CN102031135A - Comprehensive processing and utilizing method for heavy oil - Google Patents
Comprehensive processing and utilizing method for heavy oil Download PDFInfo
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Abstract
The invention belongs to the field of petroleum processing and utilization, and relates to a comprehensive processing and utilizing method for heavy oil. By integrating quick cracking of the heavy oil, pre-combustion and gasification of the generated coke, recycling of non-converted heavy oil, hydrogen production by synthetic gas generated through gasification, and a hydrofining process for cracked oil products, light oil can be prepared from the heavy oil to the greatest degree, the light oil is hydrogenated to form high-quality clean oil products, and also can generate the synthetic gas through gasification, and the synthetic gas can serve as a hydrogen production raw material to provide a cheap hydrogen source for oil product hydrofining, and also can serve as fuel gas to provide clean fuel for a refinery. The invention provides a low-cost comprehensive processing and utilizing method for converting the heavy oil into clean light oil products to the greatest degree.
Description
Technical field
The invention belongs to refining of petroleum and utilize the field, relate to a kind of heavy oil comprehensive processing and utilization method.Specifically, the present invention with the quick cracking of heavy oil, the synthetic gas hydrogen manufacturing and the cracking oil product hydrofining technology of the coke precombustion that produces and gasification, unconverted mink cell focus freshening, gasification generation carry out organic assembling, make heavy oil can not only obtain light oil to greatest extent, can obtain high-quality cleaning oil product behind the light oil hydrogenation, can also produce synthetic gas by gasification, synthetic gas can be used as hydrogen feedstock and provides cheap hydrogen source for oil hydrogenation is refining, also can be used as fuel gas and provides clean fuel for refinery etc.The present invention is the comprehensive processing and utilization method that a kind of low cost is converted into heavy oil the cleaning light oil products to greatest extent.
Background technology
Heavy along with the continuous change of crude oil, become bad, be in a high position and continue under the soaring situation in the international petroleum price, increasing inferior heavy oil need comprehensive processing and utilization.The comprehensive processing and utilization of heavy (slag) oil has become petroleum chemical industry and has constantly pursued improvement and perfect gordian technique.
Traditional heavy oil upgrading method mainly contains two classes: decarburization and hydrogenation all are to realize the lighting of heavy oil with the carbon methods many, the few characteristics of hydrogen that change heavy oil.Classical decarbonization process mainly contains: delayed coking, heavy oil fluid catalytic cracking; Hydrogenation technique has: heavy oil hydrodesulfurization (upgrading), heavy-oil hydrogenation cracking.All also there is certain problem in these traditional technologies when the processing inferior heavy oil.Heavy oil fluid catalytic cracking is a highly effective heavy oil upgrading technology, for world refining industry has been made huge contribution, but raw material properties is had strict restriction, as carbon residue ≯ 12%, heavy metal ≯ 20ppm etc., can't process increasing inferior heavy oil; Delay coking process is in crude oil price but its coking yield is too high and lacks economy under the elevated situation to raw material almost without limits, and sulfur-bearing oil Jiao of one of its main products also is not the purpose product; Heavy-oil hydrogenation cracked product all is ideal purpose products, but its equipment costliness is hung back a lot of users, and another problem is that it needs a large amount of hydrogen simultaneously, inevitable problem when how these hydrogen obtain also to become heavy-oil hydrogenation cracking application.Heavy oil hydrodesulfurization (upgrading) can be produced the low-sulfur liquid fuel oil of cleaning or supply raw materials for heavy oil fluid catalytic cracking, but raw material properties is also had certain restriction, as heavy metal ≯ 120ppm etc., also exists equipment costliness and hydrogen to come source problem simultaneously.The past people also once made up above-mentioned technology, or make up in methods such as being aided with solvent deasphalting, thermally splitting, the generating of CFB boiler, the gasification of the burnt slurry of water, but or because of long flow path, investment height, or because of pyroelectric with, produce and not match etc., all be difficult to ideally extensively the increasing inferior heavy oil of reply and carry out comprehensive processing and utilization.
The burnt slurry gasification of the delayed coking that more generally adopt in current large-scale petroleum chemical plant--CFB boiler cogeneration combination process and delayed coking-water Poly-generation combination process etc., all make inferior heavy oil obtain comprehensive processing and utilization, but because of refinery coke must be through cooling, processing, the process that heats up again, cause energy consumption higher, flow process is longer, and the lighting transformation efficiency of heavy oil feedstock is also lower.
