CN204151265U - Hexanediamine production system - Google Patents
Hexanediamine production system Download PDFInfo
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- CN204151265U CN204151265U CN201420482460.8U CN201420482460U CN204151265U CN 204151265 U CN204151265 U CN 204151265U CN 201420482460 U CN201420482460 U CN 201420482460U CN 204151265 U CN204151265 U CN 204151265U
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- Prior art keywords
- hexanediamine
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- import
- topping
- exporting
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- SYECJBOWSGTPLU-UHFFFAOYSA-N hexane-1,1-diamine Chemical compound CCCCCC(N)N SYECJBOWSGTPLU-UHFFFAOYSA-N 0.000 title claims abstract description 190
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 19
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 65
- 239000000203 mixture Substances 0.000 claims abstract description 59
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 48
- 239000001257 hydrogen Substances 0.000 claims abstract description 35
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 35
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000003054 catalyst Substances 0.000 claims abstract description 26
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 22
- 238000005235 decoking Methods 0.000 claims abstract description 20
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 18
- 230000018044 dehydration Effects 0.000 claims abstract description 17
- 238000002360 preparation method Methods 0.000 claims abstract description 17
- 238000002156 mixing Methods 0.000 claims abstract description 14
- 238000007670 refining Methods 0.000 claims abstract description 12
- BTGRAWJCKBQKAO-UHFFFAOYSA-N adiponitrile Chemical compound N#CCCCCC#N BTGRAWJCKBQKAO-UHFFFAOYSA-N 0.000 claims abstract description 11
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims abstract description 9
- 229910000564 Raney nickel Inorganic materials 0.000 claims abstract description 4
- 230000008676 import Effects 0.000 claims description 63
- 239000011269 tar Substances 0.000 claims description 37
- 238000000034 method Methods 0.000 claims description 21
- 239000000706 filtrate Substances 0.000 claims description 18
- 230000008569 process Effects 0.000 claims description 17
- 239000000463 material Substances 0.000 claims description 13
- 230000003213 activating effect Effects 0.000 claims description 12
- 239000000470 constituent Substances 0.000 claims description 10
- 230000003197 catalytic effect Effects 0.000 claims description 9
- 239000003795 chemical substances by application Substances 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 9
- 239000006227 byproduct Substances 0.000 claims description 8
- 239000011259 mixed solution Substances 0.000 claims description 8
- 239000007864 aqueous solution Substances 0.000 claims description 7
- 230000009849 deactivation Effects 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 239000002699 waste material Substances 0.000 claims description 5
- 238000005516 engineering process Methods 0.000 claims description 4
- 150000002431 hydrogen Chemical class 0.000 claims description 4
- 239000000243 solution Substances 0.000 claims description 4
- 239000002351 wastewater Substances 0.000 claims description 4
- 150000004985 diamines Chemical class 0.000 claims description 3
- KAJXSPOVKKAIJC-UHFFFAOYSA-M sodium ethene hydroxide Chemical group [OH-].C=C.[Na+] KAJXSPOVKKAIJC-UHFFFAOYSA-M 0.000 claims description 3
- 150000001412 amines Chemical class 0.000 claims description 2
- 238000005304 joining Methods 0.000 claims description 2
- 238000002161 passivation Methods 0.000 claims description 2
- 239000010802 sludge Substances 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 12
- 230000000694 effects Effects 0.000 abstract description 3
- 239000013589 supplement Substances 0.000 abstract description 2
- 230000009466 transformation Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 abstract 1
- 239000007788 liquid Substances 0.000 abstract 1
- 235000011121 sodium hydroxide Nutrition 0.000 abstract 1
- 239000007787 solid Substances 0.000 abstract 1
- 238000001914 filtration Methods 0.000 description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- JBKVHLHDHHXQEQ-UHFFFAOYSA-N epsilon-caprolactam Chemical compound O=C1CCCCCN1 JBKVHLHDHHXQEQ-UHFFFAOYSA-N 0.000 description 4
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 3
- FHKPTEOFUHYQFY-UHFFFAOYSA-N 2-aminohexanenitrile Chemical compound CCCCC(N)C#N FHKPTEOFUHYQFY-UHFFFAOYSA-N 0.000 description 2
- SVTBMSDMJJWYQN-UHFFFAOYSA-N 2-methylpentane-2,4-diol Chemical compound CC(O)CC(C)(C)O SVTBMSDMJJWYQN-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- XXMIOPMDWAUFGU-UHFFFAOYSA-N hexane-1,6-diol Chemical compound OCCCCCCO XXMIOPMDWAUFGU-UHFFFAOYSA-N 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 150000003016 phosphoric acids Chemical class 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 238000004176 ammonification Methods 0.000 description 1
- 229910052788 barium Inorganic materials 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- VNNRSPGTAMTISX-UHFFFAOYSA-N chromium nickel Chemical compound [Cr].[Ni] VNNRSPGTAMTISX-UHFFFAOYSA-N 0.000 description 1
- RYTYSMSQNNBZDP-UHFFFAOYSA-N cobalt copper Chemical compound [Co].[Cu] RYTYSMSQNNBZDP-UHFFFAOYSA-N 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000010574 gas phase reaction Methods 0.000 description 1
- NAQMVNRVTILPCV-UHFFFAOYSA-N hexane-1,6-diamine Chemical compound NCCCCCCN NAQMVNRVTILPCV-UHFFFAOYSA-N 0.000 description 1
- 229940051250 hexylene glycol Drugs 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- UGKDIUIOSMUOAW-UHFFFAOYSA-N iron nickel Chemical compound [Fe].[Ni] UGKDIUIOSMUOAW-UHFFFAOYSA-N 0.000 description 1
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 229940001516 sodium nitrate Drugs 0.000 description 1
- 235000010344 sodium nitrate Nutrition 0.000 description 1
- 239000004317 sodium nitrate Substances 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a kind of hexanediamine production system, comprise thick hexanediamine preparation system and hexanediamine refining system Liang Ge workshop section, described thick hexanediamine preparation system is primarily of catalyst activity gasifying device, mixing equipment, hydrogenation reactor, strainer, dealcoholize column, hydrogen alcohol knockout tower and decanting vessel composition, and described refining system is primarily of dehydration tower, decoking tower, first-phase topping tower, second-phase topping tower, tar filter, de-tailing column, tar stripping unit and thinning tank composition.The utility model adopts Raney's nickel to be catalyzer, reaction conditions relaxes, and react under lower pressure and lesser temps, working pressure is lower, hydrogen gas leakage danger more easily prevents, make gas (hydrogen) liquid (adiponitrile, caustic soda and ethanol), solid (Raney's nickel) three-phase with fluidized forms Homogeneous phase mixing, structure of reactor is simple, reacts very fast, remove heat convenient, transformation efficiency is high, and the replacing of catalyzer or supplement can carry out continuously, be applicable to the preparation of hexanediamine.
Description
Technical field
The utility model relates to a kind of production equipment system for the preparation of hexanediamine, belongs to chemical technology field.
Background technology
The technological line that existing hexanediamine is produced mainly comprises 3 kinds:
Hexanolactam method: hexanolactam and ammonia are under phosphoric acid salt (phosphoric acid salt as manganese, aluminium, calcium, barium or zinc) catalyzer exists, and carry out gas-phase reaction and generate aminocapronitrile, temperature of reaction about 350 DEG C, yield almost reaches 100%.The aminocapronitrile generated carries out hydrogenation reaction again and generates hexanediamine.Adopt this operational path to produce, because hexanolactam is expensive, be generally used on the small scale production plant of the products such as process hexanolactam, limits throughput.
Hexylene glycol method: adopt skeletal nickel catalyst to carry out ammonification dehydration reaction, temperature of reaction 200 DEG C by 1,6-hexylene glycol, under pressure 23.0MPa, is that under catalyzer exists, 1,6-hexylene glycol and ammonia react generate 1,6-hexanediamine with skeleton nickel.This method side reaction is more.
