CN103896806A - System for separating and purifying acrylonitrile - Google Patents
System for separating and purifying acrylonitrile Download PDFInfo
- Publication number
- CN103896806A CN103896806A CN201410132988.7A CN201410132988A CN103896806A CN 103896806 A CN103896806 A CN 103896806A CN 201410132988 A CN201410132988 A CN 201410132988A CN 103896806 A CN103896806 A CN 103896806A
- Authority
- CN
- China
- Prior art keywords
- tower
- communicated
- pipeline section
- quench tower
- separating
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a system for separating and purifying acrylonitrile. The system comprises a quench tower (1), a separation tower (2) and sulfuric acid solution conveying pipes (3), wherein the bottom of the quench tower (1) is communicated with the side wall of the top of the tower via a first communication pipe section, the material inlet of the separation tower (2) is communicated with the first communication pipe section by a second communication pipe section, the outlet of the gaseous phase material located at the top of the separation tower is in communication with the quench tower (1) and the conveying pipes (3) are communicated with the quench tower (1). The system disclosed by the invention is at least capable of improving the yield of purified acrylonitrile.
Description
Technical field
The present invention relates to organic chemicals acrylonitrile process field, more specifically, relate to a kind of vinyl cyanide system for separating and purifying.
Background technology
The production technology of vinyl cyanide is mainly taking propylene, oxidation proceses of ammonia as main in the world.This Technology is because raw material is cheaply easy to get, and production cost is lower, and product separation is relatively easy, and product purity is high, is current most advanced most economical production line.
In production process, easily there is polymerization in unsettled unsaturated nitrile under alkaline condition, greatly affects the stability of quality product and device operation, and an important factor that causes production environment to be alkalescence is exactly the ammonia of complete reaction not.At present, adopt propylene, oxidation proceses of ammonia to produce the process unit of vinyl cyanide, all adopt and in quenched water, mix sulfuric acid and remove unreacted ammonia; In this operating process, more advanced technique is to adopt one-part form quench tower, and reduces vinyl cyanide, prussic acid loss by preparing and regulating and controlling the micro-acid environment of full tower, and the ammoniumsulphate soln that tower reactor is generated is delivered to thiamines retrieving arrangement or sulphur ammonium series products production equipment.But, in actual production, find also to contain the products such as vinyl cyanide, prussic acid, acetonitrile in ammoniumsulphate soln, increase the difficulty of purification sulphur ammonium, and caused the loss of the products such as vinyl cyanide.
Summary of the invention
For the problem existing in correlation technique, the object of the present invention is to provide a kind of vinyl cyanide system for separating and purifying, at least to realize the refining yield that improves acrylonitrile process.
For achieving the above object, the invention provides a kind of vinyl cyanide system for separating and purifying, comprising: quench tower, is connected by the first connection pipeline section with its tower top sidewall at the bottom of the tower of quench tower; Knockout tower, the material inlet of knockout tower is communicated with pipeline section and is communicated with pipeline section connection by second with first, and the gaseous phase materials outlet on its top is communicated with quench tower; And sulphuric acid soln transfer lime, transfer lime is communicated with quench tower.
According to the present invention, sulphuric acid soln transfer lime is connected with the first connection pipeline section, be communicated with quench tower to be communicated with pipeline section by first, wherein, along the first connection pipeline section from the direction to its tower top sidewall at the bottom of quench tower tower, transfer lime and first is communicated with the first link position of being connected of pipeline section, is positioned at the downstream of the second link position that the second connection pipeline section and the first connection pipeline section be connected.
According to the present invention, also comprise reboiler and steam manifold, wherein, reboiler is connected with knockout tower, and steam manifold has the first branch road and the second branch road, and the first branch road is connected to reboiler, the second branch road is connected to knockout tower, wherein, by being arranged on the shifter in steam manifold, the steam of controlling in steam manifold enters the first branch road or the second branch road.
According to the present invention, between knockout tower and steam manifold, be connected with tandem setting device, tandem setting device comprises temperature monitor, flow monitor and variable valve, wherein, temperature monitor is monitored the tower top temperature of knockout tower, and regulates the aperture of variable valve according to monitor value control flow monitor.
