CN203625267U - Ammoximation reaction device - Google Patents
Ammoximation reaction device Download PDFInfo
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- CN203625267U CN203625267U CN201320793553.8U CN201320793553U CN203625267U CN 203625267 U CN203625267 U CN 203625267U CN 201320793553 U CN201320793553 U CN 201320793553U CN 203625267 U CN203625267 U CN 203625267U
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- filtration unit
- tubular reactor
- reaction device
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 73
- 238000001914 filtration Methods 0.000 claims abstract description 88
- 239000000463 material Substances 0.000 claims abstract description 33
- 238000002156 mixing Methods 0.000 claims description 42
- 239000002994 raw material Substances 0.000 claims description 13
- 239000012530 fluid Substances 0.000 claims description 6
- 238000012546 transfer Methods 0.000 claims description 6
- 230000003014 reinforcing effect Effects 0.000 claims description 5
- 230000003068 static effect Effects 0.000 claims description 5
- 239000007788 liquid Substances 0.000 abstract description 15
- 238000004519 manufacturing process Methods 0.000 abstract description 10
- 239000012295 chemical reaction liquid Substances 0.000 abstract 2
- 230000014759 maintenance of location Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 11
- 238000011010 flushing procedure Methods 0.000 description 9
- 239000007795 chemical reaction product Substances 0.000 description 6
- VEZUQRBDRNJBJY-UHFFFAOYSA-N cyclohexanone oxime Chemical compound ON=C1CCCCC1 VEZUQRBDRNJBJY-UHFFFAOYSA-N 0.000 description 6
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 5
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 description 5
- JBKVHLHDHHXQEQ-UHFFFAOYSA-N epsilon-caprolactam Chemical compound O=C1CCCCCN1 JBKVHLHDHHXQEQ-UHFFFAOYSA-N 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000009826 distribution Methods 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 239000007792 gaseous phase Substances 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000006237 Beckmann rearrangement reaction Methods 0.000 description 1
- 229920002292 Nylon 6 Polymers 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000003670 easy-to-clean Effects 0.000 description 1
- 229920006351 engineering plastic Polymers 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000003780 insertion Methods 0.000 description 1
- 230000037431 insertion Effects 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000006146 oximation reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
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Abstract
The utility model discloses an ammoximation reaction device, which is characterized by comprising a tubular reactor (1) and a filtering device (2), wherein a reaction liquid outlet (11) of the tubular reactor (1) is communicated with a feed inlet (21) of the filtering device (2), and a concentrated liquid outlet (22) of the filtering device (2) is communicated with a reaction liquid inlet (12) of the tubular reactor (1). The ammoximation reaction device not only can shorten the retention time of materials in the reactor, so that the production efficiency is improved, and materials are uneasily blocked.
Description
Technical field
The utility model relates to a kind of Ammoximation reaction device.
Background technology
Cyclohexanone-oxime is the key intermediate of synthesis of caprolactam, prepares hexanolactam after Beckmann rearrangement, is the important source material of preparing fiber and nylon 6 and engineering plastics.At present, cyclohexanone-oxime mainly utilizes cyclohexanone oxamidinating to react to prepare, and its reaction process is as follows:
Cyclohexanone oxamidinating legal system is proposed by Italian ENI company the earliest for cyclohexanone-oxime.So far successively built up tens of cover full scale plants in Japan and China, only gone into operation at home or just reach tens at the production equipment of building, overall throughput approaches 1,000,000 tons.From the full scale plant running condition of building up both at home and abroad at present, all there are some problems, as existing catalyzer filtration unit is arranged in reactor mostly, be built-in filtration unit.After oximation reaction completes, directly reaction product is separated in reactor with solid catalyst.But built-in filtration unit easily stops up, therefore need to stop production and clean and keep in repair completely, not only treatment cycle is longer, and numerous and diverse and dangerous.In addition; the described reactor that comprises built-in filtration unit is generally tank reactor; except filtration unit; in described reactor, be conventionally also provided with stirring rake, feed distribution device and baffle etc.; structure is very complicated; so not only increase facility investment, also made production process complicated.In addition, the volume of the tank reactor that uses is conventionally larger, and during so not only making to drive, material heats up slower, waste a large amount of thermals source, but also make reaction time longer, and increase the probability that side reaction occurs, reduce production efficiency and increased raw-material consumption.
