CN106833711B - A kind of organic solid waste tar and plastic refuse coprocessing method - Google Patents
A kind of organic solid waste tar and plastic refuse coprocessing method Download PDFInfo
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- CN106833711B CN106833711B CN201710155948.8A CN201710155948A CN106833711B CN 106833711 B CN106833711 B CN 106833711B CN 201710155948 A CN201710155948 A CN 201710155948A CN 106833711 B CN106833711 B CN 106833711B
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- 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
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- 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
- C10G1/008—Controlling or regulating of liquefaction processes
-
- 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
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/26—Fuel gas
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a kind of organic solid waste tar and plastic refuse coprocessing method, using organic solid waste tar as the thermal conducting agent of plastic refuse and solvent naphtha, accelerate cracking reaction speed, shorten reaction time, the thermal efficiency is high, fuel oil and industrial chemicals are produced by thermochemical study, secondary pollution can not only be reduced, and it can turn waste into wealth, reduce the consumption to petrochemical materials, the situation for creating environment and economic benefit two-win, to realizing that national energy conservation and emission reduction strategic objective has a very important significance.
Description
Technical field：
The present invention relates to organic solid waste and by-product processing technology fields, and in particular to a kind of organic solid waste tar and plastics
Waste coprocessing method.
Background technology：
With the development of organic solid waste pyrolytic gasification technology, pyrolysis gas is carried out using by the organic solid waste of representative of biomass
Elelctrochemical power generation/heat supply has become component part particularly important in the energy supply systems of the developed economies such as USA and EU,
Guangdong Province of China area has also been initially entered into the commercial application stage.During organic solid waste pyrolytic gasification, tar is can not
The by-product avoided.The chemical constituent of organic solid waste tar is mainly hydrocarbon, including long chain hydrocarbons, aromatic compound, aldehyde
And acid etc. has oxygen-containing functional group organic matter, also contains the harmful substances such as heavy metal, furans, bioxin, is a kind of very common
Hazardous chemical.
The disposition of organic solid waste tar is the problem of whole world institute facing.Its disposal of resources process mainly faces two
A essential difficult point：First, different from coal tar, organic solid waste tar is respectively provided with moisture and miscellaneous element or heavy component contains
Measure the features such as high, it is difficult to efficiently separating for all kinds of chemical constituents is realized under prior art conditions, thus can not being directly used as
Work raw material realizes recycling.Secondly, it being influenced by aromatic compound carbon content is higher, tar oxygen demand of burning is larger,
Imperfect combustion is usually undergone in air, causes its thermal conversion processes efficiency low and seriously polluted, therefore this kind of tar is also difficult
To be fully used as fuel.This unavoidable essence present situation is generated in face of organic solid waste tar, while being had
Under machine solid waste thermal transition technology is required towards " near-zero release " that extensive commercial application is proposed, exploitation is suitable for organic solid
The high-efficiency resource recycling new way of waste coke oil realizes that the disposition of its reasonable benefit/risk has become a very urgent task.
Invention content：
The object of the present invention is to provide a kind of organic solid waste tar and plastic refuse coprocessing method, discarded using plastics
Object is similar to the heat scission reaction mechanism of organic solid waste tar, produces fuel oil and industrial chemicals by thermochemical study, no
Secondary pollution can be only reduced, and can be turned waste into wealth, the consumption to petrochemical materials is reduced, creates environment and economy
The situation of benefit two-win, to realizing that national energy conservation and emission reduction strategic objective has a very important significance.
The present invention is achieved by the following technical programs：
A kind of organic solid waste tar and plastic refuse coprocessing method, the organic solid waste tar are organic solid waste pyrolysis
The by-product that gasification generates, this approach includes the following steps：
A, organic solid waste tar is mixed into thawing under the conditions of 100~250 DEG C with plastic refuse particle and tar slurry is made；
Then it is forced into 0.15MPa~15MPa and is heated to 300~400 DEG C, pressurization cracking reaction occurs for part tar slurry；
B, the product that step A is obtained is passed through H2Gas, temperature control at 400~500 DEG C, pressure control 0.15MPa~
Pressurization cracking and hydrogenation reaction occur simultaneously for 15MP；
C, the reaction product that step B is obtained carries out gas-liquid separation through MP separator, and obtained liquid phase is through being decompressed to
0.3MPa enters back into fractionating column and is detached, and isolates the liquid phase of gas, boiling point less than 200 DEG C, boiling point is 200~350 DEG C
Diesel oil distillate, boiling point>350 DEG C of heavy oil fraction；The isolated gas of fractionating column and through the isolated gas of MP separator
It mutually cleans to obtain through tail gas absorption tank together and contains H2Combustible gas；Liquid phase of the isolated boiling point of fractionating column less than 200 DEG C passes through
Enter water knockout drum, separation water outlet and boiling point after being cooled to 50 DEG C<200 DEG C of gasoline fraction.
Further, the part heavy oil fraction that step C is obtained carries out next again after being mixed with step A tar slurry as recycle oil
Step.
Preferably, the mass ratio of the recycle oil and tar slurry is 0~0.4:1.
Preferably, the temperature of the organic solid waste tar is 100~200 DEG C.
Preferably, the plastic refuse particle is polyethylene, polypropylene, polystyrene or polyvinyl chloride wastes
One or any several arbitrary weight ratio mixture in grain.
Preferably, the organic solid waste tar is 10 with plastic refuse weight ratio:1~1:1.
Preferably, the H2Gas is H2Volume content is no less than 80% industrial gasses.
Preferably, the volume ratio of the industrial gasses and tar slurry is 500~1500:1.
Beneficial effects of the present invention are as follows：
1, the present invention accelerates cracking reaction speed using organic solid waste tar as the thermal conducting agent of plastic refuse and solvent naphtha
Degree, shortens reaction time, and the thermal efficiency is high.
2, the raising of hydrogen partial pressure of the invention is conducive to hydrogenation of polymer reaction, improves the yield and matter of petrol and diesel oil fraction
Amount, realizes the high-efficiency resource recycling of organic solid waste tar and plastic refuse.
3, product of the invention is the combustible gas of gasoline fraction, diesel oil distillate, heavy oil fraction and hydrogen, without secondary dirt
Dye, achievees the purpose that " waste recycling ".
4, integrated artistic flow of the present invention is simple, and device fabrication is ripe, and practical operation is simple, is easy to amplify.
5, the present invention can entirely have directly as the subsequent processing process of organic solid waste pyrolytic gasification technique to improve
The benefit of machine solid waste pyrolytic gasification technique.
In short, the present invention accelerates cracking reaction using organic solid waste tar as the thermal conducting agent of plastic refuse and solvent naphtha
Speed shortens reaction time, and the thermal efficiency is high, produces fuel oil and industrial chemicals by thermochemical study, can not only subtract
Few secondary pollution, and can turn waste into wealth, the consumption to petrochemical materials is reduced, environment and economic benefit two-win are created
Situation, to realize national energy conservation and emission reduction strategic objective have a very important significance.
Description of the drawings：
Fig. 1 is the device structure schematic diagram of the embodiment of the present invention 1；
Wherein, 1, tar starches preparing tank；2, feed pump；3, cracking reactor；4, hydrogenation reactor；5, MP separator；
6, pressure reducing valve；7, tail gas absorption tank；8, fractionating column；9, cooler；10, water knockout drum.
Specific implementation mode：
It is the further explanation to the present invention below, rather than limiting the invention.
Embodiment 1：
A kind of organic solid waste tar and plastic refuse coprocessing method, the organic solid waste tar are organic solid waste pyrolysis
The by-product that gasification generates, this method utilize equipment as shown in Figure 1, include the following steps：
A, organic solid waste tar and polyethylene are discarded into composition granule in mass ratio 5:1 is delivered to tar slurry preparing tank 1 respectively,
Temperature control is at 150 DEG C, and organic solid waste tar and polyethylene, which discard composition granule and mix to melt, to be made after tar starches, through feed pump 2
It is forced into 5.5MPa and enters cracking reactor 3, be heated to 350 DEG C, in 5.3MPa, tar slurry in part occurs pressurization and splits for pressure control
Solution reaction, macromolecular chain occur depolymerization and are converted into low molecular compound, are mainly shown as the fracture of C-C keys, while with c h bond
Fracture；The gas that tar slurry preparing tank 1 is discharged removes tail gas absorption tank 7；
B, the product that step A is obtained enters hydrogenation reactor 4 from 4 bottom of hydrogenation reactor, while being passed through H2Volume content
The ratio of 95% industrial gasses, intake and the tar slurry of industrial gasses is 1000:1 [v/v], temperature are controlled at 400 DEG C, pressure
In 5MPa pressurization cracking and hydrogenation reaction occur simultaneously in hydrogenation reactor 4 for power control, and " weak bond " fracture of polymer generates
Unstable free radical, free radical are settled out by conjunction with hydrogen atom；
C, the reaction product that step B is obtained is gas-liquid mixture, and gas-liquid separation, obtained liquid are carried out through MP separator 5
Mutually through pressure reducing valve 6 be decompressed to 0.3MPa and enter back into fractionating column 8 and detached, isolate the liquid phase of gas, boiling point less than 200 DEG C,
Diesel oil distillate, boiling point of the boiling point for 200~350 DEG C>350 DEG C of heavy oil fraction；The gas isolated is arranged from 8 tower top of fractionating column
Go out, liquid phase of the boiling point less than 200 DEG C is discharged from 8 top of fractionating column, and the diesel oil distillate that boiling point is 200~350 DEG C is under fractionating column 8
Portion's discharge, boiling point>350 DEG C of heavy oil fraction is discharged from 8 bottom of fractionating column；It is fractionated into what the separation of tower 8 was discharged from 8 tower top of fractionating column
Gas and the gas phase being discharged from 5 top of MP separator through the separation of MP separator 5 are contained through the cleaning of tail gas absorption tank 7 together
H2Combustible gas；Liquid phase of the isolated boiling point of fractionating column less than 200 DEG C is discharged from 8 top of fractionating column to be cooled down through cooler 9
Enter water knockout drum 10, separation water outlet and boiling point after to 50 DEG C<200 DEG C of gasoline fraction.The heavy oil being discharged from 8 bottom of fractionating column
Fraction (>350 DEG C) be partly used as recycle oil and step A tar slurry mix after carry out next step again, what recycle oil and tar were starched
Mass ratio is 0.2:1.
Claims (7)
1. a kind of organic solid waste tar and plastic refuse coprocessing method, which is characterized in that the organic solid waste tar is to have
The by-product that machine solid waste pyrolytic gasification process generates, this approach includes the following steps：
A, organic solid waste tar is mixed into thawing under the conditions of 100~250 DEG C with plastic refuse particle and tar slurry is made；Then
It is forced into 0.15MPa~15MPa and is heated to 300~400 DEG C, pressurization cracking reaction occurs for part tar slurry；The organic solid waste
Tar is 10 with plastic refuse weight ratio:1~1:1；
B, the product that step A is obtained is passed through H2Gas, at 400~500 DEG C, pressure control is same in 0.15MPa~15MP for temperature control
Shi Fasheng pressurizations cracking and hydrogenation reaction；
C, the reaction product that step B is obtained carries out gas-liquid separation through MP separator, and obtained liquid phase is through being decompressed to 0.3MPa again
Detached into fractionating column, isolate gas, boiling point less than 200 DEG C liquid phase, boiling point be 200~350 DEG C diesel oil distillate,
Boiling point>350 DEG C of heavy oil fraction；The isolated gas of fractionating column and through the isolated gas phase of MP separator together through tail
Aspiration closed cans, which cleans to obtain, contains H2Combustible gas；Liquid phase of the isolated boiling point of fractionating column less than 200 DEG C is cooled to 50 DEG C
Enter water knockout drum, separation water outlet and boiling point afterwards<200 DEG C of gasoline fraction.
2. organic solid waste tar according to claim 1 and plastic refuse coprocessing method, which is characterized in that step C
Obtained part heavy oil fraction carries out next step again after being mixed with step A tar slurry as recycle oil.
3. organic solid waste tar according to claim 2 and plastic refuse coprocessing method, which is characterized in that described to follow
The mass ratio of ring oil and tar slurry is 0~0.4:1.
4. organic solid waste tar according to claim 1 or 2 and plastic refuse coprocessing method, which is characterized in that institute
The temperature for stating organic solid waste tar is 100~200 DEG C.
5. organic solid waste tar according to claim 1 or 2 and plastic refuse coprocessing method, which is characterized in that institute
It is one or any in polyethylene, polypropylene, polystyrene or polyvinyl chloride wastes particle to state plastic refuse particle
The mixture of several arbitrary weight ratios.
6. organic solid waste tar according to claim 1 or 2 and plastic refuse coprocessing method, which is characterized in that institute
State H2Gas is H2Volume content is no less than 80% industrial gasses.
7. organic solid waste tar according to claim 6 and plastic refuse coprocessing method, which is characterized in that the work
The volume ratio of industry gas and tar slurry is 500~1500:1.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201710155948.8A CN106833711B (en) | 2017-03-16 | 2017-03-16 | A kind of organic solid waste tar and plastic refuse coprocessing method |
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| CN201710155948.8A CN106833711B (en) | 2017-03-16 | 2017-03-16 | A kind of organic solid waste tar and plastic refuse coprocessing method |
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| CN106833711A CN106833711A (en) | 2017-06-13 |
| CN106833711B true CN106833711B (en) | 2018-09-28 |
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| CN110229685B (en) * | 2019-06-12 | 2020-08-25 | 中国科学院广州能源研究所 | Method for preparing fuel oil by high-pressure thermal conversion of waste plastics |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1074447C (en) * | 1999-06-08 | 2001-11-07 | 周鼎力 | Process and equipment for producing gasoline and diesel oil with waste plastics and/or heavy oil |
| US6534689B1 (en) * | 2001-08-24 | 2003-03-18 | Pyrocat Ltd. | Process for the conversion of waste plastics to produce hydrocarbon oils |
| JP2007291281A (en) * | 2006-04-27 | 2007-11-08 | Jfe Chemical Corp | Treatment method for plastic |
| CN106190213A (en) * | 2015-04-30 | 2016-12-07 | 雷建光 | A kind of technique utilizing household refuse landfill sites waste or used plastics to extract gasoline, diesel |
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