CN104178198A - Method and equipment for producing liquefied straw oil - Google Patents
Method and equipment for producing liquefied straw oil Download PDFInfo
- Publication number
- CN104178198A CN104178198A CN201410330278.5A CN201410330278A CN104178198A CN 104178198 A CN104178198 A CN 104178198A CN 201410330278 A CN201410330278 A CN 201410330278A CN 104178198 A CN104178198 A CN 104178198A
- Authority
- CN
- China
- Prior art keywords
- powder
- straw
- bed material
- oil
- liquefaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Processing Of Solid Wastes (AREA)
Abstract
The invention relates to a method and equipment for producing straw oil with relatively high heat value. The method comprises the following steps: respectively processing straw powder stocks and bed material stocks; feeding the straw powder stocks and the bed material stocks into a thermal cracking box and performing cracking reaction; condensing a cracked gas into liquid biological oil in a condenser; adding an additive which comprises straw carbonizing powder, rubber carbonizing powder and animal skeleton carbonizing powder in the process of processing straw raw materials into straw powder, wherein a bed material is a composition which comprises pottery clay powder and a catalyst, the catalyst comprises platinum, nickel, cerium oxide powder, iron powder and tourmaline powder and the weight ratio of the straw powder and the bed material which enter the thermal cracking box is 7:3; and performing cracking reaction in the thermal cracking box in vacuum at a temperature of 450 DEG C-500 DEG C for 0.3-0.5 seconds. The equipment disclosed by the invention is specially used for implementing the method. The method disclosed by the invention can be used for greatly improving the transformation rate of the straw oil and also greatly enhancing the heat value and is low in cost and easy to popularize.
Description
Technical field
The present invention relates to a kind of method and apparatus of producing liquefaction of corn straw oil.
Background technology
The stalk of farm crop contains biomass energy, liquefaction of corn straw become oil be biomass energy effectively utilize mode, obtain heat energy and compare with directly burning with stalk, the utilization ratio raising of biomass energy is more than 30%, produce multiple useful value byproduct simultaneously, have broad application prospects.In liquefaction of corn straw process, mainly comprise stalk material after pulverizing and join and in thermo-cracking case, carry out heat scission reaction as the bed material of heating working medium, by the gaseous substance forming after thermo-cracking, be condensed into liquid wet goods step, but existing processing method is due to the condition restriction of thermo-cracking case, its scission reaction speed is slower, easily produce secondary reaction, and additive is different from the selection of catalyzer in reaction process, the series of problems such as temperature of reaction control, its consequence is that the moisture of the stalk oil produced is higher, calorific value is on the low side, and stalk to be converted into the transformation efficiency of stalk oil on the low side, this is the defect of prior art.
Summary of the invention
The technical problem to be solved in the present invention is to provide a kind of more method and apparatus of the stalk oil of high heating value of tool of producing.
The method of production liquefaction of corn straw oil of the present invention, comprises and processes respectively the step that straw powder is got the raw materials ready and bed material is got the raw materials ready; Described straw powder is got the raw materials ready and bed material is got the raw materials ready enters the step of carrying out scission reaction in thermo-cracking case; Cracked gas is condensed into the step of liquid biological oil in condenser;
It is characterized in that: when processing straw powder is got the raw materials ready, add the additive being formed by straw charring powder, rubber carbonization power and animal corpse carbonization power;
Described bed material is the composition of potter's clay powder and catalyzer composition, and wherein catalyzer is comprised of platinum, nickel, cerium oxide powder, iron powder, Tourmaline powder;
The straw powder and the mass ratio of expecting that in unit time, enter in thermo-cracking case are 7:3;
Scission reaction in thermo-cracking case is carried out under the condition of vacuum, and temperature is controlled at 450 ~ 500 ℃, and the reaction times is controlled in 0.3 ~ 0.5s.
Stalk is processed into the Powdered of 1 ~ 3mm, and controls moisture content in 3 ~ 5%, and temperature is at 95 ~ 100 ℃.
