CN111996035A - Wax oil hydrogenation upgrading system - Google Patents
Wax oil hydrogenation upgrading system Download PDFInfo
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- CN111996035A CN111996035A CN202010959933.9A CN202010959933A CN111996035A CN 111996035 A CN111996035 A CN 111996035A CN 202010959933 A CN202010959933 A CN 202010959933A CN 111996035 A CN111996035 A CN 111996035A
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- wax oil
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- 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
- C10G67/14—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 including at least two different refining steps in the absence of hydrogen
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to the technical field of petrochemical industry, in particular to a wax oil hydrogenation modification system, which comprises a heating furnace, a reactor, a first heat exchanger, a hot high-pressure separator, a hot high-pressure-distribution air cooler, a cold high-pressure separator, a desulfurizing tower, a hot low-pressure separator, a hot low-pressure-distribution air cooler, a cold low-pressure separator and a sulfur-containing sewage tank, wherein an air inlet of the reactor is communicated with a hydrogen supply pipeline of a diesel hydrogenation system; the hydrogen required by the wax oil hydrogenation modification system is supplied by the diesel oil hydrogenation system, and the excessive hydrogen in the diesel oil hydrogenation system is applied to the wax oil hydrogenation modification system, so that the quality of the wax oil can be improved, the hydrogen resource in the process of a factory can be fully applied, and the waste of the resource is reduced. The wax oil hydrogenation modification system fully utilizes the existing equipment in a factory, and greatly reduces the construction cost of the wax oil hydrogenation modification system.
Description
[ technical field ] A method for producing a semiconductor device
The invention relates to the technical field of petrochemical industry, in particular to a wax oil hydrogenation modification system.
[ background of the invention ]
In recent years, with increasing shortage of petroleum resources, the trend of crude oil upgrading and degradation is getting worse, and with the development of economy, the demand for light oil products is increasing, so that maximum upgrading and benefit maximization of heavy oil become the pursuit targets of oil refining enterprises. The main means for processing heavy oil are hydrocracking, catalytic cracking and delayed coking. Hydrocracking is difficult to process coker gas oil and residual oil due to large investment and high operation cost, so that the application of the hydrocracking is limited, and delayed coking is limited due to low liquid yield, poor product quality and other factors. The catalytic cracking has low operation cost, high yield of light oil products and good quality of gasoline products, and can process heavy inferior raw materials such as wax oil, residual oil and the like, thereby obtaining wide process application.
With the increasingly stricter quality standards of gasoline and diesel oil products in China, how to solve the problems of high sulfur content of catalytic cracking gasoline, high sulfur and aromatic hydrocarbon content of catalytic cracking diesel oil and low cetane number becomes a hotspot of research in recent years. At present, a plurality of catalytic cracking catalysts, auxiliary agents and process technologies are developed, wherein the catalytic cracking raw material pre-hydrogenation technology becomes an effective means for solving the problem of high sulfur content of catalytic gasoline. The pre-hydrogenation of the catalytic cracking raw material not only reduces the contents of sulfur, nitrogen and aromatic hydrocarbon, but also is beneficial to improving the catalytic cracking conversion rate, increasing the catalytic cracking light yield, reducing the sulfur content of gasoline, and improving the cetane numbers of gasoline olefin and diesel oil.
Among various methods for converting straight-run wax oil into light-weight wax oil, the process of hydrogenating wax oil as a catalytic cracking raw material is a good process route. Most of sulfur and nitrogen impurities are removed from the wax oil after hydrotreating, and part of aromatic hydrocarbon is saturated, so that the hydrogen content is increased, further, the conversion rate of catalytic cracking raw materials can be increased, the coke yield is reduced, the yield of catalytic cracking light oil is increased, a product with improved quality is obtained, the sulfur content of the obtained gasoline is low, and the cetane numbers of gasoline olefin and diesel oil are also improved; meanwhile, the wax oil hydrotreating can also produce a byproduct of low-sulfur diesel oil with the concentration of 15 percent, and the diesel-gasoline ratio of a refinery is improved. Therefore, the process of using wax oil hydrotreating to generate oil as catalytic cracking raw material is also widely applied.
The diesel oil hydrogenation system in the existing oil refinery is widely applied, and the diesel oil hydrogenation system is built in the ordinary oil refinery, but hydrogen in the diesel oil hydrogenation system is often excessive and cannot be fully applied, so that the waste of hydrogen resources is caused.
[ summary of the invention ]
In view of the above, the invention provides a wax oil hydrogenation modification system, which solves the problem of resource waste caused by excessive hydrogen in a diesel oil hydrogenation system.
In order to solve the problems, the invention adopts the technical scheme that: a wax oil hydrogenation modification system comprises a heating furnace, a reactor, a first heat exchanger, a hot high-pressure separator, a hot high-pressure gas-air cooler, a cold high-pressure separator, a desulfurization tower, a hot low-pressure separator, a hot low-pressure gas-air cooler, a cold low-pressure separator and a sulfur-containing sewage tank, wherein an outlet of the heating furnace is connected with a liquid inlet of the reactor, an air inlet of the reactor is communicated with a hydrogen supply pipeline of a diesel hydrogenation system, a liquid outlet of the reactor is communicated with a hydrothermal solution inlet of the first heat exchanger, a cold night inlet of the first heat exchanger is connected with a wax oil supply system, a cold night outlet of the first heat exchanger is connected with an inlet of the heating furnace, and a hydrothermal solution outlet of the first heat exchanger is connected with a liquid inlet of the hot high-pressure separator; the upper outlet of the hot high-pressure separator is connected with the inlet of the hot high-pressure gas-distributing air cooler, the outlet of the hot high-pressure gas-distributing air cooler is connected with the liquid inlet of the cold high-pressure separator, the drain outlet of the cold high-pressure separator is connected with the sulfur-containing sewage tank, the upper outlet of the cold high-pressure separator is connected with the liquid inlet of the desulfurizing tower, the lean amine liquid inlet of the desulfurizing tower is communicated with the lean amine liquid pipeline of the diesel hydrogenation system, the gas outlet of the desulfurizing tower is communicated with the circulating hydrogen pipeline of the diesel hydrogenation system, and the rich amine liquid outlet of the desulfurizing tower is communicated with the sulfur recovery system; the bottom exit linkage of hot high pressure separator the inlet of hot low pressure separator, the upper portion exit linkage of hot low pressure separator the entry of hot low branch gas air cooler, the export of hot low branch gas air cooler with the lower part export of cold high pressure separator is connected respectively the inlet of cold low pressure separator, the upper portion export intercommunication diesel oil hydrogenation system's of cold low branch gas discharge pipeline, the drain of cold low pressure separator is connected contain the sulphur sewage jar, the lower part export of cold low pressure separator with the lower part export of hot low pressure separator is connected wax oil catalytic system respectively.
Furthermore, a wax oil filter, a wax oil buffer tank and a wax oil feeding pump are arranged between the cold night inlet of the first heat exchanger and the wax oil supply system, the wax oil filter, the wax oil buffer tank and the wax oil feeding pump are sequentially connected, an oil outlet of the wax oil feeding pump is communicated with the cold night inlet of the first heat exchanger, and an oil inlet of the wax oil filter is communicated with the wax oil supply system. Use wax oil filter to carry out filtration treatment to raw materials wax oil, the wax oil impurity that gets into the reactor is still less, and the hydrotreating effect is better, can avoid impurity to pile up at oil pipe moreover and cause the jam.
Further, a second heat exchanger is arranged between the hot high-pressure separator and the hot high-pressure gas-distributing air cooler, a hot gas inlet of the second heat exchanger is communicated with an outlet at the upper part of the hot high-pressure separator, a hot gas outlet of the second heat exchanger is communicated with an inlet of the hot high-pressure gas-distributing air cooler, a cold gas inlet of the second heat exchanger is communicated with a hydrogen supply pipeline of a diesel hydrogenation system, and a cold gas outlet of the second heat exchanger is communicated with a cold night inlet of the first heat exchanger. The second heat exchanger further utilizes the heat in the hot high-pressure separator, so that the energy utilization rate is improved, and the energy consumption is reduced.
Furthermore, a cyclone is arranged between the cold high-pressure separator and the desulfurizing tower, a liquid inlet of the cyclone is connected with an upper outlet of the cold high-pressure separator, an upper outlet of the cyclone is connected with a liquid inlet of the desulfurizing tower, and a lower outlet of the cyclone is connected with a liquid inlet of the cold low-pressure separator.
Further, the inlet of the hot high-pressure-distribution air cooler is communicated with a desalted water supply pipeline of a diesel hydrogenation system.
Due to the adoption of the technical scheme, the invention has the beneficial effects that:
the hydrogen required by the wax oil hydrogenation modification system is supplied by the diesel oil hydrogenation system, the hydrogen and the diesel oil hydrogenation system share one hydrogen supply system, the wax oil hydrogenation modification system and the diesel oil hydrogenation system are used together, and the hydrogen supply system and the diesel oil hydrogenation system are started and stopped simultaneously, and the surplus hydrogen in the diesel oil hydrogenation system is applied to the wax oil hydrogenation modification system, so that the quality of wax oil can be improved, hydrogen resources in the process of a factory can be fully applied, and the waste of resources is reduced. The wax oil hydrogenation modification system fully utilizes the existing equipment in a factory, and greatly reduces the construction cost of the wax oil hydrogenation modification system.
[ description of the drawings ]
FIG. 1 is a schematic diagram of a wax oil hydro-upgrading system according to the present invention;
reference numerals: 1-heating furnace, 2-reactor, 3-first heat exchanger, 4-hot high-pressure separator, 5-hot high-pressure gas air cooler, 6-cold high-pressure separator, 7-desulfurizing tower, 8-hot low-pressure separator, 9-hot low-pressure gas air cooler, 10-cold low-pressure separator, 11-sulfur-containing sewage tank, 12-second heat exchanger, 13-cyclone, 14-wax oil filter, 15-wax oil buffer tank and 16-wax oil feeding pump.
[ detailed description ] embodiments
In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in detail below. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. This invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein, but rather should be construed as broadly as the present invention is capable of modification in various respects, all without departing from the spirit and scope of the present invention.
Referring to fig. 1, a wax oil hydro-upgrading system includes a wax oil filter 14, a wax oil buffer tank 15, a wax oil feed pump 16, a heating furnace 1, a reactor 2, a first heat exchanger 3, a hot high-pressure separator 4, a second heat exchanger 12, a hot high-pressure gas-air cooler 5, a cold high-pressure separator 6, a cyclone 13, a desulfurizing tower 7, a hot low-pressure separator 8, a hot low-pressure gas-air cooler 9, a cold low-pressure separator 10, and a sulfur-containing sewage tank 11. Wax oil filter 14 carries out filtration treatment to raw materials wax oil, wax oil buffer tank 15 is saved the wax oil after filtering, wax oil feed pump 16 supplies with the wax oil in wax oil buffer tank 15 to first heat exchanger 3, first heat exchanger 3 preheats the wax oil that wax oil feed pump 16 supplied with, reduce the temperature of the wax oil that reactor 2 came out simultaneously, the heat that the make full use of reaction produced, reduce the energy consumption, first heat exchanger 3 supplies with heating furnace 1 again after preheating the wax oil and continues heating. The heating furnace 1 and the reactor 2 convert non-hydrocarbon compounds such as sulfide, nitride and the like in the raw material wax oil into H2S and NH3 which are easy to remove, simultaneously convert a small amount of heavy metal into metal sulfide to be trapped on the surface of the catalyst, and some olefins and aromatic hydrocarbons are subjected to hydrogenation saturation and a small amount of hydrocracking reaction. The hot high-pressure separator 4, the second heat exchanger 12, the hot high-pressure gas-air cooler 5, the cold high-pressure separator 6, the cyclone 13, the desulfurizing tower 7, the hot low-pressure separator 8, the hot low-pressure gas-air cooler 9 and the cold low-pressure separator 10 separate gas, oil and water from wax oil discharged from the reactor 2, the sulfur-containing sewage tank 11 stores separated sewage, and the obtained modified wax oil is sent to a catalytic system for catalytic cracking.
The oil inlet of wax oil filter 14 communicates wax oil feed system, and the oil-out of wax oil filter 14 communicates the inlet of wax oil buffer tank 15, and the oil jack of wax oil charge pump 16 is connected to the liquid outlet of wax oil buffer tank 15, and the filter screen of wax oil filter 14 needs regularly to wash the change, avoids the filter screen to be blockked up. An oil outlet of the wax oil feeding pump 16 is connected with a cold liquid inlet of the first heat exchanger 3, a cold liquid outlet of the first heat exchanger 3 is connected with an inlet of the heating furnace 1, a hot liquid inlet of the first heat exchanger 3 is connected with a liquid outlet of the reactor 2, a hot liquid outlet of the first heat exchanger 3 is connected with a liquid inlet of the thermal high-pressure separator 4, an outlet of the heating furnace 1 is connected with a liquid inlet of the reactor 2, an air inlet of the reactor 2 is communicated with a hydrogen supply pipeline of the diesel hydrogenation system, hydrogen supplied by the hydrogen supply pipeline of the diesel hydrogenation system enters the reactor 2 and then reacts with wax oil, and the reaction releases heat, so that the temperature of the wax oil in the reactor 2 is increased.
The upper outlet of the hot high-pressure separator 4 is connected with a hot gas inlet of a second heat exchanger 12, a hot gas outlet of the second heat exchanger 12 is connected with an inlet of a hot high-pressure gas-distributing air cooler 5, the inlet of the hot high-pressure gas-distributing air cooler 5 is also communicated with a demineralized water supply pipeline of a diesel hydrogenation system, a cold gas inlet of the second heat exchanger 12 is communicated with a hydrogen supply pipeline of the diesel hydrogenation system, a cold gas outlet of the second heat exchanger 12 is communicated with a cold night inlet of the first heat exchanger 3, and hydrogen is preheated by the second heat exchanger 12, mixed with wax oil supplied by a wax oil feed pump 16, and then enters the first heat exchanger 3 to be preheated again. The outlet of the hot high-pressure gas-air cooler 5 is connected with the liquid inlet of the cold high-pressure separator 6, the sewage outlet of the cold high-pressure separator 6 is connected with the sulfur-containing sewage tank 11, the upper outlet of the cold high-pressure separator 6 is connected with the liquid inlet of the cyclone 13, the cold high-pressure separator 6 is used for separating the liquid input into the cold high-pressure separator 6 from gas, oil and water, the sulfur-containing sewage is discharged from the sewage outlet of the cold high-pressure separator 6, the gas is discharged from the upper outlet of the cold high-pressure separator 6, and the oil is discharged from the lower outlet of the cold high-pressure separator 6. The lower outlet of the cyclone 13 is connected with the liquid inlet of the cold low-pressure separator 10, the upper outlet of the cyclone 13 is connected with the liquid inlet of the desulfurizing tower 7, the lean amine liquid inlet of the desulfurizing tower 7 is communicated with the lean amine liquid pipeline of the diesel hydrogenation system, the lean amine liquid flows into the desulfurizing tower 7 from the lean amine liquid pipeline of the diesel hydrogenation system, the gas outlet of the desulfurizing tower 7 is communicated with the circulating hydrogen pipeline of the diesel hydrogenation system, the gas discharged from the desulfurizing tower 7 enters the circulating hydrogen pipeline of the diesel hydrogenation system, the rich amine liquid outlet of the desulfurizing tower 7 is communicated with the sulfur recovery system, and the rich amine liquid discharged from the desulfurizing tower 7 enters the sulfur recovery system.
The bottom outlet of the hot high-pressure separator 4 is connected with the liquid inlet of a hot low-pressure separator 8, the upper outlet of the hot low-pressure separator 8 is connected with the inlet of a hot low-pressure air cooler 9, the outlet of the hot low-pressure air cooler 9 and the lower outlet of a cold high-pressure separator 6 are respectively connected with the liquid inlet of a cold low-pressure separator 10, the upper outlet of the cold low-pressure separator 10 is communicated with a cold low-pressure gas discharge pipeline of a diesel hydrogenation system, cold low-pressure gas discharged from the upper outlet of the cold low-pressure separator 10 enters the cold low-pressure gas discharge pipeline of the diesel hydrogenation system, the sewage outlet of the cold low-pressure separator 10 is connected with a sulfur-containing sewage tank 11, the lower outlet of the cold low-pressure separator 10 and the lower outlet of the hot low-pressure separator 8 are respectively connected with a wax oil catalytic system, and wax oil after being modified is conveyed to the wax oil catalytic system.
The above examples merely represent some embodiments of the present invention, and the description thereof is more specific and detailed, but not to be construed as limiting the scope of the present invention.
Claims (5)
1. A wax oil hydrogenation upgrading system is characterized in that: the device comprises a heating furnace, a reactor, a first heat exchanger, a hot high-pressure separator, a hot high-pressure-component gas-air cooler, a cold high-pressure separator, a desulfurizing tower, a hot low-pressure separator, a hot low-pressure-component gas-air cooler, a cold low-pressure separator and a sulfur-containing sewage tank, wherein an outlet of the heating furnace is connected with a liquid inlet of the reactor, an air inlet of the reactor is communicated with a hydrogen supply pipeline of a diesel hydrogenation system, a liquid outlet of the reactor is communicated with a hot liquid inlet of the first heat exchanger, a cold liquid inlet of the first heat exchanger is connected with a wax oil supply system, a cold liquid outlet of the first heat exchanger is connected with an inlet of the heating furnace, and a hot liquid outlet of the first heat exchanger is connected with a liquid inlet of the; the upper outlet of the hot high-pressure separator is connected with the inlet of the hot high-pressure gas-distributing air cooler, the outlet of the hot high-pressure gas-distributing air cooler is connected with the liquid inlet of the cold high-pressure separator, the drain outlet of the cold high-pressure separator is connected with the sulfur-containing sewage tank, the upper outlet of the cold high-pressure separator is connected with the liquid inlet of the desulfurizing tower, the lean amine liquid inlet of the desulfurizing tower is communicated with the lean amine liquid pipeline of the diesel hydrogenation system, the gas outlet of the desulfurizing tower is communicated with the circulating hydrogen pipeline of the diesel hydrogenation system, and the rich amine liquid outlet of the desulfurizing tower is communicated with the sulfur recovery system; the bottom exit linkage of hot high pressure separator the inlet of hot low pressure separator, the upper portion exit linkage of hot low pressure separator the entry of hot low branch gas air cooler, the export of hot low branch gas air cooler with the lower part export of cold high pressure separator is connected respectively the inlet of cold low pressure separator, the upper portion export intercommunication diesel oil hydrogenation system's of cold low branch gas discharge pipeline, the drain of cold low pressure separator is connected contain the sulphur sewage jar, the lower part export of cold low pressure separator with the lower part export of hot low pressure separator is connected wax oil catalytic system respectively.
2. The wax oil hydro-upgrading system according to claim 1, wherein: the wax oil supply system is characterized in that a wax oil filter, a wax oil buffer tank and a wax oil feeding pump are arranged between the cold night inlet of the first heat exchanger and the wax oil supply system, the wax oil filter, the wax oil buffer tank and the wax oil feeding pump are sequentially connected, the oil outlet of the wax oil feeding pump is communicated with the cold night inlet of the first heat exchanger, and the oil inlet of the wax oil filter is communicated with the wax oil supply system.
3. The wax oil hydro-upgrading system according to claim 1, wherein: the high-pressure separator is characterized in that a second heat exchanger is arranged between the high-pressure separator and the high-pressure gas-distributing air cooler, a hot gas inlet of the second heat exchanger is communicated with an upper outlet of the high-pressure separator, a hot gas outlet of the second heat exchanger is communicated with an inlet of the high-pressure gas-distributing air cooler, a cold gas inlet of the second heat exchanger is communicated with a hydrogen supply pipeline of a diesel hydrogenation system, and a cold gas outlet of the second heat exchanger is communicated with a cold night inlet of the first heat exchanger.
4. A wax oil hydro-upgrading system according to claim 3, wherein: a cyclone is arranged between the cold high-pressure separator and the desulfurizing tower, a liquid inlet of the cyclone is connected with an upper outlet of the cold high-pressure separator, an upper outlet of the cyclone is connected with a liquid inlet of the desulfurizing tower, and a lower outlet of the cyclone is connected with a liquid inlet of the cold low-pressure separator.
5. The wax oil hydro-upgrading system according to claim 1, wherein: and the inlet of the hot high-pressure-distribution air cooler is communicated with a desalted water supply pipeline of a diesel hydrogenation system.
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| CN202010959933.9A CN111996035A (en) | 2020-09-14 | 2020-09-14 | Wax oil hydrogenation upgrading system |
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| CN202010959933.9A CN111996035A (en) | 2020-09-14 | 2020-09-14 | Wax oil hydrogenation upgrading system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114133957A (en) * | 2021-11-10 | 2022-03-04 | 中国石油化工股份有限公司 | Catalytic diesel oil hydrogenation modification system and modification method thereof |
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| CN101412926A (en) * | 2007-10-18 | 2009-04-22 | 中国石油化工股份有限公司 | Hydro-upgrading combined method |
| CN104312625A (en) * | 2014-09-30 | 2015-01-28 | 中国石油化工股份有限公司 | Energy-saving type wax oil hydrogenation equipment in petrochemical industry |
| CN211227031U (en) * | 2020-01-06 | 2020-08-11 | 孟祥雷 | Wax oil hydrogenation device for petrochemical industry |
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2020
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| CN101412926A (en) * | 2007-10-18 | 2009-04-22 | 中国石油化工股份有限公司 | Hydro-upgrading combined method |
| CN104312625A (en) * | 2014-09-30 | 2015-01-28 | 中国石油化工股份有限公司 | Energy-saving type wax oil hydrogenation equipment in petrochemical industry |
| CN211227031U (en) * | 2020-01-06 | 2020-08-11 | 孟祥雷 | Wax oil hydrogenation device for petrochemical industry |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114133957A (en) * | 2021-11-10 | 2022-03-04 | 中国石油化工股份有限公司 | Catalytic diesel oil hydrogenation modification system and modification method thereof |
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Application publication date: 20201127 |