CN101988026A - Method and device for extracting essential oil by biomass wastes - Google Patents
Method and device for extracting essential oil by biomass wastes Download PDFInfo
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- CN101988026A CN101988026A CN2009101657039A CN200910165703A CN101988026A CN 101988026 A CN101988026 A CN 101988026A CN 2009101657039 A CN2009101657039 A CN 2009101657039A CN 200910165703 A CN200910165703 A CN 200910165703A CN 101988026 A CN101988026 A CN 101988026A
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Abstract
The invention relates to a method for extracting essential oil by biomass wastes, which comprises the following steps of: indirectly heating biomass wastes such as waste wood, wood chips, other plants or the like put in an airtight reaction pot keeping an anaerobic condition inside, to perform thermal decomposition (carbonization); leading volatile gas components distilled by decomposing biomass wastes treated into a condenser to be condensed to liquid; separating the liquid into water and oil by a water-oil separation chamber; deodorizing unliquefied gas and discharging outside; and performing high temperature carbonization on residue in the reaction pot once to obtain activated carbon. During treatment, low pressure is kept in the reaction pot by multistage control of temperature and pressure in the reaction pot and staged high-speed suction of an air pump with variable speed/flow, which reduces treatment time and obtains high-quality essential oil and byproduct (activated carbon). The invention also includes a system device for performing the method, and an ultrasonic generator can be arranged in the water-oil separation chamber of the device to promote secondary decomposition of tar components to improve quality of essential oil.
Description
Technical field
The present invention relates to a kind of by giving birth to matter waste wood extraction described method of essential oil and device thereof, especially refer to a kind of in order to will such as: carry out destructive distillation in the air hermetic reactors of life matter waste wood under the anaerobic atmosphere state such as Wood waste, wood chip or other plant, obtaining the treatment process that high-quality essential oil and residue are the byproduct activated carbon, and be used in the system and the device person of this processing method.
Background technology
General so-called essential oil, mean by extraction such as the branches and leaves of plant, rhizome, wooden skin, wood chip, fruit, petal, resin plants essential oil be main body, be aqueous usually and have the character light, and have any different with grease than water.Derived essential oil refers generally to (C
5H
8) hydrocarbons of n, but mainly be to have C
10H
16, C
15H
24, C
20H
22Deng the terpene hydrocarbons that form to divide and derivative such as arene, alcohols, aldehydes, ketone or the like compound.The extracting process of essential oil has following three kinds of methods usually, that is: (1) steam distillation, and (2) milling process and (3) solvent method, and the most frequently used person is a steam distillation.
In addition, activated carbon is because of to the inorganic or organic substance in the solution, and colloidal particle etc. have powerful adsorptive power and deodorization, decolouring and filtration capacity and are widely used in food, medicine, grease, oil, water treatment industry, requirement and increase every year.Its method for making generally is to use timber, wood chip, Exocarpium cocois (Cocos nucifera L), bagasse, coal, peat etc. to be raw material, in addition after the carbonization, and activated again processing and making.Its activation method has: other method of (1) steam activation method (2) medicine activation method (3).After the raw material pulverizing of the steam activation genealogy of law with carbonization, in the stove more than 800 ℃, pass to superheated vapour and give activation.Pharmaceutical chemicals activation method typical case person is that the raw material that will pulverize uses after the liquor zinci chloridi dipping, activation when being calcined carbonization, and the pharmaceutical chemicals composition is then removed in wash afterwards.Then calcining and activating forms under the rare gas elementes such as air, carbonic acid gas, nitrogen passing to raw material as for additive method.
Overlap different equipment and different independent respectively enforcements of processing procedure in the extraction of above-mentioned essential oil and the method for making system difference mat two of activated carbon, not only estimate and use the very big device space, and the production time is long, energy consumption is many, and operator are also many, and very difficulty meets economic benefit.
Disclose a kind of simple type essential oil extraction plant in No. 477239 communique of the novel patent in Taiwan, it is to utilize steam distillation to extract the compact simplified assembly type device of essential oil in fragrant flowers and plants, be fit to laboratory or individual DIY assembling and use, non-is the industrial production type.
In addition, disclose a kind of improved structure of essential oil extraction plant in the novel patent M266969 communique of Taiwan, this device is roughly the same with the device of No. the 477239th, above-mentioned novel patent basically, just the sweating room in big footpath and the gathering room that undergauge is formed at the bottom are formed at the interior pipe top with prolong, and the pipe lower end picks out an essential oil water return line that is communicated to the pneumatic tube that picks out from flask in this.