Adiponitrile catalytic hydrogenation method: NC (CH2) 4CN+4H2-→ H2N (CH2) 6NH2 is its principal reaction formula, industrial have high-pressure process and low-pressure process two kinds, high-pressure process adopts cobalt-copper catalyst, temperature of reaction 100 ~ 135 DEG C, pressure 60 ~ 65MPa; Also iron catalyst can be adopted, temperature of reaction 100 ~ 180 DEG C, pressure 30 ~ 35Mpa, low-pressure process adopts skeleton nickel, iron-nickel or chromium-nickel catalyzator, reaction is carried out in sodium hydroxide solution, temperature of reaction about 75 DEG C, pressure 3MPa, the selectivity of hexanediamine can reach 99%, but how to select concrete operational path and processing unit, with process simplification, improve processing condition, reducing production cost, is still the technical problem needing to be further improved and solve.
Utility model content
For overcoming the above-mentioned defect of prior art, the utility model provides a kind of hexanediamine production system, and the reaction conditions required by this generation system relaxes, and can react under lower pressure and lesser temps, side reaction is few, and raw materials cost is relatively low.
The technical scheme that the utility model adopts:
A kind of hexanediamine production system, comprises thick hexanediamine preparation system, it is characterized in that described thick hexanediamine preparation system comprises:
Mixing equipment, for deactivated catalyst, adiponitrile, sodium hydroxide and the ethanol mixing that will send in proportion, forming mixed liquor, being provided with the material inlet for sending into deactivated catalyst, adiponitrile, sodium hydroxide and ethanol and the mixed liquor output channel for exporting mixed liquor;
Hydrogenation reactor, for carrying out catalytic hydrogenation reaction to the adiponitrile in described mixed liquor, generate hexanediamine, be provided with mixed liquor import, hydrogen inlet and the hexanediamine mixture output channel of hexanediamine mixture for being formed after exporting hydrogenation, described mixed liquor import connects described mixed liquor output channel;
Strainer, for filtering described hexanediamine mixture, form the rear hexanediamine mixture of filter, be provided with hexanediamine mixture import and for export filter after hexanediamine mixed solution filter after hexanediamine mixed solution output channel, described hexanediamine mixture import connects described hexanediamine mixture output channel;
Dealcoholize column, for carrying out dealcoholation treatment to described filtration hexanediamine mixed solution, form dealcoholysis hexanediamine mixture, hexanediamine mixture import and reclaim ethanol output channel for the dealcoholysis that the dealcoholysis hexanediamine mixture output channel that exports dealcoholysis hexanediamine mixture and the dealcoholysis of separating for exporting dealcoholysis process reclaim ethanol after being provided with filter, after described filter, hexanediamine mixture import connects hexanediamine output channel after described filter;
Decanting vessel, for separating of the sodium hydroxide in described dealcoholysis hexanediamine mixture, generate thick hexanediamine, be provided with the import of dealcoholysis hexanediamine mixture and for the thick hexanediamine output channel that exports thick hexanediamine and the sodium hydroxide Ethylene recov output channel for exporting the aqueous sodium hydroxide solution separated through decant, the import of described dealcoholysis hexanediamine mixture connects described dealcoholysis hexanediamine mixture output channel.
The beneficial effects of the utility model: owing to activating in advance catalyzer, improve the activity of catalyzer, are conducive to fast reaction speed, improve processing condition; Due to preposition mixing equipment, be conducive to ensureing compounding effect, improve the admixture of reaction system in subsequent hydrogenation reactor, optimize hydrogenation condition, improve hydrogenation efficiency, structure of reactor is simple, in reaction, three-phase can with better fluidized forms Homogeneous phase mixing, reaction is very fast, and remove heat conveniently, transformation efficiency is high; Because hydrogenation, filtration, dealcoholysis and decant set gradually, optimize technological process, make each operation reasonable disposition, mutually promote, be conducive to process simplification while the every processing requirements of guarantee, reduce operational condition, the replacing of catalyzer or supplement and can carry out continuously, does not need to stop producing.
Accompanying drawing explanation
Fig. 1 is the structural representation of the thick hexanediamine preparation system that the utility model relates to;
Fig. 2 is the structural representation of the hexanediamine essence preparation system that the utility model relates to.
Embodiment
See Fig. 1 and Fig. 2, the utility model provides a kind of hexanediamine production system, comprises thick hexanediamine preparation system and hexanediamine refining system Liang Ge workshop section.
See Fig. 1, described thick hexanediamine preparation system can comprise usually:
Mixing equipment 120, such as be suitable for the mixed preparing groove that various materials is mixed in proportion preparation, for deactivated catalyst, adiponitrile, sodium hydroxide and the ethanol mixing that will send in proportion, form mixed liquor, be provided with the material inlet for sending into deactivated catalyst, adiponitrile, sodium hydroxide and ethanol and the mixed liquor output channel 121 for exporting mixed liquor, usual adiponitrile can be connected adiponitrile supply line 104 and sodium hydroxide supply line 105 with sodium hydroxide respectively by respective material inlet;
Hydrogenation reactor 130, for carrying out catalytic hydrogenation reaction to the adiponitrile in described mixed liquor, generate hexanediamine, be provided with mixed liquor import, hydrogen inlet and the hexanediamine mixture output channel 131 of hexanediamine mixture for being formed after exporting hydrogenation, described mixed liquor import connects described mixed liquor output channel;
Strainer 140, for filtering described hexanediamine mixture, form the rear hexanediamine mixture of filter, be provided with hexanediamine mixture import and for export filter after hexanediamine mixed solution filter after hexanediamine mixed solution output channel 141, described hexanediamine mixture import connects described hexanediamine mixture output channel;
Dealcoholize column 150, for carrying out dealcoholation treatment to described filtration hexanediamine mixed solution, form dealcoholysis hexanediamine mixture, hexanediamine mixture import and reclaim ethanol output channel 152 for the dealcoholysis that the dealcoholysis hexanediamine mixture output channel 151 that exports dealcoholysis hexanediamine mixture and the dealcoholysis of separating for exporting dealcoholysis process reclaim ethanol after being provided with filter, after described filter, hexanediamine mixture import connects hexanediamine output channel after described filter;
Decanting vessel 160, for separating of the sodium hydroxide in described dealcoholysis hexanediamine mixture, generate thick hexanediamine, be provided with the import of dealcoholysis hexanediamine mixture and for the thick hexanediamine output channel 161 that exports thick hexanediamine and the sodium hydroxide Ethylene recov output channel 162 for exporting the aqueous sodium hydroxide solution separated through decant, the import of described dealcoholysis hexanediamine mixture connects described dealcoholysis hexanediamine mixture output channel.
Preferably, described thick hexanediamine preparation system also comprises activating apparatus 110, for carrying out activation treatment to catalyzer, form activating catalytic agent composition, be provided with Raney's nickel catalyst import 102, sodium hydroxide import 101 and the activating catalytic agent composition output channel 111 for exporting activating catalytic agent composition, described activating catalytic agent composition output channel connects on described mixing equipment for sending into the material inlet of described deactivated catalyst.
Preferably, for sending into the material inlet of deactivated catalyst and the material inlet for sending into ethanol adopts same material inlet on described mixing equipment, the ethanol supply line 103 for inputting ethanol accesses described activating catalytic agent composition output channel.
Preferably, described thick hexanediamine preparation system also comprises hydrogen alcohol knockout tower 170, the top of described hydrogenation reactor is provided with the outlet of hydrogen alcohol mixture, described hydrogen alcohol mixture outlet connects the import of described hydrogen alcohol knockout tower by hydrogen ethanol output channel 132, nol outlet after the bottom of described hydrogen alcohol knockout tower is provided with and is separated, after described separation, nol outlet accesses described hydrogenation reactor by ethanol circulating line 171, hydrogen outlet after the top of described hydrogen alcohol knockout tower is provided with and is separated, after described separation, hydrogen outlet connects the rear hydrogen output channel 172 of separation, after described separation, hydrogen output channel is divided into two-way, one tunnel is for being separated rear hydrogen discharge pipe, hydrogen reuse pipe after another road is separated, described hydrogen reuse pipe accesses the hydrogen supply pipeline 106 of described hydrogenation reactor or directly accesses described hydrogenation reactor.
Preferably, described strainer is provided with much filtrate output channel 142, described much filtrate output channel connects catalyst deactivation device 180, the bottom of described hydrogenation reactor is provided with excess catalyst discharge line 133, described excess catalyst discharge line accesses described catalyst deactivation device, and described catalyst deactivation device is provided with passivator (such as sodium sulfate or SODIUMNITRATE) output channel 107 and passivation rear catalyst discharge tube 181.
Preferably, described dealcoholysis is reclaimed ethanol output channel and is connected described ethanol supply line, and described thick hexanediamine output channel connects thick amine relay tank, and described mixed liquor output channel is provided with surge pump, and described mixing equipment adopts mixed preparing groove structure.
See Fig. 2, described hexanediamine refining system can comprise usually:
Dehydration tower 210, for dewatering to described thick hexanediamine, form dehydration hexanediamine, be provided with thick hexanediamine import and for exporting the dehydration dehydration hexanediamine output channel 211 of hexanediamine and the waste water output channel 212 for exporting waste water, described thick hexanediamine import is connected with the thick hexanediamine input channel 201 for exporting thick hexanediamine to it usually;
Decoking tower 220, for carrying out decoking process to described dehydration hexanediamine, generate decoking hexanediamine, be provided with dehydration hexanediamine import and for the decoking hexanediamine output channel 221 that exports decoking hexanediamine and the blended tars output channel 222 for exporting the blended tars that decoking produces, the import of described dehydration hexanediamine connects described dehydration hexanediamine output channel;
First-phase topping tower 230, for pulling out the topping byproducts such as diamines basic ring in described decoking hexanediamine, hexanediamine after formation topping, be provided with the import of decoking hexanediamine and for hexanediamine output channel 231 and the topping byproduct output channel 232 for exporting topping byproduct after the topping of hexanediamine after exporting topping, the import of described decoking hexanediamine connects described decoking hexanediamine output channel;
De-tailing column 240, for removing light, the heavy constituent after described topping in hexanediamine, form pure hexanediamine, after being provided with topping hexanediamine import and for export pure hexanediamine pure hexanediamine output channel 241, for exporting the de-tail light constituent output channel 243 of de-tail light constituent and the de-cabrage component output channel 242 for exporting de-cabrage component, after described topping, hexanediamine import connects hexanediamine output channel after described topping;
Thinning tank 250, for carrying out water-soluble dilution to described pure hexanediamine, form the certain density hexanediamine aqueous solution, be provided with pure hexanediamine import, process water import and the one or more hexanediamine aqueous solution output channels 251,252 (such as inputting the 85% pure hexanediamine aqueous solution and the 99.9% pure hexanediamine aqueous solution) for exporting the certain density hexanediamine aqueous solution, described pure hexanediamine import connects described pure hexanediamine output channel, described process water import Joining Technology water supply line 202.
Preferably, described hexanediamine refining system also comprises second-phase topping tower 260, for carrying out the process of secondary topping to described topping byproduct, form secondary topping hexanediamine and secondary topping light constituent, be provided with the import of topping byproduct and for the secondary topping hexanediamine output channel 261 that exports secondary topping hexanediamine and the secondary topping light constituent output channel 262 for exporting secondary topping light constituent, described secondary topping hexanediamine output channel accesses described dehydration hexanediamine output channel or the direct described decoking tower of access.
Preferably, described hexanediamine refining system also comprises tar filter 270, for carrying out filtering separation to described blended tars, forming blended tars filtrate and blended tars waste residue, being provided with blended tars import and for the blended tars filtrate output tube road 271 that exports blended tars filtrate and the blended tars waste sludge discharge mouth 272 for exporting blended tars waste residue.
Preferably, described hexanediamine refining system also comprises tar stripping unit 280, for carrying out stripping to described blended tars filtrate, form tar after stripping hexanediamine and stripping, be provided with the import of blended tars filtrate and for the stripping hexanediamine output channel 281 that exports stripping hexanediamine and for export tar after stripping stripping after tar emission mouth 282, the import of described blended tars filtrate connects described blended tars filtrate output tube road, described de-cabrage component output channel accesses described blended tars filtrate output tube road or directly accesses described tar stripping unit, described thick hexanediamine import connects described diamines relay tank.
Claims (10)
1. a hexanediamine production system, comprises thick hexanediamine preparation system, it is characterized in that described thick hexanediamine preparation system comprises:
Mixing equipment, is provided with the material inlet for sending into deactivated catalyst, adiponitrile, sodium hydroxide and ethanol and the mixed liquor output channel for exporting mixed liquor;
Hydrogenation reactor, be provided with mixed liquor import, hydrogen inlet and the hexanediamine mixture output channel of hexanediamine mixture for being formed after exporting hydrogenation, described mixed liquor import connects described mixed liquor output channel;
Strainer, be provided with hexanediamine mixture import and for export filter after hexanediamine mixed solution filter after hexanediamine mixed solution output channel, described hexanediamine mixture import connects described hexanediamine mixture output channel;
Dealcoholize column, hexanediamine mixture import and reclaim ethanol output channel for the dealcoholysis that the dealcoholysis hexanediamine mixture output channel that exports dealcoholysis hexanediamine mixture and the dealcoholysis of separating for exporting dealcoholysis process reclaim ethanol after being provided with filter, after described filter, hexanediamine mixture import connects hexanediamine output channel after described filter;
Decanting vessel, be provided with the import of dealcoholysis hexanediamine mixture and for the thick hexanediamine output channel that exports thick hexanediamine and the sodium hydroxide Ethylene recov output channel for exporting the aqueous sodium hydroxide solution separated through decant, the import of described dealcoholysis hexanediamine mixture connects described dealcoholysis hexanediamine mixture output channel.
2. hexanediamine production system as claimed in claim 1, it is characterized in that described thick hexanediamine preparation system also comprises activating apparatus, be provided with Raney's nickel catalyst import, sodium hydroxide import and the activating catalytic agent composition output channel for exporting activating catalytic agent composition, described activating catalytic agent composition output channel connects on described mixing equipment for sending into the material inlet of described deactivated catalyst.
3. hexanediamine production system as claimed in claim 2, it is characterized in that the ethanol supply line for inputting ethanol accesses described activating catalytic agent composition output channel for sending into the material inlet of deactivated catalyst and the material inlet for sending into ethanol adopts same material inlet on described mixing equipment.
4. hexanediamine production system as claimed in claim 3, it is characterized in that described thick hexanediamine preparation system also comprises hydrogen alcohol knockout tower, the top of described hydrogenation reactor is provided with the outlet of hydrogen alcohol mixture, described hydrogen alcohol mixture outlet connects the import of described hydrogen alcohol knockout tower by hydrogen ethanol output channel, nol outlet after the bottom of described hydrogen alcohol knockout tower is provided with and is separated, after described separation, nol outlet accesses described hydrogenation reactor by ethanol circulating line, hydrogen outlet after the top of described hydrogen alcohol knockout tower is provided with and is separated, after described separation, hydrogen outlet connects the rear hydrogen output channel of separation, after described separation, hydrogen output channel is divided into two-way, one tunnel is for being separated rear hydrogen discharge pipe, hydrogen reuse pipe after another road is separated, described hydrogen reuse pipe accesses the hydrogen supply pipeline of described hydrogenation reactor or directly accesses described hydrogenation reactor.
5. hexanediamine production system as claimed in claim 4, it is characterized in that described strainer is provided with much filtrate output channel, described much filtrate output channel connects catalyst deactivation device, the bottom of described hydrogenation reactor is provided with excess catalyst discharge line, described excess catalyst discharge line accesses described catalyst deactivation device, and described catalyst deactivation device is provided with passivator output channel and passivation rear catalyst discharge tube.
6. hexanediamine production system as claimed in claim 5, it is characterized in that described dealcoholysis is reclaimed ethanol output channel and connected described ethanol supply line, described thick hexanediamine output channel connects thick amine relay tank, and described mixed liquor output channel is provided with surge pump.
7. the hexanediamine production system as described in claim 1,2,3,4,5 or 6, characterized by further comprising hexanediamine refining system, and described hexanediamine refining system comprises:
Dehydration tower, is provided with thick hexanediamine import and for exporting the dehydration dehydration hexanediamine output channel of hexanediamine and the waste water output channel for exporting waste water;
Decoking tower, be provided with dehydration hexanediamine import and for the decoking hexanediamine output channel that exports decoking hexanediamine and the blended tars output channel for exporting the blended tars that decoking produces, the import of described dehydration hexanediamine connects described dehydration hexanediamine output channel;
First-phase topping tower, be provided with the import of decoking hexanediamine and for hexanediamine output channel and the topping byproduct output channel for exporting topping byproduct after the topping of hexanediamine after exporting topping, the import of described decoking hexanediamine connects described decoking hexanediamine output channel;
De-tailing column, after being provided with topping hexanediamine import and for export pure hexanediamine pure hexanediamine output channel, for exporting the de-tail light constituent output channel of de-tail light constituent and the de-cabrage component output channel for exporting de-cabrage component, after described topping, hexanediamine import connects hexanediamine output channel after described topping;
Thinning tank, be provided with pure hexanediamine import, process water import and the one or more hexanediamine aqueous solution output channels for exporting the certain density hexanediamine aqueous solution, described pure hexanediamine import connects described pure hexanediamine output channel, described process water import Joining Technology water supply line.
8. hexanediamine production system as claimed in claim 7, it is characterized in that described hexanediamine refining system also comprises second-phase topping tower, be provided with the import of topping byproduct and for the secondary topping hexanediamine output channel that exports secondary topping hexanediamine and the secondary topping light constituent output channel for exporting secondary topping light constituent, described secondary topping hexanediamine output channel accesses described dehydration hexanediamine output channel or the direct described decoking tower of access.
9. hexanediamine production system as claimed in claim 8, it is characterized in that described hexanediamine refining system also comprises tar filter, being provided with blended tars import and for the blended tars filtrate output tube road that exports blended tars filtrate and the blended tars waste sludge discharge mouth for exporting blended tars waste residue.
10. hexanediamine production system as claimed in claim 9, it is characterized in that described hexanediamine refining system also comprises tar stripping unit, be provided with the import of blended tars filtrate and for the stripping hexanediamine output channel that exports stripping hexanediamine and for export tar after stripping stripping after tar emission mouth, the import of described blended tars filtrate connects described blended tars filtrate output tube road, described de-cabrage component output channel accesses described blended tars filtrate output tube road or directly accesses described tar stripping unit, described thick hexanediamine import connects described diamines relay tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109261085A (en) * | 2018-11-16 | 2019-01-25 | 重庆华峰化工有限公司 | Hexamethylene diamine synthesis system |
| CN109438256A (en) * | 2018-11-13 | 2019-03-08 | 中国化学赛鼎宁波工程有限公司 | A kind of production method and production system of hexamethylene diamine |
| CN112321438A (en) * | 2020-11-25 | 2021-02-05 | 重庆华峰化工有限公司 | Synthesis method of hexamethylene diamine |
| CN113105340A (en) * | 2021-04-15 | 2021-07-13 | 重庆华峰化工有限公司 | Production system and method of 2-hexanetriamine |
-
2014
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109438256A (en) * | 2018-11-13 | 2019-03-08 | 中国化学赛鼎宁波工程有限公司 | A kind of production method and production system of hexamethylene diamine |
| CN109261085A (en) * | 2018-11-16 | 2019-01-25 | 重庆华峰化工有限公司 | Hexamethylene diamine synthesis system |
| CN109261085B (en) * | 2018-11-16 | 2019-07-12 | 重庆华峰化工有限公司 | Hexamethylene diamine synthesis system |
| CN112321438A (en) * | 2020-11-25 | 2021-02-05 | 重庆华峰化工有限公司 | Synthesis method of hexamethylene diamine |
| CN112321438B (en) * | 2020-11-25 | 2024-04-16 | 重庆华峰化工有限公司 | Synthesis method of hexamethylenediamine |
| CN113105340A (en) * | 2021-04-15 | 2021-07-13 | 重庆华峰化工有限公司 | Production system and method of 2-hexanetriamine |
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