CN107216904A - A kind of vinegar liquid refining plant and method - Google Patents
A kind of vinegar liquid refining plant and method Download PDFInfo
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- CN107216904A CN107216904A CN201710485008.5A CN201710485008A CN107216904A CN 107216904 A CN107216904 A CN 107216904A CN 201710485008 A CN201710485008 A CN 201710485008A CN 107216904 A CN107216904 A CN 107216904A
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- vinegar liquid
- profit
- cut
- tank
- destilling tower
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C5/00—Production of pyroligneous acid distillation of wood, dry distillation of organic waste
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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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- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
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- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Coke Industry (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The present invention relates to a kind of vinegar liquid refining plant and the method by the device of refining vinegar liquid, the device includes profit hold-up tank, destilling tower and the part of condensing tower three, the tar that profit hold-up tank is used in oil-water separation, obtain rough vinegar liquid, rough vinegar liquid heats up after distillation in a distillation column, the cut for obtaining certain temperature enters condensing tower, and condensed rear collection cut as refines vinegar liquid.The apparatus structure is simple, automatic controlling level is high, with can quantity-produced advantage, effectively utilize biomass heat treated article, form the vinegar liquid product of different purposes.
Description
Technical field
The present invention relates to solid waste resource recovery process field, in particular it relates to a kind of vinegar liquid refining plant and make
The method that refined vinegar liquid is prepared with the device.
Background technology
Biomass refers to the various organisms produced using big gas and water, soil etc. by photosynthesis, i.e., one cuts with life
The organic substance that can be grown of life is commonly referred to as biomass.And so-called biomass energy is exactly solar energy is stored in chemical energy form
Form of energy in biomass, i.e., using biomass as the energy of carrier.So biomass is a kind of important energy source, still
Do not utilized properly at present, the biomass of large area is directly burned, so as to cause forest, range fire, is also frequently resulted in
The generation of smog, has a strong impact on traffic safety, causes the environmental pollution in area or region.A large amount of biomass combustion consumption, not only
Surface vegetation is destroyed, soil erosion is caused, and the pollutant that produces of burning also turns into causes atmosphere pollution and climate change
Major reason.
Biomass pyrolytic technology, can effectively utilize biomass energy, clean energy resource efficiently be produced, by increasing
Concern.In biomass thermal processing procedure, vinegar liquid can be produced, is that the materials such as timber, wood chip, stalk are produced by carbonization
Gaseous product is by a kind of brown liquid obtained from condensation.With the progressively development of charcoal processing industry, plant processing is remaining residual
The liquid close with pyrolkigneous liquid property can be also made by staying thing (such as bamboo wood, Maize kernel, weeds), such as bamboo vinegar, Maize kernel vinegar liquid,
Weeds vinegar liquid etc..The composition contained in vinegar liquid is extremely complex, there is the compound that numerous species are different, wherein most of is all micro
Composition, and topmost composition is water, additionally containing a variety of organic compounds such as acid, ketone, alcohol, phenol and its derivative.Acids
Material is most feature in pyrolkigneous liquid all components, and the content in pyrolkigneous liquid is also very high, about accounts for content of organics
More than half.Additionally containing alkaline matter and many minor metallic elements such as pyridine, amine, methylamines.
Pyrolkigneous liquid, which has, promotes plant growth, soil disinfection, sterilization, insect prevention, anti-corrosion, weeding, deodorization etc. are many should
With.A kind of refined equipment of vinegar liquid is introduced herein, and using biomass pyrolysis product, the refined vinegar liquid of high-efficiency and continuous production realizes pyrolysis
The high value of product.
The content of the invention
The present invention is in view of the above-mentioned problems, purpose is to provide a kind of continous way vinegar liquid refining plant and uses the device system
The method of standby refined vinegar liquid.The charcoal and profit produced after being handled using biomass thermal, continuous treating vinegar liquid.The device includes
Profit hold-up tank, destilling tower and the part of condensing tower three, the tar that profit hold-up tank is used in oil-water separation obtain rough vinegar liquid,
Rough vinegar liquid heats up after distillation in a distillation column, and the cut for obtaining certain temperature enters condensing tower, condensed to collect cut afterwards, i.e.,
To refine vinegar liquid.The apparatus structure is simple, automatic controlling level is high, with can quantity-produced advantage, effectively using biological
Matter heat treated article, forms the vinegar liquid product of different purposes.