The device of production liquefaction of corn straw oil of the present invention, comprises the vacuum bed material bin of getting the raw materials ready for storage bed material being communicated with thermo-cracking case;
For the stirrer that straw powder and additive are mixed;
For making the vacuum cooling tower of gaseous product condensation;
It is characterized in that: also comprise the vacuum drying oven being connected between stirrer and thermo-cracking case, described additive is comprised of straw charring powder, rubber carbonization power and animal corpse carbonization power; Described bed material is the composition of potter's clay powder and catalyzer composition, and wherein catalyzer is comprised of platinum, nickel, cerium oxide powder, iron powder, Tourmaline powder; Described thermo-cracking case is that an inner chamber can evacuated casing, and its inside is provided with barrel-shaped hybrid chamber and the spiral pipe being communicated with up and down, and some venting holes are set on spiral pipe.
The invention has the beneficial effects as follows:
1) quality that straw powder Minton dryer can improve straw powder is set, control moisture (3-5%) and temperature (95-100 ℃), make its temperature difference in the process reacting with bed material reduce, strengthen antioxygenation, and can reduce the moisture content of stalk oil in forming process;
2) in straw powder, add a certain amount of additive being formed by straw charring powder, rubber carbonization power and animal corpse carbonization power, in reaction process, play the effect that adds fast pyrolysis;
3) in bed material, add a certain amount of catalyzer being formed by platinum, nickel, cerium oxide powder, iron powder, Tourmaline powder, impel C-O ether-oxygen bond fracture quickening, the shortening heat pyrolysis time of stalk in cracking process, thereby being formed in reaction process, straw powder material take C-H as basic more oxy-compound, the transformation efficiency that stalk is converted into stalk oil increases greatly, and calorific value is also improved, calorific value can reach 4500 ~ 5000 kilocalories.
4) equipment manufacturing cost of the present invention is cheap, and operation cost significantly reduces, and easily promotes.
Accompanying drawing explanation
Fig. 1 is device and the process flow diagram of production liquefaction of corn straw oil of the present invention.
Fig. 2 is the enlarged view of the vacuum drying oven in Fig. 1.
Fig. 3 is the enlarged view of the thermo-cracking case in Fig. 1.
Fig. 4 is the enlarged view of the bed material heating container in Fig. 1.
Fig. 5 is the enlarged view of the vacuum cooling tower in Fig. 1.
Fig. 6 is primary oil's separator box in Fig. 1 and the enlarged view of primary oil's strainer.
Embodiment
Now in conjunction with the accompanying drawings and embodiments the present invention is described in further detail.
Fig. 1 is the setting drawing of production liquefaction of corn straw oil of the present invention, has also reacted technical process of the present invention, comprises stalk work flow, bed material work flow, stalk speed pyrolysis gasification process and liquefaction oil work flow.Whole device is placed under vehicle-mounted condition, can arrive easily different places like this, is convenient to the realization that straw powder is gathered materials on the spot.
Stalk processing is performed such: raw material stalk becomes the Powdered stalk of 1 ~ 3mm after pulverizing in pulverizer 11, this straw powder enters materials-stored box 12 via transport pipe, after the magnetic separator 13 that is positioned at materials-stored box 12 belows is processed it, straw powder falls into contaminant filter sieve 14 and removes impurity, then enter hotblast stove 15 and dry, make its moisture controlled at the state of ﹤ 10%; In additive tank 17, fill straw charring powder, rubber carbonization power and animal corpse carbonization power and take the additive that mass ratio mix to form as 1:1:1.From the straw powder in hotblast stove 15 and the additive from additive tank 17, in stirrer 16, fully stir rear (mixing quality ratio is 97:3), by transport pipe, enter in vacuum drying oven 19, please refer to Fig. 2, vacuum drying oven 19 by can evacuated casing 191 and temperature control burner form, this casing is provided with vacuum pump 192, and temperature control burner forms by being placed in the gas-cooker 193 of casing below and the temperature-sensing valve 194 being connected with this gas-cooker.Vacuum drying oven 19 can make straw powder insulation at approximately 95 ~ 100 ℃, and moisture controlled is in 3 ~ 5% state, as next step, carries out one of getting the raw materials ready of fast pyrolysis, and in the present embodiment, vacuum drying oven 19 is identical two pairs.
