CN101775309A - 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
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- CN101775309A CN101775309A CN201010115831A CN201010115831A CN101775309A CN 101775309 A CN101775309 A CN 101775309A CN 201010115831 A CN201010115831 A CN 201010115831A CN 201010115831 A CN201010115831 A CN 201010115831A CN 101775309 A CN101775309 A CN 101775309A
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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 processes that: 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 " tar sand ", " Tar sands " again, is a kind of sandstone or other rocks that contains pitch or tar.Normally the mixture of being made up of sand, pitch, tar, mineral substance, clay and water belongs to the non-conventional oil resource.Oil-sand is one of the important source of " artificial petroleum ", oil-sand through exploitation, extraction separation, carry out upgrading, 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 is than horn of plenty, and it is also very extensive to distribute, northwest, the accurate Ge Er basin edge, Chai Xi area, the Caidamu Basin, Sichuan Basin siron door that mainly is distributed in Xinjiang in front of the mountains, ground such as Qinghai, Tibet, the Inner Mongol, Guizhou.According to relevant expert's prediction, the minable oil-sand reserves of China are about about 10,000,000,000 tons, 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, because rolling up of carbonic acid gas isothermal chamber gas emissions causes the global climate rapid deterioration, existent environment of people is caused very big 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 the 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 constitutes 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 the 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 the cleaning oil product and reducing CO2 emissions.
Oil-sand exploitation in the world, processing and utilization at present, the traditional indirect method of main employing extracts through physics, chemical separation process the pitch in the oil-sand earlier from oil-sand, the asphalt oil upgrading is obtained synthetic crude, again synthetic crude is transported to refinery, refines oil.In whole process, need to consume lot of energy, give off a large amount of carbonic acid gas and chemical pollutant simultaneously, 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, as the former is to utilize the pyrogenic method of direct sulfuration bed to carry out oil-sand directly to refine oil, the horizontal destructive distillation rotary kiln of The latter carries out the direct oil refining of oil-sand, and these class methods are compared traditional indirect method all little, suitable commercial run large scale continuous prod of chemical pollution and the lower advantage of direct production cost.But these class methods also have some significant disadvantages, because composition is comparatively complicated, it is comparatively complicated that the process and the product of cracking or chemical reaction directly takes place under high temperature action oil-sand, the impurity that contains in the output oil gas is more, the inflammable gas of cooling back gained is owing to there be can't directly utilizing of a large amount of carbonic acid gas, nitrogen, CO2 emissions is difficult to adapt to the megatrend of current carbon dioxide discharge-reduction much larger than traditional indirect method in the whole process of production simultaneously.
Summary of the invention
(1) technical problem that 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., shortcomings such as the chemical pollution that has overcome traditional indirect method is big, production cost height, and the Carbon emission height of integrated high temperature oil-refining method, product oil or the high shortcoming of gas foreign matter content.
(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 are heated as 200～400 ℃ superheated vapour or saturation steam in described vapour generator after the water pump pressurization, described then superheated vapour or saturation steam enter the 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 separates purification through whizzer, be heated to 500 ℃～700 ℃ of top temperatures and be cracked into the oil gas and the dregs of fat, oil gas obtains inflammable gass such as hydrocarbon ils and Sweet natural gas by separation column.
Preferably, described rare gas element is a 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 will purifying through described whizzer in described pyrolyzer flows into described vapour generator and to described vapour generator heat supply from the effusive described rare gas element of described pyrolyzer then.
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, flow into described vapour generator and to its heat supply from the effusive rare gas element of described interchanger then, heated working medium flows into described pyrolyzer in described interchanger, and the synthetic petroleum heating after will purifying through described whizzer in described pyrolyzer, enters described interchanger from the effusive working medium of described pyrolyzer 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 used specific equipment, 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, the heat of high temperature that is used to utilize described high-temperature heat supply system to provide produces superheated vapour or saturation steam;
Distillation system comprises that the superheated vapour that is used to utilize described steam supply system to provide separates the oil-sand isolated subsystem of oil-sand with saturation steam; Be used for the heat of high temperature that the synthetic crude that described oil-sand isolated subsystem obtains utilizes described high-temperature heat supply system to provide is carried out pyrolytic, comprised the pyrolysis subsystem of the first pyrolysis tower and the oil gas that is used for described pyrolysis subsystem is obtained carries out fractionated, as to comprise separation column fractionation subsystem.