To reach above-mentioned purpose, the present invention is adopted the following technical scheme that：
According to the present invention there is provided a kind of vinegar liquid refining plant, comprising：
Profit hold-up tank, the profit hold-up tank is comprising pyrolytic carbon charging aperture and pyrolysis profit charging aperture, rotary shaft, with rotating
At least three agitator arms, pyrolytic carbon outlet and the outlet of rough vinegar liquid of axle connection；The front end of rough vinegar liquid outlet, which is provided with, to be used for
Prevent the filter screen that solid passes through；
Destilling tower, the destilling tower includes distillation tank body, distillation impurities outlet, rough vinegar liquid import, the first fraction outlets, pressure
Power table, thermometer and the electronic liquid level gauge for being arranged on distillation tank interior；Pressure gauge and thermometer are arranged on distillation tank interior
And close to fraction outlets；
Acid-proof pump, the acid-proof pump is arranged between profit hold-up tank and destilling tower, and acid-proof pump will go out from rough vinegar liquid
The rough vinegar liquid of mouth discharge is pumped in the rough vinegar liquid import of destilling tower；The pumping pressure of acid-proof pump is less than holding for the filter screen
It is stressed.
Condensing tower, the condensing tower includes fraction collector, cooling chamber, the second cut import and fraction collection mouthful, cooling chamber
Including coolant inlet, coolant outlet and at least two cut cooling ducts, cut cooling duct is used to cut being condensed into
Liquid, the cut of liquid enters in fraction collector and discharged by the fraction collection mouthful being arranged on fraction collector；
First fraction outlets of destilling tower are connected with the second cut import of condensing tower, and the second cut import is cooled down with cut
Conduit is connected.
Further, the cooling agent that cooling chamber is used is water.
Further, pyrolytic carbon charging aperture is located at directly over profit hold-up tank, and pyrolysis profit charging aperture is stored positioned at profit
Above tank front end, rotary shaft is hit exactly positioned at profit hold-up tank, and agitator arm is uniformly connected on the rotary shaft, and rough vinegar liquid outlet is located at
Below profit hold-up tank rear end.
Further, the rotary shaft upper end of profit hold-up tank is connected by the inner tip center of hinge and profit hold-up tank
Connect, rotary shaft lower end is connected by hinge with the interior bottom portion center of profit hold-up tank；Rotary shaft be uniformly arranged from top to bottom to
Few three agitator arms, at least three agitator arms are connected by way of welding with rotary shaft, and rotary shaft is driven with not by motor
Same rotational speed.
Further, a diameter of 10-20cm of rotary shaft, the rotating speed of rotary shaft is 100-500r/min, agitator arm it is straight
Footpath is 3-5cm.
Further, in profit hold-up tank, pyrolytic carbon intake port is 10-50cm, is pyrolyzed profit intake port
For 10-30cm, pyrolytic carbon outlet diameter is a diameter of 10-30cm that 10-50cm and rough vinegar liquid are exported.
Further, the thermometer that destilling tower is provided with inside heater, destilling tower is communicatedly connected with heater,
Temperature signal is sent to heater to control the temperature in destilling tower by the thermometer inside destilling tower；The outside of destilling tower is set
It is equipped with heat-insulation layer.
Further, the outside on the top of destilling tower is provided with pressure valve, and the pressure gauge of pressure valve and destilling tower is communicatedly
Connection, pressure valve is used to adjust the pressure inside destilling tower.
" communicatedly connect " used in the present invention refers to use well known to a person skilled in the art method by thermometer
Temperature signal is transmitted to heater, or manometric pressure signal is transmitted to pressure valve.Further, impurities outlet is distilled
Immediately below destilling tower.
Further, between a diameter of 2-5cm of cut cooling duct of condensing tower, at least two cut cooling ducts
Away from for 2-5cm.
Further, cut cooling duct is evenly arranged in the middle part of condensing tower, and circulating condensing water is flowed into below condensing tower,
Flowed out after heat exchange above condensing tower, fraction collection mouthful is located at immediately below condensing tower.
Further, the inlet amount of pyrolysis profit is pyrolyzed the flow of profit by observing flowmeter control by Valve controlling；
The charging of pyrolytic carbon is same by Valve controlling；Valve is opened, then is fed；Valve is closed, then stops charging.
Further, the size of filter screen mesh is 0.1-0.5cm.
Further, the top of destilling tower is provided with emergency diffusion valve.
