CN104974769A - Method for preparing fuel oil raw material by coal destructive distillation processing - Google Patents
Method for preparing fuel oil raw material by coal destructive distillation processing Download PDFInfo
- Publication number
- CN104974769A CN104974769A CN201510325242.2A CN201510325242A CN104974769A CN 104974769 A CN104974769 A CN 104974769A CN 201510325242 A CN201510325242 A CN 201510325242A CN 104974769 A CN104974769 A CN 104974769A
- Authority
- CN
- China
- Prior art keywords
- coal
- destructive distillation
- precipitation
- attapulgite
- raw material
- 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
Classifications
-
- 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
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/83—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with rare earths or actinides
Abstract
The invention discloses a method for preparing a fuel oil raw material by coal destructive distillation processing. The method comprises selecting raw material coal, putting the raw material coal into an internal heating roller furnace, feeding methane steam and a composite catalyst into the roller furnace for a reaction, feeding the reaction product hydrogen into a destructive distillation chamber at a temperature of 300-360 DEG C, carrying out a reaction process on the hydrogen and coal bed under normal pressure for 5-8min, adjusting a temperature to 600-730 DEG C, keeping the temperature for 3-8min, adjusting a temperature of to 390-460 DEG C and pressure to normal pressure, adding 0.05-0.09wt% of pre-treated carbon nanotubes into the coal bed in the stage, carrying out a reaction process for 50-80min, cooling the product and separating coal tar and hydrogen. The method utilizes a variable heating rate and has a high coal tar yield.
Description
Technical field
The present invention relates to a kind of destructive distillation production technique.
Background technology
Coal low-temperature pyrolysis started from for 19th century, compared with gasification with liquidation of coal, and its processing conditions is gentle, and less investment, production cost is low.The coal being suitable for low-temperature pyrolysis is generally low-rank coal, comprises the non caking coal of brown coal, long-flame coal and high volatile.The low-rank coal reserves of China are comparatively large, and account for more than 42% of whole coal, therefore, low-temperature pyrolysis technology effectively can utilize the resource of China, and can reduce the environmental pollution that fire coal causes.
The low-temperature pyrolysis of coal can be carried out under inert atmosphere, hydrogenation and catalytic hydrogenation conditions, and wherein its transformation efficiency of coal low-temperature pyrolysis is in an inert atmosphere lower, and tar yield is also corresponding lower; And under the condition of hydrogenation, due to using pure hydrogen as reaction gas, facility investment expense is large, running cost is higher.
Have investigator at coal situ supported transition metal catalyzer, catalyse pyrolysis is carried out to coal, but experiment shows, catalyzer major catalytic be gas-phase reaction, the productive rate of tar can not be significantly improved, and in-situ impregnation catalyzer, when product separation, the more difficult separation of catalyzer.
Summary of the invention
A kind of coal destructive distillation is the object of the present invention is to provide to process the method preparing oil fuel raw material.
Its concrete technical scheme is as follows:
Choose feed coal and put into internal heat type rotary drum furnace, methane vapor is passed in rotary drum furnace, react with composite catalyst, the hydrogen generated enters destructive distillation room and coal seam and reacts, after finally the product generated being cooled, be separated coal tar and hydrogen, and by hydrogen recycle to methane vapor ingress, thus complete the low-temperature pyrolysis of coal.
Described internal heat type rotary drum furnace comprises the catalyst chamber and destructive distillation room that interconnect, in described catalyst chamber, be provided with composite catalyst; Then in rotary drum furnace, pass into methane vapor, react with described composite catalyst, the hydrogen of generation enters described destructive distillation room, and temperature is set to 300-360 DEG C, reacts 5min-8min under normal pressure with coal seam, and adjustment temperature is 600-730 DEG C and keeps 3-8 minute; Adjustment temperature is 390-460 DEG C, pressure is normal pressure; Pre-treatment carbon nanotube in from this stage to coal seam interpolation feed coal weight 0.05-0.09%; Reaction 50-80 minute; , after being cooled by the product generated, be separated coal tar and hydrogen.
