CN112831345A - Liquid phase hydrotreating system of distillate oil - Google Patents
Liquid phase hydrotreating system of distillate oil Download PDFInfo
- Publication number
- CN112831345A CN112831345A CN202110199226.9A CN202110199226A CN112831345A CN 112831345 A CN112831345 A CN 112831345A CN 202110199226 A CN202110199226 A CN 202110199226A CN 112831345 A CN112831345 A CN 112831345A
- Authority
- CN
- China
- Prior art keywords
- gas
- liquid separation
- liquid
- separation cavity
- liquid phase
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000007791 liquid phase Substances 0.000 title claims abstract description 31
- 239000007788 liquid Substances 0.000 claims abstract description 64
- 238000000926 separation method Methods 0.000 claims abstract description 47
- 239000012071 phase Substances 0.000 claims abstract description 33
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 28
- 239000000463 material Substances 0.000 claims abstract description 15
- 238000006243 chemical reaction Methods 0.000 claims abstract description 11
- 239000003921 oil Substances 0.000 claims description 39
- 239000007789 gas Substances 0.000 claims description 27
- 239000006260 foam Substances 0.000 claims description 13
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 10
- 229910052739 hydrogen Inorganic materials 0.000 claims description 10
- 239000001257 hydrogen Substances 0.000 claims description 10
- 238000007789 sealing Methods 0.000 claims description 9
- 238000005192 partition Methods 0.000 claims description 8
- 238000000034 method Methods 0.000 abstract description 16
- 238000005516 engineering process Methods 0.000 description 11
- 239000000047 product Substances 0.000 description 8
- 238000012545 processing Methods 0.000 description 6
- 239000002994 raw material Substances 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 239000002283 diesel fuel Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000007872 degassing Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 230000002401 inhibitory effect Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000010724 circulating oil Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1048—Middle distillates
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1048—Middle distillates
- C10G2300/1055—Diesel having a boiling range of about 230 - 330 °C
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1048—Middle distillates
- C10G2300/1059—Gasoil having a boiling range of about 330 - 427 °C
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a liquid phase hydrotreating system of distillate oil, which relates to the technical field of petrochemical industry and sequentially comprises a hydrogen-oil mixer, a fixed bed hydrogenation reactor and a gas-liquid separator according to a reaction sequence, wherein a gas-liquid separation cavity is arranged in the gas-liquid separator, tangential feed inlets are arranged at two horizontal sides of the gas-liquid separation cavity so as to enable materials to rotate in the gas-liquid separation cavity, and a downward inverted cone is arranged at the top of the gas-liquid separation cavity; a liquid phase outlet is formed in the bottom of the gas-liquid separation cavity; and a gas phase outlet is formed in the top of the gas-liquid separation cavity. The gas-liquid separator can perform high-quality and high-efficiency gas-liquid separation operation, and meanwhile, the system omits a plurality of intermediate production links, simplifies the process, and reduces the equipment cost and the occupied area.
Description
Technical Field
The invention relates to the technical field of petrochemical industry, in particular to a distillate oil liquid phase hydrotreating system.
Background
The oil refining industry is a key industry in the energy industry of China, not only relates to the energy safety of the economic and social development of China, but also has great influence on improving the energy efficiency and reducing the pollutant emission. The development trend of the oil refining industry is to lighten heavy oil and produce clean fuel, the hydrogenation process can cover most of raw materials and intermediate products of a secondary processing device of a refinery, and the hydrogenation process is an effective means for producing the clean fuel, can effectively remove harmful impurities in the raw materials and the products, and can obviously improve the product quality. In recent years, the upgrading process of clean fuel product standards is accelerating, and the general trend of the clean fuel in the world is as follows: gasoline low sulfur, low olefins, low aromatics, low benzene and vapor pressure; the diesel oil has low sulfur, low aromatic hydrocarbon, low density and high cetane number.
Enterprises put forward higher and higher requirements on energy conservation and consumption reduction, and processes with high energy consumption and low efficiency are gradually eliminated. The traditional process of the hydrogenation technology is the conventional trickle bed hydrogenation technology, and the trickle bed hydrogenation technology has been gradually replaced by the liquid phase hydrogenation technology due to large energy consumption, low efficiency and high investment cost.
The liquid phase hydrogenation technology is characterized in that a circulating oil technology is used to replace a circulating hydrogen technology, hydrogen consumption is reduced, and the circulation of an oil phase ensures the amount of dissolved hydrogen in the hydrogenation reaction, so that the energy consumption of a circulating pump is increased undoubtedly, and the equipment investment is increased. Therefore, the hydrogenation degree is determined by the hydrogen mixing effect in the liquid phase hydrogenation technology, and meanwhile, the hydrogenation byproducts, such as hydrogen sulfide and ammonia, have a certain inhibiting effect on the hydrogenation reaction and need to be discharged in time so as to avoid inhibiting the hydrogenation reaction depth.
Chinese patent CN104099127A discloses a distillate oil hydrotreating process, which comprises three hydrogenation reactors, wherein a hydrogen-oil mixer is added in front of each reactor, a first separator is added behind the second reactor, a second separator is added behind the third reactor, and the generated oil of the first reactor is circulated or enters the second hydrogen mixer; the second reactor produces oil or is circulated, or enters a third reactor, or enters a first separator; the third reactor produces oil or is recycled or enters a second separator. Although the process fully considers the efficiency of hydrogen mixing and timely eliminates byproducts such as hydrogen sulfide, ammonia gas and the like generated by hydrogenation reaction, the process flow is complex, the equipment investment is large, the traditional gas-liquid separator cannot ensure that materials are subjected to gas-liquid separation under the reaction condition, and a temperature and pressure raising device is additionally arranged between two reactors.
Chinese patent CN103834433A discloses an upward reaction separator and a hydrogenation method, wherein the process comprises two parts, namely a reaction zone and a gas-liquid separation zone, the two zones are located in the same container shell, the gas-liquid separation zone is arranged at the upper part, and the reaction zone is arranged at the lower part. Although the process can reduce the pipeline connection between two independent devices, the applicability of the device is greatly reduced, and the gas-liquid separation efficiency is lower.
Disclosure of Invention
The invention provides a liquid phase hydrotreating system of distillate oil, which sequentially comprises a hydrogen-oil mixer, a fixed bed hydrogenation reactor and a gas-liquid separator according to a reaction sequence, wherein a gas-liquid separation cavity is arranged in the gas-liquid separator, tangential feed inlets are arranged at two horizontal sides of the gas-liquid separation cavity so as to enable materials to rotate in the gas-liquid separation cavity, and a downward inverted cone is arranged at the top of the gas-liquid separation cavity; a liquid phase outlet is formed in the bottom of the gas-liquid separation cavity; and a gas phase outlet is formed in the top of the gas-liquid separation cavity.
The invention is further provided with: and an upward vertical cone is arranged at the bottom of the gas-liquid separation cavity.
The invention is further provided with: the gas phase outlet is a through hole which penetrates through the sealing partition plate and the inverted cone.
The invention is further provided with: the sealing clapboard is provided with a return pipe.
The invention is further provided with: and a foam breaking net opposite to the gas phase outlet is arranged above the gas-liquid separation cavity.
The invention is further provided with: the foam breaking net adopts a flat net surface or a corrugated net surface.
The invention is further provided with: the sealing clapboard is provided with a return pipe.
The beneficial technical effects of the invention are as follows:
1. the system has simple process and small equipment investment. Compared with the conventional process, the process cancels equipment such as a high-pressure separator, a low-pressure separator and the like, has less equipment quantity, and greatly reduces one-time investment and occupied land.
2. The material processing flow is short, and the processing complexity of the device is reduced; the unit can also be used in series or in parallel with other distillate oil hydrogenation devices, so that the effective processing amount of the original device is increased or the product quality of the device is improved. The quality of the products produced by the system meets the corresponding national standard, and the sulfur content of the products is less than or equal to 5 ppm.
3. The inverted cone in the separator reduces the loss of material pressure by changing the moving direction of the material, converts the power of the material inlet into the centrifugal force moving in the gas-liquid separation cavity, and realizes gas-liquid separation under the action of the centrifugal force.
4. The vertical cone at the bottom of the separator controls the height of the gas phase enrichment area, prevents a larger gas phase enrichment area from appearing, and enables the cyclone degassing process to be controlled to be carried out in a higher tangential velocity area.
5. The foam breaking net reduces entrainment of gas phase, simultaneously can further separate oil phase carried by the gas phase, the gas phase passing through the foam breaking net is discharged from the top, and the oil phase intercepted by the foam breaking net enters an oil phase outlet through a liquid discharging pipe and is converged into the material to enter the next-stage treatment.
Drawings
FIG. 1 is a schematic view of the structure of a liquid phase hydrotreating system in accordance with the present invention;
FIG. 2 is a schematic view showing the structure of a gas-liquid separator according to the present invention.
Reference numerals: 1. a gas-liquid separator; 11. sealing the partition plate; 12. a return pipe; 2. back tapering; 3. erecting a cone; 4. a feed inlet; 5. a gas phase outlet; 6. a liquid phase outlet; 7. a foam breaking net; 8. a hydrogen-oil mixer; 9. a fixed bed liquid phase hydrogenation reactor.
Detailed Description
Preferred embodiments of the present invention are described below with reference to the accompanying drawings. It should be understood by those skilled in the art that these embodiments are only for explaining the technical principle of the present invention, and are not intended to limit the scope of the present invention.
The invention provides a distillate oil liquid phase hydrotreating system, which comprises a hydrogen-oil mixer 8, a fixed bed liquid phase reactor 9 and a gas-liquid separator 1, wherein the three devices are combined into one device and share one reactor shell, and the three devices can be detached and installed through device manholes without cutting the reactor shell.
Mixing the raw material and hydrogen in a hydrogen-oil mixer 8 by a premixing technology to generate a mixture; then the mixture enters and exits the solid-liquid bed liquid phase reactor in a mode of bottom-in and top-out, and hydrogenation reaction is carried out in the solid-liquid bed liquid phase reactor to generate reaction materials; then the reaction material enters a gas-liquid separator 1, and waste gases such as hydrogen sulfide, ammonia gas and the like generated by hydrogenation reaction are discharged by adopting a gas-liquid separation technology.
The raw material can be straight-run distillate oil and secondary processing distillate oil, including single or mixed oil products such as straight-run diesel oil, straight-run wax oil, catalytic diesel oil, catalytic slurry oil, coking diesel oil, coking wax oil and the like.
The hydrogen-oil mixer 8 adopts the following patent numbers: 201920404208.8, it is technically characterized by adopting micropore dispersion internal member structure, the pore diameter of the bottom and top of the micropore dispersion internal member for liquid circulation is 1-50mm, and the pore diameter of the side wall micropore is 0.5-1000 nm. The efficient dissolution of hydrogen in the raw materials is realized, a large amount of micro bubbles are generated, the hydrogen supply is continuously realized in the whole reaction process, and the mass transfer efficiency of the hydrogenation process is improved.
The fixed bed liquid phase hydrogenation reactor 9 is flexibly provided with 1-3 reaction beds, and preferably adopts a single-bed reactor; the catalyst adopts high-activity Ni-Co-Mo-W series hydrogenation catalysts.
The gas-liquid separator 1 is a cylindrical container, and a separate gas-liquid separation cavity is separated from the interior of the container through a sealing partition plate 11, wherein the sealing partition plate 11 is in a detachable design. Tangential feed inlets 4 are formed in the horizontal two sides of the gas-liquid separation cavity so that materials can rotate in the gas-liquid separation cavity, and gas-liquid separation is carried out in the gas-liquid separation cavity through a cyclone technology. The top of the gas-liquid separation cavity is provided with a downward inverted cone 2; the back taper 2 reduces the loss of the pressure of the material by changing the moving direction of the material, converts the power of the material inlet into the centrifugal force moving in the gas-liquid separation cavity, and realizes the gas-liquid separation by the action of the centrifugal force.
The bottom of the gas-liquid separation cavity is provided with a liquid phase outlet 6; the top of the gas-liquid separation chamber is provided with a gas phase outlet 5. The gas phase outlet 5 is a through hole which penetrates through the inverted cone 2 and the sealing partition plate 11, and the gas phase outlet 5 is arranged along the axis of the inverted cone 2. The separated gas phase is discharged from a gas phase outlet 5, and the oil phase is discharged from an oil phase outlet arranged at the bottom of the gas-liquid separation cavity.
The bottom of the gas-liquid separation cavity is provided with an upward vertical cone 3. Due to the attenuation effect of the rotational flow, the separation strength at a lower position is lower, the height of the gas phase enrichment area is controlled by the vertical cone 3 at the bottom, and a larger gas phase enrichment area is prevented, so that the rotational flow degassing process is controlled to be carried out at a higher tangential speed area.
Based on the mutual cooperation of back taper 2 and vertical taper 3, this gas-liquid shunt can realize efficient gas-liquid separation.
A foam breaking net 7 opposite to the gas phase outlet 5 is arranged above the gas-liquid separation cavity. The foam breaking net 7 is equal to the diameter of the reactor. The foam breaking net 7 is arranged in a split and detachable way. The foam breaking net 7 can adopt a flat net surface or a corrugated net surface. The gas phase discharged from the gas phase outlet 5 contacts the demister 7. Since the gas phase and the liquid phase are not completely separated during the actual operation, many bubbles are discharged from the gas phase outlet 5. The gas bubbles will be broken up after encountering the breakup net 7 and the gas phase will be discharged upwards, while the liquid phase will be left behind after having been collected. The sealed partition 11 is provided with a return pipe 12. The liquid phase after the foam breaking and gathering enters the gas-liquid separation cavity from the return pipe 12 and is finally discharged from the liquid phase outlet 6.
The hydrogen-oil mixing, the hydrogenation reaction and the gas-liquid separation in the system can be finished with high quality and high efficiency, so that a plurality of intermediate process links are saved, and equipment and floor area are saved.
The system can be used in series or in parallel according to requirements. Meanwhile, the device can also be used in series or in parallel with other distillate oil hydrogenation devices, so that the effective processing amount of the original device is increased or the product quality of the device is improved.
While the invention has been described with reference to a preferred embodiment, various changes may be made and equivalents may be substituted for elements thereof without departing from the scope of the invention, and particularly, features shown in the various embodiments may be combined in any suitable manner without departing from the scope of the invention. It is intended that the invention not be limited to the particular embodiments disclosed, but that the invention will include all embodiments falling within the scope of the appended claims.
In the description of the present invention, the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like, which indicate directions or positional relationships, are based on the directions or positional relationships shown in the drawings, which are for convenience of description only, and do not indicate or imply that the devices or elements must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
Furthermore, it should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
The terms "comprises," "comprising," or any other similar term are intended to cover a non-exclusive inclusion, such that a process, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, article, or apparatus.
So far, the technical solutions of the present invention have been described in connection with the preferred embodiments shown in the drawings, but it is easily understood by those skilled in the art that the scope of the present invention is obviously not limited to these specific embodiments. Equivalent changes or substitutions of related technical features can be made by those skilled in the art without departing from the principle of the invention, and the technical scheme after the changes or substitutions can fall into the protection scope of the invention.
Claims (7)
1. The utility model provides a liquid phase hydrotreating system of distillate oil, includes hydrogen oil blender (8), fixed bed hydrogenation ware (9) and vapour and liquid separator (1) in proper order according to the reaction sequence, its characterized in that: a gas-liquid separation cavity is arranged in the gas-liquid separator (1), tangential feed inlets (4) are arranged on two horizontal sides of the gas-liquid separation cavity so that materials can rotate in the gas-liquid separation cavity, and a downward inverted cone (2) is arranged at the top of the gas-liquid separation cavity; a liquid phase outlet (6) is formed at the bottom of the gas-liquid separation cavity; and a gas phase outlet (5) is formed in the top of the gas-liquid separation cavity.
2. The liquid phase hydroprocessing system of distillate oils of claim 1, wherein: the bottom of the gas-liquid separation cavity is provided with an upward vertical cone (3).
3. The liquid phase hydroprocessing system of distillate oils of claim 1, wherein: the gas phase outlet (5) is a through hole which penetrates through the sealing partition plate (11) and the inverted cone (2).
4. The liquid phase hydroprocessing system of distillate oils of claim 1, wherein: the gas phase outlet (5) is arranged along the axis of the inverted cone (2).
5. The liquid phase hydroprocessing system of distillate oils of claim 1, wherein: and a foam breaking net (7) opposite to the gas phase outlet (5) is arranged above the gas-liquid separation cavity.
6. The liquid phase hydroprocessing system of distillate oils of claim 5, wherein: the foam breaking net (7) adopts a flat net surface or a corrugated net surface.
7. The liquid phase hydroprocessing system of distillate oils of claim 1, wherein: the sealing partition plate (11) is provided with a return pipe (12).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110199226.9A CN112831345A (en) | 2021-02-23 | 2021-02-23 | Liquid phase hydrotreating system of distillate oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110199226.9A CN112831345A (en) | 2021-02-23 | 2021-02-23 | Liquid phase hydrotreating system of distillate oil |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112831345A true CN112831345A (en) | 2021-05-25 |
Family
ID=75932956
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110199226.9A Pending CN112831345A (en) | 2021-02-23 | 2021-02-23 | Liquid phase hydrotreating system of distillate oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112831345A (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103071318A (en) * | 2013-01-30 | 2013-05-01 | 华东理工大学 | Device for liquid degassing through swirling flow field or centrifugal field and pressure gradient field coupling |
| CN104560132A (en) * | 2013-10-29 | 2015-04-29 | 中国石油化工股份有限公司 | Method for hydrotreatment of continuous liquid-phase wax oil |
| CN214694015U (en) * | 2021-02-23 | 2021-11-12 | 盘锦浩业科技有限公司 | Liquid phase hydrotreating system of distillate oil |
-
2021
- 2021-02-23 CN CN202110199226.9A patent/CN112831345A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103071318A (en) * | 2013-01-30 | 2013-05-01 | 华东理工大学 | Device for liquid degassing through swirling flow field or centrifugal field and pressure gradient field coupling |
| CN104560132A (en) * | 2013-10-29 | 2015-04-29 | 中国石油化工股份有限公司 | Method for hydrotreatment of continuous liquid-phase wax oil |
| CN214694015U (en) * | 2021-02-23 | 2021-11-12 | 盘锦浩业科技有限公司 | Liquid phase hydrotreating system of distillate oil |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108264935B (en) | Suspension bed hydrogenation system for treating heavy oil | |
| US10889770B2 (en) | Method and device for lightening heavy oil by utilizing a suspension-bed hydrogenation process | |
| CN102443424B (en) | Method for producing clean diesel from coal tar | |
| US10449489B2 (en) | High efficient desulfurization-regeneration system using a suspension bed | |
| CN109679690A (en) | A kind of liquid-phase hydrogenatin system and liquid phase hydrogenating method | |
| CN106635157B (en) | A kind of lightening method of inferior feedstock oil | |
| CN111068589B (en) | Liquid-phase hydrogenation system and liquid-phase hydrogenation method | |
| CN111482139A (en) | Up-down opposite flushing type residual oil hydrogenation fluidized bed micro-interface strengthening reaction device and method | |
| EP0775183A1 (en) | Fcc catalyst stripper | |
| JP6140076B2 (en) | Multistage decomposition and removal process in FCC unit | |
| US20180296977A1 (en) | Integrated system for wet desulfurization using a suspension bed and regeneration | |
| CN214694015U (en) | Liquid phase hydrotreating system of distillate oil | |
| CN102250641A (en) | Method and apparatus for preparing ethylene and propylene with maximized yield | |
| CN107880927A (en) | A kind of heavy oil plasma hydroprocessing technique and system | |
| CN112831345A (en) | Liquid phase hydrotreating system of distillate oil | |
| CN201695001U (en) | Device for preparing ethylene and propylene | |
| CN1217366A (en) | Catalyst cracking method for producing in high-yield olefin and lift-leg reaction system thereof | |
| CN113083169B (en) | Fluidized bed hydrogenation reactor and using method thereof | |
| CN109679684A (en) | A kind of liquid-phase hydrogenatin reaction system and method | |
| CN109929592A (en) | A kind for the treatment of process and system of ethylene bottom oil | |
| CN210103853U (en) | Residual oil hydrogenation device | |
| CN108264933B (en) | Device for realizing heavy oil lightening by using suspension bed hydrogenation technology | |
| CN1100118C (en) | Petroleum hydrocarbon catalytic cracking process of producing diesel oil and high-octane number gasoline | |
| CN101987964B (en) | Catalytic conversion method of hydrocarbon oil | |
| CN213078417U (en) | Residual oil hydrogenation reaction equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |