CN108018058A - A kind of converting Processes and apparatus that three-phase recycling is carried out to forest products discarded object - Google Patents
A kind of converting Processes and apparatus that three-phase recycling is carried out to forest products discarded object Download PDFInfo
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- CN108018058A CN108018058A CN201610992503.0A CN201610992503A CN108018058A CN 108018058 A CN108018058 A CN 108018058A CN 201610992503 A CN201610992503 A CN 201610992503A CN 108018058 A CN108018058 A CN 108018058A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
- C10B57/06—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing additives
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
- C11C3/04—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils
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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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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a kind of converting technique that three-phase recycling is carried out to forest products discarded object; the technique dries after first by the removal of impurities of forest products discarded object, cutting, carries out sizing granulation after crushing; it is molded after being mixed using binding agent with wood fragments bits by granule-forming machine; the particle drying after shaping is sent into carbonization kettle again and carries out four-range gradient-heated; obtain multistage product liquid and gaseous product; protection cooling is carried out by being passed through nitrogen after the completion of reaction, obtains solid active product char.In addition; a kind of converting equipment for matching the technique is also disclosed in the present invention; the equipment include be linked in sequence the first drier, pulverizer, mixer, comminutor, the second drier and pyrolysis kettle, and pyrolysis kettle discharge end portion be respectively arranged with solid phase, three groups of discharge ports of liquid phase and gas phase correspond to different processing ends respectively.Of the invention simple, reliable, processing speed is fast, effectively can carry out three-phase recycling to forest products discarded object.
Description
Technical field
Upgrading processing and recovery energy technical field the invention belongs to renewable biomass forest products discarded object, are specially
A kind of converting Processes and apparatus that three-phase recycling is carried out to forest products discarded object.
Background technology
With the increasingly consumption of fossil feedstock, fossil class carbon source for the survival of mankind is faced with the awkward situation of exhaustion, at the same time
Since the main application method of this kind of fossil-carbon energy is all directly to burn, cause atmosphere pollution to aggravate, greenhouse effects by
Year is obvious so that the ecological environment of the earth also runs down.Therefore, discarded renewable carbon resource is developed, is had suitable
Social value and economic benefit.
In various renewable carbon resources, forest products discarded object has the characteristics that species is more, distribution is wide, yield is big, renewable,
And due to rich in carbon, it is considered to be prepare the important carbon raw material of novel energy and chemicals, but forest products discarded object is also deposited
Energy density is low, quantum of output is by seasonal effect is obvious, moisture-sensitive is rotted, it is big to store difficulty, a wide range of collects and long-distance fortune
The defects of defeated of high cost, so, the utilization means in traditional method to these forest products discarded objects are mainly directly burnt, general
Its chemical energy is converted into thermal energy enforcement of going forward side by side and uses, and this Application way energy transformation ratio is low, the thermal efficiency of thermal energy after conversion
It is low, more pollutant can be produced, and be not easy to focus on.
Also there are some producers to use the pyrolytic technique in thermochemical study technology that these forest products waste materials are carried out heat chemistry to turn
Change to submit the utilization rate and utilization ratio of forest products discarded object.Pyrolysis is often called cracking again, it refers in hot conditions
Under, macromolecular (hemicellulose, cellulose and lignin etc.) organic matter contained in biomass is cut off using thermal energy, makes to divide greatly
Sub- substance decomposition is carbon containing less, the relatively small organic matter of molecular weight thermochemical study process.But heat of the prior art
Solution technology is all realized simply by the pyrolysis oven of single structure, and there is no either only a small amount of pretreatment operation, production is set
Standby configuration and technological requirement are higher, and whole pyrolytic process be also easy to occur pyrolysis not exclusively, the pyrolysis cycle is long, was pyrolyzed
The problem of side reaction is more in journey, cause Related product the problem of excessive impurity content, quality decline occur, to heavy industrialization
Production brings larger obstruction.
