanying drawings:
Fig. 1 is the schematic flow diagram according at least one aspect of the present disclosure.
Fig. 2 is the schematic flow diagram according at least one aspect of the present disclosure.
Fig. 3 is the flow chart of the method 300 according to aspect of the present disclosure.
Detailed description of the invention
On the one hand, provide a kind of method or process, it comprises the step of the acid in reflux stream being added to acetonitrile fractionator.On the one hand, this process comprises reflux stream is transported to acetonitrile fractionator, acetonitrile fractionator comprises top tray and the multiple tower trays below top tray, and wherein supplying step comprises reflux stream is transported to top tray, and wherein acid alleviates the pollution in acetonitrile fractionator.
On the one hand, this process comprises and is sent to quencher by distillating stream at the bottom of the tower of acetonitrile fractionator.In one embodiment, the acid adding acetonitrile fractionator in reflux stream to is acetic acid.On the one hand, transmit from acetonitrile fractionator and to distillate stream at the bottom of tower and can comprise obtaining originally to be sent at the bottom of the acetonitrile fractionator column of recovery tower and distillate stream at least partially, and make to change route at least partially and be sent to quencher.On the one hand, acid can be added in reflux stream by LDR to prevent from or to alleviate polymer in acetonitrile fractionator being formed and reducing cleaning cost and extend the operation of acetonitrile fractionator.
The transmission that the tower bed material that can perform acetonitrile fractionator flows to quencher makes the pH value of the lower section of recovery tower maintain predeterminated level or scope, such as, lower than pH neutral 7, on the other hand, the pH value of 5 to 7.5, and on the other hand 6 to 7.5 pH.The step that lower section to recovery tower adds acid excessively can reduce the pH in recovery tower and upset the chemical balance being present in the higher-boiling compound of this position in this process.
On the one hand, when the bottomsstream of acetonitrile fractionator turns back to quench tower and turn back to the recoverer section in recovery tower unlike conventional propylene nitrile process, solve the problem that hydrogen cyanide pollutes by acid being added to the top tray that is back to acetonitrile fractionator.
Acid makes to be present in hydrogen cyanide in stream and acetonitrile fractionator not polymerization and the scope polluted and as polymerization inhibitor in acetonitrile fractionating column by being remained on by pH.Then acid get back to quencher, and wherein, pH has maintained the neutral range lower than about 4 to about 6, and can remove ammonia with the outflow stream of helping from the reactor acrylonitrile facility.
Fig. 1 and Fig. 2 is the schematic flow diagram according at least one aspect of the present disclosure.Especially, Fig. 1 and Fig. 2 is the schematic diagram of the embodiment of the present disclosure be in acrylonitrile removal process.
Comprise the rich water of acrylonitrile, acetonitrile, HCN, water and impurity from absorber 300 or aqueous solution is delivered to heat exchanger 4 by pipeline 2, wherein rich water is by poor-water/aqueous solvent 222 preheating from pipeline 223 to heat exchanger 4.After warming, Fu Shui leaves interchanger 4 via pipeline 6 and is delivered to recovery tower 7.Utilize the aqueous solvent of adding and being delivered to recovery tower by pipeline 8, in recovery tower 7, perform extractive distillation.When transmitting from heat exchanger 4 or after transmitting, poor-water/aqueous solvent 222 can split into aqueous solvent stream and poor-water stream, aqueous solvent stream is by heat exchanger 236 and pipeline 8 top 207 to recovery tower 7, and poor-water stream is by pipeline 224.Poor-water/aqueous solvent 222 can provide from heat recovery equipment 226.Heat recovery equipment 226 can receive stream 228 via pipeline 230 from recovery tower 7.Stream 228 can take from the precalculated position of recovery tower 7, above the summary of the tower tray 232 such as in the bottom 227 of recovery tower 7 or tower tray 232 place.Tower tray 232 can be the tower tray of bottommost in recovery tower 7, is also referred to as the first tower tray of recovery tower 7.Stream 228 can transfer to heat recovery equipment 226 by pump 229 from recovery tower 7.