Bed material work flow is such, please refer to Fig. 4, and the processing of bed material is mainly carried out in bed material heating container 20.Bed material is composition, and its component is 90% ceramics powder and 10% catalyzer, and wherein catalyzer is comprised of platinum, nickel, cerium oxide powder, iron powder, Tourmaline powder; The mass ratio that forms the each component of described catalyzer is 0.02:0.08:5.9:2:2.Described bed material is processed into particle 1 ~ 1.5mm spherical shape.Bed material enters in bed material heating kettle 22 via bed material entrance 21, the below of heating kettle 22 is combustion chambers 23, in it, be provided with the blowdown pipe 24 communicating with the lower end of heating kettle 22, bed material is after the interior Hybrid Heating of heating kettle 23, enter further heating in blowdown pipe 24, and via discharging pump 25, from bed material conveying belt 26, arrive bed material bins 27, it is temporary that the temperature of bed material is controlled at the state of 800 ~ 850 ℃, as next step carry out fast pyrolysis get the raw materials ready two.
Stalk speed pyrolysis gasification process is carried out in thermo-cracking case 30, referring to Fig. 3, thermo-cracking case 30 is that an inner chamber can evacuated casing, its inside is provided with barrel-shaped hybrid chamber 31 and the spiral pipe 32 being arranged above and below, the upper end of spiral pipe 32 is communicated with the bottom of barrel-shaped hybrid chamber 31, at the top of barrel-shaped hybrid chamber 31, be provided with two imports, be respectively straw powder import 311 and the import 312 of bed material, straw powder import 311 is communicated with the bottom of vacuum drying oven 19 by vacuum screw feeder 33, the import 312 of bed material is communicated with the bottom of bed material bin 27 by vacuum screw feeder 34, the bed material that is stored in the straw powder in vacuum drying oven 19 and is stored in bed material bin 27 passes through respectively vacuum screw feeder 33, 34 arrive straw powder import 311 and the import 312 of bed material, and enter barrel-shaped hybrid chamber 31, rely on action of gravity to fall, in hybrid chamber 31, be also provided with some paddles 313, it is fixed on the pivot 314 being connected with motor 36, under the fast rotational effect of paddle, straw powder and bed expect fully to mix in hybrid chamber, cracking fast, and further mix while falling within spiral pipe 32 under it, cracking, some holes 320 streams that the gaseous product generating after cracking arranges from spiral pipe 32 come, and wrapping up in part solids and altering to the vacuum gas-solid separator 39 being communicated with inner chamber, at this, solid residue is separated, and hot pyrolysis gas is transported to composite vacuum cooling tower by pipeline.After cracking, remaining solids is powdered carbon and the bed material flowing out from spiral pipe 32 lower ends, it is deposited in the intracavity bottom of thermo-cracking case 30, constantly build up to certain altitude, when it is highly enough, by the vacuum screw rod discharger 35 being communicated with thermo-cracking case 30 bottoms, be delivered to powdered carbon bed material sizing screen 36, isolated powdered carbon is transported in powdered carbon bin 37; Isolated bed material is transported in the bed material collection box 38 being communicated with bed material entrance, and under the effect of bed material discharging pump 25, the bed material in bed material collection box 38 can enter again recycling in bed material heating kettle 22.
Scission reaction is to carry out under the condition of vacuum, straw powder completes in 0.3 ~ 0.5s with the thermo-cracking of bed material, by controlling the speed of rotation ratio of the vacuum screw feeder 33,34 being communicated with vacuum drying oven 19 and bed material bin 27 respectively, in the unit time, its mass ratio entering in hybrid chamber is controlled at 7:3.The bottom of casing is provided with vibrating motor 37, and it is connected with spiral pipe 32, and in order to spiral pipe is produced to vibration upper and lower, left and right, thereby after making cracking, remaining solids more easily falls out.