Therefore, Ammoximation reaction device being improved, is in caprolactam production process, to enhance productivity, simplify the aspect urgent problem such as production process, reduction facility investment.
Utility model content
The purpose of this utility model is the above-mentioned defect in order to overcome existing Ammoximation reaction device, and a kind of new Ammoximation reaction device is provided.
The Ammoximation reaction device that the utility model provides comprises tubular reactor and filtration unit, the reaction solution outlet of described tubular reactor is communicated with the opening for feed of described filtration unit, and the concentrated solution outlet of described filtration unit is communicated with the reaction solution entrance of described tubular reactor.
Contriver of the present utility model finds, Ammoximation reaction reacts for moment in fact, and this reaction can reach more than 99.9% at the transformation efficiency in 3-5 second.And the reactor of the Ammoximation reaction device of prior art is generally tank reactor, volume is conventionally larger, and annex is more, so not only can greatly increase facility investment expense, also can make the residence time of material in reactor longer.Because Ammoximation reaction is essentially moment reaction, the long residence time not only can not obviously be improved transformation efficiency, but also can increase the probability that side reaction occurs, and reduces production efficiency.In addition, existing filtration unit is directly placed in reactor conventionally, and reaction in described reactor is normally carried out under the condition stirring, thereby has increased the probability that oximate catalyzer contacts with filtration unit, makes filtration unit be easy to obstruction.In addition, it is very inconvenient that described filtration unit is cleaned, and needs to stop completely, thereby caused the waste of resource and increased production cost.
And the Ammoximation reaction device that the utility model provides is by adopting tubular reactor filtration unit to be set to external placed type, volume of equipment is little, simple structure, not only can save so a large sum of facility investment expense, but also can shorten the residence time of material in reactor, enhance productivity, and reduce the probability of feed blocking.Infer its reason, may be volume due to: tubular reactor direction of motion less and material is more consistent conventionally, thereby can Reaction time shorten, enhance productivity; And the reaction product that contains oximate catalyzer is introduced while carrying out the separating of reaction product and oximate catalyzer in the filtration unit of external placed type, to carry out under the state not stirring, described oximate catalyzer is owing to having the bottom that is easy to be deposited in filtration unit compared with large density, therefore, can reduce the probability contacting with filtration unit, thereby make filtration unit be difficult for stopping up.In addition,, because filtration unit of the present utility model is external placed type and is preferably multiple common uses, be very easy to clean.
Preferably, the length-to-diameter ratio of described tubular reactor is 10-160:1.
Preferably, in described tubular reactor, be provided with reinforcing mass transfer structure.Now, can make the material on same cross section in tubular reactor realize more evenly mixing, thus further Reaction time shorten.
Preferably, in described filtration unit, be provided with film pipe strainer.
Preferably, the quantity of described filtration unit is 2-12; The quantity of the film pipe strainer arranging in each described filtration unit is 100-400 root independently of one another.Now, can also realize in the situation that not stopping filtration unit is cleaned in turn, thereby reduce the loss of stopping.
Preferably, along fluid flow direction, on the pipeline that is communicated with the concentrated solution outlet of described filtration unit and the reaction solution entrance of described tubular reactor, be provided with interchanger, the first mixing tank and the second mixing tank.
Preferably, raw material source is communicated with the pipeline between described interchanger and described the first mixing tank by tubular stinger.
Preferably, described interchanger is shell and tube heat exchanger; Described the first mixing tank and described the second mixing tank are identical or different, and are tubular static mixer independently of one another.