According to the present invention there is provided a kind of method that refined vinegar liquid is prepared using device as above, comprise the following steps：
1) pyrolysis profit and pyrolytic carbon enter profit hold-up tank from pyrolysis profit charging aperture and pyrolytic carbon charging aperture respectively；
2) rotary shaft of profit hold-up tank is opened, is stirred, stirring is stood after finishing, and makes to be consolidated in profit hold-up tank
Liquid is layered, and lower floor's solid is the oil of pyrolytic carbon and absorption, and supernatant liquid is rough vinegar liquid；
3) valve and acid-proof pump of rough vinegar liquid outlet are opened, rough vinegar liquid is flowed out by rough vinegar liquid exit, by resistance to
Sour pumping is to destilling tower；
4) destilling tower distills to rough vinegar liquid, after the completion of distillation, opens the valve at the first fraction outlets, gaseous
Cut enters in condensing tower；
5) gaseous cut enters after the cut cooling duct of condensing tower, valve at ON cycle cooling water and fraction collection mouthful
Door, collects condensed cut, produces refined vinegar liquid.
Further, pyrolytic carbon is graininess, and equivalent diameter is 1cm, and density is more than 1g/cm3, fixing carbon content is
55%-90%, specific surface area is 200-600m2/g。
Further, step 2) in mixing time be 10-100min, stand 15-20min.
Further, the inlet amount of pyrolytic carbon is determined according to the amount of pyrolysis profit, and pyrolytic carbon concentration is 10-100g/L,
Such as pyrolytic carbon concentration is that 10g/L represents often to feed 1L pyrolysis profits, then feeds 10g pyrolytic carbons.
Further, in still-process, using steam or the rough vinegar liquid of heat-conducting oil heating.
Further, vapo(u)rizing temperature can according to product requirement control, be specifically divided into 70 DEG C, 90 DEG C and 110 DEG C etc. it is a variety of
Situation, 70 DEG C of cut mainly includes the material such as moisture and lower boiling acetic acid, and 90 DEG C of cut is mainly high boiling phenols
Material, 110 DEG C of cut is mainly remaining high boiling substance.
Further, pyrolytic carbon is used to adsorb the tar in pyrolysis profit.
Further, step 3) in need to open destilling tower top emergency diffusion valve, root during the rough vinegar liquid of pumping
According to the reading of electronic liquid level gauge, when the volume of rough vinegar liquid occupies 2/3 volume of destilling tower, rough vinegar liquid exit valve is closed
Door, emergency diffusion valve and acid-proof pump.Now, pyrolysis profit and pyrolytic carbon, repeat step can be continuously added in profit hold-up tank
2) step in.
Further, step 4) still-process in, if destilling tower internal pressure is excessive, slowly open emergency diffusion
Valve is maintained within safety value with controlling to distill tower pressure interior force.Determine that destilling tower internal liquid level is high according to electronic liquid level gauge reading
Degree, after the distillation of rough vinegar liquid is finished, closes the outlet of destilling tower overhead fraction, opens emergency diffusion valve, open rough vinegar liquid
The valve and acid-proof pump in exit, repeat step 3).
The beneficial effects of the invention are as follows：
(1) vinegar liquid refining plant continuously-running of the invention, equipment treating capacity is changeable；
(2) automaticity is high in vinegar liquid refining plant processing procedure of the invention, without a large amount of artificial, can be achieved long-range
Operation；
(3) vinegar liquid refining plant of the invention can be connected with biomass thermal processing unit uses, and can also be used alone；
(4) charcoal is replaced using pyrolytic carbon in vinegar liquid refining plant production process of the invention, saves production cost,
And realize the comprehensive utilization of pyrolysis product.
Brief description of the drawings
Fig. 1 is the schematic diagram of the vinegar liquid refining plant according to embodiments of the invention.
Reference
1 pyrolytic carbon charging aperture, 2 flowmeters, 3 pyrolysis profit charging apertures, 5 profit hold-up tanks, 6 rotary shafts, 7 agitator arms, 8 heat
Solve charcoal outlet, 9 rough vinegar liquid outlets, 10 acid-proof pumps, 11 distill impurities outlets, it is 12 destilling towers, 13 emergency diffusion valves, 141 thick
Vinegar liquid import processed, 142 first fraction outlets, 151 pressure gauges, 152 thermometers, 16 electronic liquid level gauges, 17 condensing towers, 18 cooling agents
Outlet, 19 cut cooling ducts, 20 coolant inlets, 21 fraction collections mouth, 22 second cut imports.