Liquefaction oil work flow is to be mainly to complete in vacuum cooling tower 41, separator box 42He primary oil of primary oil strainer 43.
Please refer to Fig. 5, the outer inlet mouth 411 that is provided with of vacuum cooling tower 41, air outlet 412, oil outlet 413, water-in 414, water outlet 415, in tower, be provided with the coil pipe 416 being communicated with water-in 414 and water outlet 415, the gaseous state thing of high temperature enters in tower from inlet mouth 411, just meet with the coil pipe 416 of filling cold water and heat exchange occurs, part gaseous state thing is condensed into liquid oil and accumulates at the bottom of falling within tower, in cooling tower, be also provided with spray thrower 417, it is communicated with the oil of bottom accumulation by pipeline 418, pipeline 418 is provided with pump 419, for the cooling oil of bottom being risen to spray thrower 417 and spraying downwards, the gaseous state thing rising meets with it, thereby cooling performance is better.After heat exchange, the cold water entering from water-in 414 has become the hot water that water outlet 415 flows out, thereby takes away heat, keeps thermal equilibrium.Gas that can not be solidifying is 412 discharges from air outlet, are divided into two-way, and a road arrives the temperature control burner being connected with vacuum drying oven 19 and participates in burning; The combustion chamber 23 that another road arrives bed material heating container 20 participates in burning, make can not be solidifying gas also can play one's part to the full.
Primary oil's separator box is work like this: please refer to Fig. 6, the stalk oil of vacuum cooling tower 41 inner bottom part accumulation arrives after certain liquid, open oil outlet 413, make in the inner chamber of the whole Guo Dao of stalk oil primary oil separator box 42, through timeliness effect after a while, content is layered as the wood vinegar of lower floor and the primary oil on upper strata, sidewall in separator box 42 is provided with a drain mast 421, the primary oil on upper strata can all arrive in strainer 43 through drain mast 421, then, in separator box, the whole of remainder are wood vinegar, drainage pipe 422 by bottom can put it in wood vinegar bin 423, separator box completes elementary mask work.
Primary oil's strainer 43 comprise be placed in container 430 mesh bag 431, be placed in the oil suction pipe 432 of mesh bag 431 and the electric pump 433 being communicated with oil suction pipe 432.Enter the outside that primary oil in strainer 43 arrived mesh bag 431 before this, under the effect of electric pump 433, see through continuously mesh bag 431, via oil suction pipe 432, pumped to processed oil bin 435, in this process, impurity in primary oil is blocked in outside mesh bag 431 and precipitates, and makes primary oil obtain filtering and purifies and become processed oil.
The above is only preferred embodiment of the present invention, not the present invention is done to any pro forma restriction, although the present invention discloses as above with preferred embodiment, yet not in order to limit the present invention, any those skilled in the art, within not departing from the scope of technical solution of the present invention, when can utilizing the technology contents of above-mentioned announcement to make a little change or being modified to the equivalent embodiment of equivalent variations, in every case be the content that does not depart from technical solution of the present invention, any simple modification of above embodiment being done according to technical spirit of the present invention, equivalent variations and modification, all still belong in the scope of technical solution of the present invention.
Claims (10)
1. produce a method for liquefaction of corn straw oil, comprise and process respectively the step that straw powder is got the raw materials ready and bed material is got the raw materials ready; Described straw powder is got the raw materials ready and bed material is got the raw materials ready enters the step of carrying out scission reaction in thermo-cracking case; Cracked gas is condensed into the step of liquid biological oil in condenser; It is characterized in that: when processing straw powder is got the raw materials ready, add the additive being formed by straw charring powder, rubber carbonization power and animal corpse carbonization power; Described bed material is the composition of potter's clay powder and catalyzer composition, and wherein catalyzer is comprised of platinum, nickel, cerium oxide powder, iron powder, Tourmaline powder; The straw powder and the mass ratio of expecting that in unit time, enter in thermo-cracking case are 7:3; Scission reaction in thermo-cracking case is carried out under the condition of vacuum, and temperature is controlled at 450 ~ 500 ℃, and the reaction times is controlled in 0.3 ~ 0.5s.