Preferably, described Ammoximation reaction device also comprises discharge tank, the material inlet of described discharge tube is optionally communicated with the concentrated solution outlet of described filtration unit by valve, the material outlet of described discharge tank pass through valve optionally with the concentrated solution outlet of described filtration unit and the reaction solution entrance of described tubular reactor between pipeline be communicated with.
Other feature and advantage of the present utility model are described in detail the embodiment part subsequently.
Accompanying drawing explanation
Accompanying drawing is to be used to provide further understanding of the present utility model, and forms a part for specification sheets, is used from explanation the utility model, but does not form restriction of the present utility model with embodiment one below.In the accompanying drawings:
Fig. 1 is the structural representation of a kind of embodiment of described Ammoximation reaction device;
Fig. 2 is the structural representation of the junction of the pipeline between tubular stinger and described interchanger and described the first mixing tank.
Description of reference numerals
1-tubular reactor; The outlet of 11-reaction solution; 12-reaction solution entrance; 13-gaseous phase outlet; 2-filtration unit; 21-opening for feed; 22-concentrated solution outlet; 23-purified liquor outlet; 24-back flushing entrance; 25-pneumatic outlet; 26-film pipe strainer; 3-interchanger; 31-circulatory mediator entrance; The outlet of 32-circulatory mediator; 4-the first mixing tank; 5-the second mixing tank; 6-tubular stinger; 7-discharge tank; 71-material inlet; 72-material outlet; The outlet of 73-tail gas.
Embodiment
Below embodiment of the present utility model is elaborated.Should be understood that, embodiment described herein only, for description and interpretation the utility model, is not limited to the utility model.
In the utility model, in the situation that not doing contrary explanation, the noun of locality of use as " upper and lower, left and right, the end, top " typically refer to as described in direction in Ammoximation reaction device busy situation, the namely direction shown in accompanying drawing.
As shown in Figure 1, described Ammoximation reaction device comprises tubular reactor 1 and filtration unit 2, the reaction solution outlet 11 of described tubular reactor 1 is communicated with the opening for feed 21 of described filtration unit 2, and the concentrated solution outlet 22 of described filtration unit 2 is communicated with the reaction solution entrance 12 of described tubular reactor 1.
Described tubular reactor 1 can be for existing in a tubular form various and have the reactor of larger length-to-diameter ratio, and for example, the length-to-diameter ratio of described tubular reactor 1 can be 10-160:1.Particularly, for normally used Ammoximation reaction device, the diameter of described tubular reactor 1 can be 200-800mm, and length can be 5-20m.
Preferably, in described tubular reactor 1, be provided with reinforcing mass transfer structure, can make like this material on the interior same cross section of tubular reactor 1 realize mixing more equably, thereby further shorten the time of Ammoximation reaction.Wherein, described reinforcing mass transfer structure can be the existing various structures that can realize mixing of materials, for example, can be static mixer.The concrete quantity of described reinforcing mass transfer structure and set-up mode can carry out choose reasonable as the case may be, and therefore not to repeat here.
Preferably, in described filtration unit 2, be provided with film pipe strainer 26.According to a kind of embodiment, described filtration unit 2 can be upper and lower two parts by baffle for separating, these two portions only end of logical filmed passing tube strainer 26 are communicated with, wherein, described film pipe strainer 26 is arranged on bottom, the opening for feed 21 of described filtration unit 2 is arranged on the sidewall of bottom, the reaction solution outlet that is described reactor 1 is communicated with the bottom of filtration unit 2, the top of described dividing plate and filtration unit 2 forms clear liquid collecting zone, and the sidewall of described clear liquid collecting zone or top are provided with purified liquor outlet 23.
