CN203938664U - A kind of device of energy saving and environment friendly base-catalyzed transesterification method production biofuel - Google Patents
A kind of device of energy saving and environment friendly base-catalyzed transesterification method production biofuel Download PDFInfo
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- CN203938664U CN203938664U CN201420298855.2U CN201420298855U CN203938664U CN 203938664 U CN203938664 U CN 203938664U CN 201420298855 U CN201420298855 U CN 201420298855U CN 203938664 U CN203938664 U CN 203938664U
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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Abstract
The utility model discloses a kind of device of energy saving and environment friendly base-catalyzed transesterification method production biofuel.Device comprises raw material mixing tank, reactor, the first surge tank, methanol rectifying tower, the second surge tank, first minute flow container, second minute flow container, vaporizer, the first glycerine condenser, the second glycerine condenser and triglycerin condenser.The technical problem that the utility model solves is with base catalysis homogeneous phase ester-interchange method reaction method, to produce biodiesel processes long flow path at present, and the problem that unit output energy consumption is large, discharging of waste liquid amount is large, obviously shortens, and has lacked washing and dry step.The utility model Raw utilization ratio promotes greatly, and methyl alcohol all reclaims, and alkaline catalysts crystallizes out recycling in also evaporating in the back, therefore raw material availability is very high.
Description
Technical field
The utility model relates to bioenergy preparation and chemical process flow field, is specifically related to a kind of device of energy saving and environment friendly base-catalyzed transesterification method production biofuel.
Background technology
Due to the continuous exhaustion of the world oil energy and rising steadily of crude oil price, and the series of problems causing due to combustion of fossil fuels, as more and more significant in environmental pollution, acid rain, Greenhouse effect etc.New substitute energy is all being sought in countries in the world.
Biofuel in recent years as an alternative the energy receive much concern.According to 1992 U.S. biofuel association (NBB) definition, biofuel (Biodiesel) refers to the clean replacing fuel oil that can be used for engine of producing with the renewable biological source such as animal-plant oil.The main component of biofuel is higher fatty acid methyl esters.Biofuel has that little, renewable, the nontoxic easy degraded of environmental pollution, cetane value are high, CO
2quantity discharged is few, can reduce the advantages such as Greenhouse effect.Because the main component of biofuel is high-grade aliphatic ester, its oxygen level is high, sufficient combustion, and not containing aromatic hydrocarbon, on environment, can not cause too large impact, and similar with petrifaction diesel of the combustion heat value of biofuel, be therefore a kind of desirable substitute energy.
At present, the production method of biofuel is mainly divided into two kinds, has physical method and chemical process.Wherein the principle of physical method is mainly directly discarded animal-plant oil to be mixed with diesel oil, improves the uniformity coefficient of mixing by various means, and this method is mainly direct mixing method (or dilution method), mini-emulsion process.And chemical process is mainly, by series of chemical, animal-plant oil is decomposed into less molecule, thereby fundamentally improve the performance of biofuel, method mainly contains high temperature pyrolytic cracking and ester-interchange method.Though physical method is simple, can reduce animals and plants oil viscosity, to cure the symptoms, not the disease after all, cetane value is not high, easily produces carbon deposit in combustion processes, thus broken ring apparatus.And high-temperature cracking method to conversion unit require highly, and catalyzer is difficult to obtain, cost is high, is unfavorable for promoting.At present suitability for industrialized production biofuel mainly adopts base catalysis homogeneous phase ester-interchange method, but this technical process is long, and production process also needs more energy, and coarse biodiesel needs washing, can produce a large amount of waste water, and raw material can't obtain from a minute utilization.The utility model proposes for the problem existing in current base catalysis homogeneous phase ester-interchange method, thereby reduces energy expenditure and the waste discharge of production process self.
Utility model content
The device of a kind of energy saving and environment friendly base-catalyzed transesterification method production biofuel of the utility model, the technical problem solving is with base catalysis homogeneous phase ester-interchange method reaction method, to produce biodiesel processes long flow path, the problem (mass ratio of wastewater discharge and biofuel is at least 1:1) that unit output energy consumption is large, discharging of waste liquid amount is large at present.
A kind of device of energy saving and environment friendly base-catalyzed transesterification method production biofuel, comprise raw material mixing tank, reactor, the first surge tank, methanol rectifying tower, the second surge tank, first minute flow container, second minute flow container, vaporizer, the first glycerine condenser, the second glycerine condenser and triglycerin condenser, described raw material mixing tank outlet and reactor, the first surge tank, the first opening for feed of methanol rectifying tower connects in turn by pipeline, the tower top discharge port of methanol rectifying tower is connected with the second surge tank entrance, the top gas phase discharge port of surge tank is connected with mixing tank bottom inlet, surge tank bottom liquid phases discharge port is connected with mixing tank entrance, described methanol rectifying tower bottom discharge mouth is connected with first minute flow container entrance, the first separatory pot bottom discharge port is connected with evaporation feed liquor entrance, the first separatory tank top discharge port is connected with second minute flow container entrance, the second separatory pot bottom discharge port is connected with evaporation feed liquor entrance, vaporizer vapour outlet and the second glycerine condenser, the second opening for feed of methanol rectifying tower connects in turn, described vaporizer vapour outlet is connected with the first glycerine condenser, and the first glycerine condensator outlet is connected with second minute flow container with first minute flow container respectively, described vaporizer vapour outlet is connected with triglycerin condenser, the second opening for feed of described methanol rectifying tower is not higher than the first opening for feed of methanol rectifying tower.Described device also comprises feed preheater, methanol rectifying tower condenser, methanol rectifying tower reboiler and material cooler; Described feed preheater is connected between mixing tank and reactor by pipeline, described material cooler is connected between methanol rectifying tower bottom discharge mouth and first minute flow container by pipeline, described methanol rectifying tower condenser one end is connected with the outlet of methanol rectifying tower top gaseous phase, the other end is connected with the second surge tank with the methanol rectifying tower trim the top of column mouth of pipe respectively, and described methanol rectifying tower reboiler is connected at the bottom of methanol rectifying tower tower between liquid-phase outlet and the import of methanol rectifying tower tower spirit phase.
A kind of method of energy saving and environment friendly base-catalyzed transesterification method production biofuel, step is as follows: alkaline catalysts, after stock oil mixes in raw material mixing tank with methyl alcohol, by base-catalyzed transesterification method, in reactor, react, reacted material does not carry out stratification and directly enters methanol rectifying tower rectifying, the methyl alcohol of methanol rectification tower top is back to raw material mixing tank as charging, methanol rectification bottoms material enters first minute flow container stratification, liquid lower floor in first minute flow container is the glycerine that is dissolved with alkaline catalysts, the glycerine that is dissolved with alkaline catalysts flows to evaporator evaporation and purifies, first minute flow container is coarse biodiesel at the middle and upper levels, described coarse biodiesel enters from the second separatory pot bottom entrance, a glycerine part of being purified by evaporator evaporation enters from the second separatory tank top, then stratification, upper strata is biofuel, lower floor's glycerine flows into evaporator evaporation and purifies, the cooling rear section of glycerine that evaporation is purified is back in methanol rectifying tower, and part reclaims as glycerine byproduct, and alkaline catalysts is obtained by base of evaporator discharge port, after flow container separation in second minute, the biofuel preparing is flowed out by flow container outlet in second minute.
In aforesaid method, the mol ratio of described methyl alcohol and stock oil is (5 ~ 8): 1, and 0.7% ~ 1.4% of the quality that alkaline catalysts consumption is stock oil.
In aforesaid method, described alkaline catalysts comprises potassium hydroxide, sodium hydroxide or sodium methylate; Described stock oil comprises more than one in Vegetable oil lipoprotein and animal grease; Described methanol rectification bottoms material comprises more than one in glycerine, alkaline catalysts, biofuel and stock oil.
In aforesaid method, the methyl alcohol of methanol rectification column overhead is to carry out partial condensation, and steam finally enters from raw material mixing tank pucking bubble, and with the form heating raw directly mixing, speed and the area of controlling bubbling make gas-phase methanol all become liquid phase; Condensation portion is that boiling point is back to raw material mixing tank.
In aforesaid method, methanol rectifying tower is double-line feeding, and wherein a feed stream is the reacted material of base-catalyzed transesterification method, from the first opening for feed of methanol rectifying tower, enters; An other feed stream is glycerine, from the second opening for feed of methanol rectifying tower, enters.
In aforesaid method, after evaporator evaporation glycerine condensation out, at the bottom of a part flow back into methanol rectifying tower tower, a part enters from the second separatory tank top, and washing coarse biodiesel is remaining as by product.
In aforesaid method, first minute flow container and second minute flow container lower floor glycerine out all enters same vaporizer and evaporates purification.
In aforesaid method, described methanol rectifying tower stage number (does not comprise condenser and reboiler) between 4 ~ 13, tower top mole reflux ratio is between 0.5 ~ 2.0, and tower top pressure is at 50kPa between 150kPa, and the first feed plate (is counted from top to bottom) between 4 blocks of column plates of the 2nd block of column plate to the.
Compared with prior art, advantage of the present utility model is:
1, this device obviously shortens, and has lacked washing and dry step;
2, owing to there is no the step of washing, just there is no discharge of wastewater yet, and reduced separating difficulty;
3, raw material availability promotes greatly, and in traditional technique, alkaline catalysts is difficult to reclaim, and subsequent disposal increases cost again, Methanol Recovery amount also seldom, because when separated after reaction, biofuel can be taken away part methyl alcohol, and washing can be taken away part methyl alcohol, this part methyl alcohol is to be difficult to reclaim.And methyl alcohol all reclaims in this technique, alkaline catalysts crystallizes out recycling in also evaporating in the back, therefore raw material availability is very high.
Accompanying drawing explanation
Fig. 1 is energy saving and environment friendly base-catalyzed transesterification method production biofuel device in the utility model.
Embodiment
Below in conjunction with specific embodiment, the utility model is done specifically to describe in detail further, but embodiment of the present utility model is not limited to this, for not dated especially processing parameter, can carry out with reference to routine techniques.
As shown in Figure 1, wherein 1 for raw material mixing tank, 2 for feed preheater, 3 for reactor, 4 be the first surge tank, 5 for methanol rectifying tower, 6 be the second surge tank, 7 be first minute flow container, 8 be second minute flow container, 9 for vaporizer, 10 be the first glycerine condenser, 11 be the second glycerine condenser, 12 be triglycerin condenser, 13 for methanol rectifying tower condenser, 14 for methanol rectifying tower reboiler, 15 for material cooler, a be that the first opening for feed, b are the second opening for feed.
Produce the flow process of 30,000 tons of biofuel per year:
As described in Figure 1, stock oil (4486.29kg/h, main component (massfraction) for Uniphat A60 be 7.85%, methyl linoleate is 2.99%, Witconol 2301 is 88.04%, methyl stearate is 1.12%), methyl alcohol (430.28kg/h) and the incoming stock mixing tank 1 of potassium hydroxide (23.68kg/h), (temperature of reaction is 64 ℃ after feed preheater 2 heat exchange, to enter reactor 3 reactions, pressure is normal pressure), after reaction, enter the first surge tank 4, with the flow of 5420.43kg/h, enter methanol rectifying tower 5(methanol rectifying tower afterwards and have 4 blocks of column plates (not comprising condenser and reboiler), tower top mole reflux ratio 1.2, tower top is normal pressure, the first opening for feed a is at the 2nd block of column plate, the second opening for feed b is at the 4th block of column plate), bottom glycerine is with the boiling temperature charging under working pressure simultaneously, glycerin fed flow is 250kg/h, methanol rectifying tower 5 tower tops are normal pressure, the methyl alcohol that tower top steams (480.16kg/h) enters the second surge tank 6 after partial condensation, wherein gas phase molar fraction is 55%, incoming stock mixing tank 1 afterwards, after methanol rectifying tower 5 bottom products (5190.26kg/h) cooling (being cooled to 20 ℃), enter first minute flow container 7 stratification, upper strata is coarse biodiesel (4477.24kg/h), lower floor is raw glycerine (713.02kg/h), coarse biodiesel enters from second minute flow container 8 bottom, glycerine (654kg/h) enters from second minute flow container 8 top, stratification again after mixing, upper strata is biofuel (4475.81kg/h), lower coarse glycerine (655.43kg/h) enters vaporizer 9 reduction vaporizations purifications (evaporator temperature is 260 ℃) together with the glycerine of first minute flow container 7 lower floor, the glycerine being evaporated from vaporizer 9 (1344.76kg/h) condensation, at the bottom of a part flow back into methanol rectifying tower 5 towers, (flow is 250kg/h, temperature is 260 ℃), a part enters from second minute flow container 8 top, washing coarse biodiesel, flow is (654kg/h, temperature is 20 ℃), remaining glycerine be cooled to normal temperature as by product, its purity (massfraction) is up to 93%, potassium hydroxide is deposited in the bottom of vaporizer 9, after taking-up, can be recycled, biofuel is flowed out by flow container outlet in second minute.
