CN2116523U - Absorption condensation tower for manufacturing formaldehyde - Google Patents
Absorption condensation tower for manufacturing formaldehyde Download PDFInfo
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- CN2116523U CN2116523U CN 92203090 CN92203090U CN2116523U CN 2116523 U CN2116523 U CN 2116523U CN 92203090 CN92203090 CN 92203090 CN 92203090 U CN92203090 U CN 92203090U CN 2116523 U CN2116523 U CN 2116523U
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Abstract
The utility model relates to an absorption condensing tower for producing formaldehyde by the oxidation and the dehydrogenation of methanol (a silver method). The absorption condensing tower is integral tower equipment which is composed of upper, middle and lower three direct heat removal sections accompanied with absorption mass transfer functions. The two-stage heat transmission in the prior art is converted into one-stage heat transmission by the structure; energy loss is farthest used for impelling a transmission process; back mixing absorption is converted into countercurrent flow absorption and three-stage countercurrent flow absorption, and back mixing is completely eliminated by mass transfer. The operations of two units are combined into the operation of a unit to finish. The equipment efficiency is enhanced, the energy consumption is little, and the equipment investment is reduced more than one time than the original investment.
Description
The utility model relates to the commercial plant that formaldehyde (silver-colored method) is produced in the methanol oxidation dehydrogenation.
Up to now, both at home and abroad the contained formaldehyde gas and absorption, the condensation process of water vapour are mostly finished in three sections absorption equipments of two towers in formaldehyde (the silver-colored method gaseous oxidation) product, and accompanying drawing 1 is this equipment schematic diagram.1 is the tower I in the accompanying drawing 1, is called first section in the flow process, is packed tower.2 is tower II lower semisection, is called second section on stream, is also constituted by filler.3 is tower II upper semisection, is called the 3rd section in the flow process, by column plate is constituted.4 is water recirculator.5 is the chilled water cooler.6 is recycle liquid pump.The weak point of said process be except that the 3rd section for the counter-current absorption, first and second section is the balance back-mixing and absorbs.With regard to the 3rd section counter-current absorption, because supplementing water seldom, the water that absorbed here formaldehyde and condensation are got off also seldom only accounts for a few percent of total amount.The a large amount of formalins that surpass tens of times of product flows then circulate between absorption tower and cooler, and circulation fluid change in concentration in tower is little, and temperature rise also has only about 10 ℃.In fact, be to absorb water vapour condensation heat and formaldehyde heat of solution by the circulation fluid temperature rise, by cooler heat is drained into environment again.Whole process is that two-stage is conducted heat, the temperature difference is very limited again, so the heat transfer area that inner-tower filling material surface area and cooler need is all very big, absorption efficiency is low again, the circulating pump power consumption is many in addition, and two-stage heat transfer gained heat energy potential temperature is very low, can only be taken away by cooler, be difficult to utilize, but also must expend a large amount of recirculated waters and chilled water expense.Have the minority device to adopt two sections in single tower or three sections absorptions, but essence is still identical with above-mentioned situation.
The purpose of this utility model is to overcome above-mentioned weak point of the prior art and a kind of change two-stage heat transfer is provided is that one-level is conducted heat,
Decrease and be used to promote transmittance process to greatest extent; Become back-mixing and be absorbed as counter-current absorption, in a tower, absorption condensation and two unit operations of heat exchange are combined into the absorption condensation tower that a unit operations is finished.
The purpose of this utility model can reach by following measure:
A kind of absorption condensation tower that is used for Formaldehyde Production is characterized in that comprising in the whole tower three of upper, middle and lower and has the direct heat-obtaining section that absorbs mass transfer function concurrently.Between liquid distribution trough and the circulation fluid inlet is epimere, and it is to be arranged with level from top to bottom by the heat transfer coiled pipe to form, and the stagger mode of 45 ° of triangular in shape or square oblique commentaries on classics of per two comb dies is arranged; Between circulation fluid inlet and the outlet of product formalin be the stage casing, and circulation fluid enters the mouth and communicates with distributor, is the heat transfer coiled pipe below the distributor, and heat transfer serpentine type arrangement mode is identical with epimere heat transfer serpentine type arrangement mode; Below the product formalin outlet is hypomere, and hypomere is equipped with level and arranges, the heat transfer comb that pipe end and bobbin carriage connect mutually, 45 ° of arrangements of the triangular in shape or square oblique commentaries on classics of heat transfer comb; Be provided with the catch box of product formalin outlet between stage casing and the hypomere, catch box is one by the peripheral space that is constituted with the tower wall of riser; To the tower wall that conducts heat below the comb, offer the product inlet more than the liquid storage position at the bottom of the tower.
Heat transfer coiled pipe or heat transfer comb are rolling processing and dredge the low ribbed pipe of profile of tooth in the tower.
Accompanying drawing 1 is that prior art two towers absorb flow process and equipment schematic diagram for three sections.
Accompanying drawing 2 is the utility model absorption condensation tower structure schematic diagram, and wherein the A-A profile is the riser distribution schematic diagram, and the B-B profile is that heat transfer comb and bobbin carriage connect schematic diagram.
The utility model embodiment in conjunction with the accompanying drawings is described in further detail:
One contains the absorption condensation tower that three of upper, middle and lower have the direct heat-obtaining section that absorbs mass transfer function concurrently, between liquid distribution trough 9 and the circulation fluid inlet 22 is epimere, it is to be arranged with level from top to bottom by heat transfer coiled pipe 10 to form, and stagger triangularity or square of per two comb dies tiltedly changes 45 ° mode and arrange; Between circulation fluid inlet 22 and the product formalin outlet 14 be the stage casing, and circulation fluid inlet 22 communicates with distributor 11, and distributor 11 is following to be heat transfer coiled pipe 12, and heat transfer coiled pipe 12 arrangement modes are identical with epimere heat transfer coiled pipe 10 arrangement modes; Product formalin outlet is a hypomere below 14, and hypomere is equipped with level and arranges, the heat transfer comb 15 that pipe end and bobbin carriage 16 connect mutually, 45 ° of arrangements of heat transfer comb 15 triangular in shape or square oblique commentaries on classics; Be provided with the catch box 13 of product formalin outlet 14 between stage casing and the hypomere, catch box 13 is one by the riser 20 peripheral spaces that constituted with the tower wall; The distribution of riser 20 is shown in accompanying drawing 2A-A profile, and the top of riser 20 is provided with and prevents that liquid phase from falling into the plate washer 21 of riser 20; To the tower wall of comb below 15 that conduct heat, offer product inlet 18 more than the liquid storage position at the bottom of the tower.The 8th, window.
The product inlet 18 of product self-absorption condensing tower hypomere after chilling and heat exchange enters, liquid phase exports 19 after a circulating pump and cooler cooling by circulation liquid phase at the bottom of the tower, drench on stage casing heat transfer coiled pipe 12 by distributor 11 through circulation fluid inlet 22, make circulation liquid phase enrichment with the formaldehyde in the further absorption gas phase.When gas phase rose through hypomere heat transfer comb 15 outer surfaces, water vapour wherein was in the 15 surface condensation heat releases of heat transfer comb, and simultaneously, the water that is condensed of the formaldehyde in the gas phase absorbs heat release, and above-mentioned heat all is used to conduct heat, and soft water heat up in the comb 15.
Rise through hypomere heat transfer comb 15 back gas phases, because of the condensation of part water vapour and formaldehyde absorb lower the temperature subtract dense, subtract dense back and enter the stage casing by riser 20, in the stage casing, continue to subtract dense in the 12 outer surface condensations of heat transfer coiled pipe, absorption, heat release cooling, and then the heat transfer coiled pipe 10 of process epimere, the condensation absorption process is the same, pass through double overflow tray absorption columns section 26 at last, absorb residual formaldehyde by supplementing water, reach tail gas and discharge standard, and the mist eliminator through being positioned at cat head 7, behind the drop that capture is carried, export 28 from tower by tail gas.
The cold soft water that the heat-obtaining medium is 30～35 ℃ is entered outside the pipe of epimere heat transfer coiled pipe 10 by inlet 23, heat up with rising gas phase countercurrent flow, entering stage casing heat transfer coiled pipe (12) then continues to heat up with the gas phase countercurrent flow, entering hypomere heat transfer comb (15) again becomes 50 ℃～55 ℃ hot soft water with the gas phase countercurrent flow, supplies with low temperature heat energy by hot soft water mouth 17 outlets to the user.Lowering the temperature into cold soft water after emitting heat energy recycles.Epimere coiled pipe top is the cryogenic condensation absorber portion, and 20～25 ℃ the cooling water that comes the self-circulating water field is entered by outlet 24 by inlet 25 and draws; High temperature season is used chilled water instead.
The low temperature supplementing water is introduced through after the double overflow tray absorption columns section 26 by interface 27, spray epimere heat transfer coiled pipe 10 outer surfaces by a liquid re-distributor 9, with at heat transfer coiled pipe surface condensation with absorbed the aqueous solution of formaldehyde, conduct heat on the coiled pipe 12 in the stage casing of dripping.
The circulation fluid that comes at the bottom of tower sprays stage casing coiled pipe outer surface from circulation fluid inlet 22 through distributor 11, continue to absorb formaldehyde in the gas phase with water in the condensation of coiled pipe case surface, reach product design and in catch box 13, collect, go out tower by product formalin outlet 14.
The utility model has following advantage compared to existing technology:
1, three sections absorption equipments of former two towers change single suction of the present utility model into and receive condensing tower, bring marked change to technological process, be that former two towers become a tower, former two big pumps become with the little pump of a power much smaller than former pump, former three heat exchangers replace with a littler heat exchanger, device efficiency improves greatly, and equipment investment is than originally reducing more than one times.
2, be that one-level is conducted heat because becoming the two-stage heat transfer, and greatly reduce heat transfer
Decrease, and under the suitable driving force of heat transfer condition of maintenance, improve the heat-obtaining potential temperature of cooling medium. Except summer need to be with a small amount of chilled water, most condensations, absorb heat and take out for suitable Low Temperature Thermal user utilization in 30～50 ℃ or 35～55 ℃ of temperature ranges by circulation soft water. Thereby increased heat utilization rate, greatly saved the energy consumption of recirculated water and chilled water.
3, the three stage countercurrents absorption mass transfer of the utility model employing has been eliminated a large amount of liquid-circulatings in the back-mixing absorption flow process fully, thereby has greatly saved the power consumption of circulating pump.
Claims (2)
1, a kind of absorption condensation tower that is used for Formaldehyde Production, it is characterized in that comprising in the whole tower three of upper, middle and lower and have the direct heat-obtaining section that absorbs mass transfer function concurrently, between liquid distribution trough and the circulation fluid inlet is epimere, it is to be arranged with level from top to bottom by the heat transfer coiled pipe to form, and the stagger mode of 45 ° of triangular in shape or square oblique commentaries on classics of per two comb dies is arranged; Between circulation fluid inlet and the outlet of product formalin be the stage casing, and circulation fluid enters the mouth and communicates with distributor, is the heat transfer coiled pipe below the distributor, and heat transfer serpentine type arrangement mode is identical with epimere heat transfer serpentine type arrangement mode; Below the product formalin outlet is hypomere, and hypomere is equipped with level and arranges, the heat transfer comb that pipe end and bobbin carriage connect mutually, 45 ° of arrangements of the triangular in shape or square oblique commentaries on classics of heat transfer comb; Be provided with the catch box of product formalin outlet between stage casing and the hypomere, catch box is one by the peripheral space that is constituted with the tower wall of riser; To the tower wall that conducts heat below the comb, offer the product inlet more than the liquid storage position at the bottom of the tower.
2, a kind of absorption condensation tower that is used for Formaldehyde Production according to claim 1 is characterized in that interior heat transfer coiled pipe of tower or heat transfer comb are rolling processing and dredge the low ribbed pipe of profile of tooth.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 92203090 CN2116523U (en) | 1992-02-24 | 1992-02-24 | Absorption condensation tower for manufacturing formaldehyde |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 92203090 CN2116523U (en) | 1992-02-24 | 1992-02-24 | Absorption condensation tower for manufacturing formaldehyde |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2116523U true CN2116523U (en) | 1992-09-23 |
Family
ID=4949785
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 92203090 Granted CN2116523U (en) | 1992-02-24 | 1992-02-24 | Absorption condensation tower for manufacturing formaldehyde |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2116523U (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101486633B (en) * | 2009-02-11 | 2012-04-18 | 王承信 | Formaldehyde absorbing tower |
| CN101544550B (en) * | 2009-04-20 | 2013-03-20 | 中国蓝星（集团）股份有限公司 | Formaldehyde absorbing tower dealcoholizing technology |
| CN104174259A (en) * | 2014-08-27 | 2014-12-03 | 江苏凯茂石化科技有限公司 | Coupling device for methanol evaporation and formaldehyde absorption |
| CN104971601A (en) * | 2014-04-10 | 2015-10-14 | 中国石油化工股份有限公司 | Acid gas vertical reactor and processing method |
| CN106311091A (en) * | 2015-07-03 | 2017-01-11 | 常州乔尔塑料有限公司 | Formaldehyde oxidation reactor with two stage high efficiency heat exchange |
-
1992
- 1992-02-24 CN CN 92203090 patent/CN2116523U/en active Granted
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101486633B (en) * | 2009-02-11 | 2012-04-18 | 王承信 | Formaldehyde absorbing tower |
| CN101544550B (en) * | 2009-04-20 | 2013-03-20 | 中国蓝星（集团）股份有限公司 | Formaldehyde absorbing tower dealcoholizing technology |
| CN104971601A (en) * | 2014-04-10 | 2015-10-14 | 中国石油化工股份有限公司 | Acid gas vertical reactor and processing method |
| CN104174259A (en) * | 2014-08-27 | 2014-12-03 | 江苏凯茂石化科技有限公司 | Coupling device for methanol evaporation and formaldehyde absorption |
| CN106311091A (en) * | 2015-07-03 | 2017-01-11 | 常州乔尔塑料有限公司 | Formaldehyde oxidation reactor with two stage high efficiency heat exchange |
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| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C20 | Patent right or utility model deemed to be abandoned or is abandoned | ||
| CF01 | Termination of patent right due to non-payment of annual fee |