CN105969417A - Oil shale or oil sand downstream circulating bed millisecond pyrolysis refining device - Google Patents
Oil shale or oil sand downstream circulating bed millisecond pyrolysis refining device Download PDFInfo
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- CN105969417A CN105969417A CN201610566486.4A CN201610566486A CN105969417A CN 105969417 A CN105969417 A CN 105969417A CN 201610566486 A CN201610566486 A CN 201610566486A CN 105969417 A CN105969417 A CN 105969417A
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Classifications
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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
- 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
- C10B49/16—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 moving solid heat-carriers in divided form
- C10B49/20—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 moving solid heat-carriers in divided form in dispersed form
- C10B49/22—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 moving solid heat-carriers in divided form in dispersed form according to the "fluidised bed" technique
-
- 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
- C10B53/06—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of oil shale and/or or bituminous rocks
-
- 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
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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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)
- Dispersion Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides an oil shale or oil sand downstream circulating bed millisecond pyrolysis refining device. An oil shale or oil sand inlet is arranged on the lower part of a fume lift pipe; the top of the flue gas lift pipe is provided with a gas-solid second-stage separator; a solid outlet of a first-stage separator communicates with the top of a downstream pyrolysis reactor; a fume outlet of the second-stage separator is directly discharged, and a solid outlet is connected with the bottom of a char lift pipe; the bottom of the char lift pipe is provided with a gas distributor and a gas inlet pipe, and the top is provided with an inertia gas-solid separator, and communicates with the top of the downstream pyrolysis reactor through a high-temperature hot ash return controller; a solid outlet communicates with a fluidized state outside heat remover, a cooled ash outlet and a hot ash second-stage separator communicate with a cooled material storage bin, and a gas outlet communicates with the bottom of the fume lift pipe through a waste heat boiler and an induced fan; the bottom of the downstream pyrolysis reactor is provided with an oil-gas separator, a solid outlet communicates with the bottom of the char lift pipe, and a gas phase outlet is connected with an oil-gas fractionating tower; and the fractionating tower is provided with a pyrolysis dry gas outlet, a gasoline outlet, a diesel outlet and a heavy oil outlet from top to bottom.
Description
1. technical field
The present invention provides oil shale or oil-sand downlink cycle bed millisecond pyrolysis device for refining, belongs to PETROLEUM PROCESSING field.
2. background technology
Oil shale belongs to unconventional petroleum resources, is listed in 21 century with aboundresources and the feasibility of exploitation and very important takes over energy
Source.China's oil shale resources are enriched, technically recoverable resources about 240,000,000,000 tons, the most recyclable empyreumatic oil about 10,000,000,000 tons；China's oil-sand
Oil geological resources is 59.7 hundred million tons, and mining resources amount 22.58 hundred million tons, the most recyclable empyreumatic oil about 1,000,000,000 tons, industrialization potential is huge.
At present, oil shale/oil-sand method for destructive distillation is all studied by many countries in the world, the formation industrial production scale having.Oil page
Rock distillation process can be divided into external-heat and internal heat type two class by mode of heating: external heating type heat efficiency is low, oil shale heating inequality, the two of volatility product
Secondary decomposition is serious, and tar yield is low, and device is difficult to maximize, and the most this kind of technology is normally only used for laboratory, large industrialized oil shale pyrolysis
Process is difficulty with；Internal heat type technology utilization gas heat carrier or solid thermal carriers are directly passed to oil shale heat, make oil shale be pyrolyzed
Reaction, the shortcoming overcoming external-heat, have that Mass and heat transfer speed is fast, homogeneous heating, fugitive constituent twice decomposition are few, tar yield is high, device
It is prone to the advantages such as maximization.
Internal heat type technique includes gas heat carrier pyrolytic process and solid heat carrier pyrolysis technique, wherein: gas heat carrier pyrolytic process is typically
The flue gas of fuel combustion is introduced pyrolysis chamber, the representational double boiling bed process having the COED technique of the U.S., ENCOAL technique and Poland
Deng.Solid heat carrier pyrolysis technique then utilizes high-temperature semi-coke or other high-temp solid material to mix in pyrolysis chamber with oil shale, utilizes heat carrier
Sensible heat by oil shale pyrolysis.Compared with gas heat carrier pyrolytic process, solid heat carrier pyrolysis avoids the volatility product that oil shale pyrolysis separates out
By flue gas dilution, reducing the load of cooling system, process advantage is obvious simultaneously.But existing oil shale solid heat carrier rapid pyrolysis technology exists
The difficult problem such as band ash, mechanical moving element high temperature wear, device enlarge-effect and equipment long-period stable operation in oil, becomes restriction oil shale fast
The technical bottleneck of speed pyrolysis, is badly in need of can eliminating in oil band ash, heat transfer according to the exploitation of oil shale pyrolysis response characteristic good, reasonable energy utilization
Oil shale pyrolysis liquefaction technology and equipment.