According to the present invention, at the bottom of the tower of quench tower and between the second connection pipeline section, be connected with level monitoring device, wherein, level monitoring device, according to the liquid level of reaction mass in quench tower, is controlled the flow that is flowed into the intermediate reaction product of the second connection pipeline section by the first connection pipeline section.
According to the present invention, sulphuric acid soln transfer lime and first is communicated with and between pipeline section, is provided with pH value monitoring device, wherein, pH value monitoring device is communicated with the link position of pipeline section with first, between the first link position and the second link position, wherein, pH value monitoring device, according to the pH value of intermediate reaction product in the first connection pipeline section, is controlled the operational throughput of sulphuric acid soln transfer lime to the first connection pipeline section conveying sulphuric acid soln.
According to the present invention, knockout tower bottom is connected with material recycle pipe, is provided with fluid level control device, wherein between knockout tower bottom and material recycle pipe, fluid level control device, according to the liquid level of reaction mass in knockout tower, is controlled the flow that flows into material to be recycled in material recovery tube.
According to the present invention, the tower top of quench tower is provided with the outlet of finished product product, and quench tower inside is provided with the first spray equipment, and wherein, the first spray equipment is communicated with the first port that is communicated with pipeline section of the tower top sidewall that is communicated to quench tower.
According to the present invention, quench tower sidewall is also provided with reaction gas entrance, and quench tower inside is also provided with the second spray equipment, and wherein, reaction gas entrance is communicated with the second spray equipment.
According to the present invention, first at the bottom of the tower of quench tower and between the second link position is communicated with and in pipeline section, is in series with recycle pump.
Useful technique effect of the present invention is:
In vinyl cyanide system for separating and purifying of the present invention, sulphuric acid soln transfer lime can be carried sulphuric acid soln in quench tower, to react with the reaction gas of sending into quench tower.Wherein, in reaction gas, at least comprise propylene steam nitrile and ammonia, also can include gaseous hydrogen cyanic acid, gaseous state acetonitrile etc.In quench tower, sulphuric acid soln reacts that with this reaction gas this reaction gas is purified.Particularly, in quench tower, sulphuric acid soln and ammonia gas react generate ammoniumsulphate soln, so that the ammonia in reaction gas is removed.Propylene steam nitrile in reaction gas is towards the tower top motion of quench tower.At the bottom of the ammoniumsulphate soln generating after reaction flow to the tower of quench tower, wherein, in the process of ammoniumsulphate soln at the bottom of flowing to tower, can be mingled with the liquid propylene nitrile of condensation in quench tower, and at the bottom of unreacted sulphuric acid soln also flow to the tower of quench tower, thus, the intermediate reaction product being positioned at the bottom of quench tower tower at least comprises ammoniumsulphate soln, sulphuric acid soln, liquid propylene nitrile.By accessing knockout tower at the bottom of the tower of quench tower and between tower top sidewall, the intermediate reaction product of quench tower is carried out to secondary and separate again and required product is sent back in quench tower again.Particularly, in knockout tower, quench tower is isolated and sent back to vinyl cyanide in intermediate reaction product, and then the propylene steam nitrile of gained and form finished product product through the propylene steam nitrile of knockout tower secondary separation gained and discharged by quench tower of purifying for the first time in quench tower.In this way, on the one hand, can effectively remove the ammonia in reaction gas, on the other hand, reduce the loss of vinyl cyanide in above-mentioned removal process.Make thus the refining yield of vinyl cyanide improve, and promote the purity of propylene steam nitrile.
Brief description of the drawings
Fig. 1 is the schematic diagram of an embodiment of vinyl cyanide system for separating and purifying of the present invention.
Embodiment
Specifically describe embodiments of the invention referring to accompanying drawing.With reference to Fig. 1, show an embodiment of vinyl cyanide system for separating and purifying of the present invention, the sulphuric acid soln transfer lime 3 that it comprises quench tower 1, knockout tower 2 and is communicated in quench tower 1.Wherein, at the bottom of the tower of quench tower 1, be connected by the first connection pipeline section 8 with the tower top sidewall of quench tower 1, the material inlet of knockout tower 2 is communicated with pipeline section 8 and is communicated with by the second connection pipeline section 9 with first, the gaseous phase materials outlet on knockout tower 2 tops is communicated with by third connecting pipeline section 22 with quench tower 1.