Embodiment
In order to make the purpose , technical scheme and advantage of the present invention be clearer, below in conjunction with the accompanying drawings and embodiment, it is right
The present invention is further elaborated.It should be appreciated that specific embodiment described herein is only to explain the present invention, not
For limiting the present invention.
As shown in figure 1, realizing that vinegar liquid refining plant used in the present invention mainly includes following part：Profit hold-up tank 5,
Destilling tower 12 and condensing tower 17.Wherein, pyrolytic carbon entrance is located at directly over profit hold-up tank 5, and profit entrance is stored positioned at profit
Above the front end of tank 5, rotary shaft 6 is hit exactly positioned at profit hold-up tank 5, and agitator arm 7 is uniformly connected in rotary shaft 6, and rough vinegar liquid goes out
Mouth 9 is located at below the rear end of profit hold-up tank 5.Acid-proof pump 10 connects rough vinegar liquid outlet 9 and destilling tower 12, distills impurities outlet 11
Immediately below destilling tower 12, pressure gauge 151 and thermometer are located on the right side of the top of destilling tower 12, and electronic liquid level gauge is located at destilling tower
12 interior sides, the first fraction outlets are located at directly over destilling tower 12, the connection condensing tower 17 of destilling tower 12.Cut cooling duct 19
The middle part of condensing tower 17 is evenly arranged in, circulating condensing water is flowed into by the lower section of condensing tower 17, is flowed after heat exchange by the top of condensing tower 17
Go out, fraction collection mouthful 21 is located at immediately below condensing tower 17.
Profit hold-up tank 5 includes pyrolytic carbon charging aperture 1 and pyrolysis profit charging aperture 3, rotary shaft 6 and is connected with rotary shaft 6
Agitator arm 7, pyrolytic carbon outlet 8 and rough vinegar liquid outlet 9.Agitator arm 7 can set three and more than.Rough vinegar liquid outlet 9
There is filter screen front end, prevents pyrolytic carbon from passing through.The upper end of rotary shaft 6 is connected by hinge with the inner tip center of profit hold-up tank 5, rotation
The lower end of rotating shaft 6 is connected by hinge with the interior bottom portion center of profit hold-up tank 5, the uniform arrangement agitator arm from top to bottom of rotary shaft 6
7, agitator arm 7 is connected by way of welding with rotary shaft 6, and rotary shaft 6 is driven with different rotational speeds by motor.Pyrolysis
Profit and pyrolytic carbon enter after profit hold-up tank 5, and rotary shaft 6 starts, and drive agitator arm 7 uniformly mixing profit and pyrolytic carbon.Stir
Mix after stopping, the liquid portion that the tar ingredients in profit are pyrolyzed in charcoal absorption, profit hold-up tank 5 substantially is rough vinegar
Liquid.Rough vinegar liquid is discharged by rough vinegar liquid outlet 9, is entered via acid-proof pump 10 in destilling tower 12, the course of work of acid-proof pump 10, pressure
What power must not exceed filter screen bears pressure.
Destilling tower 12 include distillation tank body, distillation impurities outlet 11, rough vinegar liquid import 141, the first fraction outlets 142,
Pressure gauge 151, thermometer 152 and electronic liquid level gauge 16, wherein thermometer indicate temperature at fraction outlets, and electronic liquid level gauge is located at
Distill tank interior side and distillation tank body is fixed in electronic liquid level gauge lower end.Rough vinegar liquid is warming up in alembic specifies temperature
Degree, cut gushes out alembic via the outlet of tank body top center, into condensing tower.
Condensing tower 17 include fraction collector, cooling chamber and the second cut import 22, cooling chamber include coolant inlet 20,
Coolant outlet 18 and cut cooling duct 19.Cut enters condensing tower 17 from the second cut import 22 of condensing tower 17；Due to
Second cut import is connected with the cut cooling duct of cooling chamber, and cut enters the cut cooling duct of cooling chamber, now cools down
Agent enters cooling chamber to be cooled down to the cut in cut cooling duct 19 from coolant inlet 20, and cooling agent is from cooling
Flow out agent outlet 18.Cut is condensed into cooling duct as liquid, is flowed into fraction collector, as refines vinegar liquid.It is cold
But the cooling agent that room is used is water.