As a rule, described film pipe strainer 26 is enclosed construction, its membrane structure allow liquid material by and do not allow solid state material to pass through.The reaction product that contains oximate catalyzer is exported to 11 by reaction solution to be introduced and is built-in with in the filtration unit 2 of film pipe strainer 26 continuously, liquid resultant can penetrate in film pipe strainer 26 easily, and enter the clear liquid collecting region that is positioned at filtration unit 2 tops, and then draw continuously by purified liquor outlet 23, and duplicate removal row operation is for further processing; The oximate catalyzer of solid state is blocked in outside described film pipe strainer 26 and is circulated back in tubular reactor 1 by the concentrated solution outlet 22 that is arranged on described filtration unit 2 bottoms, to realize the recycle of oximate catalyzer.
The kind of described film pipe strainer 26 can be that the routine of this area is selected, and for example, can be metal film pipe strainer and/or ceramic-film tube strainer.Wherein, the particle diameter of the oximate catalyzer that the bore dia of above-mentioned film pipe strainer can use according to reality is reasonably selected, and for example, the bore dia of described metal film pipe strainer can be 0.1 μ m-10 μ m, is preferably 0.3 μ m-3 μ m.The bore dia of described ceramic-film tube strainer can be 10nm-10 μ m, is preferably 50nm-5 μ m.In addition, the quantity of the described film pipe strainer 26 arranging in each filtration unit 2 also can reasonably be selected according to practical situation, is preferably 100-400 root, can improve like this filtration efficiency.Between multiple film pipe strainers 26, can be communicated with, also can not be communicated with.
Preferably, described filtration unit 2 also comprises flushing line, the back flushing entrance 24 of described flushing line can be arranged on sidewall or the top of described clear liquid collecting zone, also can be arranged on the pipeline that described purified liquor outlet 23 is communicated with the follow-up device that clear liquid is further processed, can realize so described film pipe strainer 26 is carried out to on-line cleaning.In a kind of embodiment, as mentioned above, described filtration unit 2 is upper and lower two parts by baffle for separating, these two portions only end of logical filmed passing tube strainer 26 are communicated with, the opening for feed 21 of described filtration unit 2 is arranged on the sidewall of bottom, the top of described dividing plate and filtration unit 2 forms clear liquid collecting zone, now, described back flushing entrance 24 can be arranged on sidewall or the top of described clear liquid collecting zone, is preferably arranged on the pipeline that described purified liquor outlet 23 is communicated with the follow-up device that clear liquid is further processed.
Preferably, described filtration unit 2 also comprises the pneumatic outlet 25 that is arranged on its top, can be conducive to so the smooth discharge of gas in reaction solution (as unreacted ammonia).
Preferably, the quantity of described filtration unit 2 is 2-12.It should be noted that, 2-12 filtration unit 2 is communicated with described tubular reactor 1 respectively.Can realize like this in the situation that not stopping described filtration unit 2 is cleaned in turn, thereby reduce the loss of stopping.
As a rule; along fluid flow direction; on the pipeline that is communicated with the concentrated solution outlet 22 of described filtration unit 2 and the reaction solution entrance 12 of described tubular reactor 1, be conventionally also provided with interchanger 3, the first mixing tank 4 and the second mixing tank 5, can control better like this temperature of charge and more be conducive to even mixing the between reaction raw materials and between reaction raw materials and catalyzer.
Raw material source can directly be communicated with tubular reactor 1, also can with the concentrated solution outlet of described filtration unit 2 22 and the reaction solution entrance 12 of described tubular reactor 1 between the optional position of pipeline be communicated with, preferably, raw material source is communicated with the pipeline between described interchanger 3 and described the first mixing tank 4 by tubular stinger 6, adopt raw material that this preferred mode of communicating can make to introduce to be first introduced in the first mixing tank 3 and the second mixing tank 4 and with mix from the concentrated catalyst solution of concentrated solution outlet 22, can significantly shorten like this residence time of material in tubular reactor 1, enhance productivity.