In the time that said system is worked, sulphuric acid soln transfer lime 3 can be carried sulphuric acid soln in quench tower 1, to react with the reaction gas of sending into quench tower 1.Wherein, in reaction gas, at least comprise propylene steam nitrile and ammonia, also can include gaseous hydrogen cyanic acid, gaseous state acetonitrile etc.In quench tower 1, sulphuric acid soln reacts that with this reaction gas this reaction gas is purified.Particularly, in quench tower 1, sulphuric acid soln and ammonia gas react generate ammoniumsulphate soln, so that the ammonia in reaction gas is removed.Propylene steam nitrile in reaction gas is towards the tower top motion of quench tower 1.At the bottom of the ammoniumsulphate soln generating after reaction flow to the tower of quench tower 1, wherein, in the process of ammoniumsulphate soln at the bottom of flowing to tower, can be mingled with the liquid propylene nitrile of condensation in quench tower 1, and at the bottom of unreacted sulphuric acid soln also flow to the tower of quench tower 1, thus, the intermediate reaction product being positioned at the bottom of quench tower 1 tower at least comprises ammoniumsulphate soln, sulphuric acid soln, liquid propylene nitrile.By accessing knockout tower 2 at the bottom of the tower at quench tower 1 and between tower top sidewall, the intermediate reaction product of quench tower 1 is carried out to secondary and separate again and required product is sent back in quench tower again.Particularly, in knockout tower 2, quench tower is isolated and sent back to vinyl cyanide in intermediate reaction product, and then the propylene steam nitrile of gained and form finished product product through the propylene steam nitrile of knockout tower secondary separation gained and discharged by quench tower 1 of purifying for the first time in quench tower 1.In this way, on the one hand, can effectively remove the ammonia in reaction gas, on the other hand, reduce the loss of vinyl cyanide in above-mentioned removal process.Make thus the refining yield of vinyl cyanide improve, and promote the purity of propylene steam nitrile.
Continue with reference to Fig. 1, sulphuric acid soln transfer lime 3 is connected with the first connection pipeline section 8, to be communicated with quench tower 1 by the first connection pipeline section 8, wherein, along the first connection pipeline section 8 from the direction to its tower top sidewall at the bottom of quench tower 1 tower, sulphuric acid soln transfer lime 3 and first is communicated with the first link position 10 of being connected of pipeline section 8, is positioned at the downstream of the second link position 11 that the second connection pipeline section 9 is connected with the first connection pipeline section 8.In other words, along the first connection pipeline section 8 from the direction to its tower top sidewall at the bottom of quench tower 1 tower, set gradually above-mentioned the second link position 11 and the first link position 10.Make thus, after the intermediate reaction product of quench tower 1 is flowed out by the tower bottom outlet of quench tower 1, first through the second link position 11, the intermediate reaction product of a part enters in knockout tower 2 via the second connection pipeline section 9.The intermediate reaction product of another part flows through the second link position 11 to be continued to flow along the first connection pipeline section 8.In the time that the intermediate reaction product of above-mentioned another part flows to the first link position 10, sulphuric acid soln flows into the first connection pipeline section 8 through sulphuric acid soln transfer lime 3, and the common quench tower 1 that flows into after mixing with the intermediate reaction product of this another part.
With further reference to Fig. 1, in the present embodiment, vinyl cyanide system for separating and purifying also comprises reboiler 4 and steam manifold 5.Wherein, reboiler 4 is connected with knockout tower 2, and steam manifold 5 has the first branch road 12 and the second branch road 13, the first branch roads 12 and is connected to reboiler 4, the second branch roads 13 and is connected to knockout tower 2.Shifter 14 is set in steam manifold 5, and the steam that this shifter 14 is controlled in steam manifold 5 enters the first branch road 12 or the second branch road 13.Alternatively, above-mentioned shifter 14 is T-valve.Particularly, reboiler 4 has first channel and the second passage of heat exchange mutually.Wherein, at the bottom of the tower of the entrance of first channel and knockout tower 2, be communicated with, the outlet of first channel is communicated with the sidewall of knockout tower 2, and the entrance of second passage is communicated with the first branch road 12 of steam manifold 5, and the outlet of second passage is communicated with phlegma recovery line 25.
In the time of the vinyl cyanide system for separating and purifying of application the present embodiment, make the steam in steam manifold 5 enter the first branch road 12 if select, the material being positioned at the bottom of the tower of knockout tower 2 imports first channel, steam imports second passage through the first branch road 12, steam is for the material in first channel provides heat, leads back knockout tower 2 after making liquid in first channel heated.Wherein, in the material at the bottom of the tower of knockout tower 2, at least there is ammoniumsulphate soln, liquid propylene nitrile.Ammoniumsulphate soln and liquid propylene nitrile are heated in reboiler, the liquid propylene nitrile gasification of part forms gas-phase propene nitrile, this part gas-phase propene nitrile is led and is back in knockout tower by knockout tower sidewall together with the liquid propylene nitrile not gasifying, ammoniumsulphate soln, separate to realize secondary, secondary more isolated gas-phase propene nitrile is led back in quench tower 1 through third connecting pipeline section 22 by the tower top of knockout tower 2 again.
In the time of the vinyl cyanide system for separating and purifying of application the present embodiment, make the steam in steam manifold 5 enter the second branch road 13 if select, steam is directly imported in knockout tower 2 so that the reaction mass in knockout tower is heated, make Partial Liquid Phase vinyl cyanide wherein be gasificated into gas-phase propene nitrile, separate again to realize secondary.
To sum up, make the steam in steam manifold 5 enter the first branch road 12 or the second branch road 13 no matter select, steam has all played the effect that thermal source is provided for the reaction mass in knockout tower 2, to make the gasification of liquid propylene nitrile form gas-phase propene nitrile, and enter quench tower 1 via the third connecting pipeline section 22 being communicated with knockout tower 2 tower tops.And vapour stream is condensed into water of condensation by phlegma recovery line 25 after crossing second passage heat release.
In addition, in the present embodiment, between knockout tower 2 and steam manifold 5, be connected with tandem setting device, tandem setting device comprises temperature monitor 15, flow monitor 16 and variable valve 17.Wherein, temperature monitor 15 is monitored the tower top temperature of knockout tower 2, and regulates the aperture of variable valve 17 according to monitor value control flow monitor 16.Preferably, tower top service temperature is positioned at the scope of 105 DEG C～115 DEG C.In the present embodiment, tower top service temperature is 100 DEG C.Temperature monitor 15 detects the tower top temperature of knockout tower 2, and when tower top temperature is during higher than 100 DEG C, temperature monitor 15 sends signal to flow detector 16.Flow detector 16 resets initial value after receiving signal, and then reduces aperture to variable valve 17 signals, variable valve 17 and then reduce steam add-on.The final tower top temperature that reduces.When tower top temperature is during lower than 100 DEG C, make variable valve 17 increase aperture and then increase steam add-on.In the time that tower top temperature equals 100 DEG C, temperature monitor 15 does not carry out any operation.
In addition, in the present embodiment, at the bottom of the tower of quench tower 1 and between the second connection pipeline section 9, be connected with level monitoring device, wherein, level monitoring device, according to the liquid level of reaction mass in quench tower 1, is controlled the flow that is flowed into the intermediate reaction product of the second connection pipeline section 9 by the first connection pipeline section 8.Particularly, the liquid level detector 23 that detects quench tower liquid level is set at quench tower 1, and on the second connection pipeline section 9, valve 24 is set, in the time that liquid level detector 23 detects quench tower liquid level higher than preset value, send signal to increase the aperture of valve 24 to valve 24, and then increase the ammoniumsulphate soln flow that enters knockout tower 2.In the time that liquid level detector 23 detects quench tower liquid level lower than preset value, send signal to reduce the aperture of valve 24 to valve 24, and then reduce to enter the ammoniumsulphate soln flow of knockout tower 2.In the time that liquid level detector 23 detects that quench tower liquid level equals preset value, do not carry out any operation.Alternatively, liquid level detector 23, except having above-mentioned functions, also can have the function of instruction liquid level and warning.Preferably, first at the bottom of the tower of quench tower 1 and between the second link position 11 is communicated with and in pipeline section 8, is in series with recycle pump 7.Wherein, aborning, above-mentioned preset value definite depends primarily on two aspects: 1, the produced quantity of recycle pump 7 ensures that the amount of liquid in quench tower tower reactor has a certain amount of surge time, then sets predetermined level value (being above-mentioned preset value) according to the diameter of this amount of liquid and quench tower.2, remove outside Article 1 chief reason, in an embodiment of the present invention, more than the liquid level of the reaction gas entrance 20 of guarantee quench tower in quench tower.
