CN106833713A - Oil shale or oil-sand downlink cycle bed millisecond pyrolysis device for refining - Google Patents
Oil shale or oil-sand downlink cycle bed millisecond pyrolysis device for refining Download PDFInfo
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- CN106833713A CN106833713A CN201710171618.8A CN201710171618A CN106833713A CN 106833713 A CN106833713 A CN 106833713A CN 201710171618 A CN201710171618 A CN 201710171618A CN 106833713 A CN106833713 A CN 106833713A
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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
-
- 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
-
- 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)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides oil shale or oil-sand downlink cycle bed millisecond pyrolysis device for refining, oil shale or oil-sand entrance are arranged on flue gas riser bottom, flue gas riser top sets gas-solid second-stage separator, and primary separator solid outlet is connected with descending pyrolysis reactor top；Second-stage separator exhanst gas outlet is directly outer to be arranged, and solid outlet is connected with lifting bottom of the tube is burnt；Burn lifting bottom of the tube and gas distributor and air inlet pipe are set, top is set inertia gas-solid separator and is connected with descending pyrolysis reactor top by high-temperature hot ash returning charge controller, the another solid outlet that sets is connected with fluidisation state external warmer, the outlet of cooling ash and heat ash second-stage separator are connected with cooling feed bin, and gas vent lifts bottom of the tube and connects by waste heat boiler and air-introduced machine with flue gas；Descending pyrolysis reactor bottom sets gs-oil separator, and solid outlet is connected with lifting bottom of the tube is burnt, and gaseous phase outlet is connected with oil gas fractionating column, and fractionating column sets pyrolysis dry gas, gasoline, diesel oil and 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, and it is non-to be listed in 21 century with aboundresources and the feasibility for developing
Often important takes over the energy.China's oil shale resources are enriched, about 240,000,000,000 tons of technically recoverable resources, in theory recyclable destructive distillation
About 10,000,000,000 tons of oil；Chinese tar sand oil geological resources are 59.7 hundred million tons, 22.58 hundred million tons of mining resources amount, recyclable dry in theory
About 1,000,000,000 tons of oil is evaporated, industrialization potential is huge.
At present, many countries are all studied oil shale/oil-sand method for destructive distillation in the world, and the formation having is industrialized
Production scale.Oil shale distillation process can be divided into external-heat and the class of internal heat type two by mode of heating：External heating type heat efficiency is low, oily page
Rock heating is uneven, and the twice decomposition of volatility product is serious, and tar yield is low, and device is difficult to maximize, therefore this kind of technology is general
Laboratory is served only for, large industrialized oil shale pyrolysis process is difficult to realize；Internal heat type technology utilization gas heat carrier or solid
Heat is directly passed to oil shale by heat carrier, makes oil shale that pyrolytic reaction to occur, and the shortcoming of external-heat is overcome, with caloic
Transmission speed is fast, homogeneous heating, fugitive constituent twice decomposition are few, and tar yield is high, and device is easy 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 for the flue gas of fuel combustion to introduce pyrolysis chamber, the representational COED techniques for having the U.S., ENCOAL techniques
With double boiling bed process etc. of Poland.Solid heat carrier pyrolysis technique then using high-temperature semi-coke or other high-temp solid material with
Oil shale mixes in pyrolysis chamber, using the sensible heat of heat carrier by oil shale pyrolysis.Compared with gas heat carrier pyrolytic process, Gu
Body heat carrier pyrolysis avoid the volatility product of oil shale pyrolysis precipitation by flue gas dilution, while reducing the negative of cooling system
Lotus, process advantage is obvious.But existing oil shale solid heat carrier rapid pyrolysis technology is high in the presence of band ash, mechanical moving element in oil
The problems such as temperature abrasion, device enlarge-effect and equipment long-period stable operation, the technology as restriction oil shale fast pyrogenation
Bottleneck, is badly in need of being eliminated in oil according to the exploitation of oil shale pyrolysis response characteristics that band is grey, heat transfer is 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 hot ash content fraction
From big-and-middle particle heat ash is pyrolyzed by descending pyrolysis reactor, the outer row of molecule heat ash, eliminates what hot ash was caused from source
The grey problem of band in oil.But separation is not classified after oil shale/oil-sand particle drying, fine particle therein can also be produced from source
The grey phenomenon of band in oil.The lime-ash that can produce about 90% or so is refined additionally, due to oil shale/oil-sand pyrolysis, it is necessary to a large amount of outer rows,
It is only far from enough by the thin heat ash of discharge in former patent, in addition it is also necessary to largely to discharge big-and-middle particle heat ash, and it is residual in this part heat ash
Charcoal value is again too high, it is necessary to consider rationally to utilize, these turn into oil shale/oil-sand downlink cycle fluidized bed pyrolysis liquefaction process work
The bottleneck of industry.
