CN1101374A - Process and apparatus for utilizing negtive pressure secondary steam from oil extracting factory - Google Patents
Process and apparatus for utilizing negtive pressure secondary steam from oil extracting factory Download PDFInfo
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- CN1101374A CN1101374A CN 94100336 CN94100336A CN1101374A CN 1101374 A CN1101374 A CN 1101374A CN 94100336 CN94100336 CN 94100336 CN 94100336 A CN94100336 A CN 94100336A CN 1101374 A CN1101374 A CN 1101374A
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Abstract
In oil extracting factory, plant oil is extracted by negative pressure evaporation and secondary utilization of steam. Its apparatus includes mechanical vacuum pump, negative-pressure evaporator, vacuum condenser, and intermediate pot and pump. The process can save steam, electric power and water.
Description
The present invention discloses a kind of oil extraction plant vegetables oil reparation technology and equipment, and specifically grease leaches and adopts the negative pressure evaporation secondary steam to utilize Processes and apparatus.
The invention belongs to the Vegetable oil lipoprotein preparation technique.
Existing vegetable oil mill adopts solvent extraction legal system oil mode usually, and oil plant forms two-phase after solvent extraction, i.e. liquid phase and solid phase, and liquid phase is a mixing oil, solid phase removes solvent for the mixing oil that the wet dregs of rice contain grease and a large amount of solvents by processes such as atmospheric evaporations; The solvent-laden wet dregs of rice are used drying with steam in evapo-separated machine, be the finished product dregs of rice after volatilizing secondary steam, one of key character of this method of making oil is, mixing oil continues to be processed into the leaching crude oil after atmospheric pressure state goes out a large amount of solvents by first evaporator evaporation, first vaporizer adopts live steam as heating medium, and it consumes heat energy and accounts for 65% of mixing oil processing whole process; And the wet dregs of rice take off a large amount of secondary steams of process institute evaporable in steaming and directly go condenser condenses, and a major defect of this method of making oil is, miscella evaporation adopts live steam as heating medium, and power consumption is big; And evapo-separated machine evaporable secondary steam Yin Wendu is on the low side, and heat transfer power is little, can not be used effectively and directly goes condensation, and the water consumption power consumption also wastes energy.
The purpose of this invention is to provide a kind of negative pressure evaporation secondary steam and utilize Processes and apparatus, it evaporates mixing oil under negative pressure state, can reduce about 20 ℃ of mixing oil boiling boiling point, thereby obviously improve secondary steam and mixing oil boiling point effective temperature difference between the two, increase heat transfer power, make and effectively to utilize the evapo-separated machine secondary steam feasible, put into practice availablely, realized the saving steam and the energy-saving and water-saving of miscella evaporation and secondary steam condensation process as miscella evaporation thermal source theory.
Technical scheme of the present invention is: adopt a kind of negative pressure evaporation secondary steam to utilize Processes and apparatus, it makes rare mixing oil (vacuum tightness 5 * 10 under negative pressure state
4P
a) control from the inspiration vacuum evaporator by under meter, separating through evaporation, miscella concentration brings up to 60～65% by 15～20% before evaporating, and the gas phase that vacuum evaporator distributes is advanced the vacuum cooler-condenser condensation, and phlegma advances all stock relocations of solvent; The non-condensable gases of vacuum cooler-condenser aspirates with oil-sealed rotary pump, and forms system vacuum at this, and oil-sealed rotary pump is vented to the hot water circulation jar, and further captured gas is residual molten; The liquid phase that vacuum evaporator distributes is then advanced tundish, and is taken out continuation processing by line pump.In addition, after evapo-separated machine evaporable secondary steam (80～90 ℃ of temperature) advanced the vacuum evaporator heat exchange, liquid phase was cooled to less than 40 ℃ of laggard diversion boxs by plate cooler; Gas phase is then advanced the evapo-separated machine condenser condenses.
Characterization device of the present invention comprises: oil-sealed rotary pump, vacuum evaporator, vacuum cooler-condenser, tundish, line pump, plate cooler.
The present invention also disposes plurality of conduits, valve, instrument, pipeline visor, under meter.
The secondary steam that the present invention contains the generation after evapo-separated machine is handled of the wet dregs of rice of solvent heats thermal source as vacuum evaporator.The liquid phase of secondary steam institute's condensation after the vacuum evaporator heat exchange is cooled off laggard diversion box with plate cooler.
