CN101775309B - Method for refining from oil sand by using high-temperature gas-cooled reactor and special equipment - Google Patents
Method for refining from oil sand by using high-temperature gas-cooled reactor and special equipment Download PDFInfo
- Publication number
- CN101775309B CN101775309B CN 201010115831 CN201010115831A CN101775309B CN 101775309 B CN101775309 B CN 101775309B CN 201010115831 CN201010115831 CN 201010115831 CN 201010115831 A CN201010115831 A CN 201010115831A CN 101775309 B CN101775309 B CN 101775309B
- Authority
- CN
- China
- Prior art keywords
- oil
- sand
- high temperature
- cooled reactor
- temperature gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a method for refining from oil sand by using a high-temperature gas-cooled reactor and special equipment thereof. The method uses heat energy provided by the nuclear reaction of a high-temperature gas-cooled nuclear reactor to perform pyrolysis on the oil sand to extract hydrocarbon oil and combustible gas, and comprises the following three relatively independent processesthat: high-temperature heat supply, namely, inert gas at 200 to 300 DEG C flows through a core of the high-temperature gas-cooled reactor, is heated to 600 to 950 DEG C, supplies heat to a pyrolyzer and a steam generator, and enters the core of the high-temperature gas-cooled reactor; superheated steam supply, namely, treated water is heated into steam at 200 to 400 DEG C by the steam generator and flows into an oil sand separator; and refining, namely, the treated oil sand is sent to the oil sand separator to react with the steam, asphalt substances in the oil sand are separated from sand and are modified to form synthetic crude oil, mixed substances of the synthetic crude oil, the water and small gravels are separated, the obtained synthetic crude oil substance is heated to the maximum temperature of between 500 and 700 DEG C and is pyrolyzed into oil gas and oil residues, and the oil gas is fractionated by a fractionating tower to obtain the combustible gas such as the hydrocarbon oil, natural gas and the like.
Description
Technical field
The present invention relates to a kind of method and specific equipment thereof that utilizes high temperature gas cooled reactor to carry out refining from oil sand.
Background technology
Oil-sand claims again " tar sand ", " Tar sands ", is a kind of sandstone or other rocks that contains pitch or tar.The mixture that normally is comprised of sand, pitch, tar, mineral substance, clay and water belongs to the non-conventional oil resource.Oil-sand is one of the important sources of " artificial petroleum ", and oil-sand separates, carries out upgrading through exploitation, extraction, can obtain synthetic crude.
World's oil-sand resource mainly distributes along Pacific belt and Alps band, and resource is very abundant.There are Canada, USSR (Union of Soviet Socialist Republics), Venezuela, the U.S., China etc. in the countries and regions that reserves account for the prostatitis.China's oil-sand resource distributes also very extensive than horn of plenty, before mainly being distributed in accurate Ge Er Basin In Western the northern fringe, the Caidamu Basin Chai Xi area, Sichuan Basin Longmenshan in Xinjiang, the ground such as Qinghai, Tibet, the Inner Mongol, Guizhou.According to relevant expert's prediction, the minable oil-sand reserves of China are about 10,000,000,000 tons of left and right, account for 1/3 of China's oil gas workable reserves, may become a new growth point of Future in China oil and gas production.
Simultaneously, due to rolling up of carbonic acid gas isothermal chamber gas emissions, cause global climate sharply to worsen, the mankind's living environment is caused great threat.Cut down CO2 emissions, alleviate Greenhouse effect, become the extensive common recognition of international community.According to International Energy Agency (IEA) 2007 statistics, the Carbon emission state that the U.S., China, Russia, Japan and India in 2005 are 5 maximums accounts for 50% of world's total emission volumn.Simultaneously, the statistics of IEA shows, discharges from industry, and Oil Refining Industry is in 9 main carbonic acid gas industry emission sources, and CO2 emissions is only second to thermal power generation industry and cement industry, and China's Carbon emission industry consists of basically identical with it.For example for the refinery of a year 400 ten thousand tons of amount of finish, its year CO2 emissions can reach 0.8 hundred ten thousand tons.And account for the overwhelming majority of its discharging for the CO2 emissions that the required energy combustion fuel generation of oil refining is provided in refinery, for example this ratio is 90% for European Union's refinery.Therefore, as the refinery of the main emission source of carbonic acid gas, be faced with the challenge of producing clear gusoline and reducing CO2 emissions.