Cooling chamber in condensing tower 17 uses recirculated cooling water, and cut cooling duct 19 is vertically evenly spaced in cooling chamber
Interior, a diameter of 2-5cm of cooling duct, cooling duct spacing is 2-5cm, and the cut in destilling tower 12 is in cut cooling duct 19
It is cooled to form liquid, flow into fraction collector, i.e. required refined vinegar liquid along cut cooling duct 19.Profit hold-up tank
In 5, the pyrolytic carbon of charging is graininess, and equivalent diameter is 0.1-1cm, and density is more than 1g/cm3, fixed carbon content is 85%-
88%, specific surface area is 300-600m2/g.The inlet amount of pyrolytic carbon determines that concentration is 10- according to the amount of pyrolysis profit
100g/L, such as concentration are that 10g/L represents often to feed 1L pyrolysis profits, then feed 10g pyrolytic carbons.The diameter of rotary shaft 6 is about
10-20cm, the length of agitator arm 7 is slightly shorter than tank body radius, a diameter of 3-5cm of agitator arm 7.The rotating speed of rotary shaft 6 is 100-
500r/min, mixing time is 10-100min.Filter screen mesh size at rough vinegar liquid outlet 9 is 0.1-0.5cm.Pyrolytic carbon
Charging aperture 1 a diameter of 10-50cm, a diameter of 10-30cm of pyrolysis oil water inlet, it is 10-50cm that pyrolytic carbon, which exports 8 sizes, rough
Vinegar liquid exports 9 a diameter of 10-30cm.
Destilling tower 12 uses steam or heat-conducting oil heating, and the outer wrap of destilling tower 12 has 5-10cm heat-insulation layers.Destilling tower
12 tops are provided with pressure gauge 151 and thermometer, are respectively used to temperature at the record internal pressure signal of destilling tower 12 and fraction outlets
Signal, pressure signal is used to control the top pressure valve of destilling tower 12, adjusts the internal pressure of destilling tower 12, and temperature signal is used to control
The heater of destilling tower 12.Electronic liquid level gauge is used for the work for controlling acid-proof pump 10, so as to control the inflow of rough vinegar liquid.
Preferably, profit hold-up tank 5, destilling tower 1212 and condensing tower 17 in shape except cylinder specifically described herein
Outside shape, cone cylinder shape, the other shapes such as square, bar shaped are can also be；In addition, profit hold-up tank 5 can also be accumbency shape.
Preferably, rotary shaft 6 and agitator arm 7 are not limited to appearance described herein, can also be helical-blade sheet etc.
Other agitating devices.
Preferably, the thermal source in destilling tower 12 is not limited to the steam mentioned or heat-conducting oil heating, can also be it is other can be with
The equipment of heating, or other annealing devices used heat.
Preferably, the cooling agent in condensing tower 17 can also select other condensing agents or condensing plant in addition to water.
In addition, the shape design of cooling chamber is also not necessarily limited to described in text.
Preferably, the installation site such as valve and instrument in vinegar liquid refining plant is not limited to the appearance described in text, also
It may be at other places for not influenceing device to work.
The vinegar liquid refining plant of the present invention, specifically used method comprises the following steps：
1) pyrolysis profit and pyrolytic carbon enter profit hold-up tank from pyrolysis profit charging aperture 3 and pyrolytic carbon charging aperture 1 respectively
5, the charging of profit is pyrolyzed by Valve controlling, and the flow of profit is pyrolyzed by observing the control of flowmeter 2；The charging of pyrolytic carbon is same
By Valve controlling, pyrolytic carbon is graininess, and equivalent diameter about 1cm, density is more than 1g/cm3, fixed carbon content is 55%-90%,
Specific surface area is 200-600m2/ g, the inlet amount of pyrolytic carbon determines that concentration is 10-100g/l according to the amount of pyrolysis profit.
2) after the charging of pyrolysis profit and pyrolytic carbon is finished, material inlet valve is closed.Open rotary shaft 6, the diameter of rotary shaft 6
About 10-20cm, the length of the agitator arm 7 of attachment thereon is slightly shorter than tank body radius, a diameter of 3-5cm of agitator arm 7.Rotary shaft
6 rotating speed is 100-500r/min, and mixing time is 10-100min.After stirring is finished, rotary shaft 6 is closed, about 15- is stood
20min, makes pyrolytic carbon be deposited on the bottom of profit hold-up tank 5, now, and the liquid portion in profit hold-up tank 5 is rough vinegar liquid.