Absorber 300 can be sent to by the poor-water stream of pipeline 224.Heat exchange can occur at heat exchanger 234 place, before the poor-water stream by pipeline 224 is sent to absorber 300.Heat can be supplied by interchanger 210 and be distilled in recovery tower 7.Three kinds of streams are removed from recovery tower 7.First, the tower top of acrylonitrile, HCN, water and some impurity distillates stream and removes from recovery tower 7 via pipeline 212.Sidepiece stream 214 can remove from recovery tower 7 and be delivered to elutriator (stripper) or acetonitrile fractionator 215.The tower top comprising acetonitrile distillates stream 203 can via the top removal of pipeline 216 from acetonitrile fractionator 215.Liquid column bottoms distillate from the bottom 205 of acetonitrile fractionator 215 can turn back to recovery tower 7 by pipeline 218.Pump 219 may be used for making liquid turn back to recovery tower 7 like this by pipeline 218.But, find that it can be preferred for by pipeline 221, the bottomsstream 209 from bottom 205 being transported to quencher 10.Distillate stream at the bottom of tower from recovery tower 7 to remove via pipeline 51, and transfer to chilling tower 10 or waste disposal unit by pipeline 220 by pump 53.
In one embodiment, the stream comprising acetonitrile at pipeline 216 can be transported to condenser 235 and leave as condenser tower bottoms stream 245.Condenser tower bottoms stream 245 can split into the reflux stream 251 in reflux pipeline 217 and the crude acetonitrile stream 253 in crude acetonitrile pipeline 237 at junction surface 247 place.On the one hand, the reflux stream 251 in reflux pipeline 217 can turn back to the top tray 241 of acetonitrile fractionator 215.A part for stream 215 can be supplied to pipeline 216 via pipeline 239.
On the one hand, to extract from recovery tower 7 gas phase comprising acetonitrile, water and trace HCN and be transported to acetonitrile fractionator 215 as sidepiece stream 214.Acetonitrile fractionator 215 can be the tower comprising multiple tower tray.Pump 225 can be used for pumped back and flow through reflux pipeline 217 and/or crude acetonitrile pipeline 237.
On the one hand, process comprises to reflux stream interpolation acid.As further described, " adding acid to reflux stream " can comprise and add acid to reflux pipeline 217, adds acid, add acid to reflux pipeline 239 to the overhead in pipeline 216, and the combination of each.On the other hand, acid can be added in the upstream of condenser 235 or downstream.Add acid to condenser 235 upstream and the acid concentration of more diluting is provided.Acid will provide acid from higher concentration to acetonitrile fractionator 215 is added in the downstream of condenser.
On the other hand, acid is provided to condenser 235 to reduce the pollution in condenser.In this regard, when spraying to the acid of the tube sheet in condenser completely by acid injection covering, the acid being transported to condenser 235 is the most effective.Acid can be passed through injection nozzle (such as wholecircle conical jet nozzle) and be transported to tube sheet in condenser 235.Injection nozzle can angledly cover with the injection realizing tube sheet.Such as, nozzle can perpendicular to tube sheet and relative to the angle become perpendicular to tube sheet up to about 60 °.
On the one hand, organic acid or organic acid derivatives, such as acetic acid or glycol acid can add reflux pipeline 217 to via pipeline 213.On the other hand, organic acid or organic acid derivatives, such as acetic acid or glycol acid can add overhead pipeline 216 via pipeline 233 to from acetonitrile fractionator 215.On the other hand.Organic acid or organic acid derivatives such as acetic acid or glycol acid can add reflux pipeline 239 to via pipeline 243.On the other hand, before overhead enters condenser 235, via pipeline 213 to reflux pipeline 217 and/or via pipeline 233 and/or via pipeline 243 to reflux pipeline 239, it can be useful to reduce polymerization in acetonitrile fractionator 215, condenser 235 and/or miscellaneous equipment and pollution for adding organic acid or organic acid derivatives such as acetic acid or glycol acid to pipeline 216, such as when the bottomsstream of acetonitrile fractionator 215 is sent to quencher, instead of during to recovery tower 7.Acetonitrile fractionator 215 can be designed or be configured to the concentrated dilution water/acetonitrile stream that may be sent to miscellaneous equipment to be further purified and/or to reclaim acetonitrile.In one embodiment, the bottomsstream 211 of acetonitrile fractionator 215 can transfer to quencher 10 by pump 55 by pipeline 221.In one embodiment, the bottomsstream 211 of acetonitrile fractionator 215 can engage with the recovery tower the bottomsstream in pipeline 51 via pipeline 9, and the bottomsstream wherein combined can transfer to quencher 10 by pump 53 by pipeline 220 or to waste disposal unit.
As shown in Figure 2, quencher 10 is configured to receive reactor eluting gas or gaseous stream 12 by pipeline 14.Reactor eluting gas 12 can comprise acrylonitrile and ammonia.Reactor eluting gas 12 can cool before entering quencher 10 in reactor effluent cooler.In quencher 10, comprise the quench liquid contact and quench reactor eluting gas 12 that distillate stream at the bottom of the tower of acetonitrile fractionator.
Acid 36(such as, 98% sulfuric acid) quench liquid 16 can be added to via pipeline 38.Due to the acid in the bottomsstream 211 being sent to quencher 10, the acid amount that pipeline 38 adds can be reduced by.Quench liquid 16 comprises the liquid of the bottom 42 being left quencher 10 by pipeline 44.Water can add quencher 10 via pipeline 46 to by entrance 48, or otherwise can add quench liquid 16 to or other position in the liquid recycle loop that formed by stream 17,44 and 65.Quench liquid 16 is recycled by pipeline 44 and is used pump 50 to get back to pipeline 65 and 17.Stream 67 can as the extracting section of the liquid efflunent left by pipeline 44, to maintain relative constancy mass flow in liquid recirculation loops by making up the liquid added via pipeline 38,46,220 and 221.Stream 57 removes formed neutralization reaction product (such as, ammonium sulfate) and is also applicable to prevent undesired product from gathering in liquid recirculation loops, such as corrosion product.The effluent leaving bottom quencher 10 42 can extract from pipeline 44 at siphon point 52 place.
Tower top distillates stream 13 can flow to chilling aftercooler 240 by pipeline 15 from quencher 10.Cold water may be used for chilling aftercooler 240 and distillates stream 13 chilling aftercooler condensate liquid with cooling tower top.Rich water can be transferred to rich water pipeline 2 by pump 242 and/or get back to the top 252 of chilling aftercooler 240 to recirculation line 248 from the bottom 250 of chilling aftercooler 240.After being cooled by chilling aftercooler 340, tower top distillates stream 13 can leave chilling aftercooler 240 as stream 244.Stream 244 can be transported to absorber 300 via pipeline 246.Poor-water from pipeline 224 can enter the top 254 of absorber 300.Waste gas 256 from absorber 300 can be sent to incinerator (not shown).From bottom absorber 300 262 stream 258 can comprise rich water as described earlier.This rich water can transfer to pipeline 2 via pump 260.Stream 258 can combine with the rich water from chilling aftercooler 240, such as at joint 264.
On the one hand, controller 11 can be configured to process the one or more signals corresponding to measured parameter, the pH of the pH of the acetonitrile fractionator the bottomsstream 209 such as in the bottom 205 of acetonitrile fractionator 215 or the acetonitrile fractionator the bottomsstream 211 in pipeline 221 or pipeline 9, as measured by pH sensor (not shown in FIG).Controller 11 can be configured to judge that whether determined parameter is higher or lower than predefined parameter scope.Those skilled in the art will recognize that according to the disclosure, the parameter measured can be any suitable parameters being applicable to operate acetonitrile fractionator, such as, the pH of the acetonitrile fractionator the bottomsstream 209 or 211 previously discussed, or the liquid level measured by the fluid level controller (not shown in FIG) in the bottom 205 of acetonitrile fractionator 215 or the flow controller (not shown in FIG) that associates with the fluid mobile phase in one or more pipeline discussed in this article.Controller 11 can be configured to the operation adjusting one or more device via order wire or radio communication (not shown in FIG), if the parameter measured is below or above predefined parameter scope.Such as, controller 11 can be configured to the acid amount of adjustment by pipeline 213 or 233 interpolation to realize pH desired in reflux stream 251 to alleviate the pollution in acetonitrile fractionator 215.Those skilled in the art will recognize that according to the disclosure, controller 11 can be configured to control and be added the operation of sour (multiple) pump that is associated and/or valve by pipeline 213 and/or 233 thus satisfied (multiple) preset range.Identification controller 11 or similar control device can be positioned at from fluid level controller or flow controller (not shown in FIG) remotely or can be positioned at and comprise fluid level controller or flow controller by those skilled in the art.Those skilled in the art will recognize that according to the disclosure, the operation of (multiple) pump/valve that controller 11 can be configured to the device shown in Fig. 2 and be associated with those devices.