Oil-sand exploitation in the world, processing and utilization at present, the traditional indirect method of main employing first extracts through physics, chemical separation process the pitch in oil-sand from oil-sand, the asphalt oil upgrading is obtained synthetic crude, again synthetic crude is transported to refinery, refines oil.Need to consume a large amount of energy in whole process, give off simultaneously a large amount of carbonic acid gas and chemical pollutant, cause Financial cost and Environmental costs all very expensive.For overcoming the shortcoming of traditional indirect method, the new method from refining from oil sand has been subjected to attention, all propose the new oil-sand that utilizes as patent CN101358136A, patent CN101250421A and carried out the method for integrated oil refining, to utilize the method for direct vulcanization bed coking to carry out oil-sand directly to refine oil as the former, the horizontal destructive distillation rotary kiln of the latter carries out the direct oil refining of oil-sand, these class methods compare traditional indirect method all have chemical pollution little, be fit to commercial run large scale continuous prod and the lower advantage of direct production cost.But these class methods also have some obvious shortcomings, because composition is comparatively complicated, process and the product of cracking or chemical reaction directly occur in oil-sand under high temperature action comparatively complicated, the impurity that contains in output oil gas is more, the inflammable gas of cooling rear gained is due to can't directly utilizing of a large amount of carbonic acid gas, nitrogen being arranged, in whole production process, CO2 emissions much larger than traditional indirect method, is difficult to adapt to the megatrend of current carbon dioxide discharge-reduction simultaneously.
Summary of the invention
The technical problem that (one) will solve
The technical problem to be solved in the present invention is: can industrialization ground land oil-sand, greasy filth from oil-sand and oil field and extract hydrocarbon ils, Sweet natural gas etc., the shortcomings such as the chemical pollution that has overcome traditional indirect method is large, production cost is high, and the shortcoming that the Carbon emission of integrated high temp oil-refining method is high, product is oily or the gas foreign matter content is high.
(2) technical scheme
For achieving the above object, the invention provides a kind of method of utilizing high temperature gas cooled reactor to carry out refining from oil sand, the described method of utilizing high temperature gas cooled reactor to carry out refining from oil sand comprises three relatively independent flow processs:
The high-temperature heat supply flow process, 200 ℃～300 ℃ rare gas elementes are after the helium circulator pressurization, the high temperature gas cooled reactor of flowing through reactor core is heated to 600 ℃～950 ℃, after the vapour generator heat supply, is entered the high temperature gas cooled reactor reactor core after the pressurization of described helium circulator again after being cooled to 200 ℃～300 ℃;
Steam supply flow path, treated water is heated as superheated vapour or the saturation steam of 200～400 ℃ in described vapour generator after the water pump pressurization, and then described superheated vapour or saturation steam enter oil-sand separator;
The oil refining flow process, pretreated oil-sand is sent into oil-sand separator and described superheated vapour or saturation steam has an effect, oil-sand medium pitch class material and sand separation also tentatively are cracked into synthetic crude, after synthetic crude class material process whizzer separating-purifying, be heated to 500 ℃～700 ℃ of top temperatures and be cracked into oil gas and the dregs of fat, oil gas obtains the inflammable gass such as hydrocarbon ils and Sweet natural gas by separation column.
Preferably, described rare gas element is helium.
Preferably, in described high-temperature heat supply flow process, described rare gas element after the described high temperature gas cooled reactor reactor core of flowing through heats, enter described pyrolyzer and to its heat supply, synthetic petroleum heating after purifying through described whizzer in described pyrolyzer is then from the described rare gas element described vapour generator of inflow of described pyrolyzer outflow and to described vapour generator heat supply.
