CN1664087A - Process for producing monomeric fatty acid - Google Patents
Process for producing monomeric fatty acid Download PDFInfo
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- CN1664087A CN1664087A CN 200510042453 CN200510042453A CN1664087A CN 1664087 A CN1664087 A CN 1664087A CN 200510042453 CN200510042453 CN 200510042453 CN 200510042453 A CN200510042453 A CN 200510042453A CN 1664087 A CN1664087 A CN 1664087A
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Abstract
The invention relates to a method for preparing chemical products, especially to the method for preparing monomer aliphatic acid. The technical project is that hydrolyzing the stock to prepare crude aliphatic acid and glycerol water, distilling crude aliphatic acid to prepare the product, the character is: the said hydrolytic reaction going through more than two hydrolytic tower(25), said hydrolytic tower is heated by heat conducting oil; in said distilling process, firstly dewatering and degassing the crude aliphatic acid with vacuum distillation plant, then distilling, cooling and getting the product. The good effect is that it does not need the steam from steam boiler to produce vacuum, which can save the steam boiler and use heat conductance oil furnace, aliphatic acid line products can be produced and with good quality, and the invention is characterized by the less consumption of energy and water, little environmental pollution and small amount of investment in fixed assets. The energy consumption decreases by 50%, water consumption decreases by 60%, and the electricity consumption decreases by 40%.
Description
One, technical field: the present invention relates to a kind of Chemicals manufacture method, particularly a kind of method for manufacturing of fatty acid monomer.
Two, background technology: at present, the lipid acid process for processing, be to utilize grease to reclaim the acidifying oil of oil foot after sulfation is handled behind assorted grease or the oil and fat refining, under the effect of water, temperature is 160 ℃～240 ℃, pressure is 1.0MPa～4.0MPa and water generation hydrolysis reaction, generates croude fatty acids and glycerol liquor.
In the technology of said hydrolyzed reaction: in raw material is hydrolyzed, used hydrolysis device.Be generally stirring-type hydrolytic reaction pot or two towers and multi-tower type continuous hydrolysis reaction tower, wherein, stirring-type hydrolysis reaction pot, this is heat-conducting oil heating or steam heating, pressing mode, interrupter method production, equipment heaviness, heating system are opened, stop frequent, system pressure, temperature instability, the heat recovery weak effect; And two towers or multi-tower type continuous hydrolysis tower, it is steam boiler by higher operating pressure, (1.2MPa～2.5MPa, 160 ℃～230 ℃ of temperature) to successively heating in the tower, pressurizeing, the pump circulation reaction that is hydrolyzed, the steam boiler that needs the higher operating pressure of pressure causes the energy consumption height, therefore, adopt stirring-type hydrolytic reaction pot and multi-tower type continuous hydrolysis tower, if operating pressure is low, (1.0MPa～1.5MPa, 150 ℃～170 ℃ of temperature), then the material water consumption is bigger, cause energy consumption to increase, quantity of wastewater effluent is big, and the longer weak effect of hydrolysis time.
The further treatment process of the croude fatty acids that in to above-mentioned technology, produces: to croude fatty acids, after the degassing, the dehydration, through still kettle or distillation tower.Under vacuum condition, by heat-conducting oil heating to 220 ℃～275 ℃ of vacuum tightness≤150Pa, distill out gas phase lipid acid and residual residue, gas phase lipid acid becomes liquid phase through condenser system, receive and the product that obtains, residue by still at the bottom of or discharge at the bottom of the tower.
And the vacuum apparatus required to the further treatment process of croude fatty acids: water---vapour series connection steam jet vacuum pump or multistage steam ejection vacuum pump.The former is general, and rate of air sucked in required is less, and vacuum tightness is poor.Be applicable to the device of less output.Latter's rate of air sucked in required is bigger, but required be that water vapor fluidics forms vacuum take-off, this vapor jet pump, steam consumption quantity is big, and consume also will be through the heat exchange condensation after a large amount of water vapors and the ejection, water loss is big than the large equipment investment.Use other vacuum pump, as water ring vacuum pump, sliding vane rotary vacuum pump, water ring Roots vacuum unit equal vacuum equipment, vacuum tightness difference or work-ing life are short.Suction water vapor and when being entrained with gaseous phase materials particularly, its performance is more undesirable, and vacuum state is not good, distillation gas phase temperature height.Unstable product quality, equipment corrosion is serious, energy consumption is high, and to fatty acid monomer processing, its energy consumption accounts for more than 80% of whole expense, and particularly coal consumption accounting is great.
Three, summary of the invention: purpose of the present invention is exactly the above-mentioned defective that exists at prior art, and a kind of method for manufacturing of fatty acid monomer is provided.
Its technical scheme is: generate croude fatty acids and glycerol liquor by raw material through hydrolysis reaction, the croude fatty acids that generates forms finished product through distil process, it is characterized in that: described hydrolysis reaction is a raw material process plural hydrolysis tower (25), adopts heat-conducting oil heating in the described hydrolysis tower (25); Described distil process is to adopt vacuum pump to the dehydration degassing earlier of the croude fatty acids in the degassing tower (7) earlier, passes through distillation tower (10) again, gets product after the condensation.
Better, distil process comprises as follows: the first step, and the croude fatty acids that described hydrolysis reaction is generated drops into degassing tower (7); Second step, send into the first falling liquid film reboiler (5) with material recycle pump (6), when described croude fatty acids was heated to 220 ℃-270 ℃, described vacuum pump was evacuated to degassing tower (7)-below the 0.98MPa, when in degassing tower (7), exceeding overflow port, overflow to distillation tower (10) bottom; The 3rd step, with recycle pump (8) croude fatty acids is sent into the second falling liquid film reboiler (9) circulation heating, when being heated to 230 ℃-270 ℃, in the tower during vacuum degree deficiency 150Pa, croude fatty acids becomes the gas phase croude fatty acids, and rise to the top of distillation tower (10), become liquid and overflow by condenser (12) condensation.
Effect of the present invention is: vacuum distillation plant of the present invention, its effect is than used water---vapour series connection vacuum pump, or have incomparable advantage to need not the steam boiler water vapor with multistage steam ejection vacuum pump to produce vacuum, its running cost can economize 60%, and install simple, so can save steam boiler, only use heat-conducting oil furnace, can produce lipid acid series product, and can reach good effect, it is low to have power consumption, water consumption is little, and environmental pollution is little, and investment in fixed assets is few, produce its water consumption of fatty acid monomer with present method and reduce 60%, power consumption reduces 40%.
Four, description of drawings:
Accompanying drawing 1 is the process flow sheet of hydrolysis reaction of the present invention;
Accompanying drawing 2 is to the further distil process schema of croude fatty acids among the present invention.
Five, embodiment:
With reference to accompanying drawing 1 and accompanying drawing 2, the invention will be further described:
As accompanying drawing 1: make the acidifying wet goods material reaction synoptic diagram that is hydrolyzed continuously.200 ℃～280 ℃ thermal oils of temperature are entered by inlet 24, discharge from exporting 23.Material through 21 heat exchange of water volume pump, enters volume pump 22 by volume pump 22.21 liang of pumps of water volume pump are simultaneously to hydrolysis tower 25 chargings, by recycle pump about in the of 26 after the permutoid reaction, overflow into tower 27 again by recycle pump permutoid reaction about in the of 28, overflow in the tower 29, after recycle pump 30 permutoid reactions, enter heat exchange condenser 31 after condensation, entered in the static pot by condensator outlet 32, layering goes out croude fatty acids and glycerol liquor.
Water and acidifying wet goods material's proportion can be regulated by volume pump 22, this steam boiler water vapor that need not, and operating pressure is higher, the hydrolysis steady quality, continuous feeding and discharging, waste-heat recovery device is applicable to grease or recovery vegetable and animals oils and acidifying oil.
As accompanying drawing 2: after the acidifying profit is separated reaction, generate croude fatty acids and glycerol liquor.Wherein, croude fatty acids is sent into the first falling liquid film reboiler 5 with material recycle pump 6 under entering degassing tower by volume pump 1, and material is heated to 220 ℃～270 ℃, and the hydrojet vacuum pump is evacuated to degassing tower 7-below the 0.98MPa.Multistage water pump 2 and cyclic water tank 3 cooperate with vacuum pump unit 4, and water in the croude fatty acids and gas are extracted out.
When croude fatty acids surpasses overflow port in degassing tower, just distillation tower 10 bottoms are gone in overflow, send into the 9 circulation heating of the second falling liquid film reboiler by recycle pump 8, when material is heated to 230 ℃～270 ℃, vacuum tightness≤150Pa in the tower, the gas phase lipid acid material of generation rises to the top of distillation tower 10, becomes liquid by condenser condenses and is overflowed by outlet 12, promptly get fatty acid monomer, and the plant pitch prill by under export 11 and discharge.
In the still kettle or in the distillation tower, vacuum is by water-jet pump and Roots vaccum pump bonded, hydraulic ejector and Roots vaccum pump bonded or water ring vacuum pump and Roots vaccum pump bonded vacuum unit, its vacuum tightness≤150Pa distills with this understanding.The preceding condenser of pump is housed, with abundant condensing air phase materials between still kettle, distillation tower and the vacuum pump.Its Roots vaccum pump must be higher than the above installation of hydrojet vacuum pump 12m.