With further reference to Fig. 1, in the present embodiment, sulphuric acid soln transfer lime 3 and first is communicated with and between pipeline section 8, is provided with pH value monitoring device, wherein, pH value monitoring device is communicated with the link position of pipeline section 8 with first, between the first link position 10 and the second link position 11, wherein, pH value monitoring device, according to the pH value of intermediate reaction product in the first connection pipeline section 8, is controlled the operational throughput that sulphuric acid soln transfer lime 3 is carried sulphuric acid soln to the first connection pipeline section 8.Particularly, when the pH of intermediate reaction product value is during lower than set(ting)value, reduce the operational throughput of sulphuric acid soln.When the pH of intermediate reaction product value is during higher than set(ting)value, increase the operational throughput of sulphuric acid soln.In the time that the pH of intermediate reaction product value equals set(ting)value, do not do any operation.Wherein, preferably, above-mentioned set(ting)value is positioned at the scope of 4.8-6.0.
Continue with reference to Fig. 1, in the present embodiment, knockout tower 2 bottoms are connected with material recycle pipe 6, and in knockout tower 2, reaction mass can be discharged by material recycle pipe 6.Between knockout tower 2 bottoms and material recycle pipe 6, be provided with fluid level control device, wherein, fluid level control device, according to the liquid level of reaction mass in knockout tower 2, is controlled the flow that flows into material to be recycled in material recovery tube 6.The concrete level monitoring device being same as for regulating quench tower 1 that arranges, does not repeat them here.
By using above-mentioned tandem setting device, level monitoring device for quench tower, pH value monitoring device and one or more for separating of the fluid level control device of tower, can ensure the steady running of this vinyl cyanide system for separating and purifying, and ensure that each installs in good running status, further to improve the refining yield of vinyl cyanide, and further promote the purity of propylene steam nitrile.Certainly, the setting of above-mentioned each device is not limited to this, as long as can realize the control of liquid level, the temperature of knockout tower 2 and the flow of sulphuric acid soln of liquid level to knockout tower 2, quench tower 1.
Alternatively, be provided with finished product product outlet 18 at the tower top of quench tower 1, aforementioned finished product product is discharged by finished product product outlet 18, quench tower 1 inside is provided with the first spray equipment 19, the first spray equipment 19 is communicated with the first port that is communicated with pipeline section 8 of the tower top sidewall that is communicated to quench tower 1, ammoniumsulphate soln and sulphuric acid soln enter the first spray equipment 19 through the first connection pipeline section 8, and spray in quench tower 1 through the first spray equipment 19.By this structure, can increase sulphuric acid soln and contact area ammonia, and the liquid propylene nitrile that is conducive to carry secretly in ammoniumsulphate soln departs from ammoniumsulphate soln gasification, and then gas-phase propene nitrile after gasification can be discharged by finished product product outlet 18.
In addition, be also provided with reaction gas entrance 20 at quench tower 1 sidewall, quench tower 1 inside is also provided with the second spray equipment 21, and wherein, reaction gas entrance 20 is communicated with the second spray equipment 21.Thus, the ammonia in can augmenting response gas and the contact area of sulphuric acid soln, can react with sulphuric acid soln more ammonia and generate ammoniumsulphate soln, to reduce the ammonia in finished product product.
In addition, in knockout tower 2, tower tray is set, to strengthen separating effect.Be more preferably, 10 tower trays are set.