2. the method for production liquefaction of corn straw oil as claimed in claim 1, is characterized in that: stalk is processed into the Powdered of 1 ~ 3mm, and controls moisture content in 3 ~ 5%, and temperature is at 95 ~ 100 ℃.
3. the method for production liquefaction of corn straw oil as claimed in claim 1, is characterized in that: described bed material is processed into particle 1 ~ 1.5mm spherical shape, and the temperature of bed material is controlled at 800 ~ 850 ℃.
4. the method for production liquefaction of corn straw oil as claimed in claim 1, is characterized in that: the mass ratio that forms straw charring powder, rubber carbonization power and the animal corpse carbonization power of described additive is 1:1:1.
5. the method for production liquefaction of corn straw oil as claimed in claim 1, is characterized in that: forming the potter's clay powder of described bed material and the mass ratio of catalyzer is 90:10.
6. the method for production liquefaction of corn straw oil as claimed in claim 5, is characterized in that: form platinum, nickel, cerium oxide powder, the iron powder of described catalyzer, the mass ratio of Tourmaline powder is 0.02:0.08:5.9:2:2.
7. the method for production liquefaction of corn straw oil as claimed in claim 1, is characterized in that: described each step is all carried out under vehicle-mounted condition.
8. a device of producing liquefaction of corn straw oil, comprising: the vacuum bed material bin of getting the raw materials ready for storage bed material being communicated with thermo-cracking case; For the stirrer that straw powder and additive are mixed; For making the vacuum cooling tower of gaseous product condensation;
It is characterized in that: also comprise the vacuum drying oven being connected between stirrer and thermo-cracking case, described additive is comprised of straw charring powder, rubber carbonization power and animal corpse carbonization power; Described bed material is the composition of potter's clay powder and catalyzer composition, and wherein catalyzer is comprised of platinum, nickel, cerium oxide powder, iron powder, Tourmaline powder.
9. the device of production liquefaction of corn straw oil as claimed in claim 8, it is characterized in that: described thermo-cracking case is that an inner chamber can evacuated casing, its inside is provided with barrel-shaped hybrid chamber and the spiral pipe being communicated with up and down, and some venting holes are set on spiral pipe.
10. the device of production liquefaction of corn straw oil as claimed in claim 8, it is characterized in that: vacuum drying oven by can evacuated casing and temperature control burner form, this casing is provided with vacuum pump, and temperature control burner forms by being placed in the gas-cooker of casing below and the temperature-sensing valve being connected with this gas-cooker.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410330278.5A CN104178198B (en) | 2014-07-14 | 2014-07-14 | Produce method and the device of liquefaction of corn straw oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410330278.5A CN104178198B (en) | 2014-07-14 | 2014-07-14 | Produce method and the device of liquefaction of corn straw oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104178198A true CN104178198A (en) | 2014-12-03 |
| CN104178198B CN104178198B (en) | 2015-11-04 |
Family
ID=51959551
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410330278.5A Active CN104178198B (en) | 2014-07-14 | 2014-07-14 | Produce method and the device of liquefaction of corn straw oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104178198B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0535253A1 (en) * | 1991-08-01 | 1993-04-07 | Full Born Chen Industrial Co., Ltd. | Process for producing fuel oil and gas by cracking waste rubber |
| CN1900227A (en) * | 2006-07-12 | 2007-01-24 | 西安嘉宏石化科技有限公司 | Catalystic cracking (coking) diesel oil non-hydrogenation fine stabilizer and its method for producing product |
| CN101787312A (en) * | 2010-02-08 | 2010-07-28 | 珠海中水环保科技有限公司 | Biochar pulp prepared from garbage leachate serving as raw material and preparation process thereof |