The present inventor has invented oil shale/oil-sand downlink cycle fluidized bed pyrolysis liquefaction process, by by heat ash fractionated, big-and-middle granule heat ash
By arranging outside the pyrolysis of descending pyrolysis reactor, molecule heat ash, from source, eliminate a band ash difficult problem in the oil that hot ash causes.But oil shale/oil-sand
Non-fractionated after particle drying, fine particle therein also can produce band ash phenomenon in oil from source.Refine additionally, due to oil shale/oil-sand pyrolysis
The lime-ash of about about 90% can be produced, it is necessary to a large amount of outer rows, former patent only be nowhere near by the thin hot ash of discharge, in addition it is also necessary to big-and-middle of a large amount of discharges
Grain heat ash, and in this part of hot ash, carbon residue is the highest, it is necessary to considering Appropriate application, these all become oil shale/oil-sand downlink cycle fluid bed
The bottleneck of pyrolysis liquefaction process industry.
3. summary of the invention
A kind of oil shale that the purpose of the present invention is contemplated to overcome deficiency that existing oil shale/oil-sand pyrolysis liquefaction technology exists and proposes or oil-sand
Downlink cycle fluid bed millisecond pyrolysis device for refining, the most thoroughly solves a band ash difficult problem in the oil of oil shale/oil-sand fluidized bed pyrolysis upgrading, closes again
Reason utilizes and is pyrolyzed outer ash discharge and heat energy, and different tarry distillates and the combustion gas of high added value are also obtained.
Technical scheme:
It is an object of the invention to by oil shale or oil-sand feed particles and heat ash are realized fractionated, part big-and-middle granule heat ash and raw material pass through
The pyrolysis of descending pyrolysis reactor, thin feed particles are sent directly into riser and burn, and part big-and-middle granule heat ash air burn again reclaims heat with thin
Hot ash outer row together, eliminates band ash and heat ash in oil from source and utilizes a difficult problem for a difficult problem.It is characterized in that arranging oil shale or oil-sand entrance
In flue gas riser bottom, flue gas riser top arranges gas-solid second-stage separator, and primary separator solid outlet passes through top feed bin and feeder
Connect with descending pyrolysis reactor top；Second-stage separator exhanst gas outlet directly outer row, solid outlet passes through semicoke material returning device and burns at the bottom of riser
Portion is connected；Burning and arrange gas distributor and air inlet pipe bottom riser, top arranges inertia gas-solid separator by high-temperature hot ash returning charge controller
Connect with descending pyrolysis reactor top, inertia gas-solid separator separately set a solid outlet with fluidisation state external warmer connect, cooling ash outlet and
Cooling feed bin connection；The solid outlet of heat ash second-stage separator also connects with cooling feed bin, and gas outlet is by waste heat boiler and air-introduced machine and flue gas
Connect bottom riser；Arranging oil gas gas-solid separator bottom descending pyrolysis reactor, solid outlet passes through semicoke returning charge valve and burns at the bottom of riser
Portion connects, and gaseous phase outlet is connected with oil gas fractionating column, and fractionating column arranges pyrolysis dry gas outlet, fuel dispensing outlet, diesel oil outlet, heavy oil from top to bottom
Outlet.
Burning riser reaction temperature is 850 DEG C-1200 DEG C.
High-temperature hot ash is 2-8:1 with the mixed proportion of oil shale/oil-sand powder.
Descending pyrolysis reactor outlet reaction temperature is 450 DEG C-600 DEG C.
External warmer is to utilize air that big-and-middle granule semicoke burning and heat exchange in fluidisation state external warmer of 850 DEG C-1200 DEG C are produced high pressure to steam
Vapour, heat ash and air reclaim solid particle through bulky grain heat ash separator；Air after heating is by water inlet preheater preheated fluidification state external warmer
Water inlet, is cooled to less than 300 DEG C, utilizes circulating fan to send into bottom fluidisation state external warmer.
Embodiment is described the feature of the present invention by the present invention in detail.
4. accompanying drawing explanation
Accompanying drawing is the process schematic representation of the present invention.The drawing of accompanying drawing sets bright as follows:
1, burn riser 2, gas distributor 3, air inlet pipe 4, inertia gas-solid separator 5, high-temperature hot ash returning charge controller 6,
Heat two grades of gas-solid separators 7 of ash, heat ash cooling feed bin 8, descending pyrolysis reactor 9, oil gas gas-solid separator 10, oil gas fractionating column
11, coal tar heavy oil outlet 12, diesel oil outlet 13, fuel dispensing outlet 14, air-introduced machine 15, flue gas riser 16, flue gas one-level gas solid separation
Device 17, top feed bin 18, rotary table feeder 19, two grades of gas-solid separators 20 of flue gas, exhanst gas outlet 21, oil shale or oil-sand entrance 22,
Dry gas outlet 23, semicoke returning charge valve 24, fluidisation state external warmer 25, bulky grain heat ash separator 26, water inlet preheater 27, follow
Ring blower fan 28, waste heat boiler.
The process characteristic of the present invention is described in detail in detail with embodiment below in conjunction with the accompanying drawings.
5. detailed description of the invention
Embodiment 1, by a large number less than the oil shale of 6mm or oil-sand powder through oil shale or oil-sand entrance 21 enter flue gas riser 15 be dried and
Promoting, oil shale or oil-sand granule are by flue gas one-level gas-solid separator 16 and two grades of gas-solid separator (19) fractionated of flue gas, and flue gas is from flue gas
The outer row of outlet 20, fine grained oil shale or oil-sand are entered by semicoke returning charge valve 23 and burn riser 1, big-and-middle Oil Shale Particles or oil-sand through rotation
Rotate into glassware 18 and quickly mix liter on descending pyrolysis reactor 8 top with the high temperature circulation heat ash realization rapidly fallen by high-temperature hot ash returning charge valve 5
Temperature is pyrolyzed with millisecond, at descending pyrolysis reactor 8 standpipe bottom oil gas oil gas gas-solid separator 9 act under sharp separation grey with semicoke and heat；
Pyrolysis oil gas is fractionated into tower 10 and obtains gasoline 13, diesel oil 12, heavy oil 11 and pyrolysis dry gas 22, the semicoke that semicoke and heat ash are carried by air
Returning charge valve 23 enter burn riser 1 mix with the air of air inlet pipe 3 and gas distributor 2, combustion heating；High-temperature hot ash warp after heating
After inertia gas-solid separator 4 separates with flue gas with heat two grades of gas-solid separators 6 of ash, flue gas is guided to cigarette by air-introduced machine 14 after waste heat boiler 28
Promote and be dried the oil shale less than 6mm or oil-sand, the big-and-middle granule of part added from oil shale or oil-sand entrance 21 bottom air stripping riser 15
Heat ash enters descending pyrolysis reactor 8 top as high-temp circulating ash, it is achieved heat ash circulation heating, and part big-and-middle granule semicoke flows into outside fluidisation state
After heat collector 24 air burning takes heat drop temperature, and cooling, grey and the grey two grades of gas-solid separators 6 of heat grey entrance of thin heat of big-and-middle granule heat cools down feed bin 7
Comprehensive utilization is arranged outside rear.
Burning riser 1 reaction temperature is 850 DEG C-1200 DEG C.
High-temperature semi-coke is 2-8:1 with the mixed proportion of big-and-middle granule low-order coal.
It is 450 DEG C-600 DEG C that descending pyrolysis reactor 8 exports reaction temperature.
Heat ash fluidisation state external warmer 24 be utilize air by the big-and-middle granule semicoke of 850 DEG C-1200 DEG C in fluidisation state external warmer 24 burning and
Heat exchange produces high steam, and heat ash and air reclaim solid particle through bulky grain heat ash separator 25；Air after heating is by water inlet preheater
26 preheating external warmer water inlets, are cooled to less than 300 DEG C, utilize circulating fan 27 to send into bottom fluidisation state external warmer 24.
Oil shale provided by the present invention or oil-sand downlink cycle bed millisecond pyrolysis device for refining, by by oil shale or oil-sand and hot ash fraction
From, part big-and-middle granule heat ash is with raw material is pyrolyzed by descending pyrolysis reactor, thin feed particles is sent directly into riser and burns, big-and-middle of part
Grain heat ash reclaims heat outer row together with thin hot ash, thoroughly eliminates band ash and heat ash in oil and utilize a difficult problem for a difficult problem, tar yield from source
For the 90%-110% of theoretical oil yield, well cuts content is less than 0.1%, and Btu utilization is reasonable, it is to avoid oil shale or oil-sand pyrolysis lime-ash
Secondary pollution.