The preparation of composite catalyst:
By Ce (NO
3)
36H
2o, Zr (NO
3)
33H
2o is dissolved in deionized water, is then added drop-wise in industrial ammonia, precipitation, after roasting, and obtained Ce
0.25zr
0.75o
2nanometer cerium zirconium oxide carrier;
By obtained above-mentioned carrier impregnation in nickel salt aqueous solution, leave standstill 2-3h, add the attapulgite of the sour modification of carrier quality 0.5-1.8% in nickel salt aqueous solution, be heated to 50-60 DEG C, / hour stirring 3-6h is turned according to 20-30, drying, 350-460 DEG C of obtained composite catalyst after roasting 2-5 hour.
Be provided with gas distribution baffle plate in described catalyst chamber, described gas distribution baffle plate is it is engraved the thin plate being installed with slit, the convenient hydrogen produced through, and Hydrogen distribution is comparatively even.
Nickel salt is single nickel salt.
In reaction process, move along the axial screw of rotary drum furnace in described destructive distillation room, coal seam overturns simultaneously, makes to react the hydrogen produced and can fully contact with coal seam, thus improve speed of response and transformation efficiency.
Velocity of rotation and the inclination angle of described destructive distillation room can regulate.
Described feed coal is brown coal, long-flame coal, non-caking coal or weakly caking coal.
The pre-treatment of carbon nanotube:
8% take commercially available pretreated carbon nanotube in mass ratio, add in the N-Methyl pyrrolidone of 100mL, separated and collected precipitation after abundant dispersed with stirring, the dilute hydrochloric acid solution adding 2% in precipitation leaves standstill process 1-2h centrifugal collecting precipitation and get final product.
The attapulgite of acid modification: take 1Kg particle diameter 300 order ~ 1000 object attapulgite, use 10L distilled water wash, precipitation gets its supernatant liquid, its supernatant liquid is got after the centrifugal 1min of 500rpm, add a small amount of distilled water in supernatant liquid and mix the centrifugal 1min of rear continuation 500rpm, then its supernatant liquid is got, after repetitive scrubbing supernatant liquid like this 3 ~ 5 times, finally carry out centrifugation with 4000rpm, get its precipitation, vacuum-drying 24h at 90 DEG C, selects the sieve of corresponding order number, obtains purifying attapulgite by size after grinding.Compound concentration is the hydrochloric acid soln of 0.5mol/L ~ 3mol/L, get purifying attapulgite and 3500mL ~ 4500mL hydrochloric acid soln is uniformly mixed, after 5min, mixture is heated to 70 DEG C ~ 80 DEG C, stirs 1h ~ 2h, then sonic oscillation 30min ~ 40min, suction filtration, is washed with distilled water to pH and is about about 6, vacuum-drying 24h at 90 DEG C, select the sieve of corresponding order number after grinding by size, obtain sour attapulgite modified.
Compared with prior art, production technique of the present invention has following features:
Adopt the rate of heating of change, initial stage rate of heating is comparatively slow, and initial stage pyrolysis makes key more weak in coal molecule disconnect, and there occurs thermal polycondensation reaction that is parallel and order, defines the structure of Heat stability is good; Hot stage makes its structure adjust, and in the rapid reaction under composite catalyst effect of adjustment temperature, corresponding STRUCTURE DECOMPOSITION is many.
Embodiment
Below by embodiment, technical scheme of the present invention is described in further detail, but is not limited to the content of the present embodiment.
Embodiment 1
A kind of coal destructive distillation is the object of the present invention is to provide to process the method preparing oil fuel raw material.
Its concrete technical scheme is as follows:
Choose feed coal and put into internal heat type rotary drum furnace, methane vapor is passed in rotary drum furnace, react with composite catalyst, the hydrogen generated enters described destructive distillation room and coal seam is reacted, after finally the product generated being cooled, be separated coal tar and hydrogen, and by hydrogen recycle to methane vapor ingress, thus complete the low-temperature pyrolysis of coal.
