CN209197530U - A kind of cage heat exchanger in catalytic hydrogenation reaction device - Google Patents
A kind of cage heat exchanger in catalytic hydrogenation reaction device Download PDFInfo
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- CN209197530U CN209197530U CN201821975477.1U CN201821975477U CN209197530U CN 209197530 U CN209197530 U CN 209197530U CN 201821975477 U CN201821975477 U CN 201821975477U CN 209197530 U CN209197530 U CN 209197530U
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- heat exchanger
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- exchanger tube
- heat
- heat carrier
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- 238000009903 catalytic hydrogenation reaction Methods 0.000 title claims abstract description 20
- 238000009826 distribution Methods 0.000 claims abstract description 25
- 238000010438 heat treatment Methods 0.000 claims abstract description 19
- 239000003054 catalyst Substances 0.000 abstract description 67
- 238000004519 manufacturing process Methods 0.000 abstract description 28
- 238000005516 engineering process Methods 0.000 abstract description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 22
- 239000001257 hydrogen Substances 0.000 description 16
- 229910052739 hydrogen Inorganic materials 0.000 description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 14
- 230000004913 activation Effects 0.000 description 11
- SVTBMSDMJJWYQN-UHFFFAOYSA-N 2-methylpentane-2,4-diol Chemical compound CC(O)CC(C)(C)O SVTBMSDMJJWYQN-UHFFFAOYSA-N 0.000 description 10
- UDSFAEKRVUSQDD-UHFFFAOYSA-N Dimethyl adipate Chemical compound COC(=O)CCCCC(=O)OC UDSFAEKRVUSQDD-UHFFFAOYSA-N 0.000 description 10
- BGTOWKSIORTVQH-UHFFFAOYSA-N cyclopentanone Chemical compound O=C1CCCC1 BGTOWKSIORTVQH-UHFFFAOYSA-N 0.000 description 10
- 238000000034 method Methods 0.000 description 10
- 230000000694 effects Effects 0.000 description 8
- 229940051250 hexylene glycol Drugs 0.000 description 7
- 239000000463 material Substances 0.000 description 7
- 239000003795 chemical substances by application Substances 0.000 description 5
- 230000008602 contraction Effects 0.000 description 4
- XCIXKGXIYUWCLL-UHFFFAOYSA-N cyclopentanol Chemical compound OC1CCCC1 XCIXKGXIYUWCLL-UHFFFAOYSA-N 0.000 description 4
- XXMIOPMDWAUFGU-UHFFFAOYSA-N hexane-1,6-diol Chemical compound OCCCCCCO XXMIOPMDWAUFGU-UHFFFAOYSA-N 0.000 description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- LTBFZSXMPHXJJT-UHFFFAOYSA-N cyclopentanol;cyclopentanone Chemical compound OC1CCCC1.O=C1CCCC1 LTBFZSXMPHXJJT-UHFFFAOYSA-N 0.000 description 3
- NIQCNGHVCWTJSM-UHFFFAOYSA-N Dimethyl phthalate Chemical compound COC(=O)C1=CC=CC=C1C(=O)OC NIQCNGHVCWTJSM-UHFFFAOYSA-N 0.000 description 2
- WNLRTRBMVRJNCN-UHFFFAOYSA-N adipic acid Chemical compound OC(=O)CCCCC(O)=O WNLRTRBMVRJNCN-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000021615 conjugation Effects 0.000 description 2
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 description 2
- LQZZUXJYWNFBMV-UHFFFAOYSA-N dodecan-1-ol Chemical compound CCCCCCCCCCCCO LQZZUXJYWNFBMV-UHFFFAOYSA-N 0.000 description 2
- 150000004702 methyl esters Chemical class 0.000 description 2
- -1 pentanone cyclopentanol Chemical compound 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- LOMVENUNSWAXEN-UHFFFAOYSA-N Methyl oxalate Chemical compound COC(=O)C(=O)OC LOMVENUNSWAXEN-UHFFFAOYSA-N 0.000 description 1
- 239000001361 adipic acid Substances 0.000 description 1
- 235000011037 adipic acid Nutrition 0.000 description 1