The content of the invention
Technical problem solved by the invention is to provide a kind of to the converting of forest products discarded object progress three-phase recycling
Technique, the technique can be re-used forest products discarded object with pyrolysis way, to greatest extent will be biological in forest products discarded object
The energy contained in matter is converted into gas, liquid, solid three-phase energy products, its product energies density is high, property is stablized relatively, convenient length
Collection, transport and the storage of radius, have good development prospect and exemplary role.
Technical problem solved by the invention is realized using following technical scheme：
A kind of converting technique that three-phase recycling is carried out to forest products discarded object, specifically includes following operational phase and processing
Step：
First, the pretreatment of raw material stage：Forest products discarded object is cleaned, and the non-uniform each discarded object unit of shape is cut into
The discarded object fragment of 30cm square, then by discarded object fragment be sent into drying equipment, using drying equipment by discarded object fragment into
Row destructive distillation is so that product is ground into by the water content control of discarded object fragment in 4~10% interval range after the completion of destructive distillation
Granularity is considered to be worth doing for the wood fragments of 60~600 mesh.
2nd, sizing pelletization stage：Obtained wood fragments bits in step 1 are added in stirring container, and one in stirring container
And add account for wood fragments bits gross mass 10~30% binding agent, by binding agent and wood fragments bits be uniformly mixed after by particle into
Type machine is shaped to the particle ball of 2~5mm, and molding particle ball is carried out drying operation, by its water content control below 5%,
It is spare.
3rd, pyrolysis phase：The product grain ball prepared in step 2 is moved in carbonization kettle, completely cuts off air and carries out
Gradient-heated, the rule of its gradient-heated are：First gradient temperature range be 100~150 DEG C, heating rate for 5~20 DEG C/
Min, soaking time are 2~3h, obtain a small amount of product liquid；The second gradient temperature is warming up to, temperature range is 150~400 DEG C,
Heating rate is 2~15 DEG C/min, and soaking time is 1~4h, obtains a large amount of product liquids and gaseous product；It is warming up to the 3rd ladder
Temperature is spent, temperature range is 400~500 DEG C, and heating rate is 5~20 DEG C/min, and soaking time is 1~2h, obtains a small amount of liquid
Body product and a large amount of gaseous products；4th gradient is warming up to, temperature range is 500~800 DEG C, and heating rate is controlled 10~20
DEG C/min, soaking time is 2~4h, this process is collected without obvious liquids and gases；After close heating unit, be cooled to
Room temperature, rate of temperature fall are 2~10 DEG C/min, during be passed through nitrogen and protected, obtain Product Activity charcoal.
Further, dried in the retort process in the step 1 using blowing-type hot-air, the control of its drying temperature exists
50~100 DEG C, and in this retort process, it is 1~5 DEG C/min to control heating rate, soaking time is 3~5h.
Further, the binding agent used in the step 2 is preferably animal and plant fat, syrup, aliphatic acid, starch, plant
One or several kinds of arbitrary proportion mixtures in pitch, coal tar, according to binding agent be dry matter when, need to be mixed
Addition accounts for the pure water of mixture material total mass fraction 5~10% in compound, and pure water temperature is controlled at 15~30 DEG C, adds speed
To account for mixture material gross mass 0.2%/min, apply stirring operation in adition process, to ensure that it is uniformly mixed, with convenient
Prepare particle ball.
Further, dried in the drying course in the step 2 using blowing-type hot-air, the control of its drying temperature exists
50~100 DEG C, and in drying course, it is 0.5~2 DEG C/min to control heating rate, soaking time is 6~12h.
Further, the heating of isolation air described in the step 3 refers to completely cuts off air in overall heating process, and keeps
Nitrogen is passed through, its nitrogen is passed through 0.2~2%/min that speed is device spatial volume；And nitrogen is passed through speed in temperature-fall period
Rate is 1~5%/min of device spatial volume.