In addition, as shown in Figure 2, take the diameter D of pipeline between described interchanger 3 and described the first mixing tank 4 as benchmark, the radial depth that described tubular stinger 6 inserts in described pipeline can be D/3-2D/3 conventionally, and insertion end is provided with distribution hole, the opening of this distribution hole is toward the contrary direction of fluid flow direction in described pipeline.The quantity of described distribution hole device can be 80-150, and diameter can be Ф 3-Ф 5.In Fig. 2, in described pipeline, the direction of arrow is the mobile direction of fluid.
Main improvements of the present utility model are mainly existing tank reactor tubular reactor to substitute, and filtration unit is set to external placed type, to save residence time in reactor of facility investment, Optimization Technology, shortening material, enhance productivity and to reduce the obstruction of film pipe.And the concrete structure of described interchanger 3, the first mixing tank 4 and the second mixing tank 5 all can be same as the prior art.
For example, described interchanger 3 can be shell and tube heat exchanger.Wherein, described interchanger 3 is generally to realize the control to temperature of charge by material and heat transferring medium are carried out to heat exchange, and therefore, correspondingly, described interchanger 3 generally includes circulatory mediator entrance 31 and circulatory mediator outlet 32.Described the first mixing tank 4 and described the second mixing tank 5, also can be different in structure and in form can be identical, specifically can existing various mixing tank, and as tubular static mixer.Wherein, the caliber of described tubular static mixer can be 450-800mm, and length can be 2000-4000mm.
Preferably, described Ammoximation reaction device also comprises discharge tank 7, the material inlet 71 of described discharge tank 7 is optionally communicated with the concentrated solution outlet 22 of described filtration unit 2 by valve, the material outlet of described discharge tank 7 72 by valve optionally with the concentrated solution outlet 22 of described filtration unit 2 and the reaction solution entrance 12 of described tubular reactor 1 between pipeline be communicated with.Preferably, described discharge tank 7 also comprises the tail gas outlet 73 that is arranged on its top.In the time stopping, the material in described tubular reactor 1, filtration unit 2, interchanger 3, the first mixing tank 4, the second mixing tank 5 and pipeline can be discharged in described discharge tank 7; While restarting Ammoximation reaction device, the Matter Transfer in described discharge tank 7 can be sent again back to then reaction in tubular reactor 1.It should be noted that, due in need to be optionally in actual production process the heavy phase containing catalyzer in filtration unit 2 being back to tubular reactor 1 or be discharged in discharge tank 7, therefore, as shown in Figure 1, on the pipeline being communicated with between the concentrated solution outlet 22 of described filtration unit 2 and the reaction solution entrance 12 of described tubular reactor 1, be communicated with on the pipeline of the concentrated solution outlet 22 of described filtration unit 2 and the material inlet 71 of discharge tank 7 and be communicated with the material outlet 72 of described discharge tank 7 and all need to arrange valve on the pipeline between described concentrated solution outlet 22 and reaction solution entrance 12, concrete set-up mode can carry out choose reasonable according to practical situation, therefore not to repeat here.