Table 1 is the material balance table of the process of the refining vinyl cyanide of application said system.With reference to following table, A, B, C, D, E are five material balance points shown in Fig. 1.Wherein, A point is positioned on the pipeline being connected with reaction gas entrance 20, with component and its physical features of detection reaction gas.B point is positioned at on finished product product outlet 18 pipelines that are connected, to detect component and its physical features of finished product product.C point is positioned on the second connection pipeline section 9, to detect component and its physical features of intermediate reaction product.D point is positioned on third connecting pipeline section 22, and with secondary component and its physical features of isolated gas-phase propene nitrile again, this secondary more isolated gas-phase propene nitrile can be mingled with other gases.E point is positioned on material recycle pipe 6, to detect component and its physical features of the reaction mass of being discharged by separator 2.Said components and physical features are listed particularly in table 1.
Table 1
| Thing stream number | ? | A | B | C | D | E |
| Liquid phase fraction | ? | 0.000 | 0.000 | 0.847 | 0.000 | 0.828 |
| Temperature | ℃ | 255.0 | 82.9 | 84.1 | 109.5 | 111.0 |
| Pressure | MPA | 0.1540 | 0.1460 | 0.4600 | 0.1440 | 0.1520 |
| Mass rate | KG/HR | 135380.97 | 147005.06 | 11986.11 | 1361.35 | 10624.76 |
| Liquid phase actual flow | M 3/HR | ? | ? | 10.51 | ? | 9.24 |
| Liquid phase actual density | KG/M 3 | ? | ? | 965.93 | ? | 952.03 |
| Gas phase actual flow | M 3/HR | 141300.22 | 113943.84 | ? | 1588.36 | ? |
| Gas phase actual density | KG/M 3 | 0.96 | 1.29 | ? | 0.86 | ? |
| Constituent mass flow | KG/HR | ? | ? | ? | ? | ? |
| Vinyl cyanide | KG/HR | 16917.68 | 16607.30 | 66.89 | 66.88 | 0.00 |
| Acetonitrile | KG/HR | 613.51 | 568.89 | 8.02 | 7.94 | 0.08 |
| Prussic acid | KG/HR | 1938.67 | 1762.26 | 8.18 | 8.17 | 0.00 |
| Water | KG/HR | 24014.16 | 36723.34 | 9394.79 | 1253.28 | 8141.51 |
| Sulphur ammonium | KG/HR | 0.00 | 0.00 | 1832.59 | 0.00 | 1832.59 |
| Vinylformic acid | KG/HR | 344.63 | 252.35 | 55.64 | 11.47 | 44.17 |
| Propenal | KG/HR | 178.74 | 134.06 | 0.81 | 0.81 | 0.00 |
| Other components | KG/HR | 91373.58 | 90956.86 | 619..19 | 12.79 | 606.4 |
These are only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any amendment of doing, be equal to replacement, improvement etc., within all should being included in protection scope of the present invention.
Claims (10)
1. a vinyl cyanide system for separating and purifying, is characterized in that, comprising:
Quench tower (1), is communicated with pipeline section (8) with its tower top sidewall by first at the bottom of the tower of described quench tower (1) and is connected;
Knockout tower (2), the material inlet of described knockout tower (2) is communicated with pipeline section (8) and is communicated with pipeline section (9) connection by second with described first, and the gaseous phase materials outlet on its top is communicated with described quench tower (1); And
Sulphuric acid soln transfer lime (3), described transfer lime (3) is communicated with described quench tower (1).
2. vinyl cyanide system for separating and purifying according to claim 1, is characterized in that,
Described sulphuric acid soln transfer lime (3) and described first is communicated with pipeline section (8) and is connected, is communicated with described quench tower (1) to be communicated with pipeline section (8) by described first,
Wherein, along described first be communicated with pipeline section (8) from the direction to its tower top sidewall at the bottom of described quench tower (1) tower, described transfer lime (3) and described first is communicated with the first link position (10) of being connected of pipeline section (8), is positioned at the described second downstream that is communicated with the second link position (11) that pipeline section (9) and described the first connection pipeline section (8) be connected.
3. vinyl cyanide system for separating and purifying according to claim 2, is characterized in that, also comprises reboiler (4) and steam manifold (5),
Wherein, described reboiler (4) is connected with described knockout tower (2), and described steam manifold (5) has the first branch road (12) and the second branch road (13), and described the first branch road (12) is connected to described reboiler (4), described the second branch road (13) is connected to described knockout tower (2)
Wherein, by being arranged on the shifter (14) in described steam manifold (5), the steam of controlling in described steam manifold (5) enters the first branch road (12) or the second branch road (13).