Described internal heat type rotary drum furnace comprises the catalyst chamber and destructive distillation room that interconnect, in described catalyst chamber, be provided with composite catalyst; Then in rotary drum furnace, pass into methane vapor, react with described composite catalyst, the hydrogen of generation enters described destructive distillation room, and temperature is set to 350 DEG C, reacts 6min under normal pressure with coal seam, and adjustment temperature is 650 DEG C and keeps 6 minutes; Adjustment temperature is 430 DEG C, pressure is normal pressure; Pre-treatment carbon nanotube in from this stage to coal seam interpolation feed coal weight 0.08%; React 60 minutes; After being cooled by the product generated, be separated coal tar and hydrogen.The addition of described composite catalyst is the 2wt%. of feed coal
The preparation of composite catalyst:
By Ce (NO
3)
36H
2o, Zr (NO
3)
33H
2o is dissolved in deionized water, is then added drop-wise in industrial ammonia, precipitation, after roasting, and obtained Ce
0.25zr
0.75o
2nanometer cerium zirconium oxide carrier;
By obtained above-mentioned carrier impregnation in nickel salt aqueous solution, leave standstill 2h, add the attapulgite of the sour modification of carrier quality 1.3% in nickel salt aqueous solution, be heated to 55 DEG C, turn/hour stirring 5h according to 20-30, dry, 400 DEG C of roastings obtained composite catalyst after 4 hours.
Be provided with gas distribution baffle plate in described catalyst chamber, described gas distribution baffle plate is it is engraved the thin plate being installed with slit, the convenient hydrogen produced through, and Hydrogen distribution is comparatively even.
In reaction process, move along the axial screw of rotary drum furnace in described destructive distillation room, coal seam overturns simultaneously, makes to react the hydrogen produced and can fully contact with coal seam, thus improve speed of response and transformation efficiency.
Velocity of rotation and the inclination angle of described destructive distillation room can regulate.
Described feed coal is brown coal, long-flame coal, non-caking coal or weakly caking coal.
The pre-treatment of carbon nanotube: 8% take commercially available pretreated carbon nanotube in mass ratio, in the N-Methyl pyrrolidone added, separated and collected precipitation after abundant dispersed with stirring, the dilute hydrochloric acid solution adding 2% in precipitation leaves standstill process 1-2h centrifugal collecting precipitation and get final product.
The attapulgite of acid modification: take 1Kg particle diameter 500-600 object attapulgite, use 10L distilled water wash, precipitation gets its supernatant liquid, its supernatant liquid is got after the centrifugal 1min of 500rpm, add in supernatant liquid and mix the centrifugal 1min of rear continuation 500rpm with amount distilled water, then its supernatant liquid is got, after repetitive scrubbing supernatant liquid like this 3 ~ 5 times, finally carry out centrifugation with 4000rpm, get its precipitation, vacuum-drying 24h at 90 DEG C, selects the sieve of corresponding order number, obtains purifying attapulgite by size after grinding.Compound concentration is the hydrochloric acid soln of 2mol/L, get purifying attapulgite and 3500mL ~ 4500mL hydrochloric acid soln is uniformly mixed, after 5min, mixture is heated to 75 DEG C, stirs 1h ~ 2h, then sonic oscillation 30min ~ 40min, suction filtration, is washed with distilled water to pH and is about about 6, vacuum-drying 24h at 90 DEG C, select the sieve of corresponding order number after grinding by size, obtain sour attapulgite modified.Coal tar productive rate is 34.5%.
Embodiment 2
A kind of coal destructive distillation is the object of the present invention is to provide to process the method preparing oil fuel raw material.
Choose feed coal and put into internal heat type rotary drum furnace, methane vapor is passed in rotary drum furnace, react with composite catalyst, the hydrogen generated enters described destructive distillation room and coal seam is reacted, after finally the product generated being cooled, be separated coal tar and hydrogen, and by hydrogen recycle to methane vapor ingress, thus complete the low-temperature pyrolysis of coal.
Described internal heat type rotary drum furnace comprises the catalyst chamber and destructive distillation room that interconnect, in described catalyst chamber, be provided with composite catalyst; Then in rotary drum furnace, pass into methane vapor, react with described composite catalyst, the hydrogen of generation enters described destructive distillation room, and temperature is set to 300 DEG C, reacts 8min under normal pressure with coal seam, and adjustment temperature is 680 DEG C and keeps 3 minutes; Adjustment temperature is 410 DEG C, pressure is normal pressure; Pre-treatment carbon nanotube in from this stage to coal seam interpolation feed coal weight 0.09%; React 80 minutes; , after being cooled by the product generated, be separated coal tar and hydrogen.
The preparation of composite catalyst:
By Ce (NO
3)
36H
2o, Zr (NO
3)
33H
2o is dissolved in deionized water, is then added drop-wise in industrial ammonia, precipitation, after roasting, and obtained Ce
0.25zr
0.75o
2nanometer cerium zirconium oxide carrier;
By obtained above-mentioned carrier impregnation in nickel salt aqueous solution, leave standstill 2-3h, add the attapulgite of the sour modification of carrier quality 0.5% in nickel salt aqueous solution, be heated to 60 DEG C, turn/hour stirring 6h according to 20-30, dry, 460 DEG C of roastings obtained composite catalyst after 5 hours.
Be provided with gas distribution baffle plate in described catalyst chamber, described gas distribution baffle plate is it is engraved the thin plate being installed with slit, the convenient hydrogen produced through, and Hydrogen distribution is comparatively even.
In reaction process, move along the axial screw of rotary drum furnace in described destructive distillation room, coal seam overturns simultaneously, makes to react the hydrogen produced and can fully contact with coal seam, thus improve speed of response and transformation efficiency.
Coal tar productive rate is 36.5%.
Velocity of rotation and the inclination angle of described destructive distillation room can regulate.
Described feed coal is brown coal, long-flame coal, non-caking coal or weakly caking coal.
The pre-treatment of carbon nanotube: 8% take commercially available pretreated carbon nanotube in mass ratio, in the N-Methyl pyrrolidone added, separated and collected precipitation after abundant dispersed with stirring, the dilute hydrochloric acid solution adding 2% in precipitation leaves standstill process 1-2h centrifugal collecting precipitation and get final product.
The attapulgite of acid modification: take 1Kg particle diameter 700 order ~ 1000 object attapulgite, use 10L distilled water wash, precipitation gets its supernatant liquid, its supernatant liquid is got after the centrifugal 1min of 500rpm, add a small amount of distilled water in supernatant liquid and mix the centrifugal 1min of rear continuation 500rpm, then its supernatant liquid is got, after repetitive scrubbing supernatant liquid like this 3 ~ 5 times, finally carry out centrifugation with 4000rpm, get its precipitation, vacuum-drying 24h at 90 DEG C, selects the sieve of corresponding order number, obtains purifying attapulgite by size after grinding.Compound concentration is the hydrochloric acid soln of 0.5mol/L ~ 3mol/L, get purifying attapulgite and 3500mL ~ 4500mL hydrochloric acid soln is uniformly mixed, after 5min, mixture is heated to 70 DEG C ~ 80 DEG C, stirs 1h ~ 2h, then sonic oscillation 30min ~ 40min, suction filtration, is washed with distilled water to pH and is about about 6, vacuum-drying 24h at 90 DEG C, select the sieve of corresponding order number after grinding by size, obtain sour attapulgite modified.
Claims (9)
1. the method preparing oil fuel raw material is processed in a coal destructive distillation, choose feed coal and put into internal heat type rotary drum furnace, then in rotary drum furnace, methane vapor is passed into and composite catalyst reacts, the hydrogen generated enters described destructive distillation room, temperature is set to 300-360 DEG C, react 5min-8min with coal seam under normal pressure, adjustment temperature is 600-730 DEG C and keeps 3-8 minute; Adjustment temperature is 390-460 DEG C, pressure is normal pressure; Pre-treatment carbon nanotube in from this stage to coal seam interpolation feed coal weight 0.05-0.09%; Reaction 50-80 minute; , after being cooled by the product generated, be separated coal tar and hydrogen.
2. according to right 1, the method for oil fuel raw material is prepared in coal destructive distillation processing, the preparation of described composite catalyst:
By Ce (NO
3)
36H
2o, Zr (NO
3)
33H
2o is dissolved in deionized water, is then added drop-wise in industrial ammonia, precipitation, after roasting, and obtained Ce
0.25zr
0.75o
2nanometer cerium zirconium oxide carrier; By obtained above-mentioned carrier impregnation in nickel salt aqueous solution, leave standstill 2-3h, add the attapulgite of the sour modification of carrier quality 0.5-1.8% in nickel salt aqueous solution, be heated to 50-60 DEG C, / hour stirring 3-6h is turned according to 20-30, drying, 350-460 DEG C of obtained composite catalyst after roasting 2-5 hour.
3. according to right 1, the method for oil fuel raw material is prepared in coal destructive distillation processing, the pre-treatment of described carbon nanotube:
8% take commercially available pretreated carbon nanotube in mass ratio, add in the N-Methyl pyrrolidone of 100mL, separated and collected precipitation after abundant dispersed with stirring, the dilute hydrochloric acid solution adding 2% in precipitation leaves standstill process 1-2h centrifugal collecting precipitation and get final product.
4. according to right 1, the method for oil fuel raw material is prepared in coal destructive distillation processing, the attapulgite of described sour modification: take 1Kg particle diameter 300 order ~ 1000 object attapulgite, use 10L distilled water wash, precipitation gets its supernatant liquid, its supernatant liquid is got after the centrifugal 1min of 500rpm, add in supernatant liquid and mix the centrifugal 1min of rear continuation 500rpm with amount distilled water, then its supernatant liquid is got, after repetitive scrubbing supernatant liquid like this 3 ~ 5 times, finally carry out centrifugation with 4000rpm, get its precipitation, vacuum-drying 24h at 90 DEG C, select the sieve of corresponding order number by size after grinding, obtain purifying attapulgite, compound concentration is the hydrochloric acid soln of 0.5mol/L ~ 3mol/L, get purifying attapulgite and 3500mL ~ 4500mL hydrochloric acid soln is uniformly mixed, after 5min, mixture is heated to 70 DEG C ~ 80 DEG C, stirs 1h ~ 2h, then sonic oscillation 30min ~ 40min, suction filtration, is washed with distilled water to pH and is about about 6, vacuum-drying 24h at 90 DEG C, select the sieve of corresponding order number after grinding by size, obtain sour attapulgite modified.
5. according to right 1, the method for oil fuel raw material is prepared in coal destructive distillation processing, comprises the steps:
Choose feed coal and put into internal heat type rotary drum furnace, in rotary drum furnace, pass into methane vapor, react with composite catalyst, described internal heat type rotary drum furnace comprises the catalyst chamber and destructive distillation room that interconnect, in described catalyst chamber, be provided with composite catalyst; Then in rotary drum furnace, pass into methane vapor, react with described composite catalyst, the hydrogen of generation enters described destructive distillation room, and temperature is set to 350 DEG C, reacts 6min under normal pressure with coal seam, and adjustment temperature is 650 DEG C and keeps 6 minutes; Adjustment temperature is 430 DEG C, pressure is normal pressure; Pre-treatment carbon nanotube in from this stage to coal seam interpolation feed coal weight 0.08%; React 60 minutes; After being cooled by the product generated, be separated coal tar and hydrogen.
6. according to right 1, the method for oil fuel raw material is prepared in coal destructive distillation processing, the preparation of composite catalyst:
By Ce (NO
3)
36H
2o, Zr (NO
3)
33H
2o is dissolved in deionized water, is then added drop-wise in industrial ammonia, precipitation, after roasting, and obtained Ce
0.25zr
0.75o
2nanometer cerium zirconium oxide carrier; By obtained above-mentioned carrier impregnation in nickel salt aqueous solution, leave standstill 2h, add the attapulgite of the sour modification of carrier quality 1.3% in nickel salt aqueous solution, be heated to 55 DEG C, turn/hour stirring 5h according to 20-30, dry, 400 DEG C of roastings obtained composite catalyst after 4 hours.
7. according to right 1, the method for oil fuel raw material is prepared in coal destructive distillation processing, prepared by carbon nanotube: 8% take commercially available pretreated carbon nanotube in mass ratio, in the N-Methyl pyrrolidone added, separated and collected precipitation after abundant dispersed with stirring, the dilute hydrochloric acid solution adding 2% in precipitation leaves standstill process 1-2h centrifugal collecting precipitation and get final product.