Preferably, in described high-temperature heat supply flow process, described rare gas element after the described high temperature gas cooled reactor reactor core of flowing through heats, enter interchanger and to its heat supply, then from the rare gas element described vapour generator of inflow of described interchanger outflow and to its heat supply, heated working medium flows into described pyrolyzer in described interchanger, and the synthetic petroleum heating after purifying through described whizzer in described pyrolyzer, and the working medium that flows out from described pyrolyzer enters described interchanger after the blower fan pressurization.
For achieving the above object, the present invention also provides a kind of method of utilizing high temperature gas cooled reactor to carry out refining from oil sand specific equipment used, and described specific equipment comprises:
Utilize high temperature gas cooled reactor that the high-temperature heat supply system of heat of high temperature is provided, comprise high temperature gas cooled reactor, helium circulator and hot gas mixing section;
Steam supply system is used for utilizing the heat of high temperature that described high-temperature heat supply system provides to produce superheated vapour or saturation steam;
Distillation system comprises the oil-sand separation subsystem that oil-sand is provided with saturation steam be used to the superheated vapour that utilizes described steam supply system to provide; Be used for utilizing heat of high temperature that described high-temperature heat supply system provides to carry out pyrolysis subsystem pyrolysis, that comprise the first pyrolysis tower and the oil gas that is used for described pyrolysis subsystem is obtained carries out fractionation subsystem fractionation, that comprise separation column to the synthetic crude that described oil-sand separation subsystem obtains.
Preferably, described steam supply system comprises direct current spiral tube vapour generator.
Preferably, described oil-sand separation subsystem comprises:
Transfer roller is used for pretreated oil-sand is delivered to the Wet type drum ingress;
Wet type drum has cellular internal surface and is provided with spiral slot;
Air-supply duct is positioned at described Wet type drum center, and is connected with superheated vapour or the saturation steam outlet of described steam supply system, and described air-supply duct tube wall is provided with the duct that sprays for superheated vapour or saturation steam;
The precipitate and separate pond is communicated with the outlet of described Wet type drum by deflector chute, and bottom, described precipitate and separate pond is provided with the pond bottom outlet;
Stirrer is arranged in described precipitate and separate pond;
Whizzer, the drainage tube by being positioned at top, described precipitate and separate pond is communicated with described precipitate and separate pond;
Oil pump connects described whizzer and described the first pyrolysis tower by conduit.
Preferably, described oil-sand separation subsystem comprises:
Transfer roller is used for pretreated oil-sand is delivered to the second pyrolysis tower ingress via the first deflector chute;
The second pyrolysis tower, its bottom is provided with the tower bottom outlet;
The second stirrer is arranged in described the second pyrolysis tower;
The helix tube type air-supply duct is arranged in described the second pyrolysis tower, and is connected with superheated vapour or the saturation steam outlet of described steam supply system, and described helix tube type air-supply duct tube wall is provided with the duct for superheated vapour or saturation steam ejection;
The precipitate and separate pond, its bottom is provided with the pond bottom outlet;
Pump is arranged between described the second pyrolysis tower and precipitate and separate pond, connects described the second pyrolysis tower and described precipitate and separate pond by the second deflector chute;
Stirrer is arranged in described precipitate and separate pond;
Whizzer, the drainage tube by being positioned at top, described precipitate and separate pond is communicated with described precipitate and separate pond;
Oil pump connects described whizzer and described the first pyrolysis tower.
Preferably, described high-temperature heat supply system also comprises interchanger and blower fan, described interchanger is connected with the rare gas element outlet of described high-temperature heat supply system, is connected with described the first pyrolysis tower and supplies heat to described the first pyrolysis tower, the described blower fan described interchanger of connection and described the first pyrolysis tower.
(3) beneficial effect
The present invention compared with prior art exists obvious advantage to be:
(1), utilize high temperature gas cooled reactor to carry out the oil-sand pyrogenation oil refining for high temperature heat source, do not need to carry out the burning of fossil oil, when Financial cost obviously improves, greatly reduced the CO2 emissions in the oil refining process.
(2), utilize high temperature gas cooled reactor to carry out the oil-sand pyrogenation oil refining for high temperature heat source, substantially do not need chemical additive in the upgrading process of oil-sand separation, bitumen, environmental pollution is less.