Preferably, described steam supply system comprises direct current spiral tube vapour generator.
Preferably, described oil-sand isolated subsystem comprises:
Transfer roller is used for pretreated oil-sand is delivered to wet type cylinder ingress;
The wet type cylinder has cellular internal surface and is provided with spiral slot;
Air-supply duct is positioned at described wet type centre of the drum, and is connected with the 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 by the outlet of deflector chute with described wet type cylinder, and bottom, described precipitate and separate pond is provided with the pond bottom outlet;
Stirrer is arranged in described precipitate and separate pond;
Whizzer is communicated with described precipitate and separate pond by the drainage tube that is positioned at top, described precipitate and separate pond;
Oil pump connects described whizzer and the described first pyrolysis tower by conduit.
Preferably, described oil-sand isolated subsystem comprises:
Transfer roller is used for pretreated oil-sand is delivered to the second pyrolysis tower ingress via first deflector chute;
The second pyrolysis tower, its bottom is provided with the tower bottom outlet;
Second stirrer is arranged in the described second pyrolysis tower;
The helix tube type air-supply duct is arranged in the described second pyrolysis tower, and is connected with the 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 second pyrolysis tower and the precipitate and separate pond, connects described second pyrolysis tower and described precipitate and separate pond by second deflector chute;
Stirrer is arranged in described precipitate and separate pond;
Whizzer is communicated with described precipitate and separate pond by the drainage tube that is positioned at top, described precipitate and separate pond;
Oil pump connects described whizzer and the described 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 the described first pyrolysis tower and supplies heat to the described first pyrolysis tower, and described blower fan connects described interchanger and the described first pyrolysis tower.
(3) beneficial effect
The present invention compared with prior art exists tangible 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, separate at oil-sand, do not need chemical additive substantially in the upgrading process of bitumen, environmental pollution is less.
(3), because the flow process that adopts oil-sand separation, asphalt modifier, oil refining to carry out has continuously been saved oil-sand, the synthetic crude great amount of cost in transportation.
(4), owing to adopt the method that oil-sand separation, asphalt modifier and two steps of oil refining carry out, avoided 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.
Embodiment 1
Referring to Fig. 1, the device that utilizes high temperature gas cooled reactor to carry out refining from oil sand of 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 cylinder 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.
Transfer roller 9 will be delivered to wet type cylinder 10 ingress through pretreated oil-sand, oil-sand enters into wet type cylinder 10 through inlet, motor 19 by with the gearing of the outside surface of wet type cylinder 10, driving wet type cylinder 10 rotates, because the rotation of wet type cylinder 10, oil-sand are moved to outlet in having spiral fluted wet type cylinder 10 lentamente; 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 high temperature helium of direct current spiral tube vapour generator 6 of being flowed through is heated as superheated vapour, superheated vapour enters into the steam-supply pipe 11 that is positioned at wet type cylinder 10 centers by pipeline after flowing out spiral tube, duct ejection by air-supply duct 11 tube walls, with oil-sand in the wet type cylinder 10 in the effect of cellular wet type drum inner surface, upgrading also takes place and becomes synthetic crude in oil-sand medium pitch class material and sand separation, rotation along with wet type cylinder 10, sand, water, the mixture of synthetic crude and oil-sand is under the spiral fluted effect, outlet to cylinder is the inlet motion in precipitate and separate pond 14, deflector chute 20 along 14 ingress, precipitate and separate pond enters into precipitate and separate pond 14 then, under stirrer 13 stirrings and buoyancy, the higher sandstone of density is deposited on 14 bottoms, precipitate and separate pond, and discharge by the pond bottom outlet, synthetic crude and water, tiny silt mixture floats on the top of precipitate and separate pond 14 mixed solutions because density is less; The tiny silt of synthetic crude, water and part flow in the whizzer 15 by the drainage tube on 14 tops, precipitate and separate pond, and by the centrifugation of whizzer 15, synthetic crude and silt and water sepn obtain synthetic crude; Synthetic crude is delivered to the synthetic crude inlet of the pyrolysis tower 4 of pyrolyzer 3 by oil pump 16, enter pyrolysis tower 4 by this inlet, simultaneously, helium is after being pressurizeed by helium circulator 7, the high temperature gas cooled reactor of flowing through reactor core 1, and 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 the pyrolysis tower 4, tube wall heat transfer by spiral tube 5 makes the synthetic crude generation pyrolysis in the pyrolysis tower 4 become oil gas, oil gas enters separation column 17 by the airway that is positioned at pyrolysis tower 4 tops, in the pyrolysis tower 4 after the synthetic crude pyrolysis the remaining dregs of fat discharge by pyrolysis tower 4 bottom slag-drip openings; After oil gas enters separation column 17, obtain 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 flowed out by separation column 17 bottoms, is returned to 4 processing of pyrolysis tower once more by oil pump 18.