The solvent gas that vacuum evaporator of the present invention volatilizes is in the vacuum state condensation, and phlegma flows into solvent week stock relocation.
The present invention adopts oil-sealed rotary pump to extract non-condensable gases from vacuum cooler-condenser, and is vented to the hot water circulation jar.
Mixing oil behind the negative pressure evaporation of the present invention flows into tundish, and is taken away continuously by line pump.
Advantage of the present invention is: 1. save steam.The existing oil-producing technique that leaches is that mixing oil evaporates at atmospheric pressure state, adopts the live steam heating.Mixed oil negative pressure evaporation of the present invention adopt the heating of evapo-separated machine evaporable secondary steam, so the steam consumption of the two has obvious difference.After measured, 50 ton per day oil extraction plants adopt the present invention per hour to save quantity of steam 200～250kg; 2. economize on electricity.The oil extraction plant water coolant is generally and recycles, the existing oil-producing technique that leaches is, the direct condensation of secondary steam, must consume a large amount of water coolants, secondary steam of the present invention is process heating evaporation mixing oil earlier, condensation again behind the reduction heat energy about 55%, therefore the cooling water circulation amount of the two has obvious difference, through measuring and calculating, 50 ton per day oil extraction plants adopt per hour about 12 tons of economized cycle cooling water inflow of the present invention, therefore can have the cooling water circulation pump motor of oil extraction plant now and reduce 5KW and use; 3. water saving.The oil extraction plant recirculated cooling water needs regularly to replenish and handle, because recirculated cooling water amount of the present invention reduces the then also corresponding reduction of rate of water make-up.Through measuring and calculating, but 50 ton per day oil extraction plants adopt 2 tons of per hour conserve water of the present invention; 4. through measuring and calculating, but 50 ton per day oil extraction plants adopt every year of the present invention save energy to take 5～100,000 yuan.
Below come the present invention is further described with Figure of description and embodiment.
Figure of description 1 is process flow diagram of the present invention
Figure of description 2 is P ﹠ I diagram of the present invention
Number in the figure (1) is a miscella tank, and (2) are hot water circulating pump, and (3) are wet dregs of rice material sealing spiral conveyer, (4) be the hot water circulation jar, (5) be the wet type trap, (6) are evapo-separated machine, and (7) are vacuum evaporator, (8) be plate cooler, (9) be the shwoot case, (10) are tundish, and (11) are the evapo-separated machine condenser, (12) be line pump, (13) be vacuum cooler-condenser, (14) are solvent week stock relocation, and (15) are oil-sealed rotary pump, (16) be valve, (17) be vacuum breaker, (18) are the pipeline visor, and (19) are under meter, (20) be thermometer, (21) are tensimeter.
Embodiment
Rare mixing oil (40～50 ℃ of concentration 15～20%, temperature) is injected miscella tank (1), after treating that liquid level reaches jar high 2/3rds, control by under meter (19), from inspiration vacuum evaporator (7), simultaneously, evapo-separated machine (6) evaporable secondary steam (80～90 ℃ of temperature) enters vacuum evaporator (7) heat exchange after wet type trap (5) is with hot wash, the secondary steam after the heat release, and its liquid phase is cooled to through plate cooler (8) and removes diversion box after being lower than 40 ℃; Its gas phase is advanced evapo-separated machine condenser (11) condensation process.
Rare mixing oil is heating evaporation in negative pressure steaming device (7), and flashes into gas phase and liquid phase by shwoot case (9), and its gas phase is advanced vacuum cooler-condenser (13) condensation, and phlegma flows into solvent week stock relocation (14); Noncondensable gas is then aspirated by oil-sealed rotary pump (15), and forms system vacuum (vacuum tightness 5 * 10 at this
4P
a), oil-sealed rotary pump (15) is vented to hot water circulation jar (4), and further captured gas is residual molten.
The mixing oil liquid phase of shwoot case (9) shwoot, concentration reaches 60～65%, flows to tundish (10) certainly, is taken out continuation processing in this buffering back by line pump (12).