(3), due to the flow process that adopts oil-sand separation, asphalt modifier, oil refining to carry out continuously, saved oil-sand, the synthetic crude great amount of cost in transportation.
(4), due to the method that adopts oil-sand separation, asphalt modifier and two steps of oil refining to carry out, avoided the direct heat to sandstone, and directly compare from the method for refining from oil sand, Carbon emission is few, output quality oily and output gas is better.
Description of drawings
Fig. 1 utilizes high temperature gas cooled reactor to carry out the structural representation of the device embodiment 1 of refining from oil sand;
Fig. 2 utilizes high temperature gas cooled reactor to carry out the structural representation of the device embodiment 2 of refining from oil sand;
Fig. 3 utilizes high temperature gas cooled reactor to carry out the structural representation of the device embodiment 3 of refining from oil sand.
Embodiment
The high temperature gas cooled reactor of utilizing that the present invention proposes is carried out the device of refining from oil sand, is described in detail as follows in conjunction with the accompanying drawings and embodiments.
Referring to Fig. 1, the device that utilizes high temperature gas cooled reactor to carry out refining from oil sand of the present embodiment comprises: high temperature gas cooled reactor reactor core 1, hot gas mixing section 2, pyrolyzer 3, pyrolysis tower 4, spiral tube 5, direct current spiral tube vapour generator 6, helium circulator 7, water pump 8, transfer roller 9, Wet type drum 10, air-supply duct 11, oil-sand separator 12, stirrer 13, precipitate and separate pond 14, whizzer 15, oil pump 16, separation column 17, oil pump 18, motor 19, deflector chute 20.
In the present embodiment, the rare gas element helium is 200 ℃～300 ℃ entering the front temperature of high temperature gas cooled reactor reactor core 1, pressure is 1.5MPa～10MPa, be heated to 600 ℃～800 ℃ after the high temperature gas cooled reactor of flowing through reactor core 1, flow into pyrolysis tower 4, synthetic crude in pyrolysis tower 4 is heated to 500 ℃～700 ℃ and make it to occur cracking, the direct current spiral tube vapour generator 6 of flowing through again after the first cooling of helium, water in vapour generator 6 is heated to the superheated vapour of 200 ℃～400 ℃, helium is cooled to 200 ℃～300 ℃ after release of heat in vapour generator 6.
Embodiment 2
Referring to Fig. 2, the device that utilizes high temperature gas cooled reactor to carry out refining from oil sand of the present embodiment comprises: high temperature gas cooled reactor reactor core 1, hot gas mixing section 2, pyrolyzer 3, pyrolysis tower 4, spiral tube 5, direct current spiral tube vapour generator 6, helium circulator 7, water pump 8, transfer roller 9, Wet type drum 10, air-supply duct 11, oil-sand separator 12, stirrer 13, precipitate and separate pond 14, whizzer 15, oil pump 16, separation column 17, oil pump 18, motor 19, deflector chute 20, heat exchanger 21, blower fan 22.Due to helium flow through the high temperature gas cooled reactor reactor core, might be with radioactive substance in helium, for the safe class of 3 pairs of radioactive substances of pyrolyzer, the present embodiment is compared with embodiment 1, has increased interchanger 21 and blower fan 22.
In the present embodiment, the rare gas element helium is 200 ℃～300 ℃ entering the front temperature of high temperature gas cooled reactor reactor core 1, pressure is 1.5MPa～10MPa, be pressurized to 700 ℃～950 ℃ after the high temperature gas cooled reactor of flowing through reactor core 1, the heat exchanger 21 of flowing through, nitrogen in heat exchanger 21 is heated to be 600 ℃～800 ℃, and the nitrogen gas stream after heating is through pyrolysis tower 4, and the synthetic crude in pyrolysis tower 4 is heated to 500 ℃～700 ℃ and cracking occurs; The helium flow vapour generator 6 of flowing through again after first cooling through heat exchanger 21 is heated to the water of vapour generator 6 water sides the superheated vapour of 200 ℃～400 ℃, and helium is cooled to 200 ℃～300 ℃ after release of heat in vapour generator 6.