3. the content of the invention
The purpose of the present invention is proposed to overcome the shortcomings of existing oil shale/oil-sand pyrolysis liquefaction technology to exist
A kind of oil shale or oil-sand downlink cycle fluid bed millisecond pyrolysis device for refining, had both thoroughly solved oil shale/oil-sand fluid bed
The grey problem of band in the oil of pyrolysis upgrading, and the different tar of high added value rationally are also obtained using the outer ash discharge of pyrolysis and heat energy
Cut and combustion gas.
Technical scheme：
The purpose of the present invention is to realize that classification is separated by by oil shale or oil-sand feed particles and heat ash, big-and-middle of part
Grain heat ash is with raw material is pyrolyzed by descending pyrolysis reactor, thin feed particles are sent directly into riser and burn, the big-and-middle particle in part
Air burn reclaims heat and thin heat ash direct outer row together to hot ash again, and band ash and heat ash are eliminated in oil from source using difficult
The problem of topic.It is characterized in that oil shale or oil-sand entrance are arranged on into flue gas riser bottom, flue gas riser top sets gas
Gu second-stage separator, primary separator solid outlet is connected by top feed bin and feeder with descending pyrolysis reactor top；
Second-stage separator exhanst gas outlet is directly outer to be arranged, and solid outlet is connected by semicoke material returning device with lifting bottom of the tube is burnt；Burn and carry
Rise bottom of the tube and gas distributor and air inlet pipe be set, top set inertia gas-solid separator by high-temperature hot ash returning charge controller with
Descending pyrolysis reactor top connection, inertia gas-solid separator separately sets a solid outlet and is connected with fluidisation state external warmer, cold
But ash outlet is connected with cooling feed bin；The solid outlet of hot ash second-stage separator is also connected with cooling feed bin, and gas vent passes through
Waste heat boiler and air-introduced machine are connected with flue gas lifting bottom of the tube；Descending pyrolysis reactor bottom sets oil gas gas-solid separator, Gu
Body outlet is connected by semicoke returning charge valve with lifting bottom of the tube is burnt, and gaseous phase outlet is connected with oil gas fractionating column, and fractionating column is from upper
To lower, the outlet of pyrolysis dry gas, fuel dispensing outlet, diesel oil outlet, heavy oil outlet are set.
Riser reaction temperature is burnt for 850 DEG C -1200 DEG C.
High-temperature hot ash is 2-8 with the mixed proportion of oil shale/oil-sand powder：1.
Descending pyrolysis reactor outlet reaction temperature is 450 DEG C -600 DEG C.
External warmer is that 850 DEG C -1200 DEG C of big-and-middle particle semicoke is burnt in state external warmer is fluidized using air
With heat exchange production high steam, heat ash and air reclaim solid particle through bulky grain heat ash separator；Air after heating passes through
Enter the water inlet of water preheater preheated fluidification state external warmer, be cooled to less than 300 DEG C, using circulating fan feeding fluidisation state outside heat removing
Device bottom.
Embodiment is described the features of the present invention by the present invention in detail.