Disclose a kind of active type essential oil extraction plant in No. 481045 communique of the novel patent in Taiwan, this kind device also still utilizes steam distillation as above-mentioned two patent cases, and only scale is medium-sized and has maneuvering ability.
In addition, patent of invention No. 51708 communique in Taiwan also discloses a kind of method of producing gasoline, diesel oil and carbon black with waste rubber, system is as shop equipment and complicated operations system that above-mentioned No. 462984 the patent utilization scale is quite big, with thermo-cracking and catalystic pyrolysis with damaged tire extracting gasoline, diesel oil and carbon black.
Disclose recovery described method of extracting active carbon and devices such as a kind of continous way damaged tire in No. 462984 communique of Taiwan patent of invention, it is to be suitable for handling on a large scale tire to obtain fuel oil, combustion gas and carbon black, fuel oil and combustion gas can be for being pyrocrack furnace in the system and activation furnace fuel, and carbon black then becomes powder shape activated carbon through removing after impurity and pulverizing import the activation furnace activation.
The above back two patent, though resource is reclaimed and environmental protection has to a certain degree contribution, cost of equipment is huge, and can not be used for the production of essential oil.
In addition, disclose a kind of living mass-energy activated carbon manufacturing system and method in the 2008 No. 19525 communique of Taiwan patent of invention, can with processed raw material in system in addition carbonization and activation to become activated carbon.It is waste heating one boiler that utilizes the carbonization-activation stove to be produced, and imports to produce high-temperature vapor that the raw material to carbonization carries out activation in this carbonization-activation stove.
Yet, above-mentioned various known technology there is no exposure can get residual solid shape carbide activation activated carbon when giving birth to material extraction derived essential oil in triangular web technology, also never is disclosed in all temperature and pressure controlled operational condition in the pyrolytic process.
Summary of the invention
Purpose of the present invention is providing a kind of by the method for giving birth to matter waste wood extraction essential oil, the living matter waste wood of vegetalitas carries out destructive distillation (being thermolysis) in the air hermetic reactor of anaerobic state in order to incite somebody to action particularly, in the time of with acquisition vegetalitas oil product or essential oil, also can obtain the activated carbon of byproduct.
Another object of the present invention is providing a kind of method that can be obtained activated carbon by living matter waste wood extraction essential oil simultaneously, tie up in the manufacturing processed temperature in the reactor and the control of pressure stage property, and look pot inner pressure and distillate the situation of branch, of short duration the bleeding of mat fast pumpdown pump, to keep low pressure and to avoid distillating branch and be detained and cause overfocus in the pot too for a long time, so, can shorten treatment time and can obtain the essential oil of high-quality and high yield and the activated carbon of byproduct.
A further object of the present invention is providing a kind of device of implementing above-mentioned by the method for giving birth to matter waste wood extraction essential oil, this device comprises: one makes its pyrolytic have in the cassette air hermetic reactor of pot in order to will give birth to matter waste wood raw material indirect heating, one is condensed into the condenser of liquid in order to the gaseous constituent that thermolysis is distillated, one in order to being separated into condensed fluid the separator tank of moisture and oil content, and an off-gas pump that is located at the gas outlet end of separator tank.
Another purpose of the present invention is providing a kind of device of implementing aforesaid method, the off-gas pump of being located at the exhaust port side of separator tank is the variable off-gas pump of flow rotating speed, can quicken to increase extraction flow when surpassing institute's level pressure power so that voltage rise in reactor is high, promptly reduce in pressing in short-term in making, to keep low pressure, using promotes to volatilize and reduce in the cut delay reactor forms overfocus too for a long time.
Another purpose of the present invention is provided with the ultrasonic wave generator in that a kind of device of implementing aforesaid method is provided in the inside of separator tank, decomposes to impel tar ingredients again, can improve oil quality and output.
A further object of the present invention, a kind of device of implementing aforesaid method is being provided, look necessity and can connect one second condenser and tempering tank again at the vapor pipe of separator tank, with to not liquefaction gas carry out again lower temperature be condensed into fluid after, mix with the fluid in the self-separation groove imports tempering tank, and improve extraction quantity.
Description of drawings
Fig. 1 represents the pie graph by life matter waste wood extraction essential oil system of first embodiment of the invention.