Therefore, the comprehensive processing and utilization method that a kind of low cost is converted into heavy oil the cleaning light-end products to greatest extent need be developed in this area.
Summary of the invention
The invention provides a kind of new heavy oil comprehensive processing and utilization method, by the quick cracking of heavy oil, the synthetic gas hydrogen manufacturing and the cracking light-end products hydrofining technology of the coke precombustion that produces and gasification, unconverted mink cell focus freshening, gasification generation carry out organic assembling, heavy oil is converted into the cleaning light oil products to greatest extent.
On the one hand, the invention provides a kind of heavy oil comprehensive processing and utilization method, this method may further comprise the steps:
(A) heavy oil enters cracking reactor and gives birth to scission reaction with the carrier hybrid concurrency of making charcoal in advance from the high temperature of the device of making charcoal in advance, and wherein, the operational condition of described cracking reactor is: pressure (gauge pressure) is 0～1.0MPa, and temperature is 450～680 ℃;
(B) reaction product is isolated oil gas and is with burnt carrier after entering settling vessel, oil gas is isolated through the settling vessel gas-solid separator and is with that burnt carrier powder is laggard goes into separation column, be with burnt carrier from the settling vessel bottom to making charcoal device in advance, wherein, the operational condition of described settling vessel is: pressure (gauge pressure) is 0～1.0MPa, and temperature is 440～670 ℃;
The oil gas that settling vessel comes out enters separation column and is separated into gas, lightweight oil, middle matter oil and mink cell focus;
The burnt carrier of the band that settling vessel comes out to the device of making charcoal is in advance made charcoal, after making charcoal in advance, part is with burnt carrier heat-carrying to return the cracking reactor heat supply, after making charcoal in advance, all the other are with burnt carrier to enter gasifier, wherein, the described device operational condition of making charcoal in advance is: pressure (gauge pressure) is 0～1.0MPa, temperature is 560～900 ℃, and excess oxygen concentration is 0～5 volume %;
(C) enter on the back carrier of making charcoal in advance of gasifier coke and steam and/or oxygen-containing gas and carry out gasification reaction generation synthetic gas, wherein, the operational condition of described gasifier is: pressure (gauge pressure) is 0～1.0MPa, and temperature is 600～1150 ℃, and excessive water concentration is 0～25 volume %; And
(D) carrier after the gasification returns in the device of making charcoal in advance and circulates.
One preferred embodiment in, the cracking reactor that the mink cell focus that separation column in the step (B) is fractionated out returns in the described step (A) is proceeded scission reaction.
Another preferred embodiment in, the lightweight oil that separation column in the step (B) is fractionated out obtains petroleum naphtha and oil fuel product to the hydrogenation unit hydrogenation, partial synthesis gas goes device for producing hydrogen to produce the needs that hydrogen satisfies hydrogenation unit.
Another preferred embodiment in, middle matter oil to the hydrogenation unit hydrogenation that separation column in the step (B) is fractionated out obtains the cleaning oil product, partial synthesis gas goes device for producing hydrogen to produce the needs that hydrogen satisfies hydrogenation unit.
Another preferred embodiment in, in described step (A), the carrier main chemical compositions is a silico-aluminate, specific surface 5～1000m
2/ g, pore volume 0.03～1.0ml/g, particle diameter are 20～1000 μ m.
Another preferred embodiment in, in described step (B), described cracking reactor inside is provided with the back-mixing structure of band shunting, baffling function.
Another preferred embodiment in, in described step (A), the scission reaction time is 1～100 second; In described step (B), the time of making charcoal is 2～100 minutes in advance; In described step (C), the gasification time is 2～80 minutes.
Another preferred embodiment in, in described step (C), gasifier is stopped using, and is with burnt carrier all to return cracking reactor after entering the making charcoal in advance of gasifier; When gasifier was stopped using, hydrogen feedstock adopted dry gas, Sweet natural gas or other raw material.