In the present invention, the product liquid collected in the first gradient in the step 3 is mainly wood vinegar；Second ladder
The product liquid collected in degree is mainly wood vinegar, bio oil and alcohols, is distributed in water-oil phase, and gas is alkane containing short chain
The flammable on-condensible gas of hydrocarbon, alkene etc.；The product liquid collected in 3rd gradient is mainly bio oil；And gas is short hydrocarbon
The gases such as class.These products are carrying out storage and in use, the closed preservation by the way of room temperature damp proof insulation trapping of Product Activity charcoal,
Gaseous products can be used for the combustion heating of cracker, seals up for safekeeping and continues to employ also into gas holder.
Further, the gas-phase product separated in the step 3 can be used for the reuse of combustion furnace to heat, and returned
With combustion heating or directly before storage, it is necessary to be passed through the either potassium hydroxide or two of the sodium hydroxide containing 50~80% mass fractions
In the buck of person's arbitrary proportion mixture and acidic materials, molecular sieve dehydration is then used again.
Further, the product liquid collected in the step 3 can be focused on upon mixing, it mixes liquid phase
Produce product carry out post processing mode：Gu by the oil in liquid-phase product, water two-phase using liquid-liquid-tube centrifuge 5000~
Separated under the conditions of the centrifuge speed of 7000r/min.Water after water-oil separating is mainly mutually wood vinegar, can directly be received
Collection；And mixture oil phase is heated to 60~80 DEG C, adds mass fraction and urged for 20~40% methanol and 1~3% solid acid
Agent, 2~4h of back flow reaction, cold filtration solid phase acid catalyst, obtains product bio oil, is mainly used as fuel oil use, its
In, solid acid catalyst is zirconium oxide, p-methyl benzenesulfonic acid, aluminum sulfate, aluminium oxide, one or several kinds of any in aluminum phosphate
The mixture of ratio.
A kind of converting equipment that three-phase recycling is carried out to forest products discarded object, combination is designed based on above-mentioned technique,
It includes the first drier, pulverizer, mixer, comminutor, the second drier and the pyrolysis kettle being linked in sequence, the pyrolysis
The discharge end portion of kettle is respectively arranged with three groups of solid phase, liquid phase and gas phase discharge ports, the connection activated carbon storage of its solid phase discharge port
Groove；Gas phase discharge port connects gas storage holder；And liquid phase discharge port then connects secondary operation unit, the secondary operation unit includes cold
Condenser, centrifuge and reaction kettle, the gas outlet connection gas storage holder of the condenser, liquid outlet are connected with liquid storage tank, it is described from
Scheming is used for the water-oil separating of liquid phase, it is connected to liquid storage tank lower part, its water mutually exports connection wood vinegar storage tank, and oil phase exports then
It is connected with reaction kettle feed inlet, and the discharge port of reaction kettle is then connected with bio oil storage tank.
Further, the feed end that waste recovery pipe is connected to mixer is provided with the comminutor.
Advantages of the present invention and beneficial effect are：
1. the method for the present invention more stresses the comprehensive utilization of product compared with the prior art, and utilizes forest products pyrolysis of waste
Co-producing active carbon, bio oil and biogas, have saved the energy, improve value of the product.
2. the method for the present invention is different compared with the technique of the direct output charcoal of the prior art, by coproduction gas, oil while directly
The activated carbon of physical modification is obtained, discarded object is realized and prepares solid carbon higher value application.
3. product sulphur, the ash harmful content of material that grades are fewer in the present invention, the row of having a net increase of of CO2 during carbon cycle utilization
It is high-volume zero, is conducive to the protection of environment.
4. the energy contained in biomass can be converted into gas, liquid, solid three by pyrolytic technique to greatest extent in the present invention
Phase energy products, product energies density is high, property is stablized relatively, facilitates the transport, collection and storage of major radius, has good
Development prospect and exemplary role.
The characteristics of technique is continuous, simple, reliable 5. the present invention has, and processing speed is fast, when average response 6~8 is small
Terminate whole segment process.
6. the present invention integrates, bio oil is modified, allocates, and without increasing additional technique, product may be directly applied to boiler
Used with oil range.
Brief description of the drawings
Fig. 1 is the structure diagram of the converting equipment of the present invention.