According to a kind of embodiment, as shown in Figure 1, described Ammoximation reaction device comprises tubular reactor 1 and filtration unit 2, described tubular reactor 1 comprises that the reaction solution being arranged on its sidewall exports 11, is arranged on the reaction solution entrance 12 of its bottom and is arranged on the gaseous phase outlet 13 at its top, described filtration unit 2 comprises opening for feed 21, concentrated solution outlet 22, purified liquor outlet 23, back flushing entrance 24, pneumatic outlet 25 and film pipe strainer 26, described filtration unit 2 is upper by baffle for separating, lower two parts, these two portions only end of logical filmed passing tube strainer 26 are communicated with, described film pipe strainer 26 is arranged on bottom, the top of described dividing plate and filtration unit 2 forms clear liquid collecting zone, described opening for feed 21 is arranged on the lower sides of filtration unit 2, described concentrated solution outlet 22 is arranged on the bottom of filtration unit 2, described purified liquor outlet 23 is arranged on sidewall or the top of clear liquid collecting zone, described pneumatic outlet 25 is arranged on the top of filtration unit 2, described back flushing entrance 24 is arranged on the pipeline that described purified liquor outlet 23 is communicated with the follow-up device that clear liquid is further processed, the reaction solution outlet 11 of described tubular reactor 1 is communicated with the opening for feed 21 of described filtration unit 2, and the concentrated solution outlet 22 of described filtration unit 2 is communicated with the reaction solution entrance 12 of described tubular reactor 1, being communicated with on the concentrated solution outlet 22 of described filtration unit 2 and the pipeline of the reaction solution entrance 12 of described tubular reactor 1, be disposed with recycle pump, interchanger 3, the first mixing tank 4 and the second mixing tank 5 along the mobile direction of fluid, raw material source is communicated with the pipeline between described interchanger 3 and described the first mixing tank 4 by tubular stinger 6, described Ammoximation reaction device also comprises discharge tank 7, the material inlet 71 of described discharge tank 7 is optionally communicated with the concentrated solution outlet 22 of described filtration unit 2 by valve, the material outlet 72 of described discharge tank 7 by valve optionally with concentrated solution outlet 22 and the recycle pump of described filtration unit 2 between pipeline be communicated with, in addition, described discharge tank 7 also comprises the tail gas outlet 73 that is arranged on its top.
In the process that above-mentioned Ammoximation reaction device is produced for amidoximeization, raw material as pimelinketone, ammonia, hydrogen peroxide or aqueous hydrogen peroxide solution (being hydrogen peroxide) and oximate catalyzer by tubular stinger 7 introduce as described in interchanger 3 and as described on pipeline between the first mixing tank 4, then flow into successively the first mixing tank 4 and the second mixing tank 5 and flow into tubular reactor 1 and carry out Ammoximation reaction from being arranged in the reaction raw materials entrance 12 of tubular reactor 1 bottom after mixing, after Ammoximation reaction completes, gas phase is from being positioned at the gaseous phase outlet 13 at the tubular reactor 1 top Flash Gas Compression Skid System that truncates, reaction product exports 11 by reaction solution and enters filtration unit 2, the gas being mingled with in reaction product is by being positioned at the pneumatic outlet 25 at the filtration unit 2 tops Flash Gas Compression Skid System that truncates, reaction solution logical filmed passing tube strainer 26 filters, and the clear liquid obtaining is drawn and carried out follow-up clear liquid processing from purified liquor outlet 23, the heavy phase that contains catalyzer is deposited on the bottom of filtration unit 2, and introduce interchanger 3 by concentrated solution outlet 22, then after mixing through the first mixing tank 3 and the second mixing tank 4 successively together with the raw material of the heavy phase that contains catalyzer after heat exchange and new introducing, enter in tubular reactor 1.When parking, open the valve being communicated with between described filtration unit 2 concentrated solution outlets 22 and the material inlet 71 of discharge tank 7, material on described tubular reactor 1, filtration unit 2, interchanger 3, the first mixing tank 4, the second mixing tank 5 and pipeline is discharged in described discharge tank 7, and the tail gas in material exports 73 Flash Gas Compression Skid Systems that truncate by tail gas.After residual material in described filtration unit 2 is discharged in described discharge tank 7, flushing medium can also be introduced in filtration unit 2 so that film pipe strainer is cleaned by back flushing entrance 24.While restarting described Ammoximation reaction device, open again the valve that is communicated with the pipeline between the material outlet 22 of described discharge tank 7 and concentrated solution outlet and the recycle pump of filtration unit 2, the material in described discharge tank 7 is returned to tubular reactor 1 and continues to react with the new raw material of introducing.
More than describe preferred implementation of the present utility model in detail; but; the utility model is not limited to the detail in above-mentioned embodiment; within the scope of technical conceive of the present utility model; can carry out multiple simple variant to the technical solution of the utility model, these simple variant all belong to protection domain of the present utility model.
It should be noted that in addition each the concrete technical characterictic described in above-mentioned embodiment, in reconcilable situation, can combine by any suitable mode.For fear of unnecessary repetition, the utility model is to the explanation no longer separately of various possible array modes.
In addition, also can carry out arbitrary combination between various embodiment of the present utility model, as long as it is without prejudice to thought of the present utility model, it should be considered as content disclosed in the utility model equally.
Claims (9)
1. an Ammoximation reaction device, it is characterized in that, described Ammoximation reaction device comprises tubular reactor (1) and filtration unit (2), the reaction solution outlet (11) of described tubular reactor (1) is communicated with the opening for feed (21) of described filtration unit (2), and the concentrated solution outlet (22) of described filtration unit (2) is communicated with the reaction solution entrance (12) of described tubular reactor (1).
2. Ammoximation reaction device according to claim 1, is characterized in that, the length-to-diameter ratio of described tubular reactor (1) is 10-160:1.
3. Ammoximation reaction device according to claim 1 and 2, is characterized in that, described tubular reactor is provided with reinforcing mass transfer structure in (1).
4. Ammoximation reaction device according to claim 1 and 2, is characterized in that, is provided with film pipe strainer (26) in described filtration unit (2).
5. Ammoximation reaction device according to claim 4, is characterized in that, the quantity of described filtration unit (2) is 2-12; The quantity of the film pipe strainer (26) arranging in each described filtration unit (2) is 100-400 root independently of one another.
6. Ammoximation reaction device according to claim 1 and 2, it is characterized in that, along fluid flow direction, on the pipeline that is communicated with the concentrated solution outlet (22) of described filtration unit (2) and the reaction solution entrance (12) of described tubular reactor (1), be provided with interchanger (3), the first mixing tank (4) and the second mixing tank (5).
7. Ammoximation reaction device according to claim 6, is characterized in that, raw material source is communicated with the pipeline between described interchanger (3) and described the first mixing tank (4) by tubular stinger (6).
8. Ammoximation reaction device according to claim 7, is characterized in that, described interchanger (3) is shell and tube heat exchanger; Described the first mixing tank (4) and described the second mixing tank (5) are identical or different, and are tubular static mixer independently of one another.
9. Ammoximation reaction device according to claim 1 and 2, it is characterized in that, described Ammoximation reaction device also comprises discharge tank (7), the material inlet (71) of described discharge tank (7) is optionally communicated with the concentrated solution outlet (22) of described filtration unit (2) by valve, the material outlet (72) of described discharge tank (7) pass through valve optionally with the concentrated solution outlet (22) of described filtration unit (2) and the reaction solution entrance (12) of described tubular reactor (1) between pipeline be communicated with.
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| CN201320793553.8U CN203625267U (en) | 2013-12-04 | 2013-12-04 | Ammoximation reaction device |
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| CN201320793553.8U CN203625267U (en) | 2013-12-04 | 2013-12-04 | Ammoximation reaction device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106278922A (en) * | 2016-08-15 | 2017-01-04 | 广州天赐高新材料股份有限公司 | A kind of preparation method of fatty acid amide propyl tertiary amine |
| CN114478386A (en) * | 2022-02-24 | 2022-05-13 | 江苏扬农化工集团有限公司 | Method for preparing caprolactam by gas phase method |
-
2013
- 2013-12-04 CN CN201320793553.8U patent/CN203625267U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106278922A (en) * | 2016-08-15 | 2017-01-04 | 广州天赐高新材料股份有限公司 | A kind of preparation method of fatty acid amide propyl tertiary amine |
| CN106278922B (en) * | 2016-08-15 | 2019-01-18 | 广州天赐高新材料股份有限公司 | A kind of preparation method of fatty acid amide propyl tertiary amine |
| CN114478386A (en) * | 2022-02-24 | 2022-05-13 | 江苏扬农化工集团有限公司 | Method for preparing caprolactam by gas phase method |
| CN114478386B (en) * | 2022-02-24 | 2024-02-09 | 江苏扬农化工集团有限公司 | Process for preparing caprolactam by gas phase method |
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