4. vinyl cyanide system for separating and purifying according to claim 3, is characterized in that,
Between described knockout tower (2) and described steam manifold (5), be connected with tandem setting device, described tandem setting device comprises temperature monitor (15), flow monitor (16) and variable valve (17),
Wherein, described temperature monitor (15) is monitored the tower top temperature of described knockout tower (2), and regulates the aperture of described variable valve (17) according to flow monitor (16) described in monitor value control.
5. vinyl cyanide system for separating and purifying according to claim 3, is characterized in that, at the bottom of the tower of described quench tower (1) and between described the second connection pipeline section (9), is being connected with level monitoring device,
Wherein, described level monitoring device, according to the liquid level of reaction mass in described quench tower (1), is controlled the flow that is flowed into the intermediate reaction product of described the second connection pipeline section (9) by described the first connection pipeline section (8).
6. vinyl cyanide system for separating and purifying according to claim 3, is characterized in that,
Described sulphuric acid soln transfer lime (3) and described first is communicated with and between pipeline section (8), is provided with pH value monitoring device,
Wherein, described pH value monitoring device is communicated with the link position of pipeline section (8) with described first, be positioned between described the first link position (10) and described the second link position (11),
Wherein, described pH value monitoring device, according to the pH value of intermediate reaction product in described the first connection pipeline section (8), is controlled the operational throughput that described sulphuric acid soln transfer lime (3) is carried sulphuric acid soln to described the first connection pipeline section (8).
7. vinyl cyanide system for separating and purifying according to claim 3, is characterized in that,
Described knockout tower (2) bottom is connected with material recycle pipe (6), between described knockout tower (2) bottom and described material recycle pipe (6), is provided with fluid level control device,
Wherein, described fluid level control device, according to the liquid level of reaction mass in described knockout tower (2), is controlled the flow that flows into material to be recycled in described material recycle pipe (6).
8. according to the vinyl cyanide system for separating and purifying described in any one in claim 1-7, it is characterized in that,
The tower top of described quench tower (1) is provided with finished product product outlet (18), and described quench tower (6) inside is provided with the first spray equipment (19),
Wherein, described the first spray equipment (19) is communicated with the described first port that is communicated with pipeline section (8) of the tower top sidewall that is communicated to described quench tower (1).
9. according to the vinyl cyanide system for separating and purifying described in any one in claim 1-7, it is characterized in that,
Described quench tower (1) sidewall is also provided with reaction gas entrance (20), and described quench tower (1) inside is also provided with the second spray equipment (21),
Wherein, described reaction gas entrance (20) is communicated with described the second spray equipment (21).
10. according to the vinyl cyanide system for separating and purifying described in any one in claim 2-7, it is characterized in that,
At the bottom of the tower of described quench tower (1) and between described the second link position (11) described first is communicated with and in pipeline section (8), is in series with recycle pump (7).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410132988.7A CN103896806B (en) | 2014-04-02 | 2014-04-02 | System for separating and purifying acrylonitrile |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410132988.7A CN103896806B (en) | 2014-04-02 | 2014-04-02 | System for separating and purifying acrylonitrile |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103896806A true CN103896806A (en) | 2014-07-02 |
| CN103896806B CN103896806B (en) | 2015-07-22 |
Family
ID=50988431
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410132988.7A Active CN103896806B (en) | 2014-04-02 | 2014-04-02 | System for separating and purifying acrylonitrile |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103896806B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105425849A (en) * | 2015-08-03 | 2016-03-23 | 英尼奥斯欧洲股份公司 | Quench tower ph control |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3885928A (en) * | 1973-06-18 | 1975-05-27 | Standard Oil Co Ohio | Acrylonitrile and methacrylonitrile recovery and purification system |