Embodiment 3
Referring to Fig. 3, the device that utilizes high temperature gas cooled reactor to carry out refining from oil sand of the present embodiment comprises: high temperature gas cooled reactor reactor core 1, hot gas mixing section 2, pyrolyzer 3, the first pyrolysis tower 4, spiral tube 5, direct current spiral tube vapour generator 6, helium circulator 7, water pump 8, transfer roller 9, the second pyrolysis tower 30, helix tube type air-supply duct 31, oil-sand separator 12, the first stirrer 13, precipitate and separate pond 14, whizzer 15, oil pump 16, separation column 17, oil pump 18, the first deflector chute 19, the second deflector chute 20, the second stirrer 32, pump 33.
transfer roller 9 is delivered to the second pyrolysis tower 30 ingress with oil-sand after pretreatment, and oil-sand enters into the second pyrolysis tower 30 through the first deflector chute 19 of ingress, simultaneously, the water of treated mistake is transported in the spiral tube of direct current spiral tube vapour generator 6 by water pump 8, the helium of direct current spiral tube vapour generator 6 of being flowed through is heated as superheated vapour, superheated vapour enters into by pipeline the helix tube type air-supply duct 31 that is arranged in the second pyrolysis tower 30 after flowing out direct current spiral tube vapour generator 6, duct ejection by helix tube type air-supply duct 31 tube walls, act in the second pyrolysis tower 30 with the oil-sand in the second pyrolysis tower 30, upgrading also occurs and becomes synthetic crude in oil-sand medium pitch class material and sand separation, the sandstone that density is higher is deposited on the second pyrolysis tower 30 bottoms, and discharged by the tower bottom outlet, synthetic crude, part sand, the mixture of water and oil-sand moves to the second pyrolysis tower 30 tops under the effect of the second stirrer 32, under the effect of pump 33, by outlet conduit entrance motion of 14 to the precipitate and separate pond, the mixture of synthetic crude, part sand, water and oil-sand enters into precipitate and separate pond 14 along the second deflector chute 20 of 14 ingress, precipitate and separate pond, under stirrer 13 stirrings and buoyancy, the sandstone that density is higher and part oil-sand are deposited on 14 bottoms, precipitate and separate pond, and be expelled to transfer roller 9 by the pond bottom outlet and mix with fresh oil-sand, synthetic crude and tiny silt mixture be because density is less, floats on the top of precipitate and separate pond 14 mixed solutions, the tiny silt of synthetic crude, water and part flow into whizzer 15 by the drainage tube on 14 tops, precipitate and separate pond, by the whizzer centrifugation, synthetic crude and silt and moisture from, obtain synthetic crude, synthetic crude is by the synthetic crude entrance of the pyrolysis tower 4 that is delivered to pyrolyzer 3 of oil pump 16, enter pyrolysis tower 4 by this entrance, simultaneously, helium is after being pressurizeed by helium circulator 7, the high temperature gas cooled reactor of flowing through reactor core 1, after 1 heating of high temperature gas cooled reactor reactor core, after the high temperature helium mixes in hot gas mixing section 2, enter in the spiral tube 5 in pyrolysis tower 4, tube wall heat transfer by spiral tube 5 makes the synthetic crude generation pyrolysis in pyrolysis tower 4 become oil gas, oil gas enters separation column 17 by the airway that is positioned at pyrolysis tower 4 tops, in pyrolysis tower 4 after the synthetic crude pyrolysis the remaining dregs of fat discharged by pyrolysis tower 4 bottom slag-drip openings, after oil gas enters separation column 17, obtain the products such as Sweet natural gas, hydrocarbon ils by separation column 17 fractionation, the mixture of a small amount of residual oil and synthetic crude is returned to 4 processing of pyrolysis tower by separation column 17 bottoms outflows again by oil pump 18.