3) valve and acid-proof pump at rough vinegar liquid outlet 9 are opened, rough vinegar liquid is flowed out by rough vinegar liquid outlet 9,
And then destilling tower 12 is evacuated to by acid-proof pump.Need to open the top emergency diffusion valve 13 of destilling tower 12 during drawing liquid, according to electricity
The reading of sub- liquid level gauge, when the volume of rough vinegar liquid occupies 2/3 volume of destilling tower 12, closes valve at rough vinegar liquid outlet 9
Door, emergency diffusion valve 13 and acid-proof pump.Now, pyrolysis profit, repeat step 2 can be continuously added in hold-up tank) in pyrolysis oil
The purifying step of water, waits after terminating and continues to distill.
4) in still-process, using steam or the rough vinegar liquid of heat-conducting oil heating, vapo(u)rizing temperature is controlled according to product requirement,
A variety of conditions such as 70 DEG C, 90 DEG C and 110 DEG C are specifically divided into, 70 DEG C of cut mainly includes the thing such as moisture and lower boiling acetic acid
Matter, 90 DEG C of cut is mainly high boiling aldehydes matter, and 110 DEG C of cut is mainly remaining high boiling substance.Treat thermometer
When registration reaches assigned temperature, valve at fraction outlets is opened.Furthermore, it is necessary to pay close attention to the internal pressure of destilling tower 12, pressure is excessive
When, it is slow to open emergency diffusion valve 13 to control tower pressure interior force to maintain within safety value.It is true according to electronic liquid level gauge reading
Determine the internal liquid level of destilling tower 12 height, after the distillation of rough vinegar liquid is finished, close the outlet of the overhead fraction of destilling tower 12, open urgent
Valve 13 is diffused, valve and acid-proof pump at rough vinegar liquid outlet 9, repeat step 3 is opened).
5) cut enters after condensing tower 17, valve at ON cycle cooling water and fraction collection mouthful 21, waits and collects condensation
Cut afterwards, produces refined vinegar liquid.
In addition, should be noted the following aspects using the device of the present invention：
1) pyrolytic carbon in profit hold-up tank 5 needs cleaning daily once, so when finally distilling twice daily, should control
The charging of profit is pyrolyzed, the rough vinegar liquid in profit hold-up tank 5 can be exhausted by distillation twice.Treat that rough vinegar liquid is all entered
Enter after destilling tower 12, open hold-up tank bottom pyrolytic carbon and export 8 valves, empty the pyrolytic carbon of tank interior.
2) destilling tower 12 is needed also exist for opening the valve that impurities outlet 11 is distilled in bottom, will steamed after daily distillation is finished
Evaporate impurity discharge.
Embodiment 1
Prepared using said apparatus and method, stalk pyrolysis product pyrolytic carbon and pyrolysis profit are used as raw material, production
Acetum pyrolignosum rectificatum liquid.It is 200mg/l to be pyrolyzed profit petrochina class content, and the fixation carbon content of pyrolytic carbon is 60%, the ratio of pyrolytic carbon
Surface area is 250m2/ g, the concentration of pyrolytic carbon is 20g/L.The capacity of profit hold-up tank 5 and destilling tower is 10m3, collects 100-
Cut under the conditions of 105 DEG C, single distills treating capacity up to 6.7t, and each distillation time is 1h, daily continuous work 10h, altogether
Treating capacity is counted up to 60t, acetum pyrolignosum rectificatum liquid 55t is obtained.Obtained acetum pyrolignosum rectificatum liquid pH is 2.8, and organic acid content is 3.05%,
Density is 1.02g/cm3, color is in light brown, tar content ＜ 1%.
Embodiment 2
Prepared using said apparatus and method, giantreed pyrolysis product pyrolytic carbon and pyrolysis profit are used as raw material, production
Refined bamboo vinegar.It is 90mg/l to be pyrolyzed profit petrochina class content, and the fixation carbon content of pyrolytic carbon is 85%, the ratio table of pyrolytic carbon
Area is 500m2/ g, the concentration of pyrolytic carbon is 10g/l.The capacity of profit hold-up tank 5 and destilling tower is 10m3, collect 100-105
Cut under the conditions of DEG C, single distills treating capacity up to 6.7t, and each distillation time is 1h, and continuous work 10h, locates altogether daily
Reason amount obtains acetum pyrolignosum rectificatum liquid 55t up to 60t.Obtained acetum pyrolignosum rectificatum liquid is almost colourless, and pH is 2.3, and organic acid content is
3.6%, density is 1.01g/cm3, tar content ＜ 1%.
