CN213085891U - Heavy oil produces production system of naphtha for a long time - Google Patents
Heavy oil produces production system of naphtha for a long time Download PDFInfo
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- CN213085891U CN213085891U CN202021146711.7U CN202021146711U CN213085891U CN 213085891 U CN213085891 U CN 213085891U CN 202021146711 U CN202021146711 U CN 202021146711U CN 213085891 U CN213085891 U CN 213085891U
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Abstract
The utility model relates to a production system of heavy oil prolific naphtha, it includes one-level reaction unit: comprises an additive mixing tank, a feeding mixing tank, a fresh hydrogen machine, a primary heating furnace, a primary suspension bed hydrogenation reactor unit and a primary separation unit; a secondary reaction unit: comprises a secondary heating furnace, a secondary fixed bed hydrogenation reactor, a decompression tower and a secondary separation unit; a third-stage reaction unit: the system comprises a stripping tower, a three-stage heating furnace, a fractionating tower, a three-stage fixed bed hydrogenation reactor, a three-stage separation unit and a circulating hydrogen system: the hydrogen outlet of the second-stage separation unit is connected to a new hydrogen machine pipeline, the first-stage suspension bed hydrogenation reactor unit, the second-stage fixed bed hydrogenation reactor and the third-stage fixed bed hydrogenation reactor through a hydrogen circulating machine. The utility model discloses a heavy oil prolific naphtha production system improves the conversion rate of raw materials heavy component and asphaltene by a wide margin, realizes the high conversion rate of residual oil, improves naphtha output, and simple process simultaneously, area is compact, and the commercialization investment is reasonable, and the feeding is nimble, and hydrogen consumption is lower.
Description
Technical Field
The utility model belongs to the technical field of heavy oil hydrogenation, especially, production system of heavy oil prolific naphtha.
Background
In the next 10-15 years, the national economy of China is expected to continue to develop rapidly at a speed of about 6-7%, the consumption of petroleum products is still in a growth period, the consumption of crude oil is increased by 6.4% every year, and the annual growth rate of the domestic crude oil yield is only 1.9%. With the increasing quantity of imported crude oil, the selectivity of high-quality crude oil in the international market is reduced, the proportion of light crude oil in the imported crude oil is reduced day by day, and the proportion of various high-density heavy oil and inferior high-sulfur and high-acid heavy oil is increased continuously. The relative density of the heavy oil and the extra heavy oil is generally above 0.96, the processing difficulty is large, and how to convert a large amount of residual oil generated by the heavy oil and the extra heavy oil also becomes an important subject of the current oil refining industry,
moreover, because the domestic fuel type oil product has excess capacity, domestic refineries gradually optimize the product structure and change from fuel type refineries to chemical type refineries. The gasoline and diesel oil are converted into chemical products such as aromatic hydrocarbon and olefin, the product profit is increased, and the industrial chain is optimized.
The refinery is transformed into chemical type, and the product structure must be adjusted, such as the production of naphtha, diesel oil, gas oil, petroleum coke or products such as fuel oil, which are produced in a high yield, and the naphtha is used as the main feed of the reforming unit to produce the downstream products such as aromatics, olefins and the like.
The existing technology for producing naphtha from heavy oil cannot achieve one-step operation, heavy oil needs to be processed through three sets of independent devices, such as an independent boiling bed device or a suspended bed device and an independent fixed bed device, energy consumption is high, naphtha yield is low, and byproducts are more.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome prior art's not enough, provide a heavy oil prolificacy naphtha production system, its suspended bed and the fixed bed combination hydrogenation that adopts the heavy oil raw materials improves heavy oil conversion rate and naphtha yield by a wide margin.
The utility model provides a its technical problem realize through following technical scheme:
a heavy oil prolificacy naphtha production system which characterized in that: comprises that
A feeding unit: comprises an additive mixing tank, a feeding mixing tank and a fresh hydrogen machine, wherein the additive mixing tank is connected with the feeding mixing tank, an outlet of the feeding mixing tank and an outlet of the fresh hydrogen machine are connected with a first-stage reaction unit,
a first-stage reaction unit: the device comprises a first-stage heating furnace, a first-stage suspension bed hydrogenation reactor unit and a first-stage separation unit, wherein an outlet of a feeding mixing tank and an outlet of a new hydrogen machine are connected to the first-stage heating furnace;
a secondary reaction unit: the device comprises a secondary heating furnace, a secondary fixed bed hydrogenation reactor, a pressure reducing tower and a secondary separation unit, wherein a liquid-solid outlet of the primary separation unit is connected to an inlet of the secondary heating furnace, an outlet of the secondary heating furnace is connected to the pressure reducing tower, a gas phase outlet of the primary separation unit is connected to the secondary fixed bed hydrogenation reactor, and a liquid-solid outlet of the secondary fixed bed hydrogenation reactor is connected to the secondary separation unit;
a third-stage reaction unit: the device comprises a stripping tower, a third-stage heating furnace, a fractionating tower, a third-stage fixed bed hydrogenation reactor and a third-stage separation unit, wherein a liquid-solid outlet of the second-stage separation unit is connected to the stripping tower, an outlet of the stripping tower is connected to the third-stage heating furnace, an outlet of the third-stage heating furnace is connected to the fractionating tower, a naphtha outlet at the top of the fractionating tower is connected to the third-stage separation unit, a material outlet at the bottom of the fractionating tower is connected to the third-stage fixed bed hydrogenation reactor;
a circulating hydrogen system: the hydrogen outlet of the second-stage separation unit is connected to a new hydrogen machine pipeline, the first-stage suspension bed hydrogenation reactor unit, the second-stage fixed bed hydrogenation reactor and the third-stage fixed bed hydrogenation reactor through a hydrogen circulating machine.