In the present embodiment, the rare gas element helium is 200 ℃～300 ℃ entering the front temperature of high temperature gas cooled reactor reactor core 1, pressure is 1.5MPa～10MPa, after the high temperature gas cooled reactor of flowing through reactor core 1 is pressurized to 600 ℃～800 ℃, flow into pyrolysis tower 4, synthetic crude in pyrolysis tower 4 is heated to 500 ℃～700 ℃ and make it to occur cracking, the direct current spiral tube vapour generator 6 of flowing through again after the first cooling of helium, water in vapour generator 6 is heated to the superheated vapour of 200 ℃～400 ℃, helium is cooled to 200 ℃～300 ℃ after release of heat in vapour generator 6.
Above embodiment only is used for explanation the present invention; and be not limitation of the present invention; the those of ordinary skill in relevant technologies field; without departing from the spirit and scope of the present invention; can also make a variety of changes and modification; therefore all technical schemes that are equal to also belong to category of the present invention, and scope of patent protection of the present invention should be defined by the claims.
Claims (9)
1. a method of utilizing high temperature gas cooled reactor to carry out refining from oil sand, is characterized in that, the described method of utilizing high temperature gas cooled reactor to carry out refining from oil sand comprises three relatively independent flow processs:
The high-temperature heat supply flow process, 200 ℃ ~ 300 ℃ rare gas elementes are after the helium circulator pressurization, the high temperature gas cooled reactor of flowing through reactor core is heated to 600 ℃ ~ 950 ℃, after the vapour generator heat supply, is entered the high temperature gas cooled reactor reactor core after the pressurization of described helium circulator again after being cooled to 200 ℃ ~ 300 ℃;
Steam supply flow path, treated water is heated as superheated vapour or the saturation steam of 200 ~ 400 ℃ in described vapour generator after the water pump pressurization, and then described superheated vapour or saturation steam enter oil-sand separator;
The oil refining flow process, pretreated oil-sand is sent into oil-sand separator and described superheated vapour or saturation steam has an effect, oil-sand medium pitch class material and sand separation also tentatively are cracked into synthetic crude, after synthetic crude class material process whizzer separating-purifying, be heated to 500 ℃ ~ 700 ℃ of top temperatures and be cracked into oil gas and the dregs of fat, oil gas obtains the inflammable gass such as hydrocarbon ils and Sweet natural gas by separation column.
2. the method for utilizing high temperature gas cooled reactor to carry out refining from oil sand as claimed in claim 1, wherein, described rare gas element is helium.
3. the method for utilizing high temperature gas cooled reactor to carry out refining from oil sand as claimed in claim 1 or 2, wherein, in described high-temperature heat supply flow process, described rare gas element after the described high temperature gas cooled reactor reactor core of flowing through heats, enter pyrolyzer and to its heat supply, synthetic petroleum heating after purifying through described whizzer in described pyrolyzer is then from the described rare gas element described vapour generator of inflow of described pyrolyzer outflow and to described vapour generator heat supply.
4. the method for utilizing high temperature gas cooled reactor to carry out refining from oil sand as claimed in claim 1 or 2, wherein, in described high-temperature heat supply flow process, described rare gas element after the described high temperature gas cooled reactor reactor core of flowing through heats, enter interchanger and to its heat supply, then from the rare gas element described vapour generator of inflow of described interchanger outflow and to its heat supply, heated working medium flows into pyrolyzer in described interchanger, and the synthetic petroleum heating after purifying through described whizzer in described pyrolyzer, the working medium that flows out from described pyrolyzer enters described interchanger after the blower fan pressurization.
5. the method for utilizing high temperature gas cooled reactor to carry out refining from oil sand as described in a claim 1-4 any one specific equipment used, is characterized in that, described specific equipment comprises:
Utilize high temperature gas cooled reactor that the high-temperature heat supply system of heat of high temperature is provided, comprise high temperature gas cooled reactor, helium circulator and hot gas mixing section;
Steam supply system is used for utilizing the heat of high temperature that described high-temperature heat supply system provides to produce superheated vapour or saturation steam;
Distillation system comprises the oil-sand separation subsystem that oil-sand is provided with saturation steam be used to the superheated vapour that utilizes described steam supply system to provide; Be used for utilizing heat of high temperature that described high-temperature heat supply system provides to carry out pyrolysis subsystem pyrolysis, that comprise the first pyrolysis tower and the oil gas that is used for described pyrolysis subsystem is obtained carries out fractionation subsystem fractionation, that comprise separation column to the synthetic crude that described oil-sand separation subsystem obtains.