| CN101805910A (en) * | 2009-02-18 | 2010-08-18 | 黄富成 | Hydrogen-oxygen generating electrode plate and method for manufacturing the same |
| CN103013552A (en) * | 2012-12-17 | 2013-04-03 | 常州大学 | Method for preparing biological oil by liquefying biomass under atmospheric pressure by using solid acid catalyst |
| CN103387840A (en) * | 2013-06-27 | 2013-11-13 | 中国矿业大学 | Method for preparing biofuel through graded catalytic liquefaction of straw |
-
2014
- 2014-07-14 CN CN201410330278.5A patent/CN104178198B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0535253A1 (en) * | 1991-08-01 | 1993-04-07 | Full Born Chen Industrial Co., Ltd. | Process for producing fuel oil and gas by cracking waste rubber |
| CN1900227A (en) * | 2006-07-12 | 2007-01-24 | 西安嘉宏石化科技有限公司 | Catalystic cracking (coking) diesel oil non-hydrogenation fine stabilizer and its method for producing product |
| CN101805910A (en) * | 2009-02-18 | 2010-08-18 | 黄富成 | Hydrogen-oxygen generating electrode plate and method for manufacturing the same |
| CN101787312A (en) * | 2010-02-08 | 2010-07-28 | 珠海中水环保科技有限公司 | Biochar pulp prepared from garbage leachate serving as raw material and preparation process thereof |
| CN103013552A (en) * | 2012-12-17 | 2013-04-03 | 常州大学 | Method for preparing biological oil by liquefying biomass under atmospheric pressure by using solid acid catalyst |
| CN103387840A (en) * | 2013-06-27 | 2013-11-13 | 中国矿业大学 | Method for preparing biofuel through graded catalytic liquefaction of straw |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104178198B (en) | 2015-11-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102285650B (en) | Process for producing active carbon by using biomass for supplying heat and using fly ash | |
| CN103922334B (en) | Distillers ' grains prepares method and the device of gac | |
| CN105238432B (en) | Method and device for preparing high-quality bio-oil and white carbon black through self-heating acid pickling-pyrolysis-combustion integration | |
| CN101560405A (en) | Method for preparing liquid fuels by self-heating self-circulating thermal cracking of biomass and device thereof | |
| CN202164270U (en) | High-efficiency plant carbonization furnace capable of continuously working | |
| CN104973597A (en) | Production method of active carbon | |
| CN105399095A (en) | Apparatus and method for preparing high specific surface area active carbon through alkali activation process | |
| CN105000557A (en) | Recycling production method for agricultural wastes | |
| CN106281397B (en) | Field biomass through pyrolysis oil refining apparatus based on solar energy heating and from heat supply | |
| CN101445733A (en) | Biomass fuel charring process and equipment thereof | |
| CN106675589A (en) | Exhaust gas and waste heat recovery technology for biochar preparation by sludge reduction gasification | |
| CN105710114A (en) | Carbonization circulation overall treatment system and method for household refuse and forestry and agricultural residues | |
| CN104861997A (en) | Biomass pyrolysis reaction system and pyrolysis method | |
| CN104861993B (en) | Tower-type continuous carbonization furnace for biomass | |
| CN103773404A (en) | Combined-type poly-generation biomass rapid carbonization equipment and carbon making method thereof | |
| CN106118787A (en) | A kind of biomass molding fuel | |
| CN108929170A (en) | Intensive bamboo charcoal biomass organic fertilizer production device and method | |
| CN204079896U (en) | Produce the device of liquefaction of corn straw oil | |
| CN105036126A (en) | Device for recycling agricultural wastes | |
| CN104973598A (en) | Active carbon production apparatus | |
| CN107906529A (en) | A kind of double back rotary kiln pyrolysis system and method | |
| CN108409365A (en) | A kind of excrement charing charcoal base composite fertilizer production system | |
| CN102220178A (en) | Method for preparing firewood sticks by waste cassava residues and application on charcoal preparation | |
| CN202968463U (en) | Continuous low-temperature pyrolyzation carbonization furnace for straws | |
| CN104178198B (en) | Produce method and the device of liquefaction of corn straw oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |