CN202237308U - Rectifying device for aqueous solutions of methanol and ethanol - Google Patents
Rectifying device for aqueous solutions of methanol and ethanol Download PDFInfo
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- CN202237308U CN202237308U CN 201120348715 CN201120348715U CN202237308U CN 202237308 U CN202237308 U CN 202237308U CN 201120348715 CN201120348715 CN 201120348715 CN 201120348715 U CN201120348715 U CN 201120348715U CN 202237308 U CN202237308 U CN 202237308U
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- 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
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/52—Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to a rectifying device for aqueous solutions of methanol and ethanol. A part of the device comprises a preheater, an evaporating tower, a distilling tower, a gas-water separator, and the like, wherein the evaporating tower is partitioned into an upper part and a lower part which are independent of each other by using a clapboard; the upper part of the evaporating tower is provided with an alcohol condenser; the lower part of the evaporating tower is provided with a gradient evaporator; the lower part of the distilling tower is provided with a residual liquid gradient evaporator; the middle part of the distilling tower is a primary distilling area; and the upper part of the distilling tower is a rectifying area. In the rectifying device, the gradient evaporator and the residual liquid gradient evaporator are arranged, so that evaporation can be divided into gradient dilute liquid evaporation and gradient residual liquid evaporation, the concentration of alcohols entering a primary distilling tower and the rectifying tower is increased, and a residual liquid can be discharged continually. Due to the adoption of the device, energy is recycled; safe water is taken as a medium, and is recycled through a thermal pump; the water medium absorbs the energy of alcohol vapor in a negative pressure state in an energy form; and completely clean vapor is introduced into the rectifying tower, so that internal parts of the rectifying tower are kept clean and protected from being corroded, and a bumping phenomenon is avoided.
Description
Technical field
The utility model relates to the rectifier unit of a kind of methyl alcohol, ethanol water, belongs to technical field of chemical.
Background technology
Methyl alcohol, ethanol are the common solvent of field of medicine and chemical technology, and it is lower and can not continue to use after using, usually to dissolve in generation water and the concentration that becomes in some chemical reactions, and can only carry out using after rectifying improves concentration again.The rectifier unit of methyl alcohol, ethanol is a rectifying column in the industry at present; The bottom of tower directly feeds Steam Heating or makes the aqueous solution of methyl alcohol, the ethanol vaporization back that is heated up through tubulation partition heating; The form with liquid sprays on the column plate under the effect of mouth spray from the middle part of tower for rare methyl alcohol or ethanol water; Condensate moisture is descending after carrying out the mass transfer heat exchange with the mixed vapour of the aqueous solution of up methyl alcohol or ethanol; After becoming gas up, methyl alcohol in the weak solution or ethanol evaporation carry out getting into condenser from the cat head steam outlet pipe after the mass transfer heat exchange with the methyl alcohol of overhead reflux or the phegma of ethanol again; Condensation rear section condensate liquid is back to and participates in heat exchange in the cat head once more, and a part gets into the certified products collecting tank as accomplishing liquid.
The condensation methyl alcohol of overhead reflux, ethanol need consumption of calorie to flash to gas again, so steam consumption is big.The methyl alcohol, ethanol gas that evaporates cat head condensation once more need consume a large amount of cooling waters, has improved the cost of mating power facility.Owing to chemical reaction process can produce some accessory substances inevitably, material gets into from the tower middle part, and long-play can pollute or tower internals such as obstruction filler or column plate by burn into.
The current device tower bottoms does not carry out gradient and steams, steam but mix, in the raffinate the difficult evaporation of residual alcohol fully, the raffinate terminal point contains the alcohol amount and is difficult to accurate control, is prone to make pure composition from raffinate, to take out of to cause run material.
The utility model content
According to above deficiency of the prior art, the technical problem that the utility model will solve is: a kind of above-mentioned defective that solved is provided, has reduced steam consumption, improved evaporation effect, avoided running the methyl alcohol of material phenomenon, the rectifier unit of ethanol water.
The utility model solves the technical scheme that its technical problem adopted: the rectifier unit of described methyl alcohol, ethanol water is characterized in that: comprise preheater, evaporating column, destilling tower, steam-water separator, wherein evaporating column is divided into independently two parts up and down by dividing plate; Top is provided with pure condenser; The bottom is provided with the gradient evaporimeter, and the bottom of destilling tower is provided with raffinate gradient evaporimeter, and the middle part is the fore-running district; Top is rectification zone; Be equipped with tail gas outlet and steam inlet on gradient evaporimeter and the raffinate gradient evaporimeter, the bottom is equipped with the raffinate outlet, and gradient evaporimeter top is provided with the mixed vapour outlet;
Rare pure inlet pipe is through being connected to place, gradient evaporimeter top position behind the preheater; The tail gas outlet of gradient evaporimeter is connected with the charging aperture of steam-water separator; The water out that coagulates of steam-water separator is connected with the water inlet pipe of pure condenser; The steam outlet pipe of alcohol condenser is connected with the steam inlet of gradient evaporimeter behind heat pump; The raffinate outlet of gradient base of evaporator is connected to the place, raffinate gradient evaporimeter top position of destilling tower through pipeline; The mixed vapour outlet on gradient evaporimeter top is connected at the fore-running district of destilling tower and the air diffuser between the rectification zone through pipeline; The discharging opening at destilling tower top is connected with the import of pure condenser through pipeline, and the pure condensate outlet of pure condenser is connected with the phegma import at destilling tower top with finished product alcohol jar through pipeline respectively, wherein is equipped with pump on the pipeline at the pure condensate outlet place of the raffinate outlet of coagulating water out, gradient base of evaporator of steam-water separator and pure condenser.
Described gradient evaporimeter and raffinate gradient evaporimeter include 2～20 evaporation trays that distribute from top to bottom; The two ends of each evaporation tray are equipped with tail gas outlet and steam inlet; The number of evaporation tray is preferably 8; Gradient evaporation is all adopted in the evaporation of thin liquid and raffinate, and every grade evaporate the steam that and all with the solution of upper level mass transfer, diabatic process are arranged, and has improved determining alcohol that gets into destilling tower and the serialization that realizes that raffinate is discharged.
The steam inlet of raffinate gradient evaporimeter links to each other with steam inlet tube, in whole technical process, has only raffinate gradient evaporimeter need use extra living steam.
When this device moved for the first time, the steam that the gradient evaporimeter needs was provided by the condensing water vapor steam that heat pump compresses in the pure condenser water outlet steam pipe.
Described preheater comprises first preheater and second preheater; The tail gas outlet of the gas vent of steam-water separator and raffinate gradient evaporimeter all is connected with the thermal medium inlet pipe of first preheater, and the raffinate outlet of raffinate gradient base of evaporator is connected with the thermal medium inlet pipe of second preheater.Can the heat in discharge tail gas and the raffinate be reclaimed, reduce energy waste.
The incoagulable gas of described pure condenser goes out pipe and a small amount of pure gas exports through being connected to finished product alcohol jar behind the condenser through on-condensible gas.To carry out condensing and recycling from the alcohol the incoagulable gas that pure condenser comes out, can further improve output.
The methyl alcohol of above-mentioned rectifier unit, the rectification process of ethanol water, methyl alcohol, alcohol dilute solution are gone in the preheater through filter is laggard, adopt 60 ℃～120 ℃ pressurized water steam heated after, further comprising the steps of:
Methyl alcohol after a, the preheating, alcohol dilute solution get into the gradient evaporimeter of evaporating column bottom, adopt 60 ℃～120 ℃ heat pump pressurized water steam to carry out the gradient evaporation, evaporate 65 ℃～85 ℃ mixed vapour;
B, to evaporate the mixed vapour that up, gets into the destilling tower middle part by the road; Tail gas after the evaporation gets into steam-water separator through the tail gas outlet, and isolated water gets into the pure condenser on evaporating column top by the road, uses as condensed water; Raffinate after the evaporation comes downwards to the evaporating column bottom, gets into the raffinate gradient evaporimeter of destilling tower bottom by the road, adopts 85 ℃～115 ℃ living Steam Heating gradient to carry residual; It is up to evaporate the gas that; After the fore-running section, mix with the mixed vapour that gets into from evaporating column, mix back hydrogenesis, descending along the fore-running section; Gas continues up; After mass-and heat-transfer is isolated moisture content, become pure pure steam at rectification zone and backflow alcoholic solution, get into the pure condenser on evaporating column top through the pipeline at destilling tower top;
C, in pure condenser, the water in the pure Steam Heating alcohol condenser is moisture content absorbs the heat energy of pure steam under negative pressure state after; Under negative pressure state, vaporize; Alcohol is condensed into liquid state, and 60% gets into finished product alcohol jar, and all the other 40% get into the destilling tower top as the backflow alcoholic solution;
D, evaporate the steam that in the pure condenser under the effect of heat pump, generate 60 ℃～120 ℃ steam after, get into the gradient evaporimeter of evaporating column bottom, use as heating steam.
Residual incoagulable gas gets in the condenser by the road in the alcohol condenser, and condensation goes out a spot of alcohol and gets into finished product alcohol jar, and incoagulable gas enters atmosphere.
Get in first preheater from the isolated hot gas of steam-water separator with from the tail gas that the outlet of the tail gas of raffinate gradient evaporimeter is discharged and to use as heat transferring medium, the hot raffinate of discharging from the raffinate outlet of raffinate gradient evaporimeter gets in second preheater and uses as heat transferring medium.
The beneficial effect that the utility model had is: the utility model is through being provided with gradient evaporimeter and raffinate gradient evaporimeter; Can make evaporation divide thin liquid evaporation and raffinate evaporation two parts; The gradient evaporation is all adopted in the evaporation of thin liquid and raffinate; And every grade evaporates the steam that and all with the solution of upper level mass transfer, diabatic process is arranged, and has improved the determining alcohol that gets into primary distillation tower and rectifying column, has realized the serialization of raffinate discharge; This device has been realized the recycling of energy, and is that the safe water of employing is that medium passes through the heat pump recycling; Utilize the mode of energy to make aqueous medium under negative pressure state, absorb the energy of pure steam; Get into rectifying column with cleaning steam fully, protected rectifying column internals cleaning and do not corroded, the bumping phenomenon do not occur.
Description of drawings
Fig. 1 is the structural representation of the utility model.
Among the figure: 1, first preheater; 2, second preheater; 3, evaporating column; 4, destilling tower; 5, steam-water separator; 6, pure condenser; 7, gradient evaporimeter; 8, raffinate gradient evaporimeter; 9, fore-running district; 10, rectification zone; 11, mixed vapour outlet; 12, rare pure inlet pipe; 13, heat pump; 14, air diffuser; 15, finished product alcohol jar; 16, evaporation tray; 17, transfer jar; 18, low-temperature condenser; 19, phegma import.
The specific embodiment
Below in conjunction with accompanying drawing the embodiment of the utility model is done and to further describe:
As shown in Figure 1, the rectifier unit of methyl alcohol, ethanol water comprises first preheater 1, second preheater 2, evaporating column 3, destilling tower 4, steam-water separator 5, and wherein evaporating column 3 is divided into independently two parts up and down by dividing plate; Top is provided with pure condenser 6; The bottom is provided with gradient evaporimeter 7, and the bottom of destilling tower 4 is provided with raffinate gradient evaporimeter 8, and the middle part is fore-running district 9; Top is rectification zone 10; Be equipped with tail gas outlet and steam inlet on gradient evaporimeter 7 and the raffinate gradient evaporimeter 8, the bottom is equipped with the raffinate outlet, and gradient evaporimeter 7 tops are provided with mixed vapour outlet 11;
Rare pure inlet pipe 12 is connected to place, gradient evaporimeter 7 top positions after through first preheater 1 and second preheater 2; The tail gas outlet of gradient evaporimeter 7 is connected with the charging aperture of steam-water separator 5; The water out that coagulates of steam-water separator 5 is connected with the water inlet pipe of pure condenser 6; The steam outlet pipe of alcohol condenser 6 is connected with the steam inlet of gradient evaporimeter 7 behind heat pump 13; The raffinate outlet of gradient evaporimeter 7 bottoms is connected to the place, raffinate gradient evaporimeter 8 top positions of destilling tower 4 through pipeline; The mixed vapour on gradient evaporimeter 7 tops outlet 11 is connected at the fore-running district 9 of destilling tower 4 and the air diffuser 14 between the rectification zone 10 through pipeline; The discharging opening at destilling tower 4 tops is connected through the import of pipeline with pure condenser 6; The pure condensate outlet of alcohol condenser 6 is connected with the phegma import 19 at destilling tower 4 tops through pipeline and finished product alcohol jars 15 respectively, wherein the raffinate of water out, gradient evaporimeter 7 bottoms with fixed attention of steam-water separator 5 export and the pipeline at the pure condensate outlet place of pure condenser 6 on be equipped with pump.
Gradient evaporimeter 7 includes 2～20 evaporation trays 16 that distribute from top to bottom with raffinate gradient evaporimeter 8, and the two ends of each evaporation tray 16 are equipped with tail gas outlet and steam inlet.
The tail gas outlet of the gas vent of steam-water separator 5 and raffinate gradient evaporimeter 8 all is connected with the thermal medium inlet pipe of first preheater 1, and the raffinate outlet of raffinate gradient evaporimeter 8 bottoms is connected with the thermal medium inlet pipe of second preheater 2.
The incoagulable gas of alcohol condenser 6 goes out pipe through being connected to finished product alcohol jar 15 behind the low-temperature condenser.
The pipeline in the exit of alcohol condenser 6 is provided with transfer jar 17.
Adopt the methyl alcohol of the rectifier unit of said apparatus, the rectification process of ethanol water, methyl alcohol, alcohol dilute solution adopt 60 ℃～120 ℃ pressurized water steam heated behind filter and in first preheater 1, second preheater 2, further comprising the steps of:
Methyl alcohol after a, the preheating, alcohol dilute solution get into the gradient evaporimeter 7 of evaporating column 3 bottoms, adopt the steam of 60 ℃～120 ℃ heat pump 13 compressions to carry out the gradient evaporation, evaporate 65 ℃～85 ℃ mixed vapour;
B, to evaporate the mixed vapour that up, gets into destilling tower 4 middle parts by the road; Tail gas after the evaporation gets into steam-water separator 5 through the tail gas outlet, and isolated water gets into the pure condenser 6 on evaporating column 3 tops by the road, uses as condensed water; Raffinate after the evaporation comes downwards to evaporating column 3 bottoms, gets into the raffinate gradient evaporimeter 8 of destilling tower 4 bottoms by the road, adopts 85 ℃～115 ℃ living Steam Heating gradient to carry residual; It is up to evaporate the gas that; After fore-running section 9, mix with the mixed vapour that gets into from evaporating column 3, mix back hydrogenesis, descending along fore-running section 9; Gas continues up; After mass-and heat-transfer is isolated moisture content, become pure pure steam at rectification zone 10 and backflow alcoholic solution, get into the pure condenser 6 on evaporating column 3 tops through the pipeline at destilling tower 4 tops;
C, in pure condenser 6, the water in the pure Steam Heating alcohol condenser 6 is moisture content absorbs the heat energy of pure steam under negative pressure state after; Under negative pressure state, vaporize; Alcohol is condensed into liquid state, and 60% gets into finished product alcohol jars 15, and all the other 40% get into destilling tower 4 tops as the backflow alcoholic solution;
D, evaporate the steam that in the pure condenser 6 under the effect of heat pump 13, generate 60 ℃～120 ℃ steam after, get into the gradient evaporimeter 7 of evaporating column 3 bottoms, use as heating steam.
Residual incoagulable gas gets in the low-temperature condenser 18 by the road in the alcohol condenser 6, and the alcohol that condensation goes out gets into finished product alcohol jar 15.
The pressure of the negative pressure state in the c step is-0.090～-0.095MPa.
Get in first preheater 1 from steam-water separator 5 isolated hot gas with from the tail gas that the outlet of the tail gas of raffinate gradient evaporimeter 8 is discharged and to use as heat transferring medium, the hot raffinate of discharging from the raffinate outlet of raffinate gradient evaporimeter 8 gets in second preheater 2 and uses as heat transferring medium.
Claims (5)
1. the rectifier unit of a methyl alcohol, ethanol water, it is characterized in that: comprise preheater, evaporating column, destilling tower, steam-water separator, wherein evaporating column is divided into independently two parts up and down by dividing plate; Top is provided with pure condenser; The bottom is provided with the gradient evaporimeter, and the bottom of destilling tower is provided with raffinate gradient evaporimeter, and the middle part is the fore-running district; Top is rectification zone; Be equipped with tail gas outlet and steam inlet on gradient evaporimeter and the raffinate gradient evaporimeter, the bottom is equipped with the raffinate outlet, and gradient evaporimeter top is provided with the mixed vapour outlet;
Rare pure inlet pipe is through being connected to place, gradient evaporimeter top position behind the preheater; The tail gas outlet of gradient evaporimeter is connected with the charging aperture of steam-water separator; The water out that coagulates of steam-water separator is connected with the water inlet pipe of pure condenser; The steam outlet pipe of alcohol condenser is connected with the steam inlet of gradient evaporimeter behind heat pump; The raffinate outlet of gradient base of evaporator is connected to the place, raffinate gradient evaporimeter top position of destilling tower through pipeline; The mixed vapour outlet on gradient evaporimeter top is connected at the fore-running district of destilling tower and the air diffuser between the rectification zone through pipeline; The discharging opening at destilling tower top is connected with the import of pure condenser through pipeline, and the pure condensate outlet of pure condenser is connected with the phegma import at destilling tower top with finished product alcohol jar through pipeline respectively, wherein is equipped with pump on the pipeline at the pure condensate outlet place of the raffinate outlet of coagulating water out, gradient base of evaporator of steam-water separator and pure condenser.
2. the rectifier unit of methyl alcohol according to claim 1, ethanol water; It is characterized in that: described gradient evaporimeter and raffinate gradient evaporimeter include 2～20 evaporation trays that distribute from top to bottom, and the two ends of each evaporation tray are equipped with tail gas outlet and steam inlet.
3. the rectifier unit of methyl alcohol according to claim 1, ethanol water; It is characterized in that: described preheater comprises first preheater and second preheater; The tail gas outlet of the gas vent of steam-water separator and raffinate gradient evaporimeter all is connected with the thermal medium inlet pipe of first preheater, and the raffinate outlet of raffinate gradient base of evaporator is connected with the thermal medium inlet pipe of second preheater.
4. the rectifier unit of methyl alcohol according to claim 1, ethanol water is characterized in that: the incoagulable gas of described pure condenser goes out pipe through being connected to finished product alcohol jar behind the low-temperature condenser.
5. the rectifier unit of methyl alcohol according to claim 1, ethanol water is characterized in that: the pipeline in the exit of described pure condenser is provided with the transfer jar.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201120348715 CN202237308U (en) | 2011-09-16 | 2011-09-16 | Rectifying device for aqueous solutions of methanol and ethanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201120348715 CN202237308U (en) | 2011-09-16 | 2011-09-16 | Rectifying device for aqueous solutions of methanol and ethanol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202237308U true CN202237308U (en) | 2012-05-30 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201120348715 Expired - Lifetime CN202237308U (en) | 2011-09-16 | 2011-09-16 | Rectifying device for aqueous solutions of methanol and ethanol |
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| Country | Link |
|---|---|
| CN (1) | CN202237308U (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102430254A (en) * | 2011-09-16 | 2012-05-02 | 徐建涛 | Rectification technology and apparatus of aqueous solution of methanol or ethanol |
| CN103252105A (en) * | 2013-05-29 | 2013-08-21 | 山东道先为能源科技有限公司 | Methyl alcohol pressure reducing and distilling device |
| CN103981034A (en) * | 2014-05-19 | 2014-08-13 | 东莞新宝精化有限公司 | Method and special device for continuously recycling methanol tail gas in biodiesel production |
| CN110124357A (en) * | 2019-05-13 | 2019-08-16 | 江苏九九久科技有限公司 | Volatile impurity removes easy device in fluid |
| CN115253348A (en) * | 2022-07-11 | 2022-11-01 | 山东凯斯达机械制造有限公司 | Evaporation device and process for mixed oil of leaching system |
-
2011
- 2011-09-16 CN CN 201120348715 patent/CN202237308U/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102430254A (en) * | 2011-09-16 | 2012-05-02 | 徐建涛 | Rectification technology and apparatus of aqueous solution of methanol or ethanol |
| CN102430254B (en) * | 2011-09-16 | 2013-09-04 | 徐建涛 | Rectification technology and apparatus of aqueous solution of methanol or ethanol |
| CN103252105A (en) * | 2013-05-29 | 2013-08-21 | 山东道先为能源科技有限公司 | Methyl alcohol pressure reducing and distilling device |
| CN103252105B (en) * | 2013-05-29 | 2015-03-04 | 山东道先为能源科技有限公司 | Methyl alcohol pressure reducing and distilling device |
| CN103981034A (en) * | 2014-05-19 | 2014-08-13 | 东莞新宝精化有限公司 | Method and special device for continuously recycling methanol tail gas in biodiesel production |
| CN110124357A (en) * | 2019-05-13 | 2019-08-16 | 江苏九九久科技有限公司 | Volatile impurity removes easy device in fluid |
| CN115253348A (en) * | 2022-07-11 | 2022-11-01 | 山东凯斯达机械制造有限公司 | Evaporation device and process for mixed oil of leaching system |
| CN115253348B (en) * | 2022-07-11 | 2023-10-20 | 山东凯斯达机械制造有限公司 | Evaporation device and technology for mixed oil of leaching system |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20120530 Effective date of abandoning: 20130904 |
|
| RGAV | Abandon patent right to avoid regrant |