6. the method for utilizing high temperature gas cooled reactor to carry out refining from oil sand as claimed in claim 5 specific equipment used, wherein, described steam supply system comprises direct current spiral tube vapour generator.
7. the method for utilizing high temperature gas cooled reactor to carry out refining from oil sand as claimed in claim 6 specific equipment used, wherein, described oil-sand separation subsystem comprises:
Transfer roller is used for pretreated oil-sand is delivered to the Wet type drum ingress;
Wet type drum has cellular internal surface and is provided with spiral slot;
Air-supply duct is positioned at described Wet type drum center, and is connected with superheated vapour or the saturation steam outlet of described steam supply system, and described air-supply duct tube wall is provided with the duct that sprays for superheated vapour or saturation steam;
The precipitate and separate pond is communicated with the outlet of described Wet type drum by deflector chute, and bottom, described precipitate and separate pond is provided with the pond bottom outlet;
Stirrer is arranged in described precipitate and separate pond;
Whizzer, the drainage tube by being positioned at top, described precipitate and separate pond is communicated with described precipitate and separate pond;
Oil pump connects described whizzer and described the first pyrolysis tower by conduit.
8. the method for utilizing high temperature gas cooled reactor to carry out refining from oil sand as described in claim 5 or 6 specific equipment used, wherein, described oil-sand separation subsystem comprises:
Transfer roller is used for pretreated oil-sand is delivered to the second pyrolysis tower ingress via the first deflector chute;
The second pyrolysis tower, its bottom is provided with the tower bottom outlet;
The second stirrer is arranged in described the second pyrolysis tower;
The helix tube type air-supply duct is arranged in described the second pyrolysis tower, and is connected with superheated vapour or the saturation steam outlet of described steam supply system, and described helix tube type air-supply duct tube wall is provided with the duct for superheated vapour or saturation steam ejection;
The precipitate and separate pond, its bottom is provided with the pond bottom outlet;
Pump is arranged between described the second pyrolysis tower and precipitate and separate pond, connects described the second pyrolysis tower and described precipitate and separate pond by the second deflector chute;
Stirrer is arranged in described precipitate and separate pond;
Whizzer, the drainage tube by being positioned at top, described precipitate and separate pond is communicated with described precipitate and separate pond;
Oil pump connects described whizzer and described the first pyrolysis tower.
9. as claim 5, the 6 or 7 described method of utilizing high temperature gas cooled reactor to carry out refining from oil sand specific equipments used, wherein, described high-temperature heat supply system also comprises interchanger and blower fan, described interchanger is connected with the rare gas element outlet of described high-temperature heat supply system, be connected with described the first pyrolysis tower and supply heat to described the first pyrolysis tower, described blower fan connects described interchanger and described the first pyrolysis tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010115831 CN101775309B (en) | 2010-03-01 | 2010-03-01 | Method for refining from oil sand by using high-temperature gas-cooled reactor and special equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010115831 CN101775309B (en) | 2010-03-01 | 2010-03-01 | Method for refining from oil sand by using high-temperature gas-cooled reactor and special equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101775309A CN101775309A (en) | 2010-07-14 |
| CN101775309B true CN101775309B (en) | 2013-06-05 |
Family
ID=42511897
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201010115831 Active CN101775309B (en) | 2010-03-01 | 2010-03-01 | Method for refining from oil sand by using high-temperature gas-cooled reactor and special equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101775309B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102140359A (en) * | 2011-02-22 | 2011-08-03 | 唐山南光实业有限公司 | Cracking evaporation type oil sand and oil sludge treatment device |
| EP3055383A1 (en) * | 2013-10-11 | 2016-08-17 | Investment for Oily Shale Technologies Co. Ltd. | Use of spent shale or ash obtained from oil shale dismantling methods with or without additives as solid fuel |
| CN104560096B (en) * | 2014-11-23 | 2017-01-11 | 沈阳施博达仪器仪表有限公司 | Continuous separation technology for oil sand |
| CN105602612B (en) * | 2015-10-21 | 2017-05-10 | 清华大学 | Method for hydrofinishing biological crude oil by using high temperature gas cooled reactor |
| CN113522200A (en) * | 2021-08-19 | 2021-10-22 | 华能山东石岛湾核电有限公司 | Remote heating system |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4507195A (en) * | 1983-05-16 | 1985-03-26 | Chevron Research Company | Coking contaminated oil shale or tar sand oil on retorted solid fines |
| CN1266267A (en) * | 2000-04-24 | 2000-09-13 | 清华大学 | High temp gas cooled reactor heat-exchanger equipment |
| CN1773076A (en) * | 2005-11-11 | 2006-05-17 | 河北理工大学 | Oil-sand separator and method for removing sand and sealing |
| CN101358136A (en) * | 2008-10-07 | 2009-02-04 | 中国石油大学(北京) | Method for directly fluid coking oil sand and apparatus |
-
2010
- 2010-03-01 CN CN 201010115831 patent/CN101775309B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4507195A (en) * | 1983-05-16 | 1985-03-26 | Chevron Research Company | Coking contaminated oil shale or tar sand oil on retorted solid fines |
| CN1266267A (en) * | 2000-04-24 | 2000-09-13 | 清华大学 | High temp gas cooled reactor heat-exchanger equipment |
| CN1773076A (en) * | 2005-11-11 | 2006-05-17 | 河北理工大学 | Oil-sand separator and method for removing sand and sealing |
| CN101358136A (en) * | 2008-10-07 | 2009-02-04 | 中国石油大学(北京) | Method for directly fluid coking oil sand and apparatus |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101775309A (en) | 2010-07-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101775309B (en) | Method for refining from oil sand by using high-temperature gas-cooled reactor and special equipment | |
| CN103980948A (en) | Coal powder pyrolysis and gasification method | |
| CN102071042B (en) | Intelligentized continuous quick microwave cracking device for biomass and waste of biomass | |
| CN112412430B (en) | System and method for underground in-situ pyrolysis of coal | |
| CN104152166A (en) | Comprehensive utilization system and process for hydrogen production by gasification of oil shale refining integrated associated coal | |
| CN104593037A (en) | Composite coal hydrogenation oil refining reactor and oil refining method | |
| CN101955803A (en) | Low-rank coal carbonization method | |
| CN111396010B (en) | Clean energy-taking system and method for coal bed gas field | |
| CN113738325B (en) | System for rich oil coal normal position pyrolysis and carbon entrapment coupling | |
| Chen et al. | Simulation analysis of Co-Pyrolysis of oil shale and wheat straw based on the combination of chain reaction kinetics and improved CPD models | |
| CN101338210B (en) | System for preparing hydrocarbon fuel by cracking organics and biomass | |
| CN102304382A (en) | Process for coproducing aromatic oil, asphalt and fuel oil | |
| CN102382671A (en) | Method for separating oil and sludge | |
| CN203938647U (en) | The integrated association hydrogen production from coal gasification of a kind of oil shale oil-refining utilization system | |
| CN102964884B (en) | Hot cracking method process for preparing carbon black by using co-production of tail gas | |
| CN204589076U (en) | The resinous shale utilization system of a kind of coupled gas and solid thermal carriers | |
| CN103666575B (en) | The method of brown coal substep coal slurry gasification | |
| CN103289714A (en) | Dry distiller and oil sand pyrolysis-dry distillation system | |
| CN114790880B (en) | System and method for in-situ pyrolysis of oil-rich coal by steam heat injection | |
| CN102161900A (en) | Device and method for extracting oil from blocky oil shale with high efficiency | |
| CN203319927U (en) | Dry distiller and oil sand pyrolytic dry distillation system | |
| Yefimov | OIL SHALE PROCESSING IN ESTONIA AND RUSSIA V. YEFIMOV | |
| CN108728139A (en) | A kind of pyrolysis of coal nitrogen-free process and system | |
| CN206316130U (en) | The system for handling house refuse | |
| CN202440467U (en) | Self-heating biomass flash pyrolysis liquefying device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |