CN106833714A - Oil shale or oil-sand downlink cycle bed millisecond pyrolysis refining technique - Google Patents
Oil shale or oil-sand downlink cycle bed millisecond pyrolysis refining technique Download PDFInfo
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- CN106833714A CN106833714A CN201710171634.7A CN201710171634A CN106833714A CN 106833714 A CN106833714 A CN 106833714A CN 201710171634 A CN201710171634 A CN 201710171634A CN 106833714 A CN106833714 A CN 106833714A
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- Prior art keywords
- oil
- ash
- heat
- sand
- gas
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- 239000004058 oil shale Substances 0.000 title claims abstract description 54
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 50
- 239000003027 oil sand Substances 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 28
- 238000007670 refining Methods 0.000 title claims abstract description 12
- 239000002245 particle Substances 0.000 claims abstract description 34
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000003546 flue gas Substances 0.000 claims abstract description 28
- 239000007787 solid Substances 0.000 claims abstract description 25
- 239000007789 gas Substances 0.000 claims abstract description 22
- 238000010438 heat treatment Methods 0.000 claims abstract description 16
- 238000001816 cooling Methods 0.000 claims abstract description 10
- 238000002485 combustion reaction Methods 0.000 claims abstract description 5
- 238000005243 fluidization Methods 0.000 claims abstract description 5
- 239000000843 powder Substances 0.000 claims abstract description 5
- 239000002918 waste heat Substances 0.000 claims abstract description 5
- 238000001035 drying Methods 0.000 claims abstract description 4
- 238000006243 chemical reaction Methods 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 235000015076 Shorea robusta Nutrition 0.000 claims description 3
- 244000166071 Shorea robusta Species 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 3
- 239000000463 material Substances 0.000 abstract 1
- 239000000203 mixture Substances 0.000 abstract 1
- 239000002956 ash Substances 0.000 description 54
- 239000003921 oil Substances 0.000 description 22
- 238000005516 engineering process Methods 0.000 description 7
- 239000011269 tar Substances 0.000 description 4
- 239000000571 coke Substances 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 1
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000011275 tar sand Substances 0.000 description 1
Classifications
-
- 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
- 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
Abstract
The present invention provides oil shale or oil-sand downlink cycle bed millisecond pyrolysis refining technique, oil shale or oil-sand dry through flue gas riser and are lifted and be classified in top gas-solid and separate, arranged outside flue gas, fine grained enters semicoke material returning device, big-and-middle particle descending pyrolysis reactor top and high-temp circulating ash realize it is quick mix intensification and millisecond pyrolysis, oil air and heat ash and semicoke quick separating in reactor standpipe bottom；Pyrolysis oil gas be fractionated into tower obtain different fractions oil product and dry gas, heat ash and semicoke enter burn riser combustion heating；After high-temperature hot ash after burning is separated through two-stage gas-solid separator with flue gas, flue gas is by being introduced to flue gas lifting bottom of the tube lifting and drying oil shale or oil-sand powder after waste heat boiler, the big-and-middle particle heat ash in part enters descending pyrolysis reactor top as high temperature circulation heat ash, the big-and-middle particle heat ash in part flows into the air secondary burning of fluidisation state heat collector and takes heat, and the big-and-middle particle heat ash after fine grained heat ash and cooling enters outer row's comprehensive utilization after cooling feed bin.
Description
1. technical field
The present invention provides oil shale or oil-sand downlink cycle bed millisecond pyrolysis refining technique, 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 refining technique, 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
Hot ash reclaims heat and thin heat ash direct outer row together, and the problem that band ash and heat ash in oil utilize problem is eliminated from source.Its
It is characterized in that a large amount of oil shales less than 6mm or oil-sand powder are dried and lifting, oil shale or oil-sand particle quilt through flue gas riser
The classification of two grades of gas-solid separators is separated, and is arranged outside flue gas, and fine grained oil shale or oil-sand are entered by semicoke returning charge valve and burn lifting
Under pipe, big-and-middle Oil Shale Particles or the rotated feeder of oil-sand are on descending pyrolysis reactor top and by high-temperature hot ash returning charge valve
The high temperature circulation heat ash quick mixing of rapid realization for falling heats up and is pyrolyzed with millisecond, in reactor standpipe bottom oil gas and semicoke and heat
Ash quick separating under gas-solid separator effect；Pyrolysis oil gas is fractionated into tower and obtains different fractions oil product and dry gas, semicoke and heat
Ash burns riser combustion heating by the semicoke returning charge valve entrance that air is conveyed；High-temperature hot ash after heating is through two-stage gas-solid point
After being separated with flue gas from device, flue gas is by being introduced to flue gas lifting bottom of the tube lifting and drying less than 6mm after waste heat boiler
Oil shale or oil-sand, the big-and-middle particle in part heat ash enters descending pyrolysis reactor top as high-temp circulating ash, realizes heat ash
Circulation heating, the big-and-middle particle semicoke in part flows into external warmer air burning and takes heat drop temperature, big-and-middle after thin heat ash and cooling
Grain heat ash enters outer row's comprehensive utilization after cooling feed bin.
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
Fig. 1 is to represent that oil shale or oil-sand downlink cycle the bed millisecond involved by embodiment 1 are pyrolyzed the device of refining technique
Schematic diagram.
Accompanying drawing is process schematic representation of the invention.The drawing of accompanying drawing is described 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 flue gas one-level gas-solid separator 16 and two grades of flue gas, 19 points of gas-solid separator
Level 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 riser
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 by high-temperature hot ash returning charge valve
The 5 high temperature circulation heat ashes for falling are rapid to realize that quick mixing heats up and millisecond pyrolysis, 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 is fractionated into tower 10 and obtains gasoline 13, bavin
Oil 12, heavy oil 11 and pyrolysis dry gas 22, semicoke and heat ash by air convey semicoke returning charge valve 23 into burn riser 1 and
The air mixing of air inlet pipe 3 and gas distributor 2, combustion heating；High-temperature hot ash after heating is through the He of inertia gas-solid separator 4
After two grades of gas-solid separators 6 of hot ash are separated with flue gas, flue gas by air-introduced machine 14 after waste heat boiler 28 by guiding to flue gas riser
15 bottoms lift and dry the oil shale or oil-sand less than 6mm added from oil shale or oil-sand entrance 21, the big-and-middle particle in part
Hot 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 stream in part
Enter to fluidize the air burning of state external warmer 24 and take heat drop temperature, the big-and-middle particle heat ash after thin heat ash and cooling enters cooling feed bin 7
Outer row's comprehensive utilization afterwards.
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 refining technique, 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 (5)
1. oil shale or oil-sand downlink cycle bed millisecond pyrolysis refining technique, it is characterized in that will a large amount of oil shales less than 6mm or
Oil-sand powder is dried and lifted through flue gas riser, and oil shale or oil-sand particle are separated by two grades of gas-solid separator classifications, outside flue gas
Row, fine grained oil shale or oil-sand are by semicoke returning charge valve into riser is burnt, and big-and-middle Oil Shale Particles or oil-sand are rotated
The high temperature circulation heat ash that feeder is fallen on descending pyrolysis reactor top and by high-temperature hot ash returning charge valve is realized rapidly quick
Mixing heats up and millisecond pyrolysis, quickly divides under gas-solid separator effect with semicoke and heat ash in reactor standpipe bottom oil gas
From；Pyrolysis oil gas is fractionated into tower and obtains different fractions oil product and dry gas, the semicoke returning charge valve that semicoke and heat ash are conveyed by air
Into burning riser combustion heating；After high-temperature hot ash after heating is separated through two-stage gas-solid separator with flue gas, flue gas
By being introduced to flue gas lifting bottom of the tube lifting after waste heat boiler and drying the oil shale or oil-sand less than 6mm, big-and-middle of part
Grain heat ash enters descending pyrolysis reactor top as high-temp circulating ash, realizes heat ash circulation heating, the big-and-middle particle semicoke in part
Flow into external warmer air burning and take heat drop temperature, outer row is comprehensive after the big-and-middle particle heat ash after thin heat ash and cooling enters cooling feed bin
Close and utilize.
2. oil shale according to claim 1 or oil-sand downlink cycle bed millisecond are pyrolyzed refining technique, it is characterised in that burn
Burnt riser reaction temperature is 850 DEG C -1200 DEG C.
3. oil shale according to claim 1 or oil-sand downlink cycle bed millisecond are pyrolyzed refining technique, it is characterised in that high
The grey mixed proportion with big-and-middle Oil Shale Particles or oil-sand of warm is 2-8：1.
4. oil shale according to claim 1 or oil-sand downlink cycle bed millisecond are pyrolyzed refining technique, it is characterised in that under
Row pyrolysis reactor outlet reaction temperature is 450 DEG C -600 DEG C.
5. oil shale according to claim 1 or oil-sand downlink cycle bed millisecond are pyrolyzed refining technique, 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 |
|---|---|---|---|
| CN201710171634.7A CN106833714A (en) | 2017-03-22 | 2017-03-22 | Oil shale or oil-sand downlink cycle bed millisecond pyrolysis refining technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710171634.7A CN106833714A (en) | 2017-03-22 | 2017-03-22 | Oil shale or oil-sand downlink cycle bed millisecond pyrolysis refining technique |
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| Publication Number | Publication Date |
|---|---|
| CN106833714A true CN106833714A (en) | 2017-06-13 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710171634.7A Pending CN106833714A (en) | 2017-03-22 | 2017-03-22 | Oil shale or oil-sand downlink cycle bed millisecond pyrolysis refining technique |
Country Status (1)
| Country | Link |
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Citations (2)
| 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 |
| CN106190215A (en) * | 2016-07-18 | 2016-12-07 | 中国石油大学(华东) | Oil shale or oil-sand downlink cycle bed millisecond pyrolysis refining technique |
-
2017
- 2017-03-22 CN CN201710171634.7A patent/CN106833714A/en active Pending
Patent Citations (2)
| 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 |
| CN106190215A (en) * | 2016-07-18 | 2016-12-07 | 中国石油大学(华东) | Oil shale or oil-sand downlink cycle bed millisecond pyrolysis refining technique |
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Application publication date: 20170613 |