Wherein：1st, the first drier；2nd, pulverizer；3rd, mixer；4th, comminutor；5th, it is pyrolyzed kettle；6th, liquid storage tank；7th, condense
Device；8th, centrifuge；9th, reaction kettle；10th, bio oil storage tank；11st, wood vinegar storage tank；12nd, gas storage holder；13rd, activated carbon storage tank；14、
Second drier.
Embodiment
In order to make the technical means, the creative features, the aims and the efficiencies achieved by the present invention easy to understand, tie below
Conjunction is specifically illustrating and embodiment, and the present invention is further explained.
Referring to a kind of converting equipment that three-phase recycling is carried out to forest products discarded object of Fig. 1, in the present embodiment, equipment
Include setting the first drier 1 with front end, this first drier 1 is used to dry the forest products discarded object as raw material
Dry, its discharge end is connected with pulverizer 2, mixer 3 and comminutor 4 in turn, and wherein pulverizer 2 is used for dried forest products
Waste materials are crushed, its adjustable crushing mesh number is 60~600 mesh, and the feed end of comminutor 4 connection mixer 3
Discharge end, meanwhile, in order to improve the stability of the discharging of comminutor 4, waste recovery pipe be provided with comminutor 4 be connected to and stir
The feed end of machine 3 is mixed, and the discharge end in comminutor 4 is additionally provided with the second drier 14, and connected by the second drier 14
It is pyrolyzed kettle 5.In the present embodiment, the second drier 14 is used to carry out drying behaviour to the intermediate products for being granulated completion in comminutor
Make, and be pyrolyzed main reaction unit of the kettle 5 then as pyrolytic reaction.
It is provided with pyrolysis kettle 5 and is respectively arranged with three solid phase, liquid phase, gas phase discharge ports, wherein, the connection of solid phase discharge port
Activated carbon storage tank 13；Gas phase discharge port connects gas storage holder 12；Liquid phase discharging metastomium connection condenser 7, the outlet of this condenser 7
Mouth connection gas storage holder 12, and liquid outlet is then connected with liquid storage tank 6, and the centrifugation at outlet tube connection rear portion is provided with this liquid storage tank 6
Machine 8, Gu this centrifuge 8 is liquid-liquid-tube centrifuge, for mutually being separated with water to the oil phase in liquid phase, it is separated
Water the wood vinegar storage tank 11 of connection is mutually sent into by pipeline, and oil phase is then expired latter linked reaction kettle 9 by Pipeline transport
In, and the reaction finished product in reaction kettle 9 is then sent into biological oil tank 10.
In addition, being additionally provided with two groups of embodiments, this two groups of embodiments are carried out at material using the said equipment as Boats
It is prepared by reason, wherein：
Embodiment 1
Converting raw material is used as using industrial traditional oil tree wilson dogwood branch.
500Kg wilson dogwood branch is weighed, 2 DEG C/min heating rates keep the temperature 4h to 60 DEG C, and control moisture leads to 5% or so
Cross pulverizer and be prepared into 200 mesh or so sawdust.By sawdust and 15% adhesive (starch: vegetable oil=1: 1) uniform stirring system
Into particulate microsphere, dry heating rate is 1 DEG C/min, and pyrolysis kettle is moved to after soaking time 8h, is passed through nitrogen isolation air and carries out
Gradient-heated.
First gradient temperature is 100~150 DEG C, and heating rate control is collected on a small quantity in 5 DEG C/min, soaking time for 2h
Cool down aqueous；Second gradient temperature, temperature range are 150~400 DEG C, 10 DEG C/min, soaking time 4h, obtain a large amount of coolings
Product liquid and gaseous product；3rd gradient temperature, temperature range are 400~500 DEG C, and heating rate is controlled in 10 DEG C/min,
Soaking time obtains a small amount of product liquid and a large amount of gaseous products for 1h；Be warming up to 4th gradient, temperature range for 500~
800 DEG C, heating rate control is collected in 10 DEG C/min, soaking time 3h, no obvious liquids and gases.After close plus
Thermal, during be passed through nitrogen and protected, rate of temperature fall is 3 DEG C/min, is passed through N2 speed as device spatial volume
2%/min.
The gas-phase product separated is passed through the elution of 60% buck and molecular sieve dehydration；Liquid-phase product passes through 6000r/min
Gu liquid-liquid-tube centrifuge separates water phase and oil phase.Oil phase is heated to 80 DEG C, add methanol that mass fraction is 30% and
1.5% solid acid catalyst (p-methyl benzenesulfonic acid), back flow reaction 2.5h, cold filtration solid phase acid catalyst, obtains product life
Thing oil.
And the pyrolysis coproduction charcoal gas and oil yield and performance of each product thus prepared under the conditions of embodiment are as shown in table 1：
Table 1 is pyrolyzed coproduction charcoal gas and oil yield and performance
Embodiment 2
On the south the lumps of wood this oil crops Asiatic sweet leaf branch as converting raw material.
Weigh 1000Kg wilson dogwood branch, 3 DEG C/min heating rates keep the temperature 3h to 70 DEG C, control moisture 5% or so,
250 mesh or so sawdust is prepared into by pulverizer.Particulate microsphere is made in sawdust and 10% adhesive (starch) uniform stirring,
Dry heating rate is 1 DEG C/min, and pyrolysis kettle is moved to after soaking time 6h, is passed through N2 isolation air and carries out gradient-heated.
Remaining steps are with reference to embodiment 1.
And the pyrolysis coproduction charcoal gas and oil yield and performance of each product thus prepared under the conditions of embodiment are as shown in table 2：
Table 2 is pyrolyzed coproduction charcoal, gas, oily yield and performance
Basic principle, main feature and the advantages of the present invention of the present invention has been shown and described above.The technology of the industry
Personnel are it should be appreciated that the present invention is not limited to the above embodiments, and the above embodiments and description only describe this
The principle of invention, without departing from the spirit and scope of the present invention, various changes and modifications of the present invention are possible, these changes
Change and improvement all fall within the protetion scope of the claimed invention.The claimed scope of the invention by appended claims and its
Equivalent thereof.
Claims (10)
1. a kind of converting technique that three-phase recycling is carried out to forest products discarded object, it is characterised in that including the following operational phase
And processing step：
1. the pretreatment of raw material stage：Forest products discarded object is cleaned, and the non-uniform each discarded object unit of shape is cut into 30cm
The discarded object fragment of square, is then sent discarded object fragment into drying equipment, is done discarded object fragment using drying equipment
Evaporate so that product is ground into particle by the water content control of discarded object fragment in 4~10% interval range after the completion of destructive distillation
Spend the wood fragments bits for 60~600 mesh；
2. pelletization stage of shaping：Obtained wood fragments bits in step 1 are added in stirring container, and are added in the lump in stirring container
Enter to account for the binding agent of wood fragments bits gross mass 10~30%, pass through granule-forming machine after binding agent and wood fragments bits are uniformly mixed
The particle ball of 2~5mm is shaped to, molding particle ball is subjected to drying operation, it is spare by its water content control below 5%；
3. pyrolysis phase：The product grain ball prepared in step 2 is moved in carbonization kettle, completely cuts off air and carries out gradient
Heating, the rule of its gradient-heated are：First gradient temperature range is 100~150 DEG C, and heating rate is 5~20 DEG C/min, is protected
The warm time is 2~3h, obtains a small amount of product liquid；The second gradient temperature is warming up to, temperature range is 150~400 DEG C, heating speed
Rate is 2~15 DEG C/min, and soaking time is 1~4h, obtains a large amount of product liquids and gaseous product；It is warming up to 3rd gradient temperature
Degree, temperature range are 400~500 DEG C, and heating rate is 5~20 DEG C/min, and soaking time is 1~2h, obtain a small amount of liquid production
Thing and a large amount of gaseous products；Be warming up to 4th gradient, temperature range is 500~800 DEG C, heating rate control 10~20 DEG C/
Min, soaking time are 2~4h, this process is collected without obvious liquids and gases；After close heating unit, be cooled to room
Temperature, rate of temperature fall are 2~10 DEG C/min, during be passed through nitrogen and protected, obtain Product Activity charcoal.