According to GB GB/T 50441-2007 < < petrochemical complex design energy consumption calculation standard > >, by steam used in technique, water coolant is converted to standard coal.Wherein to be converted to standard coal be annual 1339598.49kg to steam, and it is annual 20835.87kg that recirculated cooling water is converted to standard coal, therefore general facilities total energy consumption is converted to standard coal, is annual 1360.4t.So the per-unit production energy consumption of this technique is that biofuel per ton need to consume 45.35kg standard coal.
In this scheme, wastewater discharge is 0 ton, and with tradition have the processing wastewater quantity discharged of washing process be 30,000 tons annual.
Above-described embodiment of the present utility model is only for the utility model example is clearly described, and is not the restriction to embodiment of the present utility model.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here exhaustive without also giving all embodiments.All any modifications of doing within spirit of the present utility model and principle, be equal to and replace and improvement etc., within all should being included in the protection domain of the utility model claim.
Claims (2)
1. the device of an energy saving and environment friendly base-catalyzed transesterification method production biofuel, it is characterized in that: comprise raw material mixing tank, reactor, the first surge tank, methanol rectifying tower, the second surge tank, first minute flow container, second minute flow container, vaporizer, the first glycerine condenser, the second glycerine condenser and triglycerin condenser, described raw material mixing tank outlet and reactor, the first surge tank, the first opening for feed of methanol rectifying tower connects in turn by pipeline, the tower top discharge port of methanol rectifying tower is connected with the second surge tank entrance, the top gas phase discharge port of surge tank is connected with mixing tank bottom inlet, surge tank bottom liquid phases discharge port is connected with mixing tank entrance, described methanol rectifying tower bottom discharge mouth is connected with first minute flow container entrance, the first separatory pot bottom discharge port is connected with evaporation feed liquor entrance, the first separatory tank top discharge port is connected with second minute flow container entrance, the second separatory pot bottom discharge port is connected with evaporation feed liquor entrance, vaporizer vapour outlet and the second glycerine condenser, the second opening for feed of methanol rectifying tower connects in turn, described vaporizer vapour outlet is also connected with the first glycerine condenser, and the first glycerine condensator outlet is connected with second minute flow container with first minute flow container respectively, described vaporizer vapour outlet is also connected with triglycerin condenser, the second opening for feed of described methanol rectifying tower is not higher than the first opening for feed of methanol rectifying tower.
2. the device of energy saving and environment friendly base-catalyzed transesterification method production biofuel according to claim 1, is characterized in that, described device also comprises feed preheater, methanol rectifying tower condenser, methanol rectifying tower reboiler and material cooler; Described feed preheater is connected between mixing tank and reactor by pipeline, described material cooler is connected between methanol rectifying tower bottom discharge mouth and first minute flow container by pipeline, described methanol rectifying tower condenser one end is connected with the outlet of methanol rectifying tower top gaseous phase, the other end is connected with the second surge tank with the methanol rectifying tower trim the top of column mouth of pipe respectively, and described methanol rectifying tower reboiler is connected at the bottom of methanol rectifying tower tower between liquid-phase outlet and the import of methanol rectifying tower tower spirit phase.
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| CN201420298855.2U CN203938664U (en) | 2014-06-06 | 2014-06-06 | A kind of device of energy saving and environment friendly base-catalyzed transesterification method production biofuel |
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| CN201420298855.2U CN203938664U (en) | 2014-06-06 | 2014-06-06 | A kind of device of energy saving and environment friendly base-catalyzed transesterification method production biofuel |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104087426A (en) * | 2014-06-06 | 2014-10-08 | 华南理工大学 | Energy-saving environmental-friendly base catalytic transesterification-method biodiesel production device and method |
| CN106833909A (en) * | 2016-12-28 | 2017-06-13 | 山东金冠化工有限公司 | The continuous ester exchange process with pressure of waste oil autoclave |
-
2014
- 2014-06-06 CN CN201420298855.2U patent/CN203938664U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104087426A (en) * | 2014-06-06 | 2014-10-08 | 华南理工大学 | Energy-saving environmental-friendly base catalytic transesterification-method biodiesel production device and method |
| CN104087426B (en) * | 2014-06-06 | 2016-01-06 | 华南理工大学 | A kind of device and method of energy saving and environment friendly base-catalyzed transesterification method production biofuel |
| CN106833909A (en) * | 2016-12-28 | 2017-06-13 | 山东金冠化工有限公司 | The continuous ester exchange process with pressure of waste oil autoclave |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20141112 Effective date of abandoning: 20160106 |
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| C25 | Abandonment of patent right or utility model to avoid double patenting |