4. illustrate
Accompanying drawing 1 is process schematic representation of the invention.The drawing of accompanying drawing 1 sets bright as follows：
1st, riser 2, gas distributor 3, air inlet pipe 4, inertia gas-solid separator 5, high-temperature hot ash returning charge control are burnt
Device processed 6, two grades of gas-solid separators 7 of heat ash, heat ash cooling feed bin 8, descending pyrolysis reactor 9, oil gas gas-solid separator
10th, 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
16th, flue gas one-level gas-solid separator 17, top feed bin 18, rotary table feeder 19, two grades of gas-solid separators 20, flue gas of flue gas
Outlet 21, oil shale or the outlet 23, semicoke returning charge valve 24 of oil-sand entrance 22, dry gas, fluidisation state external warmer 25, big
Grain heat ash separator 26, enter water preheater 27, circulating fan 28, waste heat boiler.
With reference to the accompanying drawings and examples in detail process characteristic of the invention is described in detail.
5. specific embodiment
A large amount of oil shales less than 6mm or oil-sand powder are entered flue gas and are lifted by embodiment 1 through oil shale or oil-sand entrance 21
Pipe 15 is dried and lifted, and oil shale or oil-sand particle are by two grades of gas-solid separators (19) of flue gas one-level gas-solid separator 16 and flue gas
Classification is separated, and flue gas is arranged from exhanst gas outlet 20 is outer, and fine grained oil shale or oil-sand are entered by semicoke returning charge valve 23 and burn lifting
Pipe 1, big-and-middle Oil Shale Particles or the rotated feeder 18 of oil-sand are on the top of descending pyrolysis reactor 8 and pass through high-temperature hot ash returning charge
The high temperature circulation heat ash quick mixing of rapid realization that valve 5 falls heats up and is pyrolyzed with millisecond, in the standpipe bottom of descending pyrolysis reactor 8
Oil gas quick separating under the effect of oil gas gas-solid separator 9 with semicoke and heat ash；Pyrolysis oil gas be fractionated into tower 10 obtain gasoline 13,
The semicoke returning charge valve 23 that diesel oil 12, heavy oil 11 and pyrolysis dry gas 22, semicoke and heat ash are conveyed by air is into burning riser 1
Mix with the air of air inlet pipe 3 and gas distributor 2, combustion heating；High-temperature hot ash after heating is through inertia gas-solid separator 4
And after heat two grades of gas-solid separators 6 of ash are separated with flue gas, flue gas by air-introduced machine 14 after waste heat boiler 28 by guiding to flue gas lifting
The bottom of pipe 15 lifts and dries the oil shale or oil-sand less than 6mm added from oil shale or oil-sand entrance 21, big-and-middle of part
Grain heat ash enters the top of descending pyrolysis reactor 8 as high-temp circulating ash, realizes heat ash circulation heating, the big-and-middle particle semicoke in part
Flow into the air burning of fluidisation state external warmer 24 and take big-and-middle particle heat ash and heat two grades of gas-solid separators of ash after heat drop temperature, and cooling
6 thin heat ash enters outer row's comprehensive utilization after cooling feed bin 7.
The reaction temperature of riser 1 is burnt for 850 DEG C -1200 DEG C.
High-temperature semi-coke is 2-8 with the mixed proportion of big-and-middle particle low-order coal：1.
The outlet reaction temperature of descending pyrolysis reactor 8 is 450 DEG C -600 DEG C.
Hot ash fluidisation state external warmer 24 is to be fluidized outside state 850 DEG C -1200 DEG C of big-and-middle particle semicoke using air
Burn and exchange heat production high steam in heat collector 24, and heat ash and air reclaim solid particle through bulky grain heat ash separator 25；
Air after heating preheats external warmer water inlet by entering water preheater 26, is cooled to less than 300 DEG C, is sent using circulating fan 27
Enter to fluidize the bottom of 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 content level are separated, and the big-and-middle particle heat ash in part is pyrolyzed with raw material by descending pyrolysis reactor, thin feed particles are direct
Feeding riser burns, and the big-and-middle particle in part heat ash reclaims heat and thin heat ash direct outer row together, is thoroughly eliminated from source
The problem of problem is utilized in oil with ash and heat ash, tar yield is the 90%-110% of theoretical oil yield, and well cuts content is small
In 0.1%, Btu utilization is reasonable, it is to avoid oil shale or oil-sand are pyrolyzed the secondary pollution of lime-ash.
Claims (4)
1. oil shale or oil-sand downlink cycle bed millisecond are pyrolyzed device for refining, it is characterized in that oil shale or oil-sand entrance are arranged on
Flue gas riser bottom, flue gas riser top sets gas-solid second-stage separator, and primary separator solid outlet is expected by top
Storehouse and feeder are connected with descending pyrolysis reactor top；Second-stage separator exhanst gas outlet is directly outer to be arranged, and solid outlet is by half
Burnt material returning device is connected with lifting bottom of the tube is burnt；Burn lifting bottom of the tube and gas distributor and air inlet pipe are set, top sets used
Property gas-solid separator connected by high-temperature hot ash returning charge controller and descending pyrolysis reactor top, inertia gas-solid separator separately sets
One solid outlet is connected with fluidisation state external warmer, and the outlet of cooling ash is connected with cooling feed bin；Hot ash second-stage separator is consolidated
Body outlet is also connected with cooling feed bin, and gas vent lifts bottom of the tube and connects by waste heat boiler and air-introduced machine with flue gas；It is descending
Pyrolysis reactor bottom sets oil gas gas-solid separator, and solid outlet is connected by semicoke returning charge valve with lifting bottom of the tube is burnt,
Gaseous phase outlet is connected with oil gas fractionating column, and fractionating column sets the outlet of pyrolysis dry gas, fuel dispensing outlet, diesel oil outlet, weight from top to bottom
Oil export.
2. oil shale according to claim 1 or oil-sand downlink cycle bed millisecond are pyrolyzed device for refining, it is characterised in that burn
Burnt riser reaction temperature is 850 DEG C -1200 DEG C, and high-temperature hot ash is 2-8 with the mixed proportion of big-and-middle Oil Shale Particles or oil-sand：
1。
3. oil shale according to claim 1 or oil-sand downlink cycle bed millisecond are pyrolyzed device for refining, it is characterised in that under
Row pyrolysis reactor outlet reaction temperature is 450 DEG C -600 DEG C.
4. oil shale according to claim 1 or oil-sand downlink cycle bed millisecond are pyrolyzed device for refining, it is characterised in that outward
Heat collector is using air burning and heat exchange production in state external warmer is fluidized by 850 DEG C -1200 DEG C of big-and-middle particle semicoke
High steam, air is taken by entering after reclaiming solid thermal ash particle through bulky grain heat ash separator outside water preheater preheated fluidification state
Hot device water inlet, is cooled to less than 300 DEG C, using circulating fan feeding fluidisation state external warmer bottom.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710171618.8A CN106833713A (en) | 2017-03-22 | 2017-03-22 | Oil shale or oil-sand downlink cycle bed millisecond pyrolysis device for refining |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710171618.8A CN106833713A (en) | 2017-03-22 | 2017-03-22 | Oil shale or oil-sand downlink cycle bed millisecond pyrolysis device for refining |
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| CN106833713A true CN106833713A (en) | 2017-06-13 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105969417A (en) * | 2016-07-18 | 2016-09-28 | 中国石油大学(华东) | Oil shale or oil sand downstream circulating bed millisecond pyrolysis refining device |
-
2017
- 2017-03-22 CN CN201710171618.8A patent/CN106833713A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105969417A (en) * | 2016-07-18 | 2016-09-28 | 中国石油大学(华东) | Oil shale or oil sand downstream circulating bed millisecond pyrolysis refining device |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
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Application publication date: 20170613 |