2. converting technique according to claim 1, it is characterised in that the step 1. in retort process in use
Blowing-type hot-air is dried, its drying temperature is controlled at 50~100 DEG C, and in this retort process, control heating rate be 1~
5 DEG C/min, soaking time is 3~5h.
3. converting technique according to claim 1, it is characterised in that 2. the middle binding agent used is the step
One or several kinds of arbitrary proportion mixtures in vegetable fat, syrup, aliphatic acid, starch, plant asphalt, coal tar, and
When binding agent uses dry matter, the pure water for accounting for mixture material total mass fraction 5~10% need to be added in the mixture, it is pure
Coolant-temperature gage is controlled at 15~30 DEG C, adds speed to account for mixture material gross mass 0.2%/min, and be uniformly mixed.
4. converting technique according to claim 1, it is characterised in that the step 2. in drying course in use
Blowing-type hot-air is dried, its drying temperature is controlled at 50~100 DEG C, and in drying course, control heating rate be 0.5~
2 DEG C/min, soaking time is 6~12h.
5. converting technique according to claim 1, it is characterised in that the step 3. described in completely cut off air heating
Finger completely cuts off air in overall heating process, and keeps being passed through nitrogen, its nitrogen be passed through that speed is device spatial volume 0.2~
2%/min.
6. converting technique according to claim 1, it is characterised in that nitrogen is passed through speed as dress in temperature-fall period
Put 1~5%/min of spatial volume.
7. converting technique according to claim 1, it is characterised in that the step 3. in separate gas phase production
Thing is first passed through sodium hydroxide or hydroxide containing 50~80% mass fractions before carrying out reuse combustion heating or directly storing
In the buck of potassium or both arbitrary proportion mixture and acidic materials, molecular sieve dehydration is then used again.
8. converting technique according to claim 1, it is characterised in that the product liquid of the step 3. middle collection exists
Focused on after mixing, liquid phase mixture product progress post processing mode is by it：
Gu the oil in liquid-phase product, water two-phase are used into liquid-liquid-tube centrifuge in the centrifugal basket of 5000~7000r/min
Separated under the conditions of speed；
Water after water-oil separating is mutually directly collected；
Mixture oil phase after water-oil separating is heated to 60~80 DEG C, adds the methanol and 1~3% that mass fraction is 20~40%
Solid acid catalyst, 2~4h of back flow reaction, cold filtration solid phase acid catalyst, obtains product bio oil.
9. converting technique according to claim 9, it is characterised in that the solid acid catalyst is zirconium oxide, right
The mixture of one or several kinds of arbitrary proportions in toluenesulfonic acid, aluminum sulfate, aluminium oxide, aluminum phosphate.