8. according to right 1, the method for oil fuel raw material is prepared in coal destructive distillation processing, the attapulgite of acid modification: take 1Kg particle diameter 500-600 object attapulgite, use 10L distilled water wash, precipitation gets its supernatant liquid, its supernatant liquid is got after the centrifugal 1min of 500rpm, add a small amount of distilled water in supernatant liquid and mix the centrifugal 1min of rear continuation 500rpm, then its supernatant liquid is got, after repetitive scrubbing supernatant liquid like this 3 ~ 5 times, finally carry out centrifugation with 4000rpm, get its precipitation, vacuum-drying 24h at 90 DEG C, select the sieve of corresponding order number by size after grinding, obtain purifying attapulgite.Compound concentration is the hydrochloric acid soln of 2mol/L, get purifying attapulgite and 3500mL ~ 4500mL hydrochloric acid soln is uniformly mixed, after 5min, mixture is heated to 75 DEG C, stirs 1h ~ 2h, then sonic oscillation 30min ~ 40min, suction filtration, is washed with distilled water to pH and is about about 6, vacuum-drying 24h at 90 DEG C, select the sieve of corresponding order number after grinding by size, obtain sour attapulgite modified.Coal tar productive rate is 34.5%.
9. the preparation of a composite catalyst: by Ce (NO
3)
36H
2o, Zr (NO
3)
33H
2o is dissolved in deionized water, is then added drop-wise in industrial ammonia, precipitation, after roasting, and obtained Ce
0.25zr
0.75o
2nanometer cerium zirconium oxide carrier; By obtained above-mentioned carrier impregnation in nickel salt aqueous solution, leave standstill 2-3h, add the attapulgite of the sour modification of carrier quality 0.5% in nickel salt aqueous solution, be heated to 60 DEG C, turn/hour stirring 6h according to 20-30, dry, 460 DEG C of roastings obtained composite catalyst after 5 hours.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710421119.XA CN107434976A (en) | 2015-06-15 | 2015-06-15 | A kind of method that coal destructive distillation processing prepares fuel oil raw material |
| CN201510325242.2A CN104974769B (en) | 2015-06-15 | 2015-06-15 | A kind of method that coal destructive distillation processing prepares fuel oil raw material |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510325242.2A CN104974769B (en) | 2015-06-15 | 2015-06-15 | A kind of method that coal destructive distillation processing prepares fuel oil raw material |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710421119.XA Division CN107434976A (en) | 2015-06-15 | 2015-06-15 | A kind of method that coal destructive distillation processing prepares fuel oil raw material |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104974769A true CN104974769A (en) | 2015-10-14 |
| CN104974769B CN104974769B (en) | 2017-11-03 |
Family
ID=54271743
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710421119.XA Withdrawn CN107434976A (en) | 2015-06-15 | 2015-06-15 | A kind of method that coal destructive distillation processing prepares fuel oil raw material |
| CN201510325242.2A Active CN104974769B (en) | 2015-06-15 | 2015-06-15 | A kind of method that coal destructive distillation processing prepares fuel oil raw material |
Family Applications Before (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710421119.XA Withdrawn CN107434976A (en) | 2015-06-15 | 2015-06-15 | A kind of method that coal destructive distillation processing prepares fuel oil raw material |
Country Status (1)
| Country | Link |
|---|---|
| CN (2) | CN107434976A (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102002378A (en) * | 2010-11-25 | 2011-04-06 | 邵素英 | Coal low-temperature dry distillation production method |
| CN102010731A (en) * | 2010-11-25 | 2011-04-13 | 邵素英 | Pyrolytic process of coal |
| CN201873641U (en) * | 2010-11-25 | 2011-06-22 | 邵素英 | Drum-type coal low-temperature destructive distillation device |
| CN102634355A (en) * | 2011-12-20 | 2012-08-15 | 华北电力大学 | Method for cracking biomass pyrolytic tar catalytically using nickel-carrying carbon nano tube |
| US20130004409A1 (en) * | 2007-03-14 | 2013-01-03 | Tucker Engineering Associates, Inc. | Pyrolysis and gasification systems, methods, and resultants derived therefrom |
| CN103480347A (en) * | 2013-10-11 | 2014-01-01 | 天津汉晴环保科技有限公司 | Preparation method of composite flat membrane for adsorbing heavy metal ions and product thereof |
-
2015
- 2015-06-15 CN CN201710421119.XA patent/CN107434976A/en not_active Withdrawn
- 2015-06-15 CN CN201510325242.2A patent/CN104974769B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130004409A1 (en) * | 2007-03-14 | 2013-01-03 | Tucker Engineering Associates, Inc. | Pyrolysis and gasification systems, methods, and resultants derived therefrom |
| CN102002378A (en) * | 2010-11-25 | 2011-04-06 | 邵素英 | Coal low-temperature dry distillation production method |
| CN102010731A (en) * | 2010-11-25 | 2011-04-13 | 邵素英 | Pyrolytic process of coal |
| CN201873641U (en) * | 2010-11-25 | 2011-06-22 | 邵素英 | Drum-type coal low-temperature destructive distillation device |
| CN102634355A (en) * | 2011-12-20 | 2012-08-15 | 华北电力大学 | Method for cracking biomass pyrolytic tar catalytically using nickel-carrying carbon nano tube |
| CN103480347A (en) * | 2013-10-11 | 2014-01-01 | 天津汉晴环保科技有限公司 | Preparation method of composite flat membrane for adsorbing heavy metal ions and product thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104974769B (en) | 2017-11-03 |
| CN107434976A (en) | 2017-12-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102344137B (en) | Preparation method of active carbon | |
| CN114522688B (en) | Porous carbon supported bimetallic catalyst and preparation and application thereof | |
| CN109482235B (en) | Preparation method and application of N-doped mesoporous carbon supported metal nano catalyst | |
| Zhang et al. | Production of biochar from lignocellulosic biomass with acidic deep eutectic solvent and its application as efficient adsorbent for Cr (VI) | |
| CN110844900B (en) | Method for preparing carbon nano tube by taking waste tire as raw material | |
| CN101786015A (en) | Hydrothermal preparation method of carbon-based solid sulfoacid | |
| CN108097332B (en) | Low-metamorphic coal-zirconium-based catalyst and preparation method and application thereof | |
| CN102002378A (en) | Coal low-temperature dry distillation production method | |
| CN107096528A (en) | A kind of bagasse carbonization load biomass-based catalyst of ruthenium and preparation method and application | |
| CN103318962A (en) | Production method for ammonium metatungstate | |
| CN113318745A (en) | Preparation method of hydrogen-rich catalyst for biomass pyrolysis | |
| CN104974769A (en) | Method for preparing fuel oil raw material by coal destructive distillation processing | |
| Gao et al. | Ni-Based multifunctional catalysts derived from layered double hydroxides for the catalytic conversion of cellulose to polyols | |
| CN112121818B (en) | Magnetic carbon-based catalyst, preparation method and application | |
| CN113797939B (en) | ZnZrO (zinc ZrO-rich alloy) x /MoS 2 Composite catalyst, preparation and application thereof | |
| CN106622203A (en) | Method for preparing levorodextrone based on pyrolytic carbon-catalyzed cellulose | |
| CN110560088A (en) | Functional carbon-based magnetic solid acid catalyst synthesized by one-pot method and application thereof in catalyzing bagasse hydrolysis to produce sugar | |
| CN110835554A (en) | Method for catalyzing steam gasification of bituminous coal by carbide slag | |
| CN117101675B (en) | High-entropy alloy modified nitrogen-doped biochar as well as preparation method and application thereof | |
| CN111420666B (en) | Catalyst prepared by utilizing waste clay ash and preparation method and application thereof | |
| Liu et al. | A glucose-derived carbonaceous solid acid catalyst for cellooligosaccharides hydrolysis in an aqueous reaction system | |
| CN113354510B (en) | Phenol selective hydrogenation method on Na modified NiCo catalyst | |
| CN117904443A (en) | Method for recovering ruthenium from ruthenium-containing catalyst | |
| CN117776177A (en) | Preparation method of high-decoloring-performance activated carbon | |
| Zhong et al. | Preparation of Ru/N-doped carbon catalysts by induction of different nitrogen source precursors for the hydroprocessing of lignin 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 | ||
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20170926 Address after: 300385 Tianjin city Xiqing District Saida emerging Xiqing economic and Technological Development Zone Industrial Park E3 block 3 room 302A-60 Applicant after: TIANJIN ZHONGTIAN JINGKE TECHNOLOGY CO., LTD. Address before: 300457 Binhai New Area of Tianjin City Fifth Street Taihua Road No. 12 TEDA SME development center room 3062 Applicant before: TIANJIN TIANLVJIAN TECHNOLOGY CO., LTD. Applicant before: Li Jianshu |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |