CN2757912Y - Combination device for aniline preparation and catalyst regeneration - Google Patents
Combination device for aniline preparation and catalyst regeneration Download PDFInfo
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- CN2757912Y CN2757912Y CNU2004201158315U CN200420115831U CN2757912Y CN 2757912 Y CN2757912 Y CN 2757912Y CN U2004201158315 U CNU2004201158315 U CN U2004201158315U CN 200420115831 U CN200420115831 U CN 200420115831U CN 2757912 Y CN2757912 Y CN 2757912Y
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- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 title claims abstract description 140
- 239000003054 catalyst Substances 0.000 title claims abstract description 116
- 230000008929 regeneration Effects 0.000 title claims abstract description 98
- 238000011069 regeneration method Methods 0.000 title claims abstract description 98
- 238000002360 preparation method Methods 0.000 title claims abstract description 28
- 239000007787 solid Substances 0.000 claims abstract description 48
- 239000000126 substance Substances 0.000 claims abstract description 6
- 230000007246 mechanism Effects 0.000 claims description 15
- 238000000926 separation method Methods 0.000 claims description 15
- 239000012530 fluid Substances 0.000 claims description 10
- 239000002994 raw material Substances 0.000 claims description 7
- 230000009719 regenerative response Effects 0.000 claims description 6
- 239000000725 suspension Substances 0.000 claims description 6
- 229910000831 Steel Inorganic materials 0.000 claims description 3
- 238000003780 insertion Methods 0.000 claims description 3
- 230000037431 insertion Effects 0.000 claims description 3
- 238000005192 partition Methods 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 3
- 239000010959 steel Substances 0.000 claims description 3
- 239000008247 solid mixture Substances 0.000 claims description 2
- LQNUZADURLCDLV-UHFFFAOYSA-N nitrobenzene Chemical compound [O-][N+](=O)C1=CC=CC=C1 LQNUZADURLCDLV-UHFFFAOYSA-N 0.000 abstract description 32
- 230000000694 effects Effects 0.000 abstract description 8
- 230000009467 reduction Effects 0.000 abstract description 5
- 238000004939 coking Methods 0.000 abstract description 3
- 230000001105 regulatory effect Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 39
- 238000000034 method Methods 0.000 description 18
- 230000008569 process Effects 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 9
- 229910052739 hydrogen Inorganic materials 0.000 description 9
- 239000001257 hydrogen Substances 0.000 description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 8
- 239000011261 inert gas Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000000839 emulsion Substances 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 230000004913 activation Effects 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical group [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 229920002635 polyurethane Polymers 0.000 description 2
- 239000004814 polyurethane Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical group [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 238000004176 ammonification Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- TVZPLCNGKSPOJA-UHFFFAOYSA-N copper zinc Chemical compound [Cu].[Zn] TVZPLCNGKSPOJA-UHFFFAOYSA-N 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000012860 organic pigment Substances 0.000 description 1
- 125000000636 p-nitrophenyl group Chemical group [H]C1=C([H])C(=C([H])C([H])=C1*)[N+]([O-])=O 0.000 description 1
- 239000005022 packaging material Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 229920000767 polyaniline Polymers 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000012958 reprocessing Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- -1 this.In like manner Chemical compound 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The utility model belongs to the technical field of chemical equipment, particularly relates to a simultaneous device for aniline preparation and catalyst regeneration. The simultaneous device comprises a fluidized bed for aniline preparation, a fluidized bed reactor for catalyst regeneration and a pipeline used for conveying catalyst and a solid conveying device which are arranged between the two fluidized beds. The coking state of the catalyst in an aniline preparing reactor can be regulated at any moment to achieve the purposes of converting nitrobenzene in high efficiency and generating aniline in high selectivity. The utility model can regulate and alter the activity and selectivity of the catalyst to improve the purity and the yield of the aniline, and at the same time, the utility model can enable the aniline preparing reactor to continuously operate without stopping, which improves aniline producing intensity and reduces operation cost during catalyst reduction and restarting up when the whole system stops.
Description
Technical field
The utility model belongs to chemical industry equipment and catalyst treatment technical field, and particularly a kind of aniline by the nitrobenzene gas phase hydrogenation prepares and catalyst regeneration simultaneous device.
Background technology
Aniline is the very important chemical products of a class.Along with the extensive use of polyurethane in fields such as building industry, automobile, electrical equipment and packaging material, the output of the primary raw material methyl vulcabond of polyurethane (be called for short MDI, got by the aniline preparation) improves rapidly, causes increasing considerably of aniline consumption figure.Aniline is mainly used in the production of MDI and rubber chemicals at present, also can be used for agricultural chemicals, organic pigment and field of medicaments etc., and the annual requirement in the world is about about 3,000,000 tons.
The method of suitability for industrialized production aniline has four kinds, i.e. nitrobenzene liquid-phase hydrogenatin method, nitrobenzene gas phase hydrogenation method, phenol ammoniation process and iron powder reducing method at present.Wherein the iron powder reducing method is owing to generate the second-rate of aniline, and is eliminated gradually.Phenol ammonification rule depends on the source of phenol strongly, and nitrobenzene liquid-phase hydrogenatin method catalyst system therefor is platinum or palladium catalyst, costs an arm and a leg and reclaims difficulty.And most of producers all adopt nitrobenzene gas phase hydrogenation legal system to be equipped with aniline.Its basic principle is that nitrobenzene and hydrogen are heated to about 200 ℃, feeds fluidized-bed reactor, under the effect of metal load type catalyst (major part is a copper catalyst), generates aniline in the time of 220-320 ℃.Reacting gas after condensation and dewatering, obtains the aniline crude product behind reactor.Remove various organic impurities through the refining operation that is equipped with then, obtain highly purified aniline product.
In the aniline building-up process, the continuous coking of catalyst meeting, activity of such catalysts constantly changes.Coking amount on catalyst is greater than 2-4%, and activity of such catalysts can descend obviously, shows as the nitrobenzene conversion ratio and is lower than 99.5%, generates the aniline selectivity simultaneously and descends.Even still very high through the nitrobenzene in the aniline behind the refining system of postorder like this, can not satisfy the requirement of most of reprocessing process (as preparation dyestuff, polyaniline, MDI preparation).At this moment catalyst generally needs regeneration, and for present domestic widely used copper zinc catalyst, its regeneration period is two to four months.Because present aniline prepares apparatus and process, is not equipped with independently catalyst regeneration system.When catalyst need be regenerated, just need whole system is all out of service.For the process of mass preparation aniline, whole system comprises the aniline subtractive process and the aniline hydrogenation process of the device and the postorder of leading portion, supporting production nitrobenzene.After catalyst is reproduced, when reruning again, whole process all need be returned to original state (comprise and heating up and pressurization).Because the auxiliary equipment in the process is very many, the start-stop car operating cost of whole system is very expensive like this.And along with the expansion of Aniline Production scale, all corresponding expansion of the scale of all accessory systems, operating cost can increase substantially.Activity of such catalysts shows unstability in such course of reaction simultaneously.Have the activity inducement phase (general one thoughtful two weeks does not wait) when just beginning, activity is lower.Catalyst enters the active stage of stable development then, can keep the conversion ratio and the selectivity that generates aniline of very high nitrobenzene.But gradually behind the inactivation, the conversion ratio of nitrobenzene descends to the later stage catalyst, and the selectivity that generates aniline descends, and the purity of corresponding aniline product reduces.For the stop aniline preparation process of the intermittently operated carry out catalyst regeneration of needs, activity of such catalysts is difficult for stable all the time, and may cause the also unstable and start-stop fare of the purity of aniline with height.
Summary of the invention
The purpose of this utility model provides the fluidized-bed reactor continued operation that can guarantee preparation aniline and does not stop, and can carry out a kind of aniline preparation and catalyst regeneration simultaneous device of catalyst regeneration simultaneously in real time, it is characterized in that: the preparation of described aniline and catalyst regeneration simultaneous device will be for preparing the fluidized-bed reactor of aniline by conveyance conduit and solids delivery device and the fluidized-bed reactor of catalyst regeneration directly couples together, the inlet 3 of gas raw material promptly is set in the bottom of reactor 1, gas distributor 5 is installed in the bottom of reactor 1, heat exchanger 6 is set then at an upper portion thereof, simultaneously member 9 is fixed on the vertical steel pipe of heat exchanger 6, and on reactor 1 wall, set up the heat exchanger suspension bracket with the middle part, the tube bank and the member 9 of heat exchanger 6 is fixing.Set up gas solid separation mechanism 14 on the top of reactor, gas solid separation mechanism 14 is fixedly connected with reactor wall, the outlet with gas solid separation mechanism 14 simultaneously links to each other with reactor 1 top, as the outlet 15 of reactor.The outlet 4 of inlet 12 with the decaying catalyst of setting up fresh catalyst inlet 11, regeneration rear catalyst respectively in the middle part and the bottom of reactor 1.In like manner, the inlet 21 of regeneration gas raw material is set in the bottom of regeneration reactor 2, regeneration gas distributor 22 is mounted and fixed on the bottom of regeneration reactor 2, regenerator 23 is set then at an upper portion thereof, regenerator inlet 24 and regenerator outlet 25 pass behind regeneration reactor 2 walls and with regenerative response wall sealing and fixing; On the regenerative response wall, set up the heat exchanger suspension bracket, the tube bank of regenerator 23 is fixed with the middle part.Set up gas-solid separator 29 on the top of regeneration reactor, gas-solid separator 29 and regeneration reactor inwall are fixedly connected, the outlet 30 with gas-solid separator simultaneously links to each other with regeneration reactor 2 tops; The inlet 27 of setting up decaying catalyst respectively in the middle part and the bottom of regeneration reactor and the outlet 20 of the catalyst after the regeneration.The catalyst outlet 4 of aniline fluid bed is linked to each other with pipeline 17 with the catalyst inlet 27 of regeneration reactor, solids delivery device 16 is set on pipeline 17 simultaneously.The regeneration rear catalyst inlet 12 of the catalyst outlet 20 of regeneration reactor and aniline fluid bed is linked to each other with pipeline 19, simultaneously solids delivery device 18 is set on pipeline 19, so just constituted that a complete aniline prepares and the simultaneous device of catalyst regeneration.
The diameter of described catalyst regeneration reactor and the diameter and 1/4～2/3 and 1/4～1 of height that are preparation aniline fluidized-bed reactor highly respectively.
The structure of described solids delivery device is higher than the position of solid inlet for the height in the insertion inner chamber 44 of wherein leading conveying airduct road, the inlet 41 that one lateral partitions formula gas distributor 42 will become flexible wind is set in inner chamber is separately positioned on different zones with the main inlet 40 of wind of carrying, the outlet 45 of this solid inlet 43 and gas and solid mixture is connected with the pipeline of conveying solid substance respectively.
The beneficial effects of the utility model are that the fluidized-bed reactor and the catalyst regeneration fluidized-bed reactor of described preparation aniline has independently distribution device in gas-fluid, heat-exchanger rig and catalyst recovery devices respectively.The fluidized-bed reactor for preparing aniline simultaneously also has the on-board components system that is used for bubble crushing.Such two covers are independent and complete system can guarantee when catalyst regeneration, do not influence the normal running of the fluidized-bed reactor of preparation aniline.Because the nitrobenzene air speed in the fluidized-bed reactor of preparation aniline only improves 10-20%, conversion that can p-nitrophenyl causes and has a strong impact on.Catalyst regeneration reactor manufacturing cost simultaneously on a small scale is lower, and the tolerance that needs during regeneration is also less, and corollary system is also fairly simple, realizes industrialization easily.
The present invention simultaneously emphasizes that the internal diameter at the pipeline that is arranged on the conveying catalyst between preparation aniline fluid bed and catalyst regeneration reactor is 100-500mm.Logical a small amount of gas in conveyance conduit just can make gas velocity wherein reach 1-30m/s like this.Catalyst can be shifted in two equipment fast like this, improve the security of process.