In the present embodiment, rare gas element helium temperature before entering high temperature gas cooled reactor reactor core 1 is 200 ℃～300 ℃, pressure is 1.5MPa～10MPa, be heated to 600 ℃～800 ℃ behind the high temperature gas cooled reactor of the flowing through reactor core 1, flow into pyrolysis tower 4, synthetic crude in the pyrolysis tower 4 is heated to 500 ℃～700 ℃ and make it to take place cracking, the direct current spiral tube vapour generator 6 of flowing through again after the first cooling of helium, water in the vapour generator 6 is heated to 200 ℃～400 ℃ superheated vapour, and helium is cooled to 200 ℃～300 ℃ after the release of heat in vapour generator 6.
Referring to Fig. 2, the device that utilizes high temperature gas cooled reactor to carry out refining from oil sand of 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 cylinder 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.Because helium flow through the high temperature gas cooled reactor reactor core, might have radioactive substance in the helium, for the safe class of 3 pairs of radioactive substances of pyrolyzer, present embodiment is compared with embodiment 1, has increased interchanger 21 and blower fan 22.
Transfer roller 9 will be delivered to wet type cylinder 10 ingress through pretreated oil-sand, oil-sand enters into wet type cylinder 10 through inlet, motor 19 by with the gearing of the outside surface of wet type cylinder 10, driving wet type cylinder 10 rotates, because the rotation of wet type cylinder 10, oil-sand has in the spiral fluted wet type cylinder 10 slowly to the outlet motion at internal surface; 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 to be superheated vapour, superheated vapour enters into the steam-supply pipe 11 that is positioned at wet type cylinder 10 centers by pipeline after flowing out spiral tube, duct ejection by air-supply duct 11 tube walls, with oil-sand in the wet type cylinder 10 in cellular internal surface effect, upgrading also takes place and becomes synthetic crude in oil-sand medium pitch class material and sand separation, rotation along with wet type cylinder 10, sand, water, the mixture of synthetic crude and oil-sand is under the spiral fluted effect, outlet to wet type cylinder 10 is the inlet motion in precipitate and separate pond 14, deflector chute 20 along 14 ingress, precipitate and separate pond enters into precipitate and separate pond 14 then, under stirrer 13 stirrings and buoyancy, the higher sandstone of density is deposited on 14 bottoms, precipitate and separate pond, and discharge by the outlet at the bottom of the pond, synthetic crude and water, the mixture of tiny silt floats on the top of the mixed solution in the precipitate and separate pond 14 because density is less; The tiny silt of synthetic crude, water and part flow into whizzer 15 by the drainage tube on 14 tops, precipitate and separate pond, and by the whizzer centrifugation, synthetic crude and silt and water sepn obtain synthetic crude; Synthetic crude is delivered to the synthetic crude inlet of the pyrolysis tower 4 in the pyrolyzer 3 by oil pump 16, enter pyrolysis tower 4 by this inlet, 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 into heat exchanger 21, heat is passed to the nitrogen of heat exchanger 21 opposite sides, nitrogen is under the driving of blower fan 22, enter the spiral tube 5 in the pyrolysis tower 4, tube wall by spiral tube 5 conducts heat and makes the synthetic crude generation pyrolysis in the pyrolysis tower 4 become oil gas, and oil gas enters separation column 17 by the airway that is positioned at pyrolysis tower 4 tops, in the pyrolysis tower 4 after the synthetic crude pyrolysis the remaining dregs of fat discharge by pyrolysis tower bottom slag-drip opening; After oil gas enters separation column 17, obtain 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 flowed out by separation column 17 bottoms, is returned to 4 processing of pyrolysis tower once more by oil pump 18.