Perform test to prove add acid to acetonitrile fractionator 215 and acetonitrile fractionator the bottomsstream be sent to quencher 10 instead of traditionally acetonitrile fractionator the bottomsstream be sent to recovery tower 7 and acid do not added to the advantage of acetonitrile fractionator 215.Obtain following test data.
The facility 1 of test data-the comprise quencher shown in Fig. 1 is formed by the ammonia operating to illustrate in the overhead pipeline 216 of acetonitrile fractionator 215 according to the disclosure.Ammonia in overhead pipeline 216 be the polymerisation of hydrogen cyanide accessory substance and therefore indicate in acetonitrile fractionator 215 improperly/undesirable polymer formed.The facility 1 of " add acid/possess acid " operates to the top tray of acetonitrile fractionator 215 to add acetic acid as described above, and acetonitrile fractionator the bottomsstream is sent to quencher 10 via pipeline 211.The facility 1 " not adding acid/anacidity " is not to add acetic acid or other acid operates, and wherein acetonitrile fractionator the bottomsstream sends back to recovery tower 7 via pipeline 18.
The result that the facility 1 running " adding acid " as described above and the facility 1 running " not adding acid " obtain illustrates in the following table.
Test data given above shows the effect of adding acetic acid to acetonitrile fractionator overhead distillate, and wherein the pH of the pH of stream from 8.9 is reduced to the pH of 6.4.On the one hand, the pH reduced in recovery tower decreases improper polymerization.This is the corresponding reduction of the ammonia density in acetonitrile fractionator overhead distillate, namely when add acetic acid time from 188ppm to 9ppm.The reduction of ammonia in this acetonitrile fractionator overhead distillate, that is, the stream flowed by pipeline 216 is considered to acetic acid and catches ammonia as the result of ammonium acetate it is removed to chilling 10 in stream 211.It also may be partly that hydrogen cyanide stays in the solution as cyanalcohol and do not resolve into its original components and the result of then polymerization (it discharges ammonia).Ammonia is the accessory substance of the polymerisation of hydrogen cyanide.Add acetic acid to stream significantly reduce the ammonia amount of existence and demonstrate effect of the present disclosure.
On the one hand, pH level is selected to be reducing to pollute the balance between the building material desired by use.In this regard, pH level as described above is used to allow to use carbon steel structure.
Fig. 3 is the flow chart of the method 300 according to aspect of the present disclosure.Previously described equipment can be used to carry out manner of execution 300.Step 301 comprises: be sent to quencher by distillating stream at the bottom of the tower of acetonitrile fractionating column.Step 302 comprises: acid is added to reflux stream to acetonitrile fractionator.On the one hand, acetonitrile fractionator comprises multiple tower tray, and acid is added to reflux stream comprises multiple tower trays acid being added to acetonitrile fractionator top tray to the step of acetonitrile fractionating column.On the one hand, acid is added to reflux stream to comprise to the step of acetonitrile fractionator and add acetic acid to reflux stream.On the one hand, perform to backflow add acid step to reduce the pH of the overhead of acetonitrile fractionator.
On the one hand, the step of adding acid to backflow causes the pH of the overhead of acetonitrile fractionating column to be reduced to pH lower than 7.0 from higher than 7.0.On the one hand, the step of adding acid to backflow causes the pH of the overhead of acetonitrile fractionating column to be reduced to pH lower than 6.5 from higher than 8.0.On the one hand, sour step is added by the pH of the overhead of acetonitrile fractionating column from the pH being reduced to about 6.4 higher than 7.0 to backflow.
On the one hand, the step distillating stream at the bottom of the tower of acetonitrile fractionator and be sent to quencher is also comprised change route transmission by distillating stream at the bottom of the tower of acetonitrile fractionator make the tower bottoms stream of acetonitrile fractionating column flow to quencher from flowing to recovery tower.
The application is applicable to any process of recover acrylonitrile, and the process of recover acrylonitrile has recovery tower and one or more extra destilling tower.Extra destilling tower generally includes HCN tower, be used for removing the drying tower of water and be used for reclaiming the product tower of product qualities acrylonitrile.But these operate separately and can combine as shown in drawings, and wherein, a destilling tower removes both HCN and water.
Although describe the disclosure about some preferred embodiment of the application, and disclosed for illustrative purposes many details, obviously the disclosure is easy to have Additional examples of composition and some in details described herein can change significantly for those skilled in the art, and does not depart from general principle of the present disclosure.Should be appreciated that feature of the present disclosure is easy to make amendment, change, change or substitutes and do not depart from the scope of spirit or scope of the present disclosure or claim.Such as, the size of various parts, quantity, size and shape can be changed to adapt to embody rule.Therefore, diagram and specific embodiment described herein are just for purpose of explanation.
Claims (13)
1., for alleviating an equipment for the pollution in acetonitrile fractionating column in acrylonitrile recovery, it comprises:
Acetonitrile fractionator, it is configured to produce the tower top comprising acetonitrile and distillates stream;
Reflux pipeline, it is configured to reflux stream to be transported to acetonitrile fractionator; And
Pipeline is added in acid, and it is configured to add acid to described reflux stream;
It is characterized in that, described acetonitrile fractionator comprises top tray and the multiple tower trays below described top tray, and described reflux pipeline is configured to described reflux stream to be transported to described top tray.
2. equipment according to claim 1, is characterized in that, it also comprises: condenser, and it is configured to cool described tower top and distillates stream and the crude acetonitrile product generating condensation, and wherein said reflux stream comprises described condensation acetonitrile product at least partially.
3. equipment according to claim 1, is characterized in that, described acid comprises acetic acid.
4. equipment according to claim 1, is characterized in that, it comprises controller, and it is configured to add for the acid to described reflux stream control.
5. equipment according to claim 4, is characterized in that, described controller is configured to control acid to be added to reduce the pH that described tower top distillates stream.
6. equipment according to claim 5, is characterized in that, described controller is configured to maintain described tower top and distillates the pH of stream in preset range.
7. equipment according to claim 5, is characterized in that, the pH that described controller is configured to described tower top to distillate stream is reduced to pH lower than 7.0 from being greater than 7.0.
8. equipment according to claim 5, is characterized in that, described controller is configured to described tower top to distillate the pH of stream from being greater than the pH that 8.0 are reduced to 6.5.
9. equipment according to claim 5, is characterized in that, described controller is configured to described tower top to distillate the pH of stream from being greater than the pH that 7.0 are reduced to 6.4.
10. equipment according to claim 2, is characterized in that, described acid is added pipeline and is configured to distillate stream interpolation acid to described tower top.
11. equipment according to claim 1, it is characterized in that, it also comprises: transfer line, and it is configured to be sent to quencher at least partially by what distillate stream at the bottom of the tower of described acetonitrile fractionator.
12. equipment according to claim 11, is characterized in that, distillate stream and comprise in the acid adding described reflux stream at least partially at the bottom of described tower.
13. equipment according to claim 12, is characterized in that, described quencher is configured to receive the gaseous stream comprising acrylonitrile and ammonia, and described gaseous stream is contacted with quench liquid, and described quench liquid comprises at the bottom of the tower of described acetonitrile fractionator and distillates stream.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104107559A (en) * | 2014-06-11 | 2014-10-22 | 英尼奥斯欧洲股份公司 | Pollution reduction in acetonitrile removing step in acrylonitrile recovery |
| CN105425849A (en) * | 2015-08-03 | 2016-03-23 | 英尼奥斯欧洲股份公司 | Quench tower ph control |
-
2014
- 2014-06-11 CN CN201420310033.1U patent/CN204233802U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104107559A (en) * | 2014-06-11 | 2014-10-22 | 英尼奥斯欧洲股份公司 | Pollution reduction in acetonitrile removing step in acrylonitrile recovery |
| WO2015191528A1 (en) * | 2014-06-11 | 2015-12-17 | Ineos Europe Ag | Fouling reduction in the acetonitrile removal steps of acrylonitrile recovery |
| EA034228B1 (en) * | 2014-06-11 | 2020-01-20 | ИНЕОС Юроп АГ | Fouling reduction in the acetonitrile removal steps of acrylonitrile recovery |
| CN105425849A (en) * | 2015-08-03 | 2016-03-23 | 英尼奥斯欧洲股份公司 | Quench tower ph control |
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