Description of drawings
Fig. 1 is aniline preparation provided by the invention and catalyst regeneration simultaneous device schematic diagram.
Fig. 2 is the structural representation of solids delivery device.
The specific embodiment
The utility model provides the fluidized-bed reactor continued operation that can guarantee preparation aniline not stop, and can prepare and catalyst regeneration simultaneous device with a kind of aniline that carries out catalyst regeneration at any time simultaneously.In aniline preparation and catalyst regeneration simultaneous device shown in Figure 1, the inlet 3 of gas raw material is set in the bottom of reactor 1, gas distributor 5 is installed in the bottom of reactor 1, heat exchanger 6 is set then at an upper portion thereof, simultaneously member 9 is fixed on the vertical steel pipe of heat exchanger 6, and on reactor 1 wall, set up the heat exchanger suspension bracket with the middle part, the tube bank and the member 9 of heat exchanger 6 is fixing.Set up gas solid separation mechanism 14 on the top of reactor, gas solid separation mechanism 14 is fixedly connected with reactor wall, the outlet with gas solid separation mechanism 14 simultaneously links to each other with reactor 1 top, as the outlet 15 of reactor.Middle part and bottom at reactor 1 are set up catalyst inlet 11, the inlet 12 of regeneration rear catalyst and the outlet 4 of decaying catalyst respectively, constitute the fluidized bed plant of complete preparation aniline like this.In like manner, the inlet 21 of regeneration gas raw material is set in the bottom of regeneration reactor 2, regeneration gas distributor 22 is mounted and fixed on the bottom of regeneration reactor 2, regenerator 23 is set then at an upper portion thereof, regenerator inlet 24 and regenerator outlet 25 pass behind regeneration reactor 2 walls and with regenerative response wall sealing and fixing; On the regenerative response wall, set up the heat exchanger suspension bracket, the tube bank of regenerator 23 is fixed with the middle part.Set up gas-solid separator 29 on the top of regeneration reactor, gas-solid separator 29 and regeneration reactor inwall are fixedly connected, the outlet 30 with gas-solid separator simultaneously links to each other with regeneration reactor 2 tops; The inlet 27 of setting up decaying catalyst respectively in the middle part and the bottom of regeneration reactor and the outlet 20 of the catalyst after the regeneration.The catalyst outlet 4 of aniline fluid bed is linked to each other with pipeline 17 with the catalyst inlet 27 of regeneration reactor, solids delivery device 16 is set on pipeline 17 simultaneously.The regeneration rear catalyst inlet 12 of the catalyst outlet 20 of regeneration reactor and aniline fluid bed is linked to each other with pipeline 19, simultaneously solids delivery device 18 is set on pipeline 19, so just constituted that a complete aniline prepares and the simultaneous device of catalyst regeneration.
Carry out aniline when preparing, at first with catalyst from catalyst inlet 11 reactor 1 of packing into, be accumulated in the catalyst emulsion zone 10 in the reactor 1 naturally, after loading catalyst finished, logical inert gas was an anaerobic state with the gas displacement in the reactor 1.Be warming up to 150-250 ℃ during this period gradually, cut hydrogen then and carry out catalyst reduction.Gas speed control during reduction in the reactor 1 guarantees that catalyst is in fluidized state between 0.05-0.3m/s, avoid the local heap knot of catalyst overstocked, causes sintering of catalyst.Simultaneously 7 feed cooling water in heat exchanger 6 through entering the mouth, cooling water raises through heat exchanger 6 back temperature, becomes steam water interface and goes out heat exchanger 6 from exporting 8.Can control reduction temperature in the reactor like this between 150-250 ℃, the recovery time was at 3-40 hour.After reduction finishes, strengthen the inlet amount of hydrogen, and reduce the inlet amount of inert gas gradually, the gas in reactor 1 all is hydrogen.When temperature of reactor is 220-250 ℃, the amount of hydrogen is increased to the process stipulation value.And, in reactor 1, feed nitrobenzene through gas distributor 5 through the gas feed 3 of reactor 1, be 7 until the mol ratio of hydrogen and nitrobenzene: 1-20: 1.Regulate the cooling water flow in the heat exchanger 6, make the mean temperature in the reactor remain on 250-270 ℃.Reactant is converted into aniline through catalyst emulsion zone 10.Product enters gas solid separation mechanism 14 from gas solid separation mechanism inlet 13, and goes out reactor from gas solid separation mechanism outlet 15.
In this process, the part catalyst in the catalyst emulsion zone 10 is carried by air-flow, enters gas solid separation mechanism 14, the dipleg return catalizer emulsion zone 10 below gas solid separation mechanism 14 from gas solid separation mechanism inlet 13.
When catalyst need be regenerated,, be anaerobic state at first with the gas displacement in the regeneration reactor 2 from regeneration gas distributor 22 logical inert gases.At the pressure that guarantees regeneration reactor 2 is under the state of pressure-fired, open the catalyst outlet 4 of aniline fluid bed and the catalyst inlet 27 of regeneration reactor, start solids delivery device 16, carbon deposition catalyst is delivered to regeneration reactor 2 from reactor 1 by conveyance conduit 17.After conveying finishes, close catalyst outlet 4 and catalyst inlet 27 and solids delivery device 16.With inert gas the atmosphere in the regeneration reactor 2 is replaced into no hydrogen state, and regeneration reactor 2 is heated to 180-240 ℃ by regenerator 23.From regeneration reactor gas distributor 22 aerating oxygens, burn the carbon reaction then.The feeding amount of control oxygen makes the maximum temperature in the regeneration reactor 2 be lower than 400 ℃, and remains on and carry out the charcoal regeneration reaction in 360-400 ℃ the temperature.When any raising oxygen content all can not be kept the temperature of regeneration, show that the carbon on the catalyst is burned fully, close oxygen.To anaerobic state, the temperature of regeneration reactor is controlled to 180-240 ℃ with the inert gas purge regeneration reactor.In regeneration reactor 2, feed hydrogen by regeneration gas distributor 22 and carry out the activation of catalyst.After the catalyst activation finishes, feed a large amount of hydrogen to regeneration reactor 2, make its pressure be higher than the pressure of the reactor 1 of aniline fluid bed.Open the regeneration rear catalyst inlet 12 of regeneration reactor catalyst outlet 20 and reactor 1, start solids delivery device 18, the catalyst that will also activate after will regenerating by conveyance conduit 19 is delivered to reactor 1 by regeneration reactor 2.After conveying finishes, close catalyst inlet 12, catalyst outlet 20 and solids delivery device 19.Guarantee the safe and continuous operation of the fluidized-bed reactor of preparation aniline.
According to the conversion ratio of phosphorus content on the catalyst or nitrobenzene, repeat aforesaid operations, can guarantee that catalyst constantly is reproduced, and the fluidized-bed reactor continuously-running of preparation aniline is produced highly purified aniline.
In conveying device shown in Figure 2, feed loosening wind by loosening airduct road inlet 41, through inner lateral partitions formula gas distributor 42, make by solid pipeline inlet 43 consubstantialities that enter conveying device to be in fluidized state.Because the height of the insertion inner chamber 44 in main conveying airduct road is higher than the position of solid pipeline 43, when feeding the conveying wind by main conveying wind inlet 40, in conveying device inner chamber 44, form a vacuum state, main outlet 45 of carrying wind meeting sorption consubstantiality to enter gas and consubstantiality mixture together, enter conveyance conduit then, arrive and carry the destination.
Main improvement of the present utility model has been to adopt the reaction unit that independently carries out catalyst regeneration, owing to independently be provided with the catalyst regeneration reactor, becomes more flexible with regard to the regeneration technology that makes catalyst.Not only can carry out the regeneration of catalyst in proportion, also can carry out the concentrated intensifying regenerating of a large amount of catalyst in a period of time in the set time.With compared in the past, can not be subjected to the restriction in equipment rebuilding equal time cycle, have the convenience that shifts out catalyst at any time and send into catalyst, improved the control ability of process.
Claims (3)
1. an aniline prepares and catalyst regeneration simultaneous device, it is characterized in that: the preparation of described aniline and catalyst regeneration simultaneous device will be for preparing the fluidized-bed reactor of aniline by conveyance conduit and solids delivery device and the fluidized-bed reactor of catalyst regeneration directly couples together, the inlet (3) of gas raw material promptly is set in the bottom of reactor (1), gas distributor (5) is installed in the bottom of reactor (1), heat exchanger (6) is set then at an upper portion thereof, simultaneously member (9) is fixed on the vertical steel pipe of heat exchanger (6), and on reactor (1) wall, set up the heat exchanger suspension bracket with the middle part, the tube bank and the member (9) of heat exchanger (6) is fixing, set up gas solid separation mechanism (14) on the top of reactor, gas solid separation mechanism (14) is fixedly connected with reactor wall, outlet with gas solid separation mechanism (14) simultaneously links to each other with reactor (1) top, as the outlet (15) of reactor, set up catalyst inlet (11) respectively in the middle part and the bottom of reactor (1), the inlet (12) of regeneration rear catalyst and the outlet (4) of decaying catalyst; In like manner, the inlet (21) of regeneration gas raw material is set in the bottom of regeneration reactor (2), regeneration gas distributor (22) is mounted and fixed on the bottom of regeneration reactor (2), regenerator (23) is set then at an upper portion thereof, regenerator inlet (24) and regenerator export (25) pass behind regeneration reactor (2) wall and with regenerative response wall sealing and fixing; On the regenerative response wall, set up the heat exchanger suspension bracket, the tube bank of regenerator (23) is fixed with the middle part; Set up gas-solid separator (29) on the top of regeneration reactor, gas-solid separator (29) and regeneration reactor inwall are fixedly connected, the outlet (30) with gas-solid separator simultaneously links to each other with regeneration reactor (2) top; The inlet (27) of setting up decaying catalyst respectively in the middle part and the bottom of regeneration reactor and the outlet (20) of the catalyst after the regeneration, the catalyst outlet (4) of aniline fluid bed is linked to each other with pipeline (17) with the catalyst inlet (27) of regeneration reactor, solids delivery device (16) is set on pipeline (17) simultaneously, the catalyst outlet (20) of regeneration reactor is linked to each other with pipeline (19) with the regeneration rear catalyst inlet (12) of aniline fluid bed, simultaneously solids delivery device (18) is set on pipeline (19), has so just constituted a complete aniline preparation and the simultaneous device of catalyst regeneration.
2. according to described aniline preparation of claim 1 and catalyst regeneration simultaneous device, it is characterized in that: the diameter of described catalyst regeneration reactor and the diameter and 1/4～2/3 and 1/4～1 of height that are preparation aniline fluidized-bed reactor highly respectively.
3. according to described aniline preparation of claim 1 and catalyst regeneration simultaneous device, it is characterized in that: the height in the inner chamber of solids delivery device in the insertion inner chamber (44) of main conveying wind inlet duct is higher than the position of solid inlet (43), the inlet (41) that one lateral partitions formula gas distributor (42) will become flexible wind is set in inner chamber is separately positioned on different zones with the main inlet (40) of wind of carrying, this solid inlet (43) is connected with the outlet (4) of decaying catalyst, the catalyst outlet (20) of regeneration reactor respectively; The outlet of gas and solid mixture (45) is connected with pipeline (17) or (19) of conveying solid substance respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2004201158315U CN2757912Y (en) | 2004-11-30 | 2004-11-30 | Combination device for aniline preparation and catalyst regeneration |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2004201158315U CN2757912Y (en) | 2004-11-30 | 2004-11-30 | Combination device for aniline preparation and catalyst regeneration |
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| CN2757912Y true CN2757912Y (en) | 2006-02-15 |
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| CNU2004201158315U Expired - Lifetime CN2757912Y (en) | 2004-11-30 | 2004-11-30 | Combination device for aniline preparation and catalyst regeneration |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101959589A (en) * | 2008-03-07 | 2011-01-26 | 国际壳牌研究有限公司 | Process for cracking a hydrocarbon feed |
| CN103623875A (en) * | 2013-11-08 | 2014-03-12 | 江苏大学 | Deactivated catalyst regeneration device and method based on boiling principle |
| CN106565504A (en) * | 2015-10-12 | 2017-04-19 | 中国石油化工股份有限公司 | Method for preparing aniline through liquid-phase hydrogenation of nitrobenzene |
| CN106732822A (en) * | 2017-01-22 | 2017-05-31 | 清华大学 | A kind of catalyst regeneration device, method and system |
| WO2020078411A1 (en) * | 2018-10-17 | 2020-04-23 | 中国石油化工股份有限公司 | Gas replacement method and device, and hydrogenation method for nitro compound |
| CN111056958A (en) * | 2018-10-17 | 2020-04-24 | 中国石油化工股份有限公司 | Coupling reaction device and reaction method for preparing aniline by nitrobenzene hydrogenation |
-
2004
- 2004-11-30 CN CNU2004201158315U patent/CN2757912Y/en not_active Expired - Lifetime
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101959589A (en) * | 2008-03-07 | 2011-01-26 | 国际壳牌研究有限公司 | Process for cracking a hydrocarbon feed |
| CN101959589B (en) * | 2008-03-07 | 2013-09-18 | 国际壳牌研究有限公司 | Reactor assembly for cracking a hydrocarbon feed |
| CN103623875A (en) * | 2013-11-08 | 2014-03-12 | 江苏大学 | Deactivated catalyst regeneration device and method based on boiling principle |
| CN103623875B (en) * | 2013-11-08 | 2015-08-26 | 江苏大学 | A kind of decaying catalyst regenerating unit based on boiling principle and renovation process |
| CN106565504B (en) * | 2015-10-12 | 2018-09-28 | 中国石油化工股份有限公司 | A kind of method of nitrobenzene liquid-phase hydrogenatin aniline |
| CN106565504A (en) * | 2015-10-12 | 2017-04-19 | 中国石油化工股份有限公司 | Method for preparing aniline through liquid-phase hydrogenation of nitrobenzene |
| CN106732822A (en) * | 2017-01-22 | 2017-05-31 | 清华大学 | A kind of catalyst regeneration device, method and system |
| WO2020078411A1 (en) * | 2018-10-17 | 2020-04-23 | 中国石油化工股份有限公司 | Gas replacement method and device, and hydrogenation method for nitro compound |
| CN111056949A (en) * | 2018-10-17 | 2020-04-24 | 中国石油化工股份有限公司 | Reaction device and reaction method for preparing aniline through continuous reaction, regeneration and activation |
| CN111056958A (en) * | 2018-10-17 | 2020-04-24 | 中国石油化工股份有限公司 | Coupling reaction device and reaction method for preparing aniline by nitrobenzene hydrogenation |
| CN111056949B (en) * | 2018-10-17 | 2021-05-11 | 中国石油化工股份有限公司 | Reaction device and reaction method for preparing aniline through continuous reaction, regeneration and activation |
| JP2022512758A (en) * | 2018-10-17 | 2022-02-07 | 中国石油化工股▲ふん▼有限公司 | Hydrogenation reaction process of nitro compounds, and hydrogenation reaction equipment |
| CN111056958B (en) * | 2018-10-17 | 2023-04-07 | 中国石油化工股份有限公司 | Coupling reaction device and reaction method for preparing aniline by nitrobenzene hydrogenation |
| JP7434307B2 (en) | 2018-10-17 | 2024-02-20 | 中国石油化工股▲ふん▼有限公司 | Nitro compound hydrogenation reaction process and hydrogenation reaction equipment |
| US12116331B2 (en) | 2018-10-17 | 2024-10-15 | China Petroleum & Chemical Corporation | Gas replacement process, gas replacement apparatus, and nitro compound hydrogenation reaction process |
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