CN205919713U - Novel heat transfer system of no tube sheet methanol oxidation ware - Google Patents
Novel heat transfer system of no tube sheet methanol oxidation ware Download PDFInfo
- Publication number
- CN205919713U CN205919713U CN201620904786.4U CN201620904786U CN205919713U CN 205919713 U CN205919713 U CN 205919713U CN 201620904786 U CN201620904786 U CN 201620904786U CN 205919713 U CN205919713 U CN 205919713U
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- China
- Prior art keywords
- barrel
- cylinder
- heat transfer
- heat exchanger
- heat
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 238000012546 transfer Methods 0.000 title claims abstract description 15
- 238000007254 oxidation reaction Methods 0.000 title abstract description 5
- 230000003647 oxidation Effects 0.000 title abstract description 4
- 238000006243 chemical reaction Methods 0.000 claims abstract description 37
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000007921 spray Substances 0.000 claims abstract description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000001301 oxygen Substances 0.000 claims abstract description 6
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 6
- 239000012495 reaction gas Substances 0.000 claims abstract description 5
- 230000008676 import Effects 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 4
- 238000005507 spraying Methods 0.000 abstract 3
- 241000270295 Serpentes Species 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 description 22
- 239000007789 gas Substances 0.000 description 8
- 238000000034 method Methods 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 5
- 238000013461 design Methods 0.000 description 4
- 238000005336 cracking Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 238000003466 welding Methods 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003287 optical effect Effects 0.000 description 1
- 238000005839 oxidative dehydrogenation reaction Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 230000000452 restraining effect Effects 0.000 description 1
Abstract
The utility model provides a novel heat transfer system of no tube sheet methanol oxidation ware, includes the barrel, the conversion zone is installed on the upper portion of barrel, the upper portion of conversion zone is formed with the oxygen reaction room, the conversion zone lower part is the fixation reaction bed, heat transfer spraying system is installed to the lower part of fixation reaction bed, heat transfer spraying system includes many snake -shaped structure's heat exchange tube, install the fin on the heat exchange tube, one side wall mounting that lies in the barrel sprays the mouth, and a lateral wall lower part that lies in the barrel is provided with reaction gas and exports, add the lower part in the barrel has high concentration formaldehyde to lateral wall bottom at the barrel sets up the discharge port. Through the heat transfer spraying system's that sets up in the barrel effect, improve equipment's life greatly, can the life -span reach 10 15 year, greatly increased the productivity, the productivity can reach more than 200, 000 tons every year, compares with equipment among the prior art, same big reaction bed area, productivity and life -span are all than higher.
Description
Technical field
This utility model is related to technical field of heat exchange equipment, the heat exchange system of especially a kind of new no tube sheet methanol oxidator
System.
Background technology
Due to needing (630 degrees Celsius ~ 650 degrees Celsius) at high operating temperatures to carry out oxidative dehydrogenation during silver-colored method technique productions formaldehyde
Reaction is obtained formaldehyde gases.Demand passes through high-temperature region within the time short to the greatest extent, prevents over oxidation from producing by-product.Oxidation
Dehydrogenation reaction is an exothermic reaction, produces substantial amounts of heat energy during the course of the reaction simultaneously, and this partial heat energy need to pass through to change in time
Hot form changes into the energy of other forms, cools down reacting gas rapidly, thus ensureing product quality indicator, not because of high-temperature acid
Changing leads to product unqualified.Methanol oxidator is the important process units all of reaction conversion of production formaldehyde is all in reactor
In complete.Because working condition is extremely harsh, equipment is caused greatly injure.General oxidator service life was in 2 ~ 3 years.
Oxidator primary structure is fixing reaction bed and fixed tube-sheet exchanger two parts composition.
The reason mainly equipment is caused damage is:
1st, contain substantial amounts of hydrogen in reaction product, under the condition of high temperature, make stainless steel material and welding position produce hydrogen embrittlement
And stress corrosion, cause weld cracking.
2nd, due to being changed using rear quality of parent material, welding performance substantially reduces, and maintenance is extremely difficult, often can only use
The method of closure heat exchange pipeline solves the problems, such as equipment leakage.Cause the forfeiture of heat exchange area, affect normal production capacity.
3rd, cooling water produces portion gas in evaporation and produces cavitation to stainless steel pipes, simultaneously as tube sheet reaction side
At 630 DEG C ~ 650 DEG C, tube sheet changes 150 DEG C ~ 155 DEG C of hot side temperature (medium is water, pressure 0.25mpa), both sides thermal expansion to temperature
Coefficient differs greatly, and causes heat exchanger tube fracture to lose efficacy.