- XXLDWSKFRBJLMX-UHFFFAOYSA-N carbon dioxide;carbon monoxide Chemical compound O=[C].O=C=O XXLDWSKFRBJLMX-UHFFFAOYSA-N 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- HPXRVTGHNJAIIH-UHFFFAOYSA-N cyclohexanol Chemical compound OC1CCCCC1 HPXRVTGHNJAIIH-UHFFFAOYSA-N 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 125000000118 dimethyl group Chemical group [H]C([H])([H])* 0.000 description 1
- FBSAITBEAPNWJG-UHFFFAOYSA-N dimethyl phthalate Natural products CC(=O)OC1=CC=CC=C1OC(C)=O FBSAITBEAPNWJG-UHFFFAOYSA-N 0.000 description 1
- 229960001826 dimethylphthalate Drugs 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- OJURWUUOVGOHJZ-UHFFFAOYSA-N methyl 2-[(2-acetyloxyphenyl)methyl-[2-[(2-acetyloxyphenyl)methyl-(2-methoxy-2-oxoethyl)amino]ethyl]amino]acetate Chemical compound C=1C=CC=C(OC(C)=O)C=1CN(CC(=O)OC)CCN(CC(=O)OC)CC1=CC=CC=C1OC(C)=O OJURWUUOVGOHJZ-UHFFFAOYSA-N 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Abstract
The utility model relates to the cage heat exchangers in a kind of catalytic hydrogenation reaction device, heating medium inlet conduit is located at the top of heat exchanger, heating medium inlet conduit is connected with heat carrier distribution pipe, heat carrier distribution pipe connects heat carrier and distributes bobbin carriage, it is ring-shaped that heat carrier, which distributes bobbin carriage, heat carrier distribution bobbin carriage is connected with multiple groups with one heart and circumferential evenly arranged heat exchanger tube, heat exchanger tube is supported by Multi-layer supporting ring, the lower end of heat exchanger tube is connected with heat carrier and collects bobbin carriage, heat carrier is collected and is connected with the helix tube that multiple groups are spiraled together on the downside of bobbin carriage, the lower end of each helix tube is all connected with heat carrier collecting pipe, the other end of heat carrier collecting pipe is connected on heat exchanger the lowermost heating medium outlet conduit.The utility model reduces the landslide of catalyst, and bias current reduces hot(test)-spot temperature in catalytic hydrogenation production technology.The service life for extending catalyst improves the selectivity and product yield of product.
Description
Technical field
The utility model belongs to chemical industry manufacturing equipment, the cage heat exchanger being related in a kind of catalytic hydrogenation reaction device.
Background technique
It is known that cocinic acid methyl ester hydrogenation produces lauric alcohol, dimethyl adipate catalytic hydrogenation production 1,6-at present
Hexylene glycol, cyclopentanone catalytic hydrogenation cyclopentanol, cyclohexanone catalytic hydrogenation cyclohexanol, carbon monoxide carbon dioxide in coal chemical industry
Catalytic hydrogenation methanol, dimethyl oxalate catalytic hydrogenation preparing ethylene glycol, is all made of fixed bed reactors.General fixed bed reaction
Device is as shown in Figure 1, be that catalyst is added in fixed bed reactors.Catalyst catalyst activation and normally produced and used
Cheng Zhong, it may appear that well-known three problems: first, cubic deformation is shunk, and volume contraction can reach 25%~33%, in fixation
So-called catalyst shrinkage landslide is formed in bed, causes the bias current phenomenon of material and hydrogen flowing in technique.Second, production operating
The forward impact power that catalyst bed is flowed by material in technique and hydrogen in the process is big.Third, the common fixed bed such as Fig. 1 are anti-
Device is answered to cause hot(test)-spot temperature too high.4th, recycle hydrogen usage amount is big.The comprehensive effect of four factors, affects Catalytic processes
Effect and the service life for reducing catalyst, the selectivity and yield of catalyst are influenced, reduces yield, influence product quality.
Utility model content
Purpose of utility model
The utility model aim is to reduce cocinic acid methyl ester hydrogenation to generate lauric alcohol and dimethyl adipate generation 1,6-
In the production process of hexylene glycol in fixed bed reactors catalyst landslide, bias current reduces in catalytic hydrogenation production technology
Hot(test)-spot temperature.The service life for extending catalyst improves the selectivity and product yield of product.
Technical solution
Cage heat exchanger in a kind of catalytic hydrogenation reaction device, it is characterised in that: including heating medium inlet conduit, heat carrier
Distribution pipe, heat carrier distribute bobbin carriage, heat exchanger tube, support ring, heat carrier collect bobbin carriage, helix tube, heat carrier collecting pipe and
Heating medium outlet conduit；The heating medium inlet conduit is located at the top of heat exchanger, and heating medium inlet conduit is connected with hot load
Body distribution pipe, heat carrier distribution pipe connect heat carrier and distribute bobbin carriage, and it is ring-shaped that heat carrier, which distributes bobbin carriage, and heat carrier distributes bobbin carriage
It is connected with multiple groups with one heart and circumferential evenly arranged heat exchanger tube, heat exchanger tube is supported by Multi-layer supporting ring, heat exchanger column
The lower end of pipe is connected with heat carrier and collects bobbin carriage, and heat carrier is collected and is connected with the spiral that multiple groups are spiraled together on the downside of bobbin carriage
Pipe, the lower end of each helix tube are all connected with heat carrier collecting pipe, and it is most lower that the other end of heat carrier collecting pipe is connected to heat exchanger
On the heating medium outlet conduit at end.
The heat exchanger tube includes inner ring heat exchanger tube, centre circle heat exchanger tube and outer ring heat exchanger tube, described
Support ring includes inner ring support ring, centre circle support ring and outer ring support ring；Inner ring support ring is equipped with air hole, inner ring support ring
Outer ring is equipped with equally distributed inner ring heat exchanger tube support slot identical with inner ring heat exchanger tube quantity, inner ring heat exchanger column
Pipe support slot is welded together with inner ring heat exchanger tube；Centre circle support ring is equipped with centre circle support ring inner cavity, centre circle support ring inner cavity
Diameter be greater than the outer diameter of inner ring support ring, the outer ring of centre circle support ring be equipped with it is identical with centre circle heat exchanger tube quantity uniformly
The centre circle heat exchanger tube support slot of distribution, centre circle heat exchanger tube support slot weld together with centre circle heat exchanger tube；Outside
It encloses support ring and is equipped with outer ring support ring inner cavity, the diameter of outer ring support ring inner cavity is greater than the outer diameter of centre circle support ring, outer ring support
The outer ring of ring is equipped with equally distributed outer ring heat exchanger tube support slot identical with outer ring heat exchanger tube quantity, outer ring heat exchange
Device tubulation support slot welds together with outer ring heat exchanger tube.
The support ring is equidistantly arranged in vertical direction.
The inner ring support ring, centre circle support ring and outer ring support ring are successively equidistantly arranged in vertical direction, are considered as one group
Support ring；There are one or more groups of support rings according to the length of cage heat exchanger.
The inner ring heat exchanger tube, centre circle heat exchanger tube and outer ring heat exchanger tube are connected to heat carrier distribution
Inner ring, lower end and the outer ring of bobbin carriage.
The heat carrier distribution pipe is the equally distributed pipeline of multiple circumferential directions, and lower end is connected to the heat carrier point of ring-shaped
Upper surface with bobbin carriage.
Advantage and effect
The utility model overcomes the frequent problem of the prior art: first, catalyst volume deformation retract is reduced, is subtracted
Small landslide amount reduces the bias current phenomenon of material and hydrogen flowing in technique.Second, reduce catalyst in production operation process
The forward impact power that bed is flowed by material in technique and hydrogen is big.Third reduces heat caused by conventional fixed bed reactors
Point temperature is too high.4th, reduce recycle hydrogen usage amount.The comprehensive effect of four factors.Improve Catalytic processes effect and
The service life for extending catalyst improves the selectivity and yield of catalyst, improves yield, improve product quality.
The cage heat exchanger of the utility model is loaded onto general fixed bed high-pressure hydrogenation inside reactor as shown in Figure 1,
The fixed bed high-pressure hydrogenation reactor for constituting built-in cage heat exchanger, is exchanged heat under Fig. 1 reactor the same terms using cage
For the fixed bed high-pressure hydrogenation catalyst in reactor of device during the activation of catalyst and normal production and application, volume contraction can
Reach 7%~10%.With under Fig. 1 reactor the same terms use cage heat exchanger fixed bed high-pressure hydrogenation reactor in be catalyzed
During the activation of catalyst and normal production and application landslide and Biased flow phenomenon do not occur for agent.
Hydrogen-oil ratio is small, and due to the addition of cage heat exchanger, a large amount of reaction heat is taken away by heat carrier.Reduce hydrogen-oil ratio.
As during 1,6-hexylene glycol of dimethyl adipate system hydrogen-oil ratio by 25000~30000:1 be reduced to 4000~6000:1(mark
State volume ratio).Hydrogen stream is decreased after reduction hydrogen-oil ratio to wash away catalyst, increases the service life of catalyst.
Reduce hot(test)-spot temperature, the conventional fixed bed hydrogenation reactor shown in Fig. 1, activation and just of the catalyst in catalyst
During often producing and using, hot(test)-spot temperature is reacted up to 260 DEG C~280 DEG C in general fixed bed high-pressure hydrogenation as shown in Figure 1
Load onto the cage heat exchanger of the utility model in device, constitute the fixed bed high-pressure hydrogenation reactor of built-in cage heat exchanger, with
Use the fixed bed high-pressure hydrogenation catalyst in reactor of cage heat exchanger in the activation of catalyst under Fig. 1 reactor the same terms
During normal produce and use, under identical operating condition, bed temperature can be made to control to equal after cage heat exchanger is added
The temperature of weighing apparatus, hence it is evident that reduce hot(test)-spot temperature.
Catalyst life increase, the conventional fixed bed hydrogenation reactor shown in Fig. 1, catalyst catalyst activation and
During normal production and application, catalyst life 3 months.It is filled in general fixed bed high-pressure hydrogenation reactor as shown in Figure 1
The cage heat exchanger of upper the utility model constitutes the fixed bed high-pressure hydrogenation reactor of built-in cage heat exchanger, reacts with Fig. 1
Using the fixed bed high-pressure hydrogenation catalyst in reactor of cage heat exchanger in the activation of catalyst and normal under device the same terms
During production and application, under identical operating condition, catalyst life can be made to rise to 12 months after cage heat exchanger is added.
The selectivity and yield for improving catalyst, improve yield, improve product quality.
Detailed description of the invention
Fig. 1 is general conventional fixed bed hydrogenation reactor；
The structure chart of Fig. 2 cage heat exchanger；
Fig. 3 inner ring supporting ring structure figure；
Fig. 4 centre circle supporting ring structure figure；
The outer ring Fig. 5 supporting ring structure figure；
The schematic top plan view of Fig. 6 cage heat exchanger superstructure；
The attachment structure schematic diagram of Fig. 7 support ring and heat exchanger tube.
Description of symbols:
1. heating medium inlet conduit, 2. heat carrier distribution pipes, 3. heat carriers distribute bobbin carriage, 4. inner ring heat exchanger tubes, 5.
Centre circle heat exchanger tube, 6. outer ring heat exchanger tubes, 7. inner ring support rings, 8. centre circle support rings, 9. outer ring support rings, 10. heat
Carrier is collected bobbin carriage, 11. helix tubes, 12. heat carrier collecting pipes, 13. heating medium outlet conduits, 14. air holes, 15. inner rings and is changed
Hot device tubulation support slot, 16. centre circle support ring inner cavities, 17. centre circle heat exchanger tube support slots, 18. outer ring support ring inner cavities,
19. outer ring heat exchanger tube support slot.
Specific embodiment
The utility model is described further with reference to the accompanying drawing:
Shown in as shown in Figure 1, Figure 2 Fig. 3, Fig. 4, Fig. 5, Fig. 6 and Fig. 7, a kind of cage heat exchanger in catalytic hydrogenation reaction device, packet
Heating medium inlet conduit 1, heat carrier distribution pipe 2, heat carrier distribution bobbin carriage 3 are included, heat exchanger tube, support ring, heat carrier are collected
Bobbin carriage 10, helix tube 11, heat carrier collecting pipe 12 and heating medium outlet conduit 13；The heating medium inlet conduit 1 is located at heat exchange
The top of device, heating medium inlet conduit 1 are connected with heat carrier distribution pipe 2, and heat carrier distribution pipe 2 is the uniform direction of multiple circumferential directions
The pipeline of distribution, lower end be connected to ring-shaped heat carrier distribution bobbin carriage 3 upper surface, heat carrier distribute 3 inner ring of bobbin carriage, under
End and outer ring, which amount to, is connected with 3 groups with one heart and circumferential evenly arranged heat exchanger tubes, and heat carries such connection type when in use
Body distribution 3 internal pressure of bobbin carriage is uniform, and heat exchanger tube is respectively inner ring heat exchanger tube 4, centre circle heat exchanger tube 5 and outer ring
Heat exchanger tube 6, support ring are respectively inner ring support ring 7, centre circle support ring 8 and outer ring support ring 9；Inner ring support ring 7 is equipped with
Air hole 14, the outer ring of inner ring support ring 7 are equipped with the equally distributed inner ring of (8) identical as 4 quantity of inner ring heat exchanger tube
Heat exchanger tube support slot 15, inner ring heat exchanger tube support slot 15 are welded together with inner ring heat exchanger tube 4；Centre circle support ring
8 are equipped with centre circle support ring inner cavity 16, and the diameter of centre circle support ring inner cavity 16 is greater than the outer diameter of inner ring support ring 7, centre circle support ring 8
Outer ring be equipped with (16) identical as 5 quantity of centre circle heat exchanger tube equally distributed centre circle heat exchanger tube support slot 17,
Centre circle heat exchanger tube support slot 17 welds together with centre circle heat exchanger tube 5；Outer ring support ring 9 is equipped in the support ring of outer ring
Chamber 18, the diameter of outer ring support ring inner cavity 18 are greater than the outer diameter of centre circle support ring 8, and the outer ring of outer ring support ring 9 is equipped with and outer ring
The equally distributed outer ring heat exchanger tube support slot 19 of 6 quantity of heat exchanger tube identical (24), outer ring heat exchanger tube branch
Support slot 19 welds together with outer ring heat exchanger tube 6.Inner ring support ring 7, centre circle support ring 8 and outer ring support ring 9 are vertical
Direction is successively equidistantly arranged, and one group of support ring is considered as；The present embodiment has used 3 groups, amount to 9 support rings, " it is interior, in, it is outer, interior,
In, it is outer, interior, in, it is outer " successively equidistant arrangement.The lower end of heat exchanger tube is connected with heat carrier and collects bobbin carriage 10, and heat carrier is collected
The downside of bobbin carriage 10 is connected with the helix tube 11 that multiple groups are spiraled together, and the lower end of each helix tube 11 is all connected with heat carrier receipts
Collector 12, the other end of heat carrier collecting pipe 12 are connected on heat exchanger the lowermost heating medium outlet conduit 13.
Multi-layer supporting ring reduces the axial direction of raw material and hydrogen stream during the activation of catalyst and normal production and application
The direct impact force in front, while reducing the gravity of catalyst itself carrying.Not plus cage heat exchanger, hydrogen stream and material are edges
The axial direction of reactor flows downward in parallel, big to catalyst generation pressure, is easy along wall bias current.There is pipe after cage heat exchanger is added
The constraint of beam and there is the carrying material of cage support ring and hydrogen stream is curvilinear flow in reactor, reduces catalyst forward direction
Impact, reduce volume contraction and landslide cause, reduce the damage of catalyst, reduce bias current and showing along wall bias current
As increasing the service life of catalyst, improving the utilization rate of reactor, improve selectivity and yield.
The fixed bed high-pressure hydrogenation reactor of cage heat exchanger, passes through the wall of cage heat exchanger, catalyst in reactor
Bed reactant release heat reaction mass and circulating hydrogen can also pass to heat carrier, exchanged with cage heat exchanger wall to
Internal heat carrier moves down bed hot(test)-spot temperature is flat-pushing, achievees the effect that reduction hot(test)-spot temperature.
Using heat exchanger in cage, the comparison of catalyst in reactor volume contraction is made not add the 25%~33% of cage heat exchanger
Drop to 7%~10%, catalyst agent bed hot(test)-spot temperature reduces, and catalyst life was increased to 12 by original 3 months
Month, the selectivity of catalytic hydrogenation product increases, and product yield increases.
Heat carrier is passed to inside cage heat exchanger, heat carrier can be conduction oil, circulating hydrogen, cyclic steam.
Embodiment 1
Dimethyl adipate system 1, the life of 6- hexylene glycol are carried out in general fixed bed high-pressure hydrogenation reactor as shown in Figure 1
It produces, reactor diameter 600mm, 3 cubic metres of dimethyl adipate systems 1,6- hexylene glycol catalyst, catalysis is added in the reactor
After agent is activated, dimethyl adipate system 1 is carried out, the production of 6- hexylene glycol, reaction condition in production process, adipic acid when charging
Dimethyl ester and circulating hydrogen normal volume ratio press 1:25000 ~ 30000, and reactor inlet feeding temperature controls the reaction at 190 degree
The control of device bed layer pressure is in 16 ~ 18MPa, 260 ~ 280 degree of reactor catalyst bed hot(test)-spot temperature after tested, dimethyl adipate
Conversion ratio 100% generates the selectivity 85% ~ 90% of 1,6- hexylene glycol, finds that catalyst bed has bias current after production operation 1 month
Phenomenon, catalyst life 3 months, catalyst volume landslide 32%.
Embodiment 2
Cage heat exchanger as shown in Figure 2 is added in general fixed bed high-pressure hydrogenation reactor as shown in Figure 1, carries out oneself
Same as Example 13 are added in acid dimethyl system 1, the production of 6- hexylene glycol, reactor diameter 600mm in the reactor
Cubic meter dimethyl adipate system 1,6- hexylene glycol catalyst, catalyst carry out oneself two after side's activation same as Example 1
Dimethyl phthalate system 1, the production of 6- hexylene glycol, reaction condition in production process, dimethyl adipate and circulating hydrogen mark when charging
Quasi- volume ratio presses 1:4000 ~ 6000, the control of reactor inlet feeding temperature at 190 degree, reactor beds stressor layer controls 16 ~
18MPa, 195 ~ 210 degree of reactor catalyst bed hot(test)-spot temperature, dimethyl adipate conversion ratio 100% generate 1,6- after tested
The selectivity 99.47% ~ 98.50% of hexylene glycol has bias current phenomenon, catalyst life without discovery catalyst bed after production operation
12 months, catalyst volume landslide 7 ~ 8%.
It can be seen that from embodiment 1 and 2 comparative test of embodiment and cage be added in general fixed bed high-pressure hydrogenation reactor
Formula heat exchanger reduces hot(test)-spot temperature in production, and conversion rate of products improves, and selectivity improves, and catalyst landslide amount reduces, and urges
Agent life.Good conjugation effect is obtained.
Embodiment 3
The production of cyclopentanone cyclopentanol, reactor are carried out in general fixed bed high-pressure hydrogenation reactor as shown in Figure 1
The catalyst of 3 cubic metres of cyclopentanone cyclopentanol is added in diameter 600mm in the reactor, after catalyst upon activation, carries out ring
The production of pentanone cyclopentanol, reaction condition in production process, cyclopentanone and circulating hydrogen normal volume ratio press 1 when charging:
5000 ~ 8000, at 130 degree, reactor beds stressor layer is controlled in 10 ~ 11MPa, after tested anti-the control of reactor inlet feeding temperature
Device catalyst bed 160 ~ 180 degree of hot(test)-spot temperature is answered, cyclopentanone conversion ratio 100% generates the selectivity 80% ~ 95% of cyclopentanol, raw
Discovery catalyst bed has a bias current phenomenon after producing operation 1.5 months, and catalyst life 3 months, catalyst volume landslide 25%.
Embodiment 4
Cage as shown in Figure 2 is added in general fixed bed high-pressure hydrogenation reactor as shown in Figure 1 and shows heat exchanger, carries out ring
3 cubic metres of rings penta same as Example 3 are added in the production of pentanone cyclopentanol, reactor diameter 600mm in the reactor
Ketone cyclopentanol catalyst, catalyst carry out the production of cyclopentanone cyclopentanol after method activation same as Example 3,
Reaction condition in production process, cyclopentanone and circulating hydrogen normal volume ratio press 1:1000 ~ 1200 when charging, reactor inlet into
The control of material temperature degree is at 130 degree, and reactor beds stressor layer is controlled in 10 ~ 11MPa, after tested reactor catalyst bed hot(test)-spot temperature
135 ~ 140 degree, cyclopentanone conversion ratio 100% generates the selectivity 99.80% of cyclopentanol, without discovery catalyst after production operation
Bed has a bias current phenomenon, and catalyst life 12 months, catalyst volume landslide 7%.
Find out from embodiment 3 is same as 4 comparative test of embodiment, cage is added in general fixed bed high-pressure hydrogenation reactor
Formula heat exchanger reduces hot(test)-spot temperature in production, and conversion rate of products improves, and selectivity improves, and catalyst landslide amount reduces, and urges
Agent life.Good conjugation effect is obtained.
Claims (6)
1. the cage heat exchanger in a kind of catalytic hydrogenation reaction device, it is characterised in that: carried including heating medium inlet conduit (1), heat
Body distribution pipe (2), heat carrier distribution bobbin carriage (3), heat exchanger tube, support ring, heat carrier collect bobbin carriage (10), helix tube
(11), heat carrier collecting pipe (12) and heating medium outlet conduit (13)；The heating medium inlet conduit (1) is located at heat exchanger most
Upper end, heating medium inlet conduit (1) are connected with heat carrier distribution pipe (2), and heat carrier distribution pipe (2) connects heat carrier and distributes bobbin carriage
(3), heat carrier distribution bobbin carriage (3) is ring-shaped, and it is with one heart and circumferentially evenly arranged that heat carrier distribution bobbin carriage (3) is connected with multiple groups
Heat exchanger tube, heat exchanger tube are supported by Multi-layer supporting ring, and the lower end of heat exchanger tube is connected with heat carrier and collects bobbin carriage
(10), heat carrier is collected and is connected with the helix tube (11) that multiple groups are spiraled together, each helix tube (11) on the downside of bobbin carriage (10)
Lower end be all connected with heat carrier collecting pipe (12), the other end of heat carrier collecting pipe (12) is connected to heat exchanger the lowermost heat
On carrier outlet conduit (13).
2. the cage heat exchanger in catalytic hydrogenation reaction device according to claim 1, it is characterised in that: the heat exchanger column
Pipe includes inner ring heat exchanger tube (4), centre circle heat exchanger tube (5) and outer ring heat exchanger tube (6), and the support ring includes interior
Enclose support ring (7), centre circle support ring (8) and outer ring support ring (9)；Inner ring support ring (7) is equipped with air hole (14), inner ring support
The outer ring of ring (7) is equipped with equally distributed inner ring heat exchanger tube support slot identical with inner ring heat exchanger tube (4) quantity
(15), inner ring heat exchanger tube support slot (15) is welded together with inner ring heat exchanger tube (4)；During centre circle support ring (8) is equipped with
It encloses support ring inner cavity (16), the diameter of centre circle support ring inner cavity (16) is greater than the outer diameter of inner ring support ring (7), centre circle support ring
(8) outer ring is equipped with equally distributed centre circle heat exchanger tube support slot (17) identical with centre circle heat exchanger tube (5) quantity,
Centre circle heat exchanger tube support slot (17) welds together with centre circle heat exchanger tube (5)；Outer ring support ring (9) is equipped with outer ring branch
Pushing out ring inner cavity (18), the diameter of outer ring support ring inner cavity (18) are greater than the outer diameter of centre circle support ring (8), outer ring support ring (9)
Outer ring is equipped with equally distributed outer ring heat exchanger tube support slot (19) identical with outer ring heat exchanger tube (6) quantity, outer ring
Heat exchanger tube support slot (19) welds together with outer ring heat exchanger tube (6).
3. the cage heat exchanger in catalytic hydrogenation reaction device according to claim 1, it is characterised in that: the support ring exists
Vertical direction is equidistantly arranged.
4. the cage heat exchanger in catalytic hydrogenation reaction device according to claim 2, it is characterised in that: the inner ring support
Ring (7), centre circle support ring (8) and outer ring support ring (9) are successively equidistantly arranged in vertical direction, are considered as one group of support ring；According to
The length of cage heat exchanger has one or more groups of support rings.
5. the cage heat exchanger in catalytic hydrogenation reaction device according to claim 2, it is characterised in that: the inner ring heat exchange
Device tubulation (4), centre circle heat exchanger tube (5) and outer ring heat exchanger tube (6) are connected to the interior of heat carrier distribution bobbin carriage (3)
Circle, lower end and outer ring.
6. the cage heat exchanger in catalytic hydrogenation reaction device according to claim 1, it is characterised in that: the heat carrier point
Being piped (2) is the equally distributed pipeline of multiple circumferential directions, and lower end is connected to the upper end of heat carrier distribution bobbin carriage (3) of ring-shaped
Face.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821975477.1U CN209197530U (en) | 2018-11-28 | 2018-11-28 | A kind of cage heat exchanger in catalytic hydrogenation reaction device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821975477.1U CN209197530U (en) | 2018-11-28 | 2018-11-28 | A kind of cage heat exchanger in catalytic hydrogenation reaction device |
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| Publication Number | Publication Date |
|---|---|
| CN209197530U true CN209197530U (en) | 2019-08-02 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201821975477.1U Withdrawn - After Issue CN209197530U (en) | 2018-11-28 | 2018-11-28 | A kind of cage heat exchanger in catalytic hydrogenation reaction device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109186292A (en) * | 2018-11-28 | 2019-01-11 | 辽阳恒业化工有限公司 | A kind of cage heat exchanger in catalytic hydrogenation reaction device |
| CN115025722A (en) * | 2022-06-27 | 2022-09-09 | 辽阳恒业化工有限公司 | Equipment and method for producing cyclic ketone by oxidizing cycloolefin with nitrous oxide |
-
2018
- 2018-11-28 CN CN201821975477.1U patent/CN209197530U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109186292A (en) * | 2018-11-28 | 2019-01-11 | 辽阳恒业化工有限公司 | A kind of cage heat exchanger in catalytic hydrogenation reaction device |
| CN109186292B (en) * | 2018-11-28 | 2024-01-16 | 辽阳恒业化工有限公司 | Cage type heat exchanger in catalytic hydrogenation reactor |
| CN115025722A (en) * | 2022-06-27 | 2022-09-09 | 辽阳恒业化工有限公司 | Equipment and method for producing cyclic ketone by oxidizing cycloolefin with nitrous oxide |
| CN115025722B (en) * | 2022-06-27 | 2024-03-26 | 辽阳恒业化工有限公司 | Equipment and method for producing cyclic ketone by oxidizing cyclic olefin with nitrous oxide |
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