10. a kind of converting equipment that three-phase recycling is carried out to forest products discarded object, it is characterised in that the equipment is based on above-mentioned work
Skill is designed combination, and converting for coming to carry out forest products discarded object in any technique in claim 1~9
Processing, it includes the first drier, pulverizer, mixer, comminutor, the second drier and the pyrolysis kettle being linked in sequence, institute
The discharge end portion for stating pyrolysis kettle is respectively arranged with three groups of solid phase, liquid phase and gas phase discharge ports, and the connection of its solid phase discharge port is lived
Property charcoal storage tank；Gas phase discharge port connects gas storage holder；And liquid phase discharge port then connects secondary operation unit, the secondary operation unit
Including condenser, centrifuge and reaction kettle, the gas outlet connection gas storage holder of the condenser, liquid outlet is connected with liquid storage tank,
The centrifuge is used for the water-oil separating of liquid phase, it is connected to liquid storage tank lower part, its water mutually exports connection wood vinegar storage tank, oil phase
Outlet is then connected with reaction kettle feed inlet, and the discharge port of reaction kettle is then connected with bio oil storage tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610992503.0A CN108018058A (en) | 2016-11-04 | 2016-11-04 | A kind of converting Processes and apparatus that three-phase recycling is carried out to forest products discarded object |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610992503.0A CN108018058A (en) | 2016-11-04 | 2016-11-04 | A kind of converting Processes and apparatus that three-phase recycling is carried out to forest products discarded object |
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| CN108018058A true CN108018058A (en) | 2018-05-11 |
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| CN111849529A (en) * | 2020-07-20 | 2020-10-30 | 中国工程物理研究院材料研究所 | Thermal cracking treatment device and method for radioactive waste resin |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3221495A1 (en) * | 1982-06-07 | 1983-12-08 | Linde Ag, 6200 Wiesbaden | Process and device for converting sewage sludge into oil and coal |
| CN101875845A (en) * | 2010-07-08 | 2010-11-03 | 浙江工业大学 | Process for co-producing bio-oil and biological carbon by utilizing crop straws and special device |
| CN102226095A (en) * | 2011-05-27 | 2011-10-26 | 中国科学院过程工程研究所 | Device and method for preparing fuel and chemicals by gradient pyrolysis of biomass and step-by-step collection |
| CN102277188A (en) * | 2011-07-25 | 2011-12-14 | 青岛福瑞斯生物能源科技开发有限公司 | Biomass thermal cracking liquefying fuel oil technology |
| CN102653691A (en) * | 2012-02-29 | 2012-09-05 | 东南大学 | Device and method for preparing oxygen-containing liquid fuel by catalytically converting biological oil |
| KR20120104066A (en) * | 2011-03-11 | 2012-09-20 | 구자숭 | Method for making bio-oil and carbide using bio-mass |
| CN103695014A (en) * | 2013-12-11 | 2014-04-02 | 吉林大学 | Method for preparing methyl alcohol biomass oil through rice husk |
| CN104498065A (en) * | 2014-12-25 | 2015-04-08 | 刘荣 | High-efficiency biomass pyrolysis and purification technology |
-
2016
- 2016-11-04 CN CN201610992503.0A patent/CN108018058A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3221495A1 (en) * | 1982-06-07 | 1983-12-08 | Linde Ag, 6200 Wiesbaden | Process and device for converting sewage sludge into oil and coal |
| CN101875845A (en) * | 2010-07-08 | 2010-11-03 | 浙江工业大学 | Process for co-producing bio-oil and biological carbon by utilizing crop straws and special device |
| KR20120104066A (en) * | 2011-03-11 | 2012-09-20 | 구자숭 | Method for making bio-oil and carbide using bio-mass |
| CN102226095A (en) * | 2011-05-27 | 2011-10-26 | 中国科学院过程工程研究所 | Device and method for preparing fuel and chemicals by gradient pyrolysis of biomass and step-by-step collection |
| CN102277188A (en) * | 2011-07-25 | 2011-12-14 | 青岛福瑞斯生物能源科技开发有限公司 | Biomass thermal cracking liquefying fuel oil technology |
| CN102653691A (en) * | 2012-02-29 | 2012-09-05 | 东南大学 | Device and method for preparing oxygen-containing liquid fuel by catalytically converting biological oil |
| CN103695014A (en) * | 2013-12-11 | 2014-04-02 | 吉林大学 | Method for preparing methyl alcohol biomass oil through rice husk |
| CN104498065A (en) * | 2014-12-25 | 2015-04-08 | 刘荣 | High-efficiency biomass pyrolysis and purification technology |
Non-Patent Citations (3)
| Title |
|---|
| 刘汉湖: "《固体废物处理与处置》", 31 August 2009, 中国矿业大学出版社 * |
| 李方正: "《无处不有的生物质能》", 31 August 2013, 吉林出版集团有限责任公司 * |
| 肖波: "《生物质热化学转化技术》", 30 June 2016, 冶金工业出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111849529A (en) * | 2020-07-20 | 2020-10-30 | 中国工程物理研究院材料研究所 | Thermal cracking treatment device and method for radioactive waste resin |
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