4th, the restriction of production capacity: production capacity is directly proportional by catalyst reaction area to reactant, and response area is bigger, and production capacity is got over
Greatly.Due to the particularity of working condition, device structure, domestic and international single device maximum production capacity at 80,000 tons/year, get over by production capacity now
Big equipment produces the probability higher (mainly heat exchanger tube and weld cracking) losing efficacy.So going back below 80,000 tons/year in production capacity
It is both economical (reactor changing 80,000 tons/year of a production capacity is about at 2,000,000 yuans).
Utility model content
The applicant is directed to the shortcoming in above-mentioned existing production technology, provides a kind of new no tube sheet methanol rational in infrastructure
The heat-exchange system of oxidator, such that it is able to improve reactor heat-exchange system service life, reduces production cost.
The technical scheme that this utility model is adopted is as follows:
A kind of heat-exchange system of new no tube sheet methanol oxidator, including cylinder, the top of described cylinder is provided with reaction
Layer, the top of described conversion zone is formed with oxygen reaction room, and described conversion zone bottom is fixing reaction bed, described fixing reaction bed
Bottom heat transfer spray system is installed, described heat transfer spray system includes the heat exchanger tube of many u shape structures, on described heat exchanger tube
Fin is installed；On the side wall of cylinder, mouth spray is installed, the lower sidewall positioned at cylinder is provided with reacting gas
Outlet, in described cylinder, bottom adds high-concentration formaldehyde, and the sidewall bottom setting outlet in cylinder.
Improvement further as technique scheme:
The inside of described cylinder is distributed with the heat exchanger tube of many u shape structures, the heat exchanger tube of many u shape structures from front to back according to
Secondary arrangement, the outer wall extending to cylinder imported and exported by every heat exchanger tube, and all in the same side.
Mouth spray is located at the bottom of heat exchanger tube.
The beneficial effects of the utility model are as follows:
This utility model compact conformation, reasonable, easy to operate, the work of the heat transfer spray system by arranging in cylinder
With the service life of equipment can be greatly improved, and the life-span, up to 10-15, considerably increases production capacity, and production capacity can reach 20 every year
More than ten thousand tons, compared with equipment in prior art, equally big reaction bed area, production capacity and the life-span all higher.
This utility model advantage also specific as follows:
(1) improve reactor heat-exchange system service life, reduce production cost.
(2) improve the coefficient of heat conduction of heat-exchange system it is ensured that heat transfer effect, for improving production capacity service.
(3) reduce device fabrication cost.
(4) technology of high-performance reactor of the present utility model is to initiate both at home and abroad, maintains the leading position, equipment uses the longevity
Up to 10 ~ 15 years, production capacity can reach more than 200,000 tons/year to life.Market prospect is considerable.
(5) this utility model solves the problems, such as frequent leakage failure that fixed tube-sheet exchanger form brought, solves
The thermal expansion stress problem being caused due to high temperature, increases the heat exchanger tube coefficient of expansion；Also improve the heat exchanger coefficient of conductivity.
Brief description
Fig. 1 is structural representation of the present utility model.
Fig. 2 is the scattergram of the heat exchanger tube of this utility model heat-exchange system.
Wherein: 1, oxygen reaction room；2nd, fixing reaction bed；3rd, conversion zone；4th, heat transfer spray system；5th, mouth spray；6th, cylinder
Body；7th, high-concentration formaldehyde；8th, reaction gas outlet；9th, outlet；10th, heat exchanger tube；11st, fin.
Specific embodiment
Below in conjunction with the accompanying drawings, specific embodiment of the present utility model is described.
As depicted in figs. 1 and 2, the heat-exchange system of the new no tube sheet methanol oxidator of the present embodiment, including cylinder 6, cylinder
The top of body 6 is provided with conversion zone 3, and the top of conversion zone 3 is formed with oxygen reaction room 1, and conversion zone 3 bottom is fixing reaction bed
2, the bottom of fixing reaction bed 2 is provided with heat transfer spray system 4, and heat transfer spray system 4 includes the heat exchanger tube of many serpentine configuration
10, heat exchanger tube 10 is provided with fin 11；Mouth spray 5 is provided with the side wall of cylinder 6, positioned at the side wall of cylinder 6
Bottom is provided with reaction gas outlet 8, and in cylinder 6, bottom adds high-concentration formaldehyde 7, and the sidewall bottom in cylinder 6 sets
Put outlet 9.
The inside of cylinder 6 is distributed with the heat exchanger tube 10 of many serpentine configuration, and the heat exchanger tube 10 of many serpentine configuration is from going to
After be arranged in order, the outer wall extending to cylinder 6 imported and exported by every heat exchanger tube 10, and all in the same side.
Mouth spray 5 is located at the bottom of heat exchanger tube 10.
During actually used, in oxygen reaction room 1, carry out oxidation reaction, be arranged on heat transfer spray system 4 work of bottom
Make, lowered the temperature, worked by heat exchanger tube 10 and mouth spray 5 simultaneously, the effect of rapid cooling, institute in temperature-fall period can be reached
The steam part producing can be discharged recovery and be recycled in systems, and another part can supply outward；Reacted gas is from reaction
Gas outlet 8 discharges, and discharges high-concentration formaldehyde 7 in the bottom discharge outlet 9 of cylinder 6.
This utility model arranges chilling under no tube sheet support reaction bed and but sprays water spray system, make reacting gas temperature from
650 DEG C are quenched to 300 DEG C, and (cooling water can be used as GAS ABSORPTION, and reduces absorption tower water consumption, is so also beneficial to produce
The formaldehyde of high concentration (up to more than 57%)) so ensure that reacting gas and liquid temperature when through heat exchanger tube 10 substantially reduce,
Improve heat exchanger tube 10 allowable stress at the working temperature, increase the intensity of heat exchanger tube 10.Reduce and allowable answering is caused due to high temperature
Power declines and causes heat exchanger tube 10 cracking risk that intensity deficiency brings.
Heat exchanger tube 10 of the present utility model adopts u shape structure, is conducive to restraining the raising of bulk expansion coefficient.Once changing
When heat pipe 10 lost efficacy, cost that can be minimum more renews tube bank, causes the device to run well again.
Heat exchanger tube 10 of the present utility model adopts fin 11 form, rather than Conventional optical tube, substantially increases the coefficient of heat conduction
And heat exchange efficiency, reduce material cost.
The reasonability of this utility model manufacturing process: all design premises must assure that equipment in process can be complete
Implement, it is to avoid cause difficulty of processing and increase processing cost.For this reason, before construction coordinate design, production, technology, technique
Determine rational production technology it is ensured that the quality of product and project can reach design effect.
This utility model heat-exchange system leakage probability designs than original device and declines raising 80%, and thermal coefficient of expansion improves 50%,
The coefficient of heat conduction improves 30%～35%, and service life of equipment reaches more than 10～15 years.
Above description is to explanation of the present utility model, is not the restriction to utility model, and this utility model is limited
Scope, referring to claim, within protection domain of the present utility model, can make any type of modification.
Claims (3)
1. a kind of heat-exchange system of new no tube sheet methanol oxidator it is characterised in that: include cylinder (6), described cylinder (6)
Top is provided with conversion zone (3), and the top of described conversion zone (3) is formed with oxygen reaction room (1), described conversion zone (3) bottom
For fixing reaction bed (2), the bottom of described fixing reaction bed (2) is provided with heat transfer spray system (4), described heat transfer spray system
(4) include the heat exchanger tube (10) of many serpentine configuration, described heat exchanger tube (10) is provided with fin (11)；Positioned at cylinder (6)
Mouth spray (5) is provided with the wall of side, a lower sidewall of cylinder (6) is provided with reaction gas outlet (8), described cylinder
(6) interior bottom adds high-concentration formaldehyde (7), and sidewall bottom setting outlet (9) in cylinder (6).
2. as claimed in claim 1 new no tube sheet methanol oxidator heat-exchange system it is characterised in that: described cylinder (6)
Inside the heat exchanger tube (10) of many piece u shape structures is distributed with, the heat exchanger tube (10) of many serpentine configuration is arranged in order from front to back,
Every heat exchanger tube (10) imports and exports the outer wall extending to cylinder (6), and all in the same side.
3. as claimed in claim 1 new no tube sheet methanol oxidator heat-exchange system it is characterised in that: mouth spray (5) position
Bottom in heat exchanger tube (10).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620904786.4U CN205919713U (en) | 2016-08-19 | 2016-08-19 | Novel heat transfer system of no tube sheet methanol oxidation ware |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620904786.4U CN205919713U (en) | 2016-08-19 | 2016-08-19 | Novel heat transfer system of no tube sheet methanol oxidation ware |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205919713U true CN205919713U (en) | 2017-02-01 |
Family
ID=57871613
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620904786.4U Active CN205919713U (en) | 2016-08-19 | 2016-08-19 | Novel heat transfer system of no tube sheet methanol oxidation ware |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205919713U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106123642A (en) * | 2016-08-19 | 2016-11-16 | 无锡市华立石化工程有限公司 | The heat-exchange system of the novel oxidator of methanol without tube sheet |
-
2016
- 2016-08-19 CN CN201620904786.4U patent/CN205919713U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106123642A (en) * | 2016-08-19 | 2016-11-16 | 无锡市华立石化工程有限公司 | The heat-exchange system of the novel oxidator of methanol without tube sheet |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 214126 Gedai Community, Xuelang Street, Binhu District, Wuxi City, Jiangsu Province Patentee after: Wuxi Huali Juneng Equipment Co.,Ltd. Address before: 214126 Gedai Community, Xuelang Street, Binhu District, Wuxi City, Jiangsu Province Patentee before: WUXI HUALI PETROLEUM AND CHEMICAL ENGINEERING Co.,Ltd. |
|
| CP01 | Change in the name or title of a patent holder |