| CN2386046Y (en) * | 1998-12-31 | 2000-07-05 | 中国石化集团齐鲁石油化工公司 | Automatic control device for quench tower acid feeding in acrylonitrile technology |
-
2014
- 2014-04-02 CN CN201410132988.7A patent/CN103896806B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3885928A (en) * | 1973-06-18 | 1975-05-27 | Standard Oil Co Ohio | Acrylonitrile and methacrylonitrile recovery and purification system |
| CN2386046Y (en) * | 1998-12-31 | 2000-07-05 | 中国石化集团齐鲁石油化工公司 | Automatic control device for quench tower acid feeding in acrylonitrile technology |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105425849A (en) * | 2015-08-03 | 2016-03-23 | 英尼奥斯欧洲股份公司 | Quench tower ph control |
| CN105425849B (en) * | 2015-08-03 | 2020-06-26 | 英尼奥斯欧洲股份公司 | Quench tower pH control |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103896806B (en) | 2015-07-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| RU2019123934A (en) | REACTORS, SYSTEMS AND METHODS OF FERMENTATION WITH A GAS SUPPLY WITH THE APPLICATION OF A VERTICAL FLOW ZONE | |
| CN102256697B (en) | High pressure polymerization process | |
| CN103304692B (en) | Olefinic polymerization device and olefine polymerizing process | |
| CN109070043B (en) | Urea production with controlled biuret | |
| TWI715532B (en) | Fouling reduction in the acetonitrile removal steps of acrylonitrile recovery | |
| MX2012009395A (en) | Process for the production of anhydrides. | |
| CN103896806B (en) | System for separating and purifying acrylonitrile | |
| CN203355710U (en) | Rapid fluidized bed reactor for producing butadiene by butylene oxydehydrogenation | |
| CN105214572A (en) | The reaction-regenerative device of methanol-to-olefins and reaction method thereof | |
| TWI698273B (en) | Quench column operation and bottom processing | |
| CN106278844B (en) | Device and method for reducing raw material consumption in propylene carbonylation process | |
| CN102963944B (en) | Stripping tower for CO conversion condensate | |
| CN212025224U (en) | Fine separation device for olefin catalytic cracking products | |
| CN106102894B (en) | High-pressure reactor and method for production of melamine | |
| CN204973834U (en) | Device of high concentration acetylene hydrogenation system ethylene | |
| CN211159192U (en) | Processing apparatus of acid water is retrieved to claus sulphur | |
| CN105164094B (en) | There is the aldehyde production technology of multi-stage condensing | |
| CN206121310U (en) | Styrene technology condensate stripper gas separation purifier | |
| CN103159363B (en) | Gasification waste liquid treatment method and system | |
| CN104773781A (en) | Energy-saving stripping deamination process | |
| CN205368203U (en) | Improve concentrated system of third of ten heavenly stems millet dipeptide yield | |
| CN204147575U (en) | Adiponitrile half nitrile evaporimeter | |
| CN105396310B (en) | One kind is used for chlorination, photochemical chemical industry liquid material dewatering process and device | |
| CN208356735U (en) | A kind of reactor cooling system producing TW component | |
| CN205182686U (en) | Methyl alcohol system petrol reaction unit |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CB03 | Change of inventor or designer information |
Inventor after: Li Dawei Inventor after: Liu Qingjuan Inventor after: Song Shunli Inventor after: Zhao Liyan Inventor after: Xiao Shufan Inventor after: Geng Jinwei Inventor after: Zhou Qingjiao Inventor after: Zhao Hui Inventor before: Li Dawei Inventor before: Lang Lang Inventor before: Zhou Qingjiao Inventor before: Zhao Hui Inventor before: Liu Qingjuan Inventor before: Yang Jun Inventor before: Song Shunli Inventor before: Huo Guangwen Inventor before: Zhao Liyan Inventor before: Xiao Shufan Inventor before: Wang Zuocheng Inventor before: Geng Jinwei |
|
| CB03 | Change of inventor or designer information | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20190924 Address after: 132002 3-6 and 9-13 floors of Block A, Jihua Economic and Trade Center, Tongtan Road, Changyi District, Jilin Province Patentee after: PetroChina Jilin Chemical Engineering Co., Ltd. Address before: 132021, Jilin, Jilin Province tung Chi Road East Economic and Trade Building Patentee before: Jilin Design Institute of Northeast Refining & Chemical Engineering Co., Ltd., CNPC |
|
| TR01 | Transfer of patent right |