In the present embodiment, rare gas element helium temperature before entering high temperature gas cooled reactor reactor core 1 is 200 ℃～300 ℃, pressure is 1.5MPa～10MPa, be pressurized to 700 ℃～950 ℃ behind the high temperature gas cooled reactor of the flowing through reactor core 1, the heat exchanger 21 of flowing through, nitrogen in the heat exchanger 21 is heated to be 600 ℃～800 ℃, and the nitrogen gas stream after the heating is through pyrolysis tower 4, and the synthetic crude in the pyrolysis tower 4 is heated to 500 ℃～700 ℃ and cracking takes place; The helium flow vapour generator 6 of flowing through again after the first cooling through heat exchanger 21 is heated to 200 ℃～400 ℃ superheated vapour with the water of vapour generator 6 water sides, and helium is cooled to 200 ℃～300 ℃ after the 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 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, first stirrer 13, precipitate and separate pond 14, whizzer 15, oil pump 16, separation column 17, oil pump 18, first deflector chute 19, second deflector chute 20, second stirrer 32, pump 33.
Transfer roller 9 will be delivered to the second pyrolysis tower, 30 ingress through pretreated oil-sand, and oil-sand enters into the second pyrolysis tower 30 through 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 flows out direct current spiral tube vapour generator 6 backs and enters into the helix tube type air-supply duct 31 that is arranged in the second pyrolysis tower 30 by pipeline, 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 takes place and becomes synthetic crude in oil-sand medium pitch class material and sand separation, the higher sandstone of density is deposited on the second pyrolysis tower, 30 bottoms, and discharge 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 second stirrer 32, under the effect of pump 33, by the inlet motion of outlet conduit to precipitate and separate pond 14; The mixture of synthetic crude, part sand, water and oil-sand enters into precipitate and separate pond 14 along second deflector chute 20 of 14 ingress, precipitate and separate pond, under stirrer 13 stirrings and buoyancy, 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 float on the top of precipitate and separate pond 14 mixed solutions because density is less; The tiny silt of synthetic crude, water and part flow into whizzer 15 by the drainage tube on 14 tops, precipitate and separate pond, and by the whizzer centrifugation, synthetic crude and silt and water sepn obtain synthetic crude; Synthetic crude is by the synthetic crude inlet of the pyrolysis tower 4 that is delivered to pyrolyzer 3 of oil pump 16, enter pyrolysis tower 4 by this inlet, 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 the pyrolysis tower 4, tube wall heat transfer by spiral tube 5 makes the synthetic crude generation pyrolysis in the pyrolysis tower 4 become oil gas, oil gas enters separation column 17 by the airway that is positioned at pyrolysis tower 4 tops, in the pyrolysis tower 4 after the synthetic crude pyrolysis the remaining dregs of fat discharge by pyrolysis tower 4 bottom slag-drip openings; After oil gas enters separation column 17, obtain 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 flowed out by separation column 17 bottoms, is returned to 4 processing of pyrolysis tower once more by oil pump 18.
In the present embodiment, rare gas element helium temperature before entering high temperature gas cooled reactor reactor core 1 is 200 ℃～300 ℃, 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 the pyrolysis tower 4 is heated to 500 ℃～700 ℃ and make it to take place cracking, the direct current spiral tube vapour generator 6 of flowing through again after the first cooling of helium, water in the vapour generator 6 is heated to 200 ℃～400 ℃ superheated vapour, and helium is cooled to 200 ℃～300 ℃ after the release of heat in vapour generator 6.
Above embodiment only is used to illustrate the present invention; and be not limitation of the present invention; the those of ordinary skill in relevant technologies field; under the situation that does not break away from the spirit and scope of the present invention; can also make various variations 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 are heated as 200～400 ℃ superheated vapour or saturation steam in described vapour generator after the water pump pressurization, described then superheated vapour or saturation steam enter the 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 separates purification through whizzer, be heated to 500 ℃～700 ℃ of top temperatures and be cracked into the oil gas and the dregs of fat, oil gas obtains 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 a 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 described pyrolyzer and to its heat supply, synthetic petroleum heating after will purifying through described whizzer in described pyrolyzer flows into described vapour generator and to described vapour generator heat supply from the effusive described rare gas element of described pyrolyzer then.