Fig. 2 represents the pie graph of the essential oil extracting system of second embodiment of the invention.
Fig. 3 represents the pie graph of the essential oil extracting system of third embodiment of the invention.
[main element nomenclature]
1 reactor
11 outer pan bodies
Pot in 12
13 lids
14 electric heating devices
15 heat-insulation and heat-preservation materials
16 air outlets
17 safety valve
18 tensimeters
2, the 2A condenser
21 closed cell bodies
22 spiral interior pipes
23 gas collection portions
24 water jackets
25 cooling water inlets
26 cooling water outlets
3 oil-water separation tanks
31 dividing plates
32 liquid collecting room
33 overflow chambers
34, the 34a valve
35, the 35a oil exit pipe
36 oil-collecting buckets
37 water shoots
4 off-gas pumps
5 controlling boxs
51 pressure transmitters
52 temperature sensors
6 water-sealed tanks
7 tempering tanks
71 agitators
8 ultrasonic wave generators
The P output tube
P1, the P2 vapor pipe
P flows pipe
The M raw material
Lead
The L supply lead
Embodiment
Other purpose of the present invention and effect then can be with reference to the detailed descriptions of following conjunction with figs. and obtain further to understand.
In the accompanying drawings, Fig. 1 represents the pie graph by life matter waste wood extraction essential oil system of first embodiment of the invention.Fig. 2 represents the pie graph of the essential oil extracting system of second embodiment of the invention.Fig. 3 represents the pie graph of the essential oil extracting system of third embodiment of the invention.
The essential oil extracting system of first embodiment shown in Figure 1 comprises: reactor 1, mat pipeline are located at the condenser 2 in its downstream successively, water oil separate chamber 3, off-gas pump 4 and controlling box 5.
Reactor 1 comprises that outer pan body 11, the one demountable interior pots 12 and that are equipped with electric heating device 14 and the heat insulation material 15 of preserving moisture around can closely be placed on the airtight lid 13 of the opening of outer pan body 11.Top one sidewall of outer pan body 11 is provided with an air outlet 16, and air outlet 16 connects the entrance end that a pneumatic tube P passes to condenser 2 since then.Lid 13 is provided with a safety valve 17 and tensimeter 18.
Condenser 2 has a closed cell body 21, and is installed with the interior pipe 22 of spiral or winding type of portion within it.One end of cell body 21 connects the exit end of pneumatic tube P, and the part of this exit end is preferably formed as the gas collection portion 23 in big footpath, and an end of this gas collection portion 23 connects an end of above-mentioned interior pipe 22, and the other end of interior pipe 22 then is connected to water oil separate chamber 3.In addition, cell body 21 perisporiums form water jacket 24, and have water coolant (or refrigerant) inlet 25 and export 26, water coolant or refrigerant can be introduced and are discharged.Condenser 2 is not limited to use the described pattern of present embodiment, and any suitable traditional condenser all can use, and comprises not having a condenser of gas collection portion 23.
Water oil separate chamber 3 is the groove that is separated into moisture and oil content in order to the phlegma with condenser 2, be provided with dividing plate 31 in the groove and will be separated into liquid collecting room 32 and overflow chamber 33 in the groove, after phlegma enters liquid collecting room 32, light specific gravity and the oil content of bubbling through the water column from liquid collecting room's 32 overflows to overflow chamber 33, Ye Hua gas then is not disposed in the atmosphere through vapor pipe P1 by off-gas pump 4 suctions at the liquid level superjacent air space, for exempting from hot gas or smell polluted air, discharge after preferably gas being imported a water-sealed tank 6 cooling deodorizing.
Controlling box 5 is to be located to be easy in the system monitor and to control part, this controlling box 5 has power switch, tensimeter, thermometer and is used for regulating and controlling button and the alarm to exception status lamp and/or the warning horn etc. of reactor 1 internal pressure and temperature, this controlling box 5 is pressure transmitter 51, temperature sensor 52, electric heating device 14 and the off-gas pump 4 that the mat lead is connected to reactor 1, also has supply lead L certainly and is connected to power supply.
Secondly constituting as above system is used for the method that the autobiotic waste wood extracts fluid and is described as follows:
At first, will be for example through suitable clean dry, pulverizing or slicing treatment, after the residual branch of Chinese juniper wood, root are done etc. in the interior pot 11 that waste wood raw material M drops into reactor 1, with pot cover 13 lids tightly to keep the airtight of reactor 1 inside.Thereupon, utilize off-gas pump 4 to bleed with to scavenging in the reactor 1, and make pot inner pressure reduce to 0.5～0.8kg/cm
2, be low vacuum state.In case of necessity, also can charge rare gas element as nitrogen in pot.Then, mat controlling box 5 starts power supply, make electric heating device 14 give birth to heat, and mat temperature push button control kettle temperature is at for example 150 ℃～200 ℃, and after for some time, a raw material M promptly decomposes and produces cigarette shape gas in the pot, this gas major part is a boiling point at 100 ℃ moisture and small part lightweight oil content, this gas flows into the gas collection portion 23 of condenser 2 through pipe P, and pipe is 22 o'clock in the spiral of flowing through again, flows into separator tank 3 after being subjected to cooling water condensation in the water jacket 24 to become liquid.Contain most of phlegma this moment and flow into liquid collecting room 32 when its water level surpasses dividing plate 31 tops for moisture, light specific gravity and the oil content of bubbling through the water column promptly from liquid collecting room's 32 overflows to the overflow chamber 33 and store up in this chamber, when being stored to suitable capacity, can opening valve 34 and this oil is collected in oil-collecting bucket 36 via oil exit pipe 35.The water level of liquid collecting room 32 is that mat water level gauge (not shown) or other means remain on certain water level, and the water of excess is discharged outside via water shoot 37.
In pyrolysis is in the retort process, produces a large amount of gases to interior pressure in the reactor 1 and is increased to above predetermined pressure, for example 1.2kg/cm
2When above, after learning from the tensimeter of controlling box 5 and attention device, but the electric control loop of mat and this tensimeter interlock or computer software (all not icon) control or mat operator are automatically manually controlled off-gas pump 4 with high speed rotating or increase the flow running and implement blink, 1 minute to several minutes bleed for example makes the gas that boosts enter gas collection portion 23 in a large number and presses the short period of time promptly to reduce to for example 0.8kg/cm in making
2Below, to keep the low pressure destructive distillation, volatile matter can also be made simultaneously with the lesser temps evaporable distillate branchs and exempt to be detained in the pot and produce the more situation generation of heavy tar after causing the overfocus result for a long time.When pressure returns back to former predetermined pressure state, and almost frozen-free liquid continue to produce or free air delivery when having subtracted greatly, mat controlling box 4 changes temperature of reaction and is set in for example 250 ℃～350 ℃, to implement the subordinate phase pyrolysis, pressure still remains on 0.5～0.8kg/cm
2Because moisture big induced evaporation in the decomposition course of aforementioned fs is most, this stage has only most high boiling point derived essential oil more than 250 ℃ to evaporate into gas under this temperature, and after pipe P inflow condenser 2 is condensed into liquid, enter separator tank 3 overflows to the overflow chamber 33, Ye Hua gas is not then discharged by vapor pipe P1.At high temperature, pot inner pressure will produce along with the rising of temperature and gas are a large amount of and raise, at this moment, but off-gas pump 4 just as described above the control of mat automatic or manual carry out of short duration high flow capacity and bleed, descend during compacting in making and keep default 0.5～0.8kg/cm
2Low-pressure state so that oil content volatilization is very fast and volatilization gas can not be detained in the high temperature pot after forming overfocus for a long time or reassembling into situation such as heavy tar and takes place.Therefore, can be under lower temperature and the short period internal reaction guaranteeing safety, and improve production capacity and oil quality.
When nearly not having fluid continuing to produce in pot inner pressure keep not to have the sign that boosts and separator tank 3, the reaction of expression subordinate phase finishes.At this moment, temperature can be set in for example 350 ℃～500 ℃, and at 0.5～0.8kg/cm
2Implement the pyrolysis of phase III under the internal pressure, have only a small amount of boiling point to resolve into gas at the mink cell focus more than 350 ℃ this moment, and as the aforementioned separator tank 3 that after condenser 2 is condensed into fluid, enters after gas-liquid separation, the fluid overflow is to the overflow chamber 33, gas is then discharged the outside.When carrying out this high temperature pyrolysis, pot inner pressure also as described above the control of mat off-gas pump 4 and shorten the reaction times and guarantee safety keeping low pressure, can improve production capacity and oil quality simultaneously.When pot inner pressure descends and dangerous frozen-free liquid and gas when producing, represent that the 3rd section pyrolytic process finishes, and and the raw material M residues in the interior pot 11 experience above-mentioned three stages and form solid shape carbide from low temperature to pyritous destructive distillation carbonization.Subsequently, kettle temperature is set in 500 ℃～700 ℃ activation temperature, and intermittent of short duration the bleeding of keeping low-pressure state of cooperation off-gas pump 4, handle to carry out that solid shape carbide is implemented activatory quadravalence section, have only this moment the high boiling point gas as heavy metal etc. of denier to produce, and after for some time of 1～2 hour for example, Gu the shape carbide promptly becomes activated carbon.Powered-down shut-down operation thereupon, when treating that kettle temperature is reduced to normal temperature, behind the breakdown lid 13, mat lifting machine or chain barrel (not shown) shift out the outside with interior pot 12, unload activated carbon, and inside has been equipped with pot 12 mat lifting machines hang in the outer pan body 11 in another of raw material waste wood, cover tight lid 13 and can implement the second round-robin pyrolysis processing.
So, implement repeatedly, can be very effective from oil products such as raw material abstraction such as essential oils in the treatment time shorter than traditional method, and can obtain activated carbon simultaneously.
In the pyrolytic process of previous embodiment, system is divided into four-stage with whole process and handles under differing temps, but above-mentioned first to phase III also can be divided into the more thermograde stage, for example implement every 100 ℃ or 150 ℃, if with phase III and stage of quadravalence Duan Bingwei, heighten to also can with the pyrolysis and the carbide activation treatment of carrying out mink cell focus more than 500 ℃ and after finishing subordinate phase, be about to temperature.At least to be approximately the aforementioned the 3rd and quadravalence section treatment time sum this moment the treatment time.In addition, the temperature range in aforementioned each stage and the gradient of intensification are an example, and this equitemperature can be managed kind, character and the shape of raw material and changes according to difference.In addition, separator tank 3 is not limited to illustrated embodiment, and known various suitable type for sleeping in or upright type separator tank all can adopt.In addition, do not establish in addition as reactor 1 in pot 12 also feasible.
Fig. 2 represents second embodiment of system of the present invention, all in this embodiment members identical or suitable with the first embodiment system with identical symbology it, and omit its explanation.
In this embodiment, its formation is identical with previous embodiment basically, only at the vapor pipe P1 of the separator tank 3 adjunction second condenser 2A, the outlet pipe end of this condenser 2A connects a tempering tank 7, and the bottom of tempering tank 7 is provided with an oil exit pipe 35a and valve 34a in order to the oil in the groove is imported in the oil-collecting bucket 36.The top of tempering tank 7 is provided with vapor pipe P2, and off-gas pump 4 is to be arranged at this pipe P2 to go up with on the pipe P1 that replaces first embodiment.In addition, the oil exit pipe with valve 34 35 of separator tank 3 is to the other end of tempering tank 7, be provided with an electric mixer 71 in the tempering tank 7 so that self-separation groove 3 is mixed with the fluid that drips in the tempering tank 7 through the second condenser 2A condensation through managing 35 fluid that flow into tempering tank 7, mixed oil liquid then can flow into oil-collecting bucket 36 through oil exit pipe 35a.The system of this embodiment also have first embodiment system not the ultrasonic wave generator 8 of tool be located at the bottom of separator tank 3 make its decomposition so that the mat action of ultrasonic waves is cut off the macromolecular structure of fluid in the groove, and obtain more low molecule light oil composition.Ultrasonic wave generator 8 should adopt output rating 50w/cm
3Above person, and with for example when 20 kilo hertzs (kilo-herzz) output rating at 100～200w/cm
2Be advisable.The cooling temperature system of the second condenser 2A is set at lower than first condenser 2, is generally for example below 15 ℃, so that the gas of self-separation groove 3 is cooled to fluid more in the future.Outer cell body 21 inside of the second condenser 2A do not form collection chamber 23, and only have been installed with pipe 22 in the spiral.The condenser of this kind pattern is the person that generally do not commonly see, and also can use the condenser of other pattern certainly, and is self-evident.Outer cell body 21 also is provided with the import and export of cooling fluid, and cooling fluid can be cold water or refrigerant.
Formation system as above is when implementing the oil product extracting process, 3 operation and reaction process from reactor 1 to separator tank, basically the process with first embodiment is identical, only in separator tank 3 not the gas of liquefaction be imported into the second condenser 2A and cool off once more with low temperature and make its part condense into fluid and flow into tempering tank 7, and mat agitator 8 with this fluid with after fluid from separator tank 3 mixes, be collected in oil-collecting bucket 6, Ye Hua gas is not then discharged the not same of outside via vapor pipe P2 yet.Simple speech, the raw material M gas that pyrolysis produced under the vacuum anaerobic state in reactor 1 flows into first condenser 2 and flow into separator tank 3 after being cooled to liquid, the ultrasonic wave effect that fluid is produced at this mat ultrasonic wave generator 8 and cut off the macromolecular structure of mink cell focus, can increase the harvest yield of lightweight oil, Ye Hua gas is not then cooled off once more by the second condenser 2A, make part condense into the fluid storage and combine in tempering tank 7, and mix with fluid from separator tank 3, can increase and receive oil mass and improve quality.The gas that does not liquefy in tempering tank 7 then mat off-gas pump 4 emits.When implementing this method, mat controlling box 5 and pump 4 are with the temperature in the control pot stage by stage and pumped down power is similar to the method for aforementioned first embodiment at any time, for exempting from repetition, do not repeat them here.After a pyrolysis working cycle is finished, except the oil product that can obtain and higher quality many at oil-collecting bucket 6, also can obtain the activated carbon of high value in the pot than the first embodiment amount, can be rated as and kill two birds with one stone.
In addition, off-gas pump 4 in this embodiment also can be arranged on vapor pipe P1 midway as first embodiment, i.e. the upstream extremity of the second condenser 2A.
Fig. 3 represents the 3rd embodiment of system of the present invention, this system system with first embodiment in fact is identical, just at the exit end of condenser 2, the pneumatic tube P of (being the inlet end of separator tank 3) picks out the return line p that a upper end is communicated with the upstream extremity (being the inlet end of condenser 2) of pneumatic tube P.So, the gas of liquefaction partly can not be back among the pneumatic tube P and distillate the gas back inflow condenser 2 that confluxes and accept condensation through return line p thus.So, can increase the receipts oil mass.In addition, also be provided with ultrasonic wave generator 8 in separator tank 3 bottoms, its effect and effect are identical with second embodiment.
Constituting as above system, to be used for the pyrolysis feed waste wood identical with first embodiment in fact with the operating process that makes fluid, is that the part of the gas of uncooled liquefaction can be back to and is subjected to condensation in the condenser 2 again, to increase income oil mass.For exempting from repetition, do not give unnecessary details in addition.
More than be to be illustrated with regard to preferred embodiment of the present invention, under separated principle of the present invention of nothing and spirit, obviously also can do all modifications and change, for example, separator tank 3 in the system of first embodiment is provided with ultrasonic wave generator 8, in the system of second embodiment, the fluid of separator tank 3 and tempering tank 7 is collected respectively, also can and will not mix.At this moment, on not shown oil exit pipes with two outlets, a two-way change over valve should be set so that fluid is imported tempering tank or another oil-collecting bucket gets final product.All this should be considered as being encompassed in the protection domain of this patent.
Claims (15)
1. the method by living matter waste wood extraction essential oil comprises the following steps:
A. will give birth in the air hermetic reactor of matter waste wood raw material under inside maintenance rough vacuum and anaerobic state and carry out indirect heating, and make it produce the step of pyrolytic reaction (being destructive distillation);
B. above-mentioned raw materials is imported the step that condenser is condensed into liquid through pyrolysis distilled cigarette shape gas;
C. above-mentioned condensed fluid is imported the step that separator tank is separated into water and oil; And
D. step that will poor off-gas pump is discharged through the gas that above-mentioned condensation and separating step do not liquefy;
And state on the implementation in the process of step, the temperature of reactor and pressure are divided into that the two-stage is controlled at least, this control comprises that the mat automatic or manual controls the capable in good time transience of above-mentioned off-gas pump and bleed in a large number at a high speed, so that pyrolysis gas unlikely delay in pot is crossed of a specified duration and heavy constituent, and keep pot inner pressure at any time in predetermined low-pressure state.
2. the method for claim 1, wherein the internal pressure of this reactor in this pyrolytic reaction step remains on 1kg/cm
2Below.
3. method as claimed in claim 1 or 2, wherein the internal pressure of the reactor in this pyrolytic reaction step remains on 0.5～0.8kg/cm
2
4. the method for claim 1, wherein the temperature in this pyrolytic reaction step be controlled to be from 130 ℃ to being divided into a plurality of stages more than 500 ℃, be preferably three phases with on implement.
5. as claim 1 or 4 described methods, wherein this separating step also is included in separator tank imposes cut-out to the macromolecule component in the liquid in the separator tank with the ultrasonic wave generator step.
6. the method by living matter waste wood extraction essential oil comprises the following steps:
A. will give birth in the air hermetic reactor of matter waste wood raw material under inside maintenance rough vacuum and anaerobic state and carry out indirect heating, and make it produce the step of pyrolytic reaction (being destructive distillation);
B. above-mentioned raw materials is imported the step that first condenser is condensed into liquid through pyrolysis distilled cigarette shape gas;
C. above-mentioned condensed fluid is imported the step that separator tank is separated into water and oil; And
D. will import second condenser through the gas that above-mentioned condensation and separating step do not liquefy and impose, and make its portion gas be condensed into the step of liquid again than the cryogenic cooling of first condenser;
E. will import fluid blended step in tempering tank and the aforesaid liquid that imports this tempering tank from above-mentioned separator tank through the liquid of second condenser condenses; And
F. with the gas mat off-gas pump step of being discharged of liquefaction not in the above-mentioned tempering tank;
And state on the implementation in the process of step, the temperature of reactor and pressure are divided into that the two-stage is controlled at least, this control comprises that the mat automatic or manual controls the capable in good time transience of above-mentioned off-gas pump and bleed in a large number at a high speed, so that pyrolysis gas unlikely delay in pot is crossed of a specified duration and heavy constituent, and keep pot inner pressure at any time in predetermined low-pressure state.
7. method as claimed in claim 6, wherein the internal pressure of this reactor in this pyrolytic reaction step remains on 1kg/cm
2Below.
8. method as claimed in claim 6, wherein the internal pressure of the reactor in this pyrolytic reaction step remains on 0.5～0.8kg/cm
2
9. method as claimed in claim 6, wherein the temperature in this pyrolytic reaction step be controlled to be from 130 ℃ to being divided into a plurality of stages more than 500 ℃, be preferably three phases with on implement.
10. method as claimed in claim 6, wherein this separating step also is included in separator tank imposes cut-out to the macromolecule component in the liquid in the separator tank with the ultrasonic wave generator step.
11. the device by living matter waste wood extraction essential oil comprises:
A. one has the outer pan body that periphery wall is provided with electric heating device and heat-insulation and heat-preservation material, and removable being installed with in this outer pan body in order to adorn interior pot reactor of raw material;
B. a condenser that is located at the gas that goes out in order to the above-mentioned reactor of condensation institute gold-plating in reactor downstream side;
C. a downstream side that is located at condenser becomes water and oil separating groove in order to the liquid separation with this condenser condenses, and
D. one be located at the downstream side of separator tank in order to the gas of uncooled liquefaction is discharged the off-gas pump outside the system; And
E. one in order to regulation and control in the reactor temperature and pressure and can even control the controlling box of above-mentioned off-gas pump.
12. device as claimed in claim 11, wherein the bottom land of this separator tank also is provided with the ultrasonic wave generator.
13. device as claimed in claim 11, wherein the nearly exit of this condenser also connects the return line that an end is communicated with the condenser inlet place.
14. one kind by giving birth to the described device of matter waste wood extraction essential oil, comprising:
A. one has the outer pan body that periphery wall is provided with electric heating device and heat-insulation and heat-preservation material, and removable being installed with in this outer pan body in order to adorn interior pot reactor of raw material;
B. first condenser that is located at the gas that goes out in order to the above-mentioned reactor of condensation institute gold-plating in reactor downstream side;
C. a downstream side that is located at condenser becomes water and oil separating groove in order to the liquid separation with this condenser condenses;
D. a downstream side that is located at separator tank is in order to the gas of the uncooled liquefaction of first condenser second condenser of condensation in addition again;
E. a downstream side that is located at second condenser is in order to the liquid of second condenser condenses and tempering tank from the liquid mixing of first condenser condenses of separator tank;
F. a downstream side that is located at tempering tank is used uncooled gas is discharged the off-gas pump of taking out outside the system; And
G. one in order to regulation and control in the reactor temperature and pressure and can even control the controlling box of above-mentioned off-gas pump.
15. device as claimed in claim 14, wherein the bottom land of this separator tank also is provided with the ultrasonic wave generator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009101657039A CN101988026A (en) | 2009-08-06 | 2009-08-06 | Method and device for extracting essential oil by biomass wastes |
Applications Claiming Priority (1)
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| CN2009101657039A CN101988026A (en) | 2009-08-06 | 2009-08-06 | Method and device for extracting essential oil by biomass wastes |
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| CN102380231A (en) * | 2011-11-03 | 2012-03-21 | 李发中 | Oil-water separation device for recovering turpentine |
| CN103756787A (en) * | 2013-12-26 | 2014-04-30 | 中国林业科学研究院林产化学工业研究所 | Method for extracting essential oil from wood processing waste Chinese fir chips to co-produce chemical method activated carbon |
| CN104056673A (en) * | 2014-06-10 | 2014-09-24 | 苏州培英实验设备有限公司 | Novel temperature-control alarming beaker |
| CN104789356A (en) * | 2015-04-20 | 2015-07-22 | 江南大学 | Method for preparing yellow wine smoke gas fragrance reference sample |
| CN104830528A (en) * | 2015-04-23 | 2015-08-12 | 东莞波顿香料有限公司 | Preparation method and use method of aquilaria wood perfume |
| CN106987318A (en) * | 2017-05-03 | 2017-07-28 | 安徽忠盛新型装饰材料有限公司 | A kind of fragrant Chinese fir root-bark essential oil device for refining and its preparation technology |
| CN108026475A (en) * | 2015-08-05 | 2018-05-11 | 伊森舍创新有限责任公司 | The system and method for extracting essential oil |
| CN108485815A (en) * | 2018-05-29 | 2018-09-04 | 云南养瑞科技集团有限公司 | A kind of distillation apparatus of dynamic circulation extraction fragrance |
| CN110772825A (en) * | 2019-12-31 | 2020-02-11 | 潍坊科技学院 | Vegetable waste extract preparation separator |
| CN113083190A (en) * | 2021-03-31 | 2021-07-09 | 西安石油大学 | Microwave thermogravimetric reaction and pyrolysis product staged collection and analysis system and method |
| CN114181777A (en) * | 2021-12-22 | 2022-03-15 | 山东省食品发酵工业研究设计院 | Essential oil aging and quality improvement system and manufacturing method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102380231A (en) * | 2011-11-03 | 2012-03-21 | 李发中 | Oil-water separation device for recovering turpentine |
| CN103756787A (en) * | 2013-12-26 | 2014-04-30 | 中国林业科学研究院林产化学工业研究所 | Method for extracting essential oil from wood processing waste Chinese fir chips to co-produce chemical method activated carbon |
| CN104056673A (en) * | 2014-06-10 | 2014-09-24 | 苏州培英实验设备有限公司 | Novel temperature-control alarming beaker |
| CN104789356A (en) * | 2015-04-20 | 2015-07-22 | 江南大学 | Method for preparing yellow wine smoke gas fragrance reference sample |
| CN104830528A (en) * | 2015-04-23 | 2015-08-12 | 东莞波顿香料有限公司 | Preparation method and use method of aquilaria wood perfume |
| CN108026475A (en) * | 2015-08-05 | 2018-05-11 | 伊森舍创新有限责任公司 | The system and method for extracting essential oil |
| CN106987318A (en) * | 2017-05-03 | 2017-07-28 | 安徽忠盛新型装饰材料有限公司 | A kind of fragrant Chinese fir root-bark essential oil device for refining and its preparation technology |
| CN108485815A (en) * | 2018-05-29 | 2018-09-04 | 云南养瑞科技集团有限公司 | A kind of distillation apparatus of dynamic circulation extraction fragrance |
| CN110772825A (en) * | 2019-12-31 | 2020-02-11 | 潍坊科技学院 | Vegetable waste extract preparation separator |
| CN110772825B (en) * | 2019-12-31 | 2020-03-17 | 潍坊科技学院 | Vegetable waste extract preparation separator |
| CN113083190A (en) * | 2021-03-31 | 2021-07-09 | 西安石油大学 | Microwave thermogravimetric reaction and pyrolysis product staged collection and analysis system and method |
| WO2022215661A1 (en) * | 2021-04-05 | 2022-10-13 | 修 杉澤 | Pyrolysis device and liquefaction processing device in which same is used |
| CN114181777A (en) * | 2021-12-22 | 2022-03-15 | 山东省食品发酵工业研究设计院 | Essential oil aging and quality improvement system and manufacturing method |
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