Embodiment 3
Prepared using said apparatus and method, thermal decomposition of wood product pyrolytic carbon and pyrolysis profit are used as raw material, production
Acetum pyrolignosum rectificatum liquid.It is 60mg/l to be pyrolyzed profit petrochina class content, and the fixation carbon content of pyrolytic carbon is 90%, the ratio table of pyrolytic carbon
Area is 600m2/ g, the concentration of pyrolytic carbon is 10g/L.The capacity of profit hold-up tank 5 and destilling tower is 10m3, collect 100-105
Cut under the conditions of DEG C, single distills treating capacity up to 6.7t, and each distillation time is 1h, and continuous work 10h, locates altogether daily
Reason amount obtains acetum pyrolignosum rectificatum liquid 55t up to 60t.Obtained acetum pyrolignosum rectificatum liquid pH is 2.7, and organic acid content is 3.4%, density
For 1.02g/cm3, color is in colourless, tar content ＜ 1%.
Embodiment 4
Prepared using said apparatus and method, weeds pyrolysis product pyrolytic carbon and pyrolysis profit are used as raw material, production
Refined bamboo vinegar.It is 150mg/l to be pyrolyzed profit petrochina class content, and the fixation carbon content of pyrolytic carbon is 55%, the ratio of pyrolytic carbon
Surface area is 200m2/ g, the concentration of pyrolytic carbon is 100g/l.The capacity of profit hold-up tank 5 and destilling tower is 10m3, collect 100-
Cut under the conditions of 105 DEG C, single distills treating capacity up to 6.7t, and each distillation time is 1h, daily continuous work 10h, altogether
Treating capacity is counted up to 60t, refined weeds vinegar liquid 55t is obtained.Obtained refined weeds vinegar liquid is almost colourless, and pH is 2.9, organic acid
Content is 3.05%, and density is 1.01g/cm3, tar content ＜ 1%.
The foregoing is only presently preferred embodiments of the present invention, not for limit the present invention practical range；If do not taken off
From the spirit and scope of the present invention, the present invention is modified or equivalent substitution, all should covered in the claims in the present invention
Among protection domain.
Claims (10)
1. a kind of vinegar liquid refining plant, it is characterised in that include：
Profit hold-up tank, the profit hold-up tank includes pyrolytic carbon charging aperture and pyrolysis profit charging aperture, rotary shaft and the rotation
At least three agitator arms, pyrolytic carbon outlet and the outlet of rough vinegar liquid of rotating shaft connection；The front end of rough vinegar liquid outlet is provided with use
In the filter screen for preventing solid from passing through；
Destilling tower, the destilling tower includes distillation tank body, distillation impurities outlet, rough vinegar liquid import, the first fraction outlets, pressure
Table, thermometer and the electronic liquid level gauge for being arranged on the distillation tank interior；The pressure gauge and the thermometer are arranged on institute
State distillation tank interior and close to the fraction outlets；
Acid-proof pump, the acid-proof pump is arranged between the profit hold-up tank and the destilling tower, and the acid-proof pump will be from
The rough vinegar liquid of the rough vinegar liquid outlet discharge is pumped in the rough vinegar liquid import of the destilling tower；
Condensing tower, the condensing tower includes fraction collector, cooling chamber, the second cut import and fraction collection mouthful, the cooling
Room includes coolant inlet, coolant outlet and at least two cut cooling ducts, and the cut cooling duct is used for cut
Liquid is condensed into, the cut of liquid enters in the fraction collector and the cut by being arranged on the fraction collector
Collection port is discharged；
First fraction outlets of the destilling tower are connected with the second cut import of the condensing tower, the second cut import and cut
Cooling duct is connected.
2. vinegar liquid refining plant as claimed in claim 1, it is characterised in that the rotary shaft upper end of the profit hold-up tank
It is connected by hinge with the inner tip center of the profit hold-up tank, the rotary shaft lower end is store by hinge and the profit
Deposit the interior bottom portion center connection of tank；The rotary shaft is uniformly arranged at least three agitator arm from top to bottom, it is described at least
Three agitator arms are connected by way of welding with rotary shaft, and rotary shaft is driven with different rotational speeds by motor.
3. vinegar liquid refining plant as claimed in claim 1, it is characterised in that a diameter of 10-20cm of the rotary shaft, described
The rotating speed of rotary shaft is 100-500r/min, a diameter of 3-5cm of the agitator arm.
4. vinegar liquid refining plant as claimed in claim 1, it is characterised in that in the profit hold-up tank, the pyrolytic carbon
Intake port is 10-50cm, and the pyrolysis profit intake port is 10-30cm, and the pyrolytic carbon outlet diameter is 10-
50cm and a diameter of 10-30cm of the rough vinegar liquid outlet.
5. vinegar liquid refining plant as claimed in claim 1, it is characterised in that the destilling tower is provided with heater, described
The thermometer inside destilling tower is communicatedly connected with the heater；The outside of the destilling tower is provided with heat-insulation layer.
6. vinegar liquid refining plant as claimed in claim 1, it is characterised in that the outside on the top of the destilling tower is provided with pressure
Power valve, the pressure valve is communicatedly connected with the pressure gauge of the destilling tower, and the pressure valve is used to adjust the distillation
Pressure inside tower.
7. vinegar liquid refining plant as claimed in claim 1, it is characterised in that the cut cooling duct of the condensing tower is straight
Footpath is 2-5cm, and the spacing between at least two cuts cooling duct is 2-5cm.
8. a kind of usage right requires the method that the device described in any one of 1-7 prepares refined vinegar liquid, it is characterised in that including with
Lower step：
1) pyrolysis profit and pyrolytic carbon enter profit hold-up tank from pyrolysis profit charging aperture and pyrolytic carbon charging aperture respectively；
2) rotary shaft of profit hold-up tank is opened, is stirred, stirring is stood after finishing, makes to carry out solid-liquid point in profit hold-up tank
Layer, lower floor's solid is the oil of pyrolytic carbon and absorption, and supernatant liquid is rough vinegar liquid；
3) valve and acid-proof pump of rough vinegar liquid outlet are opened, rough vinegar liquid is flowed out by rough vinegar liquid exit, by acid-proof pump
It is evacuated to destilling tower；
4) destilling tower distills to rough vinegar liquid, after the completion of distillation, opens the valve at the first fraction outlets, gaseous cut
Into in condensing tower；
5) gaseous cut enters after the cut cooling duct of condensing tower, valve at ON cycle cooling water and fraction collection mouthful,
Condensed cut is collected, refined vinegar liquid is produced.
9. method as claimed in claim 8, it is characterised in that pyrolytic carbon is graininess, equivalent diameter is 1cm, and density is more than
1g/cm3, fixed carbon content is 55%-90%, and specific surface area is 200-600m2/g。
10. method as claimed in claim 8, it is characterised in that step 2) in mixing time be 10-100min, stand 15-
20min。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710485008.5A CN107216904A (en) | 2017-06-22 | 2017-06-22 | A kind of vinegar liquid refining plant and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710485008.5A CN107216904A (en) | 2017-06-22 | 2017-06-22 | A kind of vinegar liquid refining plant and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107216904A true CN107216904A (en) | 2017-09-29 |
Family
ID=59950548
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710485008.5A Pending CN107216904A (en) | 2017-06-22 | 2017-06-22 | A kind of vinegar liquid refining plant and method |
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| Country | Link |
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| CN (1) | CN107216904A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107312562A (en) * | 2017-07-13 | 2017-11-03 | 山东东盟生物科技发展有限公司 | A kind of utilization wood material refines the refinement system and its technique of pyrolkigneous liquid |
| CN110229683A (en) * | 2019-04-01 | 2019-09-13 | 谷峻峰 | A kind of carbonization production wood vinegar biological flue gas system |
-
2017
- 2017-06-22 CN CN201710485008.5A patent/CN107216904A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107312562A (en) * | 2017-07-13 | 2017-11-03 | 山东东盟生物科技发展有限公司 | A kind of utilization wood material refines the refinement system and its technique of pyrolkigneous liquid |
| CN107312562B (en) * | 2017-07-13 | 2023-04-21 | 山东东盟生物科技发展有限公司 | Refining system and process for refining wood vinegar by using wood raw materials |
| CN110229683A (en) * | 2019-04-01 | 2019-09-13 | 谷峻峰 | A kind of carbonization production wood vinegar biological flue gas system |
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