On the other hand, the invention provides a kind of device that is used for heavy oil comprehensive processing and utilization (especially above-mentioned heavy oil comprehensive processing and utilization method), this device comprises:
Be used for the cracked cracking reactor;
The settling vessel that is connected with described cracking reactor, be used to load cleavage reaction product, the device of making charcoal in advance that is connected with described settling vessel, be used for fractionated separation column and be used to make charcoal;
Be used to carry out the gasifier of gasification reaction.
Description of drawings
Fig. 1 is the heavy oil comprehensive processing and utilization set technique schematic flow sheet according to an embodiment of the invention.
Embodiment
The present inventor finds after having passed through extensive and deep research, by with the quick cracking of heavy oil, the synthetic gas hydrogen manufacturing and the cracking oil product hydrofining technology of the coke precombustion that produces and gasification, unconverted mink cell focus freshening, gasification generation carry out organic assembling, make heavy oil can not only obtain light oil to greatest extent, can obtain high-quality cleaning oil product behind the light oil hydrogenation, can also produce synthetic gas by gasification, synthetic gas can be used as hydrogen feedstock and provides cheap hydrogen source for oil hydrogenation is refining, also can be used as fuel gas and provides clean fuel for the refinery.Based on above-mentioned discovery, the present invention is accomplished.
In a first aspect of the present invention, a kind of heavy oil comprehensive processing and utilization set technique is provided, it may further comprise the steps: heavy oil enters cracking reactor to be mixed with the carrier of making charcoal in advance from the high temperature of the device of making charcoal in advance, and enters cracking reactor and carry out scission reaction by promoting dry gas; Cleavage reaction product enters settling vessel to be separated, and oil gas advances light, middle matter oil that separation column fractionates out and obtains the high-quality oil product to oil hydrogenation after refining, and the mink cell focus that fractionates out returns cracking reactor and proceeds scission reaction; Be with burnt carrier behind stripping, to deliver to make charcoal in advance device to make charcoal; Be with a burnt carrier part to return cracking reactor after making charcoal in advance anti-use heat is provided, all the other enter gasifier, gasification generates synthetic gas under the condition of water vapor and/or oxygen-containing gas, and synthetic gas obtains the required hydrogen of oil hydrogenation device behind device for producing hydrogen, and unnecessary synthetic gas is as product; Make charcoal in advance high-temperature flue gas that device and gasifier top discharge through the waste heat recovery facility produce steam satisfying personal after, directly outer defeated or generating is outer defeated.
Preferably, heavy oil comprehensive processing and utilization method of the present invention may further comprise the steps:
(A) heavy oil enters cracking reactor and gives birth to scission reaction with the carrier hybrid concurrency of making charcoal in advance from the high temperature of the device of making charcoal in advance, and wherein, the operational condition of described cracking reactor is: pressure (gauge pressure) is 0～1.0MPa, and temperature is 450～680 ℃.Scission reaction institute heat requirement is provided by the thermal zone burnt carrier from the device of making charcoal in advance, by the heat transfer between thermal zone burnt carrier and the cold raw material, realizes a more uniform temperature of reaction in cracking reactor, makes scission reaction reach the highest light oil productive rate;
(B) reaction product is isolated oil gas and is with burnt carrier after entering settling vessel, oil gas is isolated through the settling vessel gas-solid separator and is with that burnt carrier powder is laggard goes into separation column, be with burnt carrier from the settling vessel bottom to making charcoal device in advance, wherein, the operational condition of described settling vessel is: pressure (gauge pressure) is 0～1.0MPa, and temperature is 440～670 ℃.The purpose of settling vessel is to realize separating of oil gas and the burnt carrier of solid band, in the oil gas uphill process, gas-solid separator is set to be forced to separate to the solid particulate in the oil gas and has significantly reduced the solids content in the oil gas, help the long-term stability operation of follow-up separation column, in solid semicoke decline process, can inject the small amount of steam stripping and remove most of oil gas that the burnt carrier of solid band is carried secretly;
The oil gas that settling vessel comes out enters separation column and is separated into gas, lightweight oil, middle matter oil and mink cell focus;