Claims (4)
1. oil shale or oil-sand downlink cycle bed millisecond pyrolysis device for refining, is characterized in that being arranged under flue gas riser oil shale or oil-sand entrance
Portion, flue gas riser top arranges gas-solid second-stage separator, and primary separator solid outlet is by top feed bin and feeder and descending pyrolytic reaction
Device top connects；Second-stage separator exhanst gas outlet directly outer row, solid outlet is connected bottom riser with burning by semicoke material returning device；Burn and carry
Arranging gas distributor and air inlet pipe bottom riser, top arranges inertia gas-solid separator by high-temperature hot ash returning charge controller and descending pyrolytic reaction
Device top connects, and inertia gas-solid separator separately sets a solid outlet and connects with fluidisation state external warmer, and cooling ash outlet connects with cooling feed bin；
The solid outlet of heat ash second-stage separator also connects with cooling feed bin, and gas outlet is connected with air-introduced machine by waste heat boiler bottom flue gas riser；
Arranging oil gas gas-solid separator bottom descending pyrolysis reactor, solid outlet is connected bottom riser with burning by semicoke returning charge valve, gaseous phase outlet
Being connected with oil gas fractionating column, fractionating column arranges pyrolysis dry gas outlet, fuel dispensing outlet, diesel oil outlet, heavy oil outlet from top to bottom.
Oil shale the most according to claim 1 or oil-sand downlink cycle bed millisecond pyrolysis device for refining, it is characterised in that burn riser reaction
Temperature is 850 DEG C-1200 DEG C, and high-temperature hot ash is 2-8:1 with the mixed proportion of big-and-middle Oil Shale Particles or oil-sand.
Oil shale the most according to claim 1 or oil-sand downlink cycle bed millisecond pyrolysis device for refining, it is characterised in that descending pyrolysis reactor
Outlet reaction temperature is 450 DEG C-600 DEG C.
Oil shale the most according to claim 1 or oil-sand downlink cycle bed millisecond pyrolysis device for refining, it is characterised in that external warmer is to utilize
Big-and-middle granule semicoke burning and heat exchange in fluidisation state external warmer of 850 DEG C-1200 DEG C are produced high steam by air, and air is through bulky grain heat ash
Separator is intake by water inlet preheater preheated fluidification state external warmer after reclaiming solid thermal ash particle, is cooled to less than 300 DEG C, utilizes circulated air
Machine is sent into bottom fluidisation state external warmer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610566486.4A CN105969417A (en) | 2016-07-18 | 2016-07-18 | Oil shale or oil sand downstream circulating bed millisecond pyrolysis refining device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610566486.4A CN105969417A (en) | 2016-07-18 | 2016-07-18 | Oil shale or oil sand downstream circulating bed millisecond pyrolysis refining device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105969417A true CN105969417A (en) | 2016-09-28 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610566486.4A Withdrawn CN105969417A (en) | 2016-07-18 | 2016-07-18 | Oil shale or oil sand downstream circulating bed millisecond pyrolysis refining device |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106833714A (en) * | 2017-03-22 | 2017-06-13 | 中国石油大学(华东) | Oil shale or oil-sand downlink cycle bed millisecond pyrolysis refining technique |
| CN106833713A (en) * | 2017-03-22 | 2017-06-13 | 中国石油大学(华东) | Oil shale or oil-sand downlink cycle bed millisecond pyrolysis device for refining |
| CN108485704A (en) * | 2018-04-17 | 2018-09-04 | 中国石油大学(华东) | Crude oil millisecond classification gas phase catalysis, which cracks and hydrogen combination is added to maximize, produces industrial chemicals technique |
| CN108504387A (en) * | 2018-04-17 | 2018-09-07 | 中国石油大学(华东) | Heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins technique |
-
2016
- 2016-07-18 CN CN201610566486.4A patent/CN105969417A/en not_active Withdrawn
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106833714A (en) * | 2017-03-22 | 2017-06-13 | 中国石油大学(华东) | Oil shale or oil-sand downlink cycle bed millisecond pyrolysis refining technique |
| CN106833713A (en) * | 2017-03-22 | 2017-06-13 | 中国石油大学(华东) | Oil shale or oil-sand downlink cycle bed millisecond pyrolysis device for refining |
| CN108485704A (en) * | 2018-04-17 | 2018-09-04 | 中国石油大学(华东) | Crude oil millisecond classification gas phase catalysis, which cracks and hydrogen combination is added to maximize, produces industrial chemicals technique |
| CN108504387A (en) * | 2018-04-17 | 2018-09-07 | 中国石油大学(华东) | Heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins technique |
| US10508247B2 (en) | 2018-04-17 | 2019-12-17 | China University Of Petroleum (East China) | Process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation |
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Application publication date: 20160928 |