And the first-stage suspension bed hydrogenation reactor unit comprises 2-4 suspension bed reactors connected in series.
And 3-6 quench gas injection layers are arranged in the suspended bed reactor along the longitudinal direction, each quench gas injection layer comprises 3-8 quench gas injection points, the quench gas injection points are connected with a hydrogen outlet of the secondary separation unit, and the temperature of the reactor in the suspended bed reactor is adjusted by adjusting the injection amount of the quench gas of each injection point.
And the second-stage fixed bed hydrogenation reactor is provided with 2-3 hydrofining beds and 2-3 hydrocracking beds, each bed is provided with a quenching gas injection point, and the quenching gas injection points are connected with a hydrogen outlet of the second-stage separation unit.
Moreover, the additive mixing tank is connected with an additive pipeline, the additive is coal-based activated carbon, and the specific surface area of the additive mixing tank is 300 or 400m2(g) the particle size is not more than 4 mm.
The utility model discloses an advantage and beneficial effect do:
1. the utility model discloses a heavy oil productive naphtha production system, including the heavy oil raw materials, the reaction feeding of hydrogen and additive gets into one-level reaction unit in proper order, second grade reaction unit and tertiary reaction unit, carry out the suspension hydrogenation reaction in the one-level suspension bed hydrogenation ware unit of one-level reaction unit, carry out second grade fixed bed hydrogenation reaction in the second grade fixed bed hydrogenation ware of second grade reaction unit, carry out third grade fixed bed hydrogenation reaction in the third grade fixed bed hydrogenation ware of third grade reaction unit, one-level suspension bed hydrogenation ware unit, second grade fixed bed hydrogenation ware and the sharing circulating hydrogen system of third grade fixed bed hydrogenation ware, second grade fixed bed hydrogenation ware can produce fuel type product, the naphtha diesel oil of Europe six standard, utilize third grade fixed bed hydrogenation ware to carry out deep-processing, only produce the naphtha product and regard as the feeding of chemical industry type refinery reforming unit, high conversion rate and high naphtha yield.
2. The utility model discloses a heavy oil prolificacy naphtha production system, one-level suspension bed hydrogenation reactor unit include 2-4 series connection's suspension bed reactor, further improve suspension bed hydrogenation's product yield.
3. The utility model discloses a naphtha production system is produced to heavy oil fecundation, vertically be equipped with 3-6 layers of quench gas injection layers in the suspended bed reactor, every layer of quench gas injection layer includes 3-8 quench gas injection points, adjusts through the quench gas injection volume of adjusting each injection point reactor temperature in the suspended bed reactor, the reaction temperature of each reactor is preferred to be kept in 450 ability 470 ℃ of honour within range, and the suspended bed reactor generally moves at the constant temperature within range, keeps device safe operation and design performance.
4. The utility model discloses a heavy oil prolificacy naphtha production system, additive blending tank connect the additive pipeline, and the additive is coal-based active carbon, and specific surface area is 300 or 400m2The particle size is not more than 4mm, the additive can adsorb unreacted heavy components such as asphaltene or colloid in the suspension bed reactor, and during reaction, the unreacted asphaltene is adhered in the additive, so that the coking tendency of the asphaltene serving as a coking precursor is hindered, and a coke layer can be prevented from being formed on the inner surface of the suspension bed reactor.
5. The utility model discloses a heavy oil prolific naphtha production system improves the conversion rate of raw materials heavy component and asphaltene by a wide margin, realizes the high conversion rate of residual oil, improves naphtha output, and simple process simultaneously, area is compact, and the commercialization investment is reasonable, and the feeding is nimble, and hydrogen consumption is lower.
Drawings
Fig. 1 is a flow chart of the system of the present invention.
Description of the reference numerals
1-an additive mixing tank, 2-a feeding mixing tank, 3-a new hydrogen machine, 4-a first-stage heating furnace, 5-a first-stage suspension bed hydrogenation reactor unit, 6-a first-stage separation unit, 7-a second-stage heating furnace, 8-a decompression tower, 9-a second-stage separation unit, 10-a stripping tower, 11-a third-stage heating furnace, 12-a fractionating tower, 13-a third-stage fixed bed hydrogenation reactor, 14-a third-stage separation unit, 15-a hydrogen circulating machine, 16-a quenching gas injection layer and 17-a second-stage fixed bed hydrogenation reactor.
Detailed Description
The present invention will be described in further detail with reference to specific examples, which are provided for illustrative purposes only, and are not intended to be limiting, and the scope of the present invention should not be limited thereby.
A heavy oil productive naphtha production system comprises the following units:
a feeding unit: comprises an additive mixing tank 1, a feeding mixing tank 2 and a fresh hydrogen machine 3, wherein the additive mixing tank 1 is connected with the feeding mixing tank 2, and the feeding is mixedThe outlet of the combination tank 2 and the outlet of the new hydrogen machine 3 are connected to a first-stage reaction unit, the additive mixing tank 1 is connected with an additive pipeline, the additive is coal-based activated carbon, and the specific surface area is 300 or 400m2(g) the particle size is not more than 4 mm.
A first-stage reaction unit: the device comprises a primary heating furnace 4, a primary suspension bed hydrogenation reactor unit 5 and a primary separation unit 6, wherein the outlet of a feeding mixing tank 2 and the outlet of a new hydrogen machine 3 are connected to the primary heating furnace 4, the outlet of the primary heating furnace 4 is connected to the primary suspension bed hydrogenation reactor unit, and the outlet of the primary suspension bed hydrogenation reactor unit is connected to the primary separation unit 6; the primary suspension bed hydrogenation reactor unit 5 comprises 2-4 suspension bed reactors connected in series. Further improving the product yield of the suspension bed hydrogenation reaction. And 3-6 quench gas injection layers 16 are longitudinally arranged in the suspended bed reactor, each quench gas injection layer 16 comprises 3-8 quench gas injection points, the quench gas injection points are connected with a hydrogen outlet of the secondary separation unit, and the temperature of the reactor in the suspended bed reactor is adjusted by adjusting the injection amount of the quench gas of each injection point.
A secondary reaction unit: the device comprises a secondary heating furnace 7, a secondary fixed bed hydrogenation reactor 17, a decompression tower 8 and a secondary separation unit 9, wherein a liquid-solid outlet of the primary separation unit 6 is connected to an inlet of the secondary heating furnace 7, an outlet of the secondary heating furnace 7 is connected to the decompression tower 8, a gas phase outlet of the primary separation unit 6 is connected to the secondary fixed bed hydrogenation reactor, and a liquid-solid outlet of the secondary fixed bed hydrogenation reactor is connected to the secondary separation unit 9; the second-stage fixed bed hydrogenation reactor is provided with 2-3 hydrofining beds and 2-3 hydrocracking beds, each bed is provided with a quench gas injection point, and the quench gas injection points are connected with a hydrogen outlet of the second-stage separation unit 9.
A third-stage reaction unit: the device comprises a stripping tower 10, a third-level heating furnace 11, a fractionating tower 12, a third-level fixed bed hydrogenation reactor 13 and a third-level separation unit 14, wherein a liquid-solid outlet of the second-level separation unit 9 is connected to the stripping tower 10, an outlet of the stripping tower 10 is connected to the third-level heating furnace 11, an outlet of the third-level heating furnace 11 is connected to the fractionating tower 12, a naphtha outlet at the top of the fractionating tower 12 is connected to the third-level separation unit 14, a material outlet at the bottom of the fractionating tower 12 is connected to the third-level fixed bed hydrogenation reactor, and.
A circulating hydrogen system: the hydrogen outlet of the second-stage separation unit 9 is connected to the pipeline of the new hydrogen machine 3, the first-stage suspension bed hydrogenation reactor unit, the second-stage fixed bed hydrogenation reactor and the third-stage fixed bed hydrogenation reactor through the hydrogen circulating machine 15.
The working process of the heavy oil productive naphtha production system is as follows:
and carrying out the suspension bed hydrogenation reaction in a primary suspension bed hydrogenation reactor unit of the primary reaction unit.
And products of the suspension bed reactor of the first-stage reaction unit are subjected to further hydrofining and hydrocracking reaction. Because the atmospheric and vacuum unit at the front end of the refinery has products such as direct flow diesel oil, wax oil and the like, the products can also be directly treated as the single feed of the secondary reaction unit. The second-stage separation unit 9 of the second-stage reaction unit mainly comprises a product separation tank, a stripping tower 10 and a fractionating tower 12, and products of the second-stage reaction unit are separated to obtain products such as the Europe-standard naphtha, diesel oil and wax oil.
And the third-stage reaction unit is a diesel oil and wax oil deep processing unit, a third-stage fixed bed hydrogenation reactor is adopted, and quenching gas injection is arranged between bed layers of the third-stage fixed bed hydrogenation reactor to adjust the reactor temperature in the third-stage fixed bed hydrogenation reactor. Products of the second-stage reaction unit, mainly diesel oil, wax oil and the like in the fractionating tower 12, continue to pass through the three-stage fixed bed hydrogenation reactor for hydrocracking reaction to obtain a final product naphtha.
Although the embodiments of the present invention and the accompanying drawings have been disclosed for illustrative purposes, those skilled in the art will appreciate that various substitutions, alterations, and modifications are possible without departing from the spirit and scope of the invention and the appended claims, and thus the scope of the invention is not limited to the embodiments and drawings disclosed.
Claims (5)
1. A production system for heavy oil and productive naphtha is characterized in that: comprises that
A feeding unit: comprises an additive mixing tank, a feeding mixing tank and a fresh hydrogen machine, wherein the additive mixing tank is connected with the feeding mixing tank, an outlet of the feeding mixing tank and an outlet of the fresh hydrogen machine are connected with a first-stage reaction unit,
a first-stage reaction unit: the device comprises a first-stage heating furnace, a first-stage suspension bed hydrogenation reactor unit and a first-stage separation unit, wherein an outlet of a feeding mixing tank and an outlet of a new hydrogen machine are connected to the first-stage heating furnace;
a secondary reaction unit: the device comprises a secondary heating furnace, a secondary fixed bed hydrogenation reactor, a pressure reducing tower and a secondary separation unit, wherein a liquid-solid outlet of the primary separation unit is connected to an inlet of the secondary heating furnace, an outlet of the secondary heating furnace is connected to the pressure reducing tower, a gas phase outlet of the primary separation unit is connected to the secondary fixed bed hydrogenation reactor, and a liquid-solid outlet of the secondary fixed bed hydrogenation reactor is connected to the secondary separation unit;
a third-stage reaction unit: the device comprises a stripping tower, a third-stage heating furnace, a fractionating tower, a third-stage fixed bed hydrogenation reactor and a third-stage separation unit, wherein a liquid-solid outlet of the second-stage separation unit is connected to the stripping tower, an outlet of the stripping tower is connected to the third-stage heating furnace, an outlet of the third-stage heating furnace is connected to the fractionating tower, a naphtha outlet at the top of the fractionating tower is connected to the third-stage separation unit, a material outlet at the bottom of the fractionating tower is connected to the third-stage fixed bed hydrogenation reactor;
a circulating hydrogen system: the hydrogen outlet of the second-stage separation unit is connected to a new hydrogen machine pipeline, the first-stage suspension bed hydrogenation reactor unit, the second-stage fixed bed hydrogenation reactor and the third-stage fixed bed hydrogenation reactor through a hydrogen circulating machine.
2. The system for producing naphtha as heavy oil in high yield according to claim 1, wherein: the first-stage suspension bed hydrogenation reactor unit comprises 2-4 suspension bed reactors connected in series.
3. The system for producing naphtha as heavy oil in high yield according to claim 2, wherein: and 3-6 quench gas injection layers are longitudinally arranged in the suspended bed reactor, each quench gas injection layer comprises 3-8 quench gas injection points, the quench gas injection points are connected with a hydrogen outlet of the secondary separation unit, and the temperature of the reactor in the suspended bed reactor is adjusted by adjusting the injection amount of the quench gas of each injection point.
4. The system for producing naphtha as heavy oil in high yield according to claim 1, wherein: the second-stage fixed bed hydrogenation reactor is provided with 2-3 hydrofining beds and 2-3 hydrocracking beds, each bed is provided with a quench gas injection point, and the quench gas injection points are connected with a hydrogen outlet of the second-stage separation unit.
5. The system for producing naphtha as heavy oil in high yield according to claim 1, wherein: moreover, the additive mixing tank is connected with an additive pipeline, the additive is coal-based activated carbon, and the specific surface area of the additive mixing tank is 300 or 400m2(g) the particle size is not more than 4 mm.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111909719A (en) * | 2020-06-19 | 2020-11-10 | 张家港保税区慧鑫化工科技有限公司 | Production system and production method for heavy oil to produce naphtha in large quantity |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111909719A (en) * | 2020-06-19 | 2020-11-10 | 张家港保税区慧鑫化工科技有限公司 | Production system and production method for heavy oil to produce naphtha in large quantity |
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