Water-jet pump, hydraulic ejector, water ring vacuum pump should be selected stainless steel for use or do anti-corrosive treatment.
Its effect of this vacuum distillation plant is than used water---vapour series connection vacuum pump, or have incomparable advantage to need not the steam boiler water vapor with multistage steam ejection vacuum pump to produce vacuum, its running cost can economize 60%, and install simple, so can save steam boiler, only use heat-conducting oil furnace, can produce lipid acid series product, and can reach good effect, it is low to have power consumption, and water consumption is little, and environmental pollution is little, investment in fixed assets is few, and producing its energy consumption of fatty acid monomer with present method is present 50%.(whole energy consumption) water consumption reduces 60%, and power consumption reduces 40%.
Claims (7)
1, a kind of method for manufacturing of fatty acid monomer, generate croude fatty acids and glycerol liquor by raw material through hydrolysis reaction, the croude fatty acids that generates forms finished product through distil process, it is characterized in that: described hydrolysis reaction is a raw material process plural hydrolysis tower (25), adopts heat-conducting oil heating in the described hydrolysis tower (25); Described distil process is to adopt vacuum distillation plant to the dehydration degassing earlier of the croude fatty acids in the degassing tower (27) earlier, through distillation, gets product after the condensation again.
2, the method for manufacturing of fatty acid monomer according to claim 1 is characterized in that: described distil process comprises as follows:
The first step, the croude fatty acids that described hydrolysis reaction is generated drops into degassing tower (7);
Second step, send into the first falling liquid film reboiler (5) with material recycle pump (6), when described croude fatty acids was heated to 220 ℃-270 ℃, described vacuum pump was evacuated to degassing tower (7)-below the 0.98MPa, when in degassing tower (7), exceeding overflow port, overflow to distillation tower (10) bottom;
The 3rd step, with recycle pump (8) croude fatty acids is sent into the second falling liquid film reboiler (9) circulation heating, when being heated to 230 ℃-270 ℃, in the tower during vacuum degree deficiency 150Pa, croude fatty acids becomes the gas phase croude fatty acids, and rise to the top of distillation tower (10), become liquid and overflow by condenser (12) condensation.
3, the method for manufacturing of fatty acid monomer according to claim 2 is characterized in that: croude fatty acids drops into degassing tower (7) by volume pump (1); Condenser (13) before described condenser (12) top also connects pump is in order to capture a spot of gas phase croude fatty acids.
4, the method for manufacturing of fatty acid monomer according to claim 3 is characterized in that: condenser (13) also connects vacuum unit (15,16) before the described pump, and vacuum unit is equipped with the vacuum breaker that prevents the recirculated water suck-back in (15,16).
5, the method for manufacturing of fatty acid monomer according to claim 1 is characterized in that: described vacuum distillation plant is hydraulic ejector vacuum pump and Roots vaccum pump combination.
6, the method for manufacturing of fatty acid monomer according to claim 1 is characterized in that: described vacuum distillation plant can also be water ring vacuum pump and Roots vaccum pump combination.
7, the method for manufacturing of fatty acid monomer according to claim 1 is characterized in that: described vacuum distillation plant also can be water-jet pump and Roots vaccum pump combination.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200510042453 CN1664087A (en) | 2005-02-03 | 2005-02-03 | Process for producing monomeric fatty acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200510042453 CN1664087A (en) | 2005-02-03 | 2005-02-03 | Process for producing monomeric fatty acid |
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| CN1664087A true CN1664087A (en) | 2005-09-07 |
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| CN 200510042453 Pending CN1664087A (en) | 2005-02-03 | 2005-02-03 | Process for producing monomeric fatty acid |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102344855A (en) * | 2011-10-17 | 2012-02-08 | 渭南市油脂化工有限责任公司 | Rectifying system device and method for preparing fine fatty acid |
| CN110669590A (en) * | 2019-09-30 | 2020-01-10 | 郑州远洋油脂工程技术有限公司 | System and method for continuously producing fatty acid by soapstock |
| CN112500933A (en) * | 2020-11-20 | 2021-03-16 | 汕头市天汇健生物技术有限公司 | Process for purification of crude fatty acids |
-
2005
- 2005-02-03 CN CN 200510042453 patent/CN1664087A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102344855A (en) * | 2011-10-17 | 2012-02-08 | 渭南市油脂化工有限责任公司 | Rectifying system device and method for preparing fine fatty acid |
| CN110669590A (en) * | 2019-09-30 | 2020-01-10 | 郑州远洋油脂工程技术有限公司 | System and method for continuously producing fatty acid by soapstock |
| CN112500933A (en) * | 2020-11-20 | 2021-03-16 | 汕头市天汇健生物技术有限公司 | Process for purification of crude fatty acids |
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Open date: 20050907 |