The burnt carrier of the band that settling vessel comes out to the device of making charcoal is in advance made charcoal, after making charcoal in advance, part is with burnt carrier heat-carrying to return the cracking reactor heat supply, after making charcoal in advance, all the other are with burnt carrier to enter gasifier, wherein, the described device operational condition of making charcoal in advance is: pressure (gauge pressure) is 0～1.0MPa, temperature is 560～900 ℃, and excess oxygen concentration is 0～5 volume %.The device of making charcoal in advance on the one hand provides heat by making charcoal in advance for cracking reactor, also be to enter the pre-treatment before gasifier carries out gasification reaction with burnt carrier on the other hand, with burnt carrier by burning at the device of making charcoal in advance, reduced foreign matter contents such as the sulphur that enters in the gasifier, nitrogen, the synthetic gas of producing in the gasifier will more be cleaned;
(C) enter on the back carrier of making charcoal in advance of gasifier coke and steam and/or oxygen-containing gas and carry out gasification reaction generation synthetic gas, wherein, the operational condition of described gasifier is: pressure (gauge pressure) is 0～1.0MPa, and temperature is 600～1150 ℃, and excessive water concentration is 0～25 volume %; Gasification reaction is the carbon on the carrier and the reaction of steam and/or oxygen-containing gas, and steam is from device and the gasifier waste heat recovery facility institute producing steam of making charcoal in advance, and oxygen-containing gas can be an air, it also can be pure oxygen, oxygen purity is high more, and the synthetic gas foreign matter content is low more, and the synthetic gas calorific value is high more;
(D) carrier after the gasification returns in the device of making charcoal in advance and circulates, and the existence of carrier has realized the fluidisation function of system on the one hand in the system, plays the effect that appendix coke and heat transmit on the other hand.
In described step (B), the mink cell focus that separation column fractionates out returns cracking reactor and proceeds scission reaction, and the mink cell focus freshening can significantly improve the productive rate of lightweight oil.For this part mink cell focus, as little, therefore, return the further cracking of cracking reactor and generate light-end products as end-use, solved the purposes problem of mink cell focus on the one hand, improved clean or white on the other hand again, reach the effect of killing two birds with one stone;
In described step (B), the lightweight oil that separation column fractionates out to hydrogenation unit hydrogenation obtains petroleum naphtha and oil fuel product, the middle matter oil that separation column fractionates out to hydrogenation unit hydrogenation obtains cleaning product, partial synthesis gas goes device for producing hydrogen to produce the needs that hydrogen satisfies hydrogenation unit, and unnecessary synthetic gas is as product.
In described step (A), the scission reaction time is preferably 1～100 second, and the best is 3～30 seconds; In described step (B), the time of making charcoal is preferably 5～100 minutes in advance, and the best is 20～60 minutes; In described step (C), the gasification time is preferably 2～80 minutes, and the best is 20～50 minutes.
Below referring to accompanying drawing.
As shown in Figure 1, heavy oil 1 enters the cracking reactor 15 and carrier 38 hybrid reactions of making charcoal in advance from the high temperature of the device 37 of making charcoal in advance, the carrier 38 of making charcoal in advance promotes by promoting gas 31, simultaneously, freshening heavy oil 22 also enters and carries out quick scission reaction in the cracking reactor 15, cleavage reaction product enters settling vessel 16 and carries out gas solid separation, and the burnt carrier 17 of band that removes the oil gas of carrying secretly through steam 7 strippings is discharged in the bottom, and cracking oil gas 18 enters separation column 19 bottoms after isolating most of solid powder/particle through settling vessel 16;
Heavy oil is through transferpump 20 with after taking off solid device 21 at the bottom of separation column 19 towers, and freshening heavy oil 22 returns the 15 further cracking of dry distillation reactor device, and circulation heavy oil 23 returns tower weight oil 25 and returns separation column 19 through behind the interchanger 24 at the bottom of the tower, and part heavy oil is as heavy oil product 26; Enter return tank 29 after 28 condensations of fractionation cat head oil gas 27 process overhead condensers and carry out gas, oil, water three phase separation; Isolated gas phase further is separated into dry gas and liquefied gas through compressor 30 compression backs as gas products 32, and circulation gas is as promoting gas 31; Isolated oil phase is through trim the top of column pump 33, and part is a trim the top of column 34, and all the other are lightweight oil 35, and isolated sewage 48 send sewage treatment facility; Obtain naphtha product 45 and oil fuel product 46 behind lightweight oil 35 that separation column 19 is extracted out and 36 to the hydrogenation unit 11-1 hydrogenation; The middle matter oil 39 that separation column 19 is extracted out obtains wax oil product 47 to hydrogenation unit 11-2 hydrogenation.