Claims (3)
1, a kind of negtive pressure secondary steam from oil extracting factory utilizes Processes and apparatus, it is characterized in that mixing oil passes through under meter (19) control, from inspiration vacuum evaporator (7), evaporates and is separated into gas-liquid two-phase; Liquid phase flows to tundish (10) certainly, and extracts continuation processing continuously out with line pump (12); Gas phase is advanced vacuum cooler-condenser (13) condensation, and the liquid of condensation flows into solvent week stock relocation (14), and non-condensable gases is then used oil-sealed rotary pump (15) suction, and further captured gas is residual molten to be vented to hot water circulation jar (4).
2, oil extraction plant negative pressure evapo-separated machine according to claim 1 (6) evaporable secondary steam all advances vacuum evaporator (7) heat exchange, and the phlegma that forms after the heat release enters diversion box after cooling off with plate cooler (8).
3, negtive pressure secondary steam from oil extracting factory according to claim 1 utilizes Processes and apparatus, it is characterized in that in technical process, being provided with oil-sealed rotary pump (15), vacuum evaporator (7), plate cooler (8), line pump (12), vacuum cooler-condenser (13), vacuum breaker (17), under meter (19).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 94100336 CN1101374A (en) | 1994-01-13 | 1994-01-13 | Process and apparatus for utilizing negtive pressure secondary steam from oil extracting factory |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 94100336 CN1101374A (en) | 1994-01-13 | 1994-01-13 | Process and apparatus for utilizing negtive pressure secondary steam from oil extracting factory |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1101374A true CN1101374A (en) | 1995-04-12 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 94100336 Pending CN1101374A (en) | 1994-01-13 | 1994-01-13 | Process and apparatus for utilizing negtive pressure secondary steam from oil extracting factory |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1101374A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102068877A (en) * | 2010-11-14 | 2011-05-25 | 河南永昌飞天淀粉糖有限公司 | New process for reclaiming starch factory steam pipe bundle exhaust |
| CN102390833A (en) * | 2011-08-03 | 2012-03-28 | 乐山乐电天威硅业科技有限责任公司 | Method for recycling waste chlorosilane in polycrystalline silicon, produced by using modified Siemens process, under negative pressure |
| WO2013185438A1 (en) * | 2012-06-11 | 2013-12-19 | 山东星隆能源科技有限公司 | Evaporation-energy conversion device automatically boiling water at room temperature |
| CN103773600A (en) * | 2012-10-22 | 2014-05-07 | 北京中天金谷粮油工程技术有限公司 | Full negative pressure vacuum system leaching process |
| CN108837542A (en) * | 2018-06-28 | 2018-11-20 | 上海新奥新能源技术有限公司 | A kind of evaporation concentration system |
| CN109504532A (en) * | 2018-11-23 | 2019-03-22 | 东北农业大学 | A kind of hot wind method using evaporator solvent vapo(u)r heating evapo-separated machine |
-
1994
- 1994-01-13 CN CN 94100336 patent/CN1101374A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102068877A (en) * | 2010-11-14 | 2011-05-25 | 河南永昌飞天淀粉糖有限公司 | New process for reclaiming starch factory steam pipe bundle exhaust |
| CN102390833A (en) * | 2011-08-03 | 2012-03-28 | 乐山乐电天威硅业科技有限责任公司 | Method for recycling waste chlorosilane in polycrystalline silicon, produced by using modified Siemens process, under negative pressure |
| CN102390833B (en) * | 2011-08-03 | 2013-06-05 | 乐山乐电天威硅业科技有限责任公司 | Method for recycling waste chlorosilane in polycrystalline silicon, produced by using modified Siemens process under negative pressure |
| WO2013185438A1 (en) * | 2012-06-11 | 2013-12-19 | 山东星隆能源科技有限公司 | Evaporation-energy conversion device automatically boiling water at room temperature |
| CN103773600A (en) * | 2012-10-22 | 2014-05-07 | 北京中天金谷粮油工程技术有限公司 | Full negative pressure vacuum system leaching process |
| CN108837542A (en) * | 2018-06-28 | 2018-11-20 | 上海新奥新能源技术有限公司 | A kind of evaporation concentration system |
| CN109504532A (en) * | 2018-11-23 | 2019-03-22 | 东北农业大学 | A kind of hot wind method using evaporator solvent vapo(u)r heating evapo-separated machine |
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| WD01 | Invention patent application deemed withdrawn after publication |