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, flow into described vapour generator and to its heat supply from the effusive rare gas element of described interchanger then, heated working medium flows into described pyrolyzer in described interchanger, and the synthetic petroleum heating after in described pyrolyzer, will purifying through described whizzer, after the blower fan pressurization, enter described interchanger from the effusive working medium of described pyrolyzer.
5. the specific equipment that the method for utilizing high temperature gas cooled reactor to carry out refining from oil sand is 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, the heat of high temperature that is used to utilize described high-temperature heat supply system to provide produces superheated vapour or saturation steam;
Distillation system comprises that the superheated vapour that is used to utilize described steam supply system to provide separates the oil-sand isolated subsystem of oil-sand with saturation steam; Be used for the heat of high temperature that the synthetic crude that described oil-sand isolated subsystem obtains utilizes described high-temperature heat supply system to provide is carried out pyrolytic, comprised the pyrolysis subsystem of the first pyrolysis tower and the oil gas that is used for described pyrolysis subsystem is obtained carries out fractionated, as to comprise separation column fractionation subsystem.
6. the used specific equipment of the method for utilizing high temperature gas cooled reactor to carry out refining from oil sand as claimed in claim 5, wherein, described steam supply system comprises direct current spiral tube vapour generator.
7. the used specific equipment of the method for utilizing high temperature gas cooled reactor to carry out refining from oil sand as claimed in claim 6, wherein, described oil-sand isolated subsystem comprises:
Transfer roller is used for pretreated oil-sand is delivered to wet type cylinder ingress;
The wet type cylinder has cellular internal surface and is provided with spiral slot;
Air-supply duct is positioned at described wet type centre of the drum, and is connected with the 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 by the outlet of deflector chute with described wet type cylinder, and bottom, described precipitate and separate pond is provided with the pond bottom outlet;
Stirrer is arranged in described precipitate and separate pond;
Whizzer is communicated with described precipitate and separate pond by the drainage tube that is positioned at top, described precipitate and separate pond;
Oil pump connects described whizzer and the described first pyrolysis tower by conduit.
8. as claim 5 or the used specific equipment of the 6 described methods of utilizing high temperature gas cooled reactor to carry out refining from oil sand, wherein, described oil-sand isolated subsystem comprises:
Transfer roller is used for pretreated oil-sand is delivered to the second pyrolysis tower ingress via first deflector chute;
The second pyrolysis tower, its bottom is provided with the tower bottom outlet;
Second stirrer is arranged in the described second pyrolysis tower;
The helix tube type air-supply duct is arranged in the described second pyrolysis tower, and is connected with the 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 second pyrolysis tower and the precipitate and separate pond, connects described second pyrolysis tower and described precipitate and separate pond by second deflector chute;
Stirrer is arranged in described precipitate and separate pond;
Whizzer is communicated with described precipitate and separate pond by the drainage tube that is positioned at top, described precipitate and separate pond;
Oil pump connects described whizzer and the described first pyrolysis tower.
9. as claim 5, the used specific equipment of the 6 or 7 described methods of utilizing high temperature gas cooled reactor to carry out refining from oil sand, 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 the described first pyrolysis tower and to described first pyrolysis tower supply heat, described blower fan connects described interchanger and the described first pyrolysis tower.
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| 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 |
| CN104560096A (en) * | 2014-11-23 | 2015-04-29 | 沈阳施博达仪器仪表有限公司 | Continuous separation technology for oil sand |
| CN105602612A (en) * | 2015-10-21 | 2016-05-25 | 清华大学 | Method for hydrofinishing biological crude oil by using high temperature gas cooled reactor |
| CN105765051A (en) * | 2013-10-11 | 2016-07-13 | 油页岩技术投资有限公司 | High range temperature thermal dismantling method in processing oil shale |
| CN113522200A (en) * | 2021-08-19 | 2021-10-22 | 华能山东石岛湾核电有限公司 | Remote heating system |
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| 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 |
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| CN104560096A (en) * | 2014-11-23 | 2015-04-29 | 沈阳施博达仪器仪表有限公司 | Continuous separation technology for oil sand |
| 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 |
| CN105602612A (en) * | 2015-10-21 | 2016-05-25 | 清华大学 | Method for hydrofinishing biological crude oil by using high temperature gas cooled reactor |
| 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 |
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