Settling vessel 16 bottoms are discharged and to be with burnt carrier 17 to be delivered to the reaction of making charcoal of make charcoal in advance device 37 and air 2 by air 2, and 8 pairs of processes of making charcoal of oxygen-containing gas are carried out temperature regulation; Carrier 38 parts were returned cracking reactor after the high temperature that discharge the bottom was made charcoal in advance, and scission reaction institute heat requirement is provided, and all the other enter gasifier 42; The high-temperature flue gas 40 that the device top produces of making charcoal in advance carries out desulfurization as required and handles the back discharging behind waste heat recovery facility 4;
The back carrier 41 of making charcoal in advance is delivered to gasifier 42 by steam 7 and carries out gasification reaction with the steam 7 and the oxygen-containing gas 8 that feed, the synthetic gas 44 of gasifier top output is sent into the hydrogen feedstock of device for producing hydrogen 9 as the high-quality cheapness behind waste heat recovery facility 5, the hydrogen 10 of output provides hydrogen source for hydrogenation unit 11-1 and 11-2, and unnecessary is synthetic gas product 6; Gasification back carrier 43 recycles by carrying air 2 to be back to the device 37 of making charcoal in advance.
As required, the device 37 of making charcoal in advance in the operational process is interrupted discharges useless carrier 13, and gasifier 42 interruptions are discharged useless carrier 12, are interrupted and discharge when giving up carrier, replenish fresh carrier 3 to the device 37 of making charcoal in advance.
Major advantage of the present invention is:
1, the present invention has realized that the quick cracking of heavy oil improves light oil productive rate, institute's coke precombustion that produces and the production synthetic gas that gasifies, unconverted mink cell focus freshening further improve the light oil productive rate.
2, make charcoal in advance among the present invention and be with burnt carrier to enter gasifier to carry out gasification reaction, the synthetic gas that can obtain to clean provides hydrogen source as the hydrogen feedstock of high-quality cheapness for oil hydrogenation or as clean fuel gas product, the cost of institute's hydrogen producing descends 50% than conventional hydrogen manufacturing.
3, the present invention compares with heavy-oil hydrogenation cracking technology, have investment low, do not need the external hydrogen outside advantage of hydrogen supply also simultaneously.
4, the present invention compares with heavy oil hydrodesulfurization-heavy oil fluid catalytic cracking combination process, has that adaptability to raw material is strong, diesel and gasoline ratio is high, the measured advantage of diesel product matter, helps satisfying the growth of future market to the diesel oil demand.
5, the present invention and delayed coking-CFB boiler pneumoelectric coproduction combination process, the burnt slurry gasification Poly-generation combination process of delayed coking-water or solvent deasphalting-asphalt gasification Poly-generation combination process are compared, light oil productive rate height, advantage such as thermosteresis is little, oxygen consumption is low, flow process is short, investment is low.
6, the present invention has flexibility of operation preferably, can adjust the freshening amount and the quantum of output of intermediate oil flexibly according to the configuration of refinery or the needs of production decision, and it is moved between maximum light oil productive rate and maximum upgrading liquid yield.
7, application of the present invention can make the more environmental protection of full factory.When processing sulfur-bearing oil, only need adopt appropriate means to carry out desulfurization to the flue gas of making charcoal, sulphur whole in the raw material then can both be easy to controlled.Especially for the heavier refinery of crude oil, heavy oil uses the cleaning synthetic gas of this technology institute output to use for full factory more for a long time, and all process furnace no longer include environmental issue, also no longer need to consider to blow ash and sulfur corrosion problem.
8, the present invention will make refinery can tackle the processing of all kinds crude oil in the application of refinery, products scheme is more flexible, tooling cost is lower and the investment still less.
Further set forth the present invention below in conjunction with specific embodiment.But, should be understood that these embodiment only are used to the present invention is described and do not constitute limitation of the scope of the invention.The test method of unreceipted actual conditions in the following example, usually according to normal condition, or the condition of advising according to manufacturer.
Embodiment
Present embodiment is 500,000 tons of/year heavy oil comprehensive utilization processing unit (plant)s building in certain refinery, and handling heavy oil is the oil long residuum.
Feedstock property:
The main character of oil long residuum sees Table 1 respectively.
Table 1 heavy oil main character
| Project | Unit | Numerical value | Remarks |
| Relative density | d 4 20 | 0.923 | |
| Carbon residue | Weight % | 13.0 | Conradson carbon residue |
| Viscosity | Centistokes(cst), 100 ℃ | 2580 | |
| S content | Weight % | 1.5 |
| N content | Weight % | 0.43 | |
| Ni | ppm | 36 | |
| V | ppm | 14 |
Main operational condition:
The operational condition of cracking reactor is: pressure is 0.12MPa (G), and temperature is 490～500 ℃;
The operational condition of settling vessel is: pressure is 0.1MPa (G), and temperature is 480～490 ℃;
The operational condition of device of making charcoal in advance is: pressure is 0.1MPa (G), and temperature is 690～710 ℃, and excess oxygen concentration is 0.5 volume %;
The operational condition of gasifier is: pressure is 0.1MPa (G), and temperature is 700～750 ℃, and excessive water concentration is 8.0 volume %;
Product distributes and product main character or composition:
The product distribution situation sees Table 2.
Table 2 product distributes
Petroleum naphtha is in harmonious proportion component as gasoline, and oil fuel is as the derv fuel oil product, and wax oil is as fine quality catalytic cracking raw material, and synthetic gas and dry gas are as clean fuel, and liquefied gas is as product, and steam supplies outward as product.
Table 3 petroleum naphtha main character
| Project | Data |
| Relative density, d 4 20 | 0.745 |
| Sulphur content, ppm | 33.0 |
| Boiling range, ℃ | |
| IP/10％ | 96/107 |
| 30％/50％ | 114/124 |
| 70％/90％ | 139/157 |
| 95％/EP | 168/188 |
Table 4 oil fuel main character
| Project | Data |
| Relative density, d 4 20 | 0.854 |
| Sulphur content, |
46 |
| Cetane value | 49 |
| Boiling range, ℃ | |
| IP/10％ | 194/208 |
| 30％/50％ | 229/248 |
| 70％/90％ | 274/322 |
| 95％/EP | 344/365 |
Table 5 wax oil main character
| Project | Data |
| Relative density, d 4 20 | 0.904 |
| Condensation point, |
27 |
| Boiling range, ℃ | |
| IP/10％ | 340/383 |
| 30％/50％ | 417/444 |
| 70％/90％ | 477/500 |
| 95％/EP | 515/525 |
Table 6 synthetic gas is mainly formed
| Component (volume %) | Data |
| Carbon monoxide | 25.0 |
| Carbonic acid gas | 10.0 |
| Hydrogen | 53.0 |
| Water | 10.5 |
| Methane | 1.5 |
Table 7 dry gas is mainly formed
| Component (volume %) | Data |
| Hydrogen | 16.55 |
| Methane | 46.07 |
| Ethane | 14.85 |
| Propane | 1.78 |
| Nitrogen | 14.36 |
| Hydrogen sulfide | 0.65 |
Table 8 liquefied gas is mainly formed
| Component (volume %) | Data |
| Propane | 43.89 |
| Propylene | 18.30 |
| Ethane | 18.30 |
| Ethene | 15.64 |
All quote in this application as a reference at all documents that the present invention mentions, just quoted as a reference separately as each piece document.Should be understood that in addition those skilled in the art can make various changes or modifications the present invention after having read above-mentioned teachings of the present invention, these equivalent form of values fall within the application's appended claims institute restricted portion equally.
Claims (8)
1. heavy oil comprehensive processing and utilization method, this method may further comprise the steps:
(A) heavy oil enters cracking reactor and gives birth to scission reaction with the carrier hybrid concurrency of making charcoal in advance from the high temperature of the device of making charcoal in advance, obtains cleavage reaction product, and wherein, the operational condition of described cracking reactor is: pressure is 0～1.0MPa gauge pressure, and temperature is 450～680 ℃;
(B) described cleavage reaction product is isolated oil gas and is with burnt carrier after entering settling vessel, oil gas is isolated through the settling vessel gas-solid separator and is with that burnt carrier powder is laggard goes into separation column, be with burnt carrier from the settling vessel bottom to making charcoal device in advance, wherein, the operational condition of described settling vessel is: pressure is 0～1.0MPa gauge pressure, and temperature is 440～670 ℃;
The described oil gas that settling vessel comes out enters separation column and is separated into gas, lightweight oil, middle matter oil and mink cell focus;
The burnt carrier of described band that settling vessel comes out to the device of making charcoal is in advance made charcoal, after making charcoal in advance, part is with burnt carrier heat-carrying to return the cracking reactor heat supply, after making charcoal in advance, all the other are with burnt carrier to enter gasifier, wherein, the described device operational condition of making charcoal in advance is: pressure is 0～1.0MPa gauge pressure, temperature is 560～900 ℃, and excess oxygen concentration is 0～5 volume %;
(C) coke of back on the carrier of making charcoal in advance that enters gasifier carries out gasification reaction generation synthetic gas with steam and/or oxygen-containing gas, wherein, the operational condition of described gasifier is: pressure is 0～1.0MPa gauge pressure, and temperature is 600～1150 ℃, and excessive water concentration is 0～25 volume %; And
(D) carrier after the gasification returns in the device of making charcoal in advance and circulates.
2. the method for claim 1 is characterized in that, this method also comprises: the cracking reactor that the mink cell focus that separation column in the step (B) is fractionated out returns in the described step (A) is proceeded scission reaction.
3. the method for claim 1 is characterized in that, this method also comprises: the lightweight oil that separation column in the step (B) is fractionated out obtains petroleum naphtha and oil fuel product to the hydrogenation unit hydrogenation, and partial synthesis gas goes device for producing hydrogen to produce hydrogen.
4. the method for claim 1 is characterized in that, this method also comprises: middle matter oil to the hydrogenation unit hydrogenation that separation column in the step (B) is fractionated out obtains the cleaning oil product, and partial synthesis gas goes device for producing hydrogen to produce hydrogen.
5. as each described method among the claim 1-4, it is characterized in that in described step (A), carrier is the silico-aluminate base carrier, specific surface area is 5～1000m
2/ g, pore volume are 0.03～1.0ml/g, and particle diameter is 20～1000 μ m.
6. as each described method among the claim 1-4, it is characterized in that, in described step (B), the back-mixing structure of band shunting, baffling function is set in described cracking reactor inside.
7. as each described method among the claim 1-4, it is characterized in that in described step (A), the scission reaction time is 1～100 second; In described step (B), the time of making charcoal is 2～100 minutes in advance; In described step (C), the gasification time is 2～80 minutes.
8. device that is used for the heavy oil comprehensive processing and utilization is characterized in that it comprises:
The cracking reactor (15) that is used for heavy oit pyrolysis;
The settling vessel (16) that is connected with described cracking reactor, be used to load the cracked reaction product, the device of making charcoal in advance (37) that is connected with described settling vessel, be used for fractionated separation column (19) and be used to make charcoal; And
With described that device is connected, as to be used to the carry out gasification reaction gasifier (42) of making charcoal in advance.
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| CN103224808A (en) * | 2013-01-10 | 2013-07-31 | 上海河图工程股份有限公司 | Inferior heavy oil fluidization conversion technology |
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| CN104232147B (en) * | 2013-06-21 | 2016-04-13 | 中国科学院过程工程研究所 | A kind of heavy oil lightweight treatment technique |
| CN106753557A (en) * | 2016-12-09 | 2017-05-31 | 上海河图工程股份有限公司 | A kind of high-efficiency heavy oil conversion process |
| CN109536207A (en) * | 2018-11-23 | 2019-03-29 | 龙正环保股份有限公司 | A kind of atmospheric fixed bed biomass gasifying furnace and biomass normal pressure gasification process |
| CN110283626A (en) * | 2019-07-10 | 2019-09-27 | 北京石油化工工程研究院 | Coal cracks gasification reactor apparatus and method |
| CN110283626B (en) * | 2019-07-10 | 2024-04-26 | 北京石油化工工程研究院 | Oil-coal slurry cracking gasification reaction device and method |
| CN110396426A (en) * | 2019-07-26 | 2019-11-01 | 南京绿帝环保能源科技有限公司 | Heavy oil continous way produces fuel oil device |
| CN111704934A (en) * | 2020-07-21 | 2020-09-25 | 洛阳石化工程设计有限公司 | Device for thermal cracking of heavy oil by using pulverized coal and petroleum coke gasification |
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Application publication date: 20110427 |