CN110499190B - Residual oil hydrotreating system and residual oil hydrotreating method - Google Patents
Residual oil hydrotreating system and residual oil hydrotreating method Download PDFInfo
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- CN110499190B CN110499190B CN201810473712.3A CN201810473712A CN110499190B CN 110499190 B CN110499190 B CN 110499190B CN 201810473712 A CN201810473712 A CN 201810473712A CN 110499190 B CN110499190 B CN 110499190B
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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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- 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
- C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1077—Vacuum residues
-
- 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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
Abstract
The invention discloses a residual oil hydrotreating system and a residual oil hydrotreating method, and belongs to the field of petroleum processing. The system comprises: residual oil hydrogenation reaction device; the inlet of the thermal high-pressure separator is communicated with the outlet of the residual oil hydrogenation reaction device; the inlet of the hot low-pressure separator is communicated with the liquid outlet of the hot high-pressure separator; the first inlet and the second inlet are respectively communicated with an exhaust port and a liquid outlet of the thermal low-pressure separator; the shell side inlet is communicated with the exhaust port of the hot high-pressure separator, the first outlet and the second outlet of the residual oil hydrogenation fractionation device; the inlet of the hydrofining reaction device is communicated with the shell pass outlet of the heat exchange device, and the outlet of the hydrofining reaction device is communicated with the tube pass inlet of the heat exchange device; the inlet of the cold high-pressure separator is communicated with the tube pass outlet of the heat exchange device; the inlet of the cold low-pressure separator is communicated with the liquid outlet of the cold high-pressure separator; the inlet of the hydrorefining fractionating device is communicated with the liquid outlet of the cold low-pressure separator; and the hydrogenation pipeline is communicated with the inlets of the residual oil hydrogenation reaction device and the hydrofining reaction device.
Description
Technical Field
The invention relates to the field of petroleum processing, in particular to a residual oil hydrotreating system and a residual oil hydrotreating method.
Background
The residual oil is residual oil obtained by vacuum distillation of crude oil and is commonly used for preparing products such as naphtha, diesel oil and the like. Because the residual oil contains a large amount of harmful substances such as sulfur, nitrogen, metal and the like, the residual oil is usually treated by a residual oil hydrogenation process, so that the residual oil reacts to generate a hydrogenation product, the hydrocarbon ratio of naphtha and diesel oil is improved, the residual carbon content is reduced, and the cracking performance is improved. Based on the above, it is necessary to provide a residual oil hydrotreating system.
The prior art provides a residuum hydroprocessing system, comprising: a hydrogenation line; the inlet of the residual oil hydrogenation reaction device is communicated with the hydrogenation pipeline and is used for enabling the residual oil to react to generate a first-stage hydrogenation product; the inlet of the thermal high-pressure separator is communicated with the outlet of the residual oil hydrogenation reaction device and is used for separating the primary hydrogenation product into thermal high-pressure separation gas and thermal high-pressure separation liquid; the inlet of the cooler is communicated with the exhaust port of the hot high-pressure separator and is used for cooling hot high-pressure gas; the inlet of the cold high-pressure separator is communicated with the outlet of the cooler and is used for separating the cooled hot high-pressure gas into cold high-pressure gas and cold high-pressure liquid; the inlet of the cold low-pressure separator is communicated with the liquid outlet of the cold high-pressure separator and is used for separating the cold high-pressure liquid into cold low-pressure gas and cold low-pressure liquid; the inlet of the thermal low-pressure separator is communicated with the liquid outlet of the thermal high-pressure separator and is used for separating the thermal high-pressure gas into thermal low-pressure gas and thermal low-pressure liquid; the first inlet, the second inlet and the third inlet are respectively communicated with a liquid outlet of the cold low-pressure separator, a liquid outlet of the hot low-pressure separator and an exhaust port, and the fractionating device is used for separating hot low-pressure gas, hot low-pressure liquid and cold low-pressure liquid into naphtha products, diesel oil products, hydrogenation residual oil and gas.
The inventor finds that the prior art has at least the following problems:
after the residual oil is treated by the residual oil hydrotreating system, the sulfur content of the separated naphtha product is 50 wppm-200 wppm, and the requirement of a catalytic reforming device on feeding can not be met; the sulfur content of the diesel product is 300 wppm-500 wppm, and the national VI standard of diesel and gasoline can not be met; meanwhile, the cetane number is 40-45, which affects the use performance of diesel oil products, so that naphtha products and diesel oil products need to be further processed by a diesel oil hydrogenation device, and the construction investment and the operation cost are increased.
Disclosure of Invention
The embodiment of the invention provides a residual oil hydrotreating system and a residual oil hydrotreating method, which can solve the problems. The technical scheme is as follows:
in one aspect, a resid hydrotreating system is provided, the treating system comprising: the residual oil hydrogenation reaction device is used for reacting residual oil to generate a primary hydrogenation product;
the inlet of the thermal high-pressure separator is communicated with the outlet of the residual oil hydrogenation reaction device and is used for separating the primary hydrogenation product into thermal high-pressure separation gas and thermal high-pressure separation liquid;
the inlet of the thermal low-pressure separator is communicated with the liquid outlet of the thermal high-pressure separator and is used for separating the thermal high-pressure liquid into thermal low-pressure gas and thermal low-pressure liquid;
the residual oil hydrogenation fractionation device is communicated with the exhaust port and the liquid discharge port of the thermal low-pressure separator through a first inlet and a second inlet respectively, and is used for separating the thermal low-pressure gas and the thermal low-pressure liquid into primary naphtha, primary diesel oil, hydrogenation residual oil and gas;
the shell side inlet is communicated with the exhaust port of the hot high-pressure separator, the first outlet and the second outlet of the residual oil hydrogenation fractionation device, and the heat exchange devices are used for heating the hot high-pressure separation gas, the first-stage naphtha and the first-stage diesel;
the inlet of the hydrofining reaction device is communicated with the shell pass outlet of the heat exchange device and is used for enabling the heated primary naphtha, the heated primary diesel oil and the heated high-molecular gas to react to generate a secondary hydrogenation product, and the outlet of the hydrofining reaction device is communicated with the tube pass inlet of the heat exchange device and is used for cooling the secondary hydrogenation product;
the inlet of the cold high-pressure separator is communicated with the tube pass outlet of the heat exchange device and is used for separating the cooled secondary hydrogenation product into cold high-pressure gas and cold high-pressure liquid;
the inlet of the cold low-pressure separator is communicated with the liquid outlet of the cold high-pressure separator and is used for separating the cold high-pressure liquid into cold low-pressure liquid and cold low-pressure liquid;
the inlet of the hydrofining and fractionating device is communicated with the liquid outlet of the cold low-pressure separator and is used for separating the cold low-pressure liquid into naphtha products, diesel products and gas;
and a hydrogenation pipeline communicated with the residual oil hydrogenation reaction device and the inlet of the hydrofining reaction device.
In one possible design, the hydrofinishing reaction unit includes: a shell, at least one catalyst bed;
the catalyst bed layer is arranged in the shell;
the inlet of the shell is communicated with the hydrogenation pipeline and the shell pass outlet of the heat exchange device, and the outlet is communicated with the tube pass inlet of the heat exchange device.
In one possible design, the number of catalyst beds is 1 to 3.
In one possible design, when the catalyst bed is provided in plurality, a plurality of the catalyst beds are provided at intervals in the axial direction of the casing.
In one possible design, the residuum hydroprocessing reaction unit includes: at least one residuum hydrogenation reactor;
when a plurality of residual oil hydrogenation reactors are arranged, the plurality of residual oil hydrogenation reactors are sequentially communicated according to the flow direction of the residual oil, and the inlets of the plurality of residual oil hydrogenation reactors are communicated with the hydrogenation pipeline.
In one possible design, the number of the residual oil hydrogenation reactors is 1-7.
In one possible design, the vent of the cold high pressure separator is in communication with the hydrogenation line for discharging the cold high partial gas into the hydrogenation line.
In one possible design, the processing system further includes: and the inlet of the desulfurization device is communicated with the exhaust port of the cold high-pressure separator, and the outlet of the desulfurization device is communicated with the hydrogenation pipeline.
In one possible design, the processing system further includes: and an inlet of the cooler is communicated with a tube side outlet of the heat exchange device, and an outlet of the cooler is communicated with an inlet of the cold high-pressure separator.
In another aspect, a process for hydrotreating a residuum is also provided, the process comprising:
conveying residual oil into a residual oil hydrogenation reaction device, and conveying hydrogen into the residual oil hydrogenation reaction device by using a hydrogenation pipeline to react the residual oil to generate a primary hydrogenation product;
separating the first-stage hydrogenation product into a hot high-pressure separation gas and a hot high-pressure separation liquid by using a hot high-pressure separator;
separating the hot high-separation liquid into hot low-separation gas and hot low-separation liquid by using a hot low-pressure separator;
separating the hot low-fraction gas and the hot low-fraction liquid into primary naphtha, primary diesel oil, hydrogenated residual oil and gas by using a residual oil hydrogenation fractionation device;
heating the hot high-molecular gas, the primary naphtha and the primary diesel oil in the shell pass by using a heat exchange device, and cooling a secondary hydrogenation product which is from a hydrofining reaction device and is positioned in the tube pass;
conveying hydrogen into the hydrofining reaction device by utilizing the hydrofining reaction device and the hydrogenation pipeline, and reacting the heated hot high-molecular gas, primary naphtha and primary diesel to generate a secondary hydrogenation product;
separating the cooled secondary hydrogenation product into cold high-pressure gas and cold high-pressure liquid by using a cold high-pressure separator;
separating the cold high-liquid into cold low-liquid and cold low-liquid by using a cold low-pressure separator;
and fractionating the cold low-fraction liquid into a naphtha product, a diesel product and a gas by using a hydrofining fractionating device.
In one possible design, the residuum hydroprocessing reaction unit is operated at a pressure of 17.5MPag to 18.5 MPag;
the operating pressure of the hot high-pressure separator is 15.3 MPag-16.3 MPag, and the operating temperature is 330-350 ℃;
the operating pressure of the hot low-pressure separator is 2.4 MPag-3.4 MPag, and the operating temperature is 330-360 ℃;
the operating pressure of the hydrofining reaction device is 9.5 MPag-10.5 MPag, and the operating temperature is 330-350 ℃;
the operating pressure of the cold high-pressure separator is 7.1 MPag-8.1 MPag, and the operating temperature is 40-60 ℃;
the operation pressure of the cold low-pressure separator is 2.3 MPag-3.3 MPag, and the operation temperature is 40-60 ℃.
The technical scheme provided by the embodiment of the invention has the following beneficial effects:
according to the residual oil hydrotreating system provided by the embodiment of the invention, the residual oil hydrotreating device is arranged between the hot low-pressure separator and the heat exchange device, and the hydrofining reaction device is arranged between the heat exchange device and the cold high-pressure separator, so that the first-stage diesel oil and the first-stage naphtha in the hot high-pressure gas and the hot low-pressure liquid can be hydrotreated to reduce the sulfur content of a diesel oil product and a naphtha product, wherein the sulfur content of the naphtha product can be less than 0.5wppm, the sulfur content of the diesel oil product can be less than 10wppm, and the cetane number of the diesel oil product is more than 51. The residual oil hydrotreating system provided by the embodiment of the invention can enable a naphtha product separated from residual oil to meet the feeding requirement of a catalytic reforming device, simultaneously enable a diesel product to meet the national VI standard of diesel oil and gasoline, improve the service performance of the diesel product, avoid secondary processing of the diesel product and the naphtha product, further avoid additional use of devices for feeding, separation, fractionation, discharging and the like, and reduce construction investment and operation cost.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings needed to be used in the description of the embodiments will be briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without creative efforts.
FIG. 1 is a schematic diagram of a residuum hydroprocessing system of the type provided by an embodiment of the present invention;
FIG. 2 is a schematic structural diagram of a hydrorefining reaction apparatus according to an embodiment of the present invention;
FIG. 3 is a schematic diagram of another type of resid hydrotreating system in accordance with an embodiment of the present invention.
Wherein the various reference numbers in the drawings are described below:
1-residual oil hydrogenation reaction device;
2-a hot high pressure separator;
3-a hot low pressure separator;
4-residuum hydro-fractionation unit;
5-a heat exchange device;
6-a hydrofining reaction device;
601-a housing;
602-catalyst bed layer;
7-a cold high-pressure separator;
8-a cold low pressure separator;
9-hydrofining fractionation unit;
10-a hydrogenation line;
11-a desulfurization unit;
12-cooler.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, embodiments of the present invention will be described in detail with reference to the accompanying drawings.
In one aspect, an embodiment of the present invention provides a residual oil hydrotreating system, as shown in fig. 1, including: a residual oil hydrogenation reaction device 1 for reacting residual oil to generate a first-stage hydrogenation product; the inlet of the thermal high-pressure separator 2 is communicated with the outlet of the residual oil hydrogenation reaction device 1 and is used for separating the first-stage hydrogenation product into thermal high-pressure separation gas and thermal high-pressure separation liquid; the inlet of the thermal low-pressure separator 3 is communicated with the liquid outlet of the thermal high-pressure separator 2 and is used for separating the thermal high-pressure liquid into thermal low-pressure gas and thermal low-pressure liquid; the residual oil hydrogenation fractionation device 4 is communicated with an exhaust port and a liquid discharge port of the thermal low-pressure separator 3 through a first inlet and a second inlet respectively, and is used for separating thermal low-fraction gas and thermal low-fraction liquid into primary naphtha, primary diesel oil, hydrogenation residual oil and gas; the heat exchange device 5 is communicated with the exhaust port of the hot high-pressure separator 2, the first outlet and the second outlet of the residual oil hydrogenation fractionation device 4 at the shell pass inlet and is used for heating hot high-pressure gas, primary naphtha and primary diesel oil; a hydrofining reaction device 6 with an inlet communicated with a shell pass outlet of the heat exchange device 5 and used for enabling the heated primary naphtha, the heated primary diesel and the heated high-molecular gas to react to generate a secondary hydrogenation product, and the outlet is communicated with a tube pass inlet of the heat exchange device 5 and used for cooling the secondary hydrogenation product; a cold high-pressure separator 7 with an inlet communicated with the tube pass outlet of the heat exchange device 5 and used for separating the cooled secondary hydrogenation product into cold high-pressure gas and cold high-pressure liquid; the inlet of the cold low-pressure separator 8 is communicated with the liquid outlet of the cold high-pressure separator 7 and is used for separating the cold high-pressure liquid into cold low-pressure gas and cold low-pressure liquid; a hydrofining fractionating device 9 with an inlet communicated with a liquid outlet of the cold low-pressure separator 8 and used for separating cold low-pressure liquid into naphtha products, diesel products and gas; and a hydrogenation pipeline 10 communicated with the inlets of the residual oil hydrogenation reaction device 1 and the hydrofining reaction device 6.
The following description is given of the working principle and effect of the residue hydrotreating system provided in the embodiment of the present invention:
when the hydrogenation reactor is used, residual oil is conveyed into the residual oil hydrogenation reactor 1, and hydrogen is conveyed into the residual oil hydrogenation reactor 1 by using the hydrogenation pipeline 10, so that the residual oil reacts to generate a primary hydrogenation product. The first-stage hydrogenation product flows into a thermal high-pressure separator 2 through an outlet of the residual oil hydrogenation reaction device 1 to be separated into thermal high-pressure separation gas and thermal high-pressure separation liquid.
The hot high-pressure liquid flows into the hot low-pressure separator 3 through a liquid outlet of the hot high-pressure separator 2 to be separated into hot low-pressure gas and hot low-pressure liquid. Wherein, the hot low-fraction gas and the hot low-fraction liquid flow into the residual oil hydrogenation fractionation device 4 to be separated into primary naphtha, primary diesel oil, hydrogenation residual oil and gas.
The hot high-molecular gas, the primary naphtha and the primary diesel oil flow into the shell pass of the heat exchange device 5, and exchange heat with the previous round of secondary hydrogenation products (namely, the secondary hydrogenation products from the hydrofining reaction device 6) in the tube pass to heat the hot high-molecular gas, the primary naphtha and the primary diesel oil and cool the previous round of secondary hydrogenation products.
The heated hot high-molecular gas, the first-stage naphtha and the first-stage diesel oil enter a hydrofining reaction device 6, and hydrogen is conveyed into the hydrofining reaction device 6 by a hydrogenation pipeline 10, so that the hot high-molecular gas, the first-stage naphtha and the first-stage diesel oil react to generate a second-stage hydrogenation product of the current round.
And the secondary hydrogenation product of the current round enters a tube pass of the heat exchange device 5 to exchange heat with the hot high-temperature gas, the primary naphtha and the primary diesel oil of the next round so as to cool the secondary hydrogenation product of the current round.
And the cooled secondary hydrogenation product of the current wheel enters a cold high-pressure separator 7 for separation so as to be separated into cold high-pressure separation gas and cold high-pressure separation liquid. Wherein, the cold high-pressure liquid flows into a cold low-pressure separator 8 through a liquid outlet of the cold high-pressure separator 7 for separation so as to be separated into cold low-pressure gas and cold low-pressure liquid.
The cold low-pressure liquid flows into a hydrofining fractionating device 9 through a liquid outlet of the cold low-pressure separator 8 for separation so as to be separated into naphtha products, diesel products and gas.
It should be noted that the gas separated by the residue hydro-fractionation unit 4 and the hydrofinishing fractionation unit 9 mainly contains H2Light hydrocarbon (C)1～C4)、H2S; the cold high-pressure gas mainly comprises: h2Light hydrocarbon (C)1～C4)、H2S; the cold low-pressure gas mainly comprises: h2Light hydrocarbon (C)1～C4)、H2S; the hot high-pressure gas mainly comprises: h2Light hydrocarbon (C)1～C4)、H2S, naphtha and diesel oil; the hot low-temperature gas mainly comprises: h2Light hydrocarbon (C)1～C4)、H2S; the hot high-speed liquid mainly comprises: h2Light hydrocarbon (C)1～C2) Diesel oil, hydrogenated residue oil; the hot low-temperature liquid comprises: diesel oil, hydrogenated residual oil; the cold high-liquid separation comprises the following steps: h2Light hydrocarbon (C)1～C4)、H2S, naphtha and diesel oil; the cold low-liquid comprises the following components: h2Light hydrocarbon (C)1～C4)、H2S, naphtha and diesel oil. In addition, the primary naphtha has the same components as the naphtha product, but the concentration of harmful substances in the primary naphtha is greater than that in the naphtha product; the concentration of harmful substances in the first-grade diesel oil is greater than that of the diesel oil product.
According to the residual oil hydrotreating system provided by the embodiment of the invention, the residual oil hydrotreating device 4 is arranged between the hot low-pressure separator 3 and the heat exchange device 5, and the hydrofining reaction device 6 is arranged between the heat exchange device 5 and the cold high-pressure separator 7, so that the first-stage diesel oil and the first-stage naphtha in the hot high-fraction gas and the hot low-fraction liquid can be hydrotreated to reduce the sulfur content of a diesel oil product and a naphtha product, wherein the sulfur content of the naphtha product can be less than 0.5wppm, the sulfur content of the diesel oil product can be less than 10wppm, and the cetane number of the diesel oil product is more than 51.
Therefore, the residual oil hydrotreating system provided by the embodiment of the invention can enable the naphtha product separated from the residual oil to meet the feeding requirement of the catalytic reforming device, simultaneously enable the diesel oil product to meet the national VI standard of diesel oil and gasoline, improve the service performance of the diesel oil product, avoid secondary processing of the diesel oil product and the naphtha product, further avoid additional use of devices such as feeding, separation, fractionation and discharging, and reduce the construction investment and the operation cost.
On the premise of simple structure, as shown in fig. 2, the hydrorefining reaction apparatus 6 includes: a shell 601, at least one catalyst bed 602; the catalyst bed 602 is arranged in the shell 601; the inlet of the shell 601 is communicated with the hydrogenation pipeline 10 and the shell pass outlet of the heat exchange device 5, and the outlet is communicated with the tube pass inlet of the heat exchange device 5.
Wherein the catalyst bed 602 may be mounted within the housing 601 through a grid. It will be appreciated that the baffle plate abuts against the inner wall of the shell 601 to prevent catalyst particles in the catalyst bed 602 from flowing from the gap between the baffle plate and the shell 601 to the bottom of the shell 601, thereby preventing the catalyst particles from blocking the outlet at the bottom of the shell 601; and the pore diameters of the plurality of vent holes on the grid plate are smaller than the particle size of the catalyst particles of the catalyst bed layer 602, so that the catalyst particles can be prevented from falling to block the outlet of the shell 601.
The grid plate can be welded in the shell 601, and is convenient to produce and process.
In addition, the structure of the housing 601 may be variously configured, for example, the housing 601 includes: the spherical upper end enclosure, the cylinder and the spherical lower end enclosure are smoothly communicated from top to bottom; the upper end enclosure and the lower end enclosure are respectively welded on the upper end and the lower end of the cylinder body.
A manhole may be provided in the casing 601 to facilitate the mounting and dismounting of the hydrorefining reactor 6.
Regarding the number of catalyst beds 602, in the embodiment of the present invention, the number of catalyst beds 602 is 1 to 3, for example, 1, 2, or 3 catalyst beds 602 may be provided. Through such setting, can carry out effective processing to hot high branch gas, first-order naphtha, first-order diesel oil, can avoid the waste of catalyst again.
When the catalyst beds 602 are arranged in plurality, the catalyst beds 602 are arranged at intervals along the axial direction of the shell 601, so that the hot high-pressure gas, the first-stage naphtha and the first-stage diesel oil can smoothly pass through the catalyst beds 602, and the pressure loss of the hot high-pressure gas, the first-stage naphtha and the first-stage diesel oil is reduced.
In the embodiment of the present invention, the residue hydrogenation reaction apparatus 1 includes: at least one residuum hydrogenation reactor; when a plurality of residual oil hydrogenation reactors are arranged, the plurality of residual oil hydrogenation reactors are sequentially communicated according to the flow direction of residual oil, and the inlets of the plurality of residual oil hydrogenation reactors are communicated with the hydrogenation pipeline 10.
The structure of the residual oil hydrogenation reactor may be the same as that of the hydrofining reaction device 6, except that the kind of the catalyst in the inner catalyst bed 602 is different, for example, the kind of the catalyst of the residual oil hydrogenation reactor is a protective agent, a hydrodemetallization catalyst, a hydrodesulfurization catalyst, and a hydrodecarbonization catalyst; the catalyst types of the hydrorefining reaction device 6 are a protective agent and a hydrodesulfurization catalyst.
In addition, in order to improve the treatment effect on the residual oil, in the embodiment of the present invention, the number of the residual oil hydrogenation reactors is 1 to 7, preferably 1 to 5, and for example, 1, 2, 3, 4, or 5 may be provided.
After the residual oil is subjected to hydrotreating and the thermal high-temperature-index gas, the first-level naphtha and the first-level diesel oil are subjected to hydrotreating, hydrogen does not completely participate in the reaction, if the hydrogen is directly discharged, the waste of the hydrogen can be caused, and the dehydrogenation cost is increased. To avoid this, in the embodiment of the present invention, as shown in fig. 1, the exhaust port of the cold high-pressure separator 7 is communicated with the hydrogenation line 10 for discharging the cold high-pressure gas into the hydrogenation line 10.
Further, in order to avoid the cold high-pressure gas discharged from the cold high-pressure separator 7 from contaminating the hydrogen gas in the hydrogenation line 10, in the embodiment of the present invention, as shown in fig. 3, the processing system further includes: and an inlet of the desulfurization device 11 is communicated with the exhaust port of the cold high-pressure separator 7, and an outlet of the desulfurization device is communicated with the hydrogenation pipeline 10.
In order to enhance the separation effect of the cold high-pressure separator 7 on the secondary hydrogenation product, as shown in fig. 3, the processing system further comprises: and an inlet of the cooler 12 is communicated with a tube side outlet of the heat exchange device 5, and an outlet of the cooler is communicated with an inlet of the cold high-pressure separator 7.
By the above arrangement, the secondary hydrogenation product can be cooled to a preset temperature (for example, 50 ℃) without affecting the heating of the hot high-molecular gas, the primary naphtha and the primary diesel.
In the embodiment of the present invention, the residue hydrocracking apparatus 4 and the hydrofinishing fractionation apparatus 9 are well known in the art and will not be described in detail herein.
In another aspect, an embodiment of the present invention further provides a residual oil hydrotreating method using the above residual oil hydrotreating system, where the method includes:
and (3) conveying residual oil into the residual oil hydrogenation reaction device 1, and conveying hydrogen into the residual oil hydrogenation reaction device 1 by using a hydrogenation pipeline 10 to react the residual oil to generate a primary hydrogenation product.
The first-stage hydrogenation product is separated into hot high-pressure separation gas and hot high-pressure separation liquid by using a hot high-pressure separator 2.
The hot high-pressure liquid is separated into hot low-pressure gas and hot low-pressure liquid by a hot low-pressure separator 3.
And separating the hot low-fraction gas and the hot low-fraction liquid into primary naphtha, primary diesel oil, hydrogenated residual oil and gas by using a residual oil hydrogenation fractionation device 4.
And heating the hot high-molecular gas, the primary naphtha and the primary diesel oil in the shell pass by using a heat exchange device 5, and cooling a secondary hydrogenation product which is from a hydrofining reaction device 6 and is positioned in the tube pass.
The hydrorefining reaction device 6 is utilized, and the hydrogenation pipeline 10 is utilized to convey hydrogen into the hydrorefining reaction device 6, so that the heated hot high-molecular gas, the primary naphtha and the primary diesel oil react to generate a secondary hydrogenation product.
And separating the cooled secondary hydrogenation product into cold high-pressure gas and cold high-pressure liquid by using a cold high-pressure separator 7.
The cold high-pressure liquid is separated into cold low-pressure gas and cold low-pressure liquid by using a cold low-pressure separator 8.
The cold low-fraction liquid is fractionated into a naphtha product, a diesel product and a gas by means of a hydrorefining fractionator 9.
In the embodiment of the present invention, in order to improve the quality of naphtha products and diesel products, the operating pressure of the residual oil hydrogenation reactor 1 is 17.5MPag to 18.5MPag (for example, 17.5MPag, 18MPag, 18.5MPag, etc.) may be set; the operating pressure of the hot high-pressure separator 2 is 15.3MPag to 16.3MPag (for example, 15.3MPag, 15.8MPag, 16.3MPag, etc. may be set), and the operating temperature is 330 ℃ to 350 ℃ (for example, 330 ℃, 340 ℃, 350 ℃, etc. may be set); the operating pressure of the hot low-pressure separator 3 is 2.4MPag to 3.4MPag (for example, 2.4MPag, 2.9MPag, 3.4MPag, etc. may be set), and the operating temperature is 330 ℃ to 350 ℃ (for example, 330 ℃, 340 ℃, 350 ℃, etc. may be set); the hydrorefining reactor 6 has an operating pressure of 9.5MPag to 10.5MPag (for example, 9.5MPag, 10MPag, 10.5MPag, etc. may be set), and an operating temperature of 330 ℃ to 350 ℃ (for example, 330 ℃, 340 ℃, 350 ℃, etc. may be set); the cold high-pressure separator 7 has an operating pressure of 7.1MPag to 8.1MPag (for example, 7.1MPag, 7.6MPag, 8.1MPag, etc. may be set), and an operating temperature of 40 ℃ to 60 ℃ (for example, 40 ℃, 50 ℃, 60 ℃, etc. may be set); the cold low-pressure separator 8 has an operating pressure of 2.3MPag to 3.3MPag (for example, 2.3MPag, 2.8MPag, 3.3MPag and the like may be set), and an operating temperature of 40 ℃ to 60 ℃ (for example, 40 ℃, 50 ℃, 60 ℃ and the like may be set).
All the above optional technical solutions may be combined arbitrarily to form the optional embodiments of the present disclosure, and are not described herein again.
The above description is only an illustrative embodiment of the present invention, and should not be taken as limiting the scope of the invention, and any modifications, equivalents, improvements and the like that are within the spirit and principle of the present invention should be included in the scope of the present invention.
Claims (7)
1. A residuum hydroprocessing system, characterized in that the processing system comprises: the residual oil hydrogenation reaction device (1) is used for reacting residual oil to generate a primary hydrogenation product;
the inlet of the thermal high-pressure separator (2) is communicated with the outlet of the residual oil hydrogenation reaction device (1) and is used for separating the first-stage hydrogenation product into thermal high-pressure separation gas and thermal high-pressure separation liquid;
the inlet of the hot low-pressure separator (3) is communicated with the liquid outlet of the hot high-pressure separator (2) and is used for separating the hot high-pressure liquid into hot low-pressure gas and hot low-pressure liquid;
the residual oil hydrogenation fractionation device (4) is communicated with the exhaust port and the liquid discharge port of the hot low-pressure separator (3) through a first inlet and a second inlet respectively, and is used for separating the hot low-pressure gas and the hot low-pressure liquid into primary naphtha, primary diesel oil, hydrogenated residual oil and gas;
the heat exchange device (5) is communicated with the exhaust port of the hot high-pressure separator (2), the first outlet and the second outlet of the residual oil hydrogenation fractionation device (4) at the shell side inlet and is used for heating the hot high-pressure separation gas, the primary naphtha and the primary diesel oil;
the inlet of the hydrofining reaction device (6) is communicated with the shell pass outlet of the heat exchange device (5) and is used for enabling the heated primary naphtha, the heated primary diesel and the heated high-temperature-distribution gas to react to generate a secondary hydrogenation product, and the outlet of the hydrofining reaction device is communicated with the tube pass inlet of the heat exchange device (5) and is used for cooling the secondary hydrogenation product;
the inlet of the cold high-pressure separator (7) is communicated with the tube pass outlet of the heat exchange device (5) and is used for separating the cooled secondary hydrogenation product into cold high-pressure separation gas and cold high-pressure separation liquid;
the inlet of the cold low-pressure separator (8) is communicated with the liquid outlet of the cold high-pressure separator (7) and is used for separating the cold high-pressure liquid into cold low-pressure gas and cold low-pressure liquid;
the inlet of the hydrofining and fractionating device (9) is communicated with the liquid outlet of the cold low-pressure separator (8) and is used for separating the cold low-pressure liquid into naphtha products, diesel products and gas;
and a hydrogenation pipeline (10) communicated with the inlets of the residue hydrogenation reaction device (1) and the hydrofining reaction device (6);
the processing system further comprises: the inlet of the desulfurization device (11) is communicated with the exhaust port of the cold high-pressure separator (7), and the outlet of the desulfurization device is communicated with the hydrogenation pipeline (10);
the processing system further comprises: the inlet of the cooler (12) is communicated with the tube side outlet of the heat exchange device (5), and the outlet of the cooler is communicated with the inlet of the cold high-pressure separator (7);
the hydrorefining reaction apparatus (6) comprises: a shell (601), at least one catalyst bed (602);
the catalyst bed (602) is arranged in the shell (601);
an inlet of the shell (601) is communicated with the hydrogenation pipeline (10) and a shell pass outlet of the heat exchange device (5), and an outlet is communicated with a tube pass inlet of the heat exchange device (5);
the catalyst bed layer (602) is arranged in the shell (601) through a grid plate, and the grid plate is abutted against the inner wall of the shell (601);
and the exhaust port of the cold high-pressure separator (7) is communicated with the hydrogenation pipeline (10) and is used for discharging the cold high-pressure gas into the hydrogenation pipeline (10).
2. The treatment system according to claim 1, wherein the number of catalyst beds (602) is 1 to 3.
3. The treatment system according to claim 1, wherein when the catalyst bed (602) is provided in plurality, a plurality of catalyst beds (602) are provided at intervals in the axial direction of the housing (601).
4. The treatment system according to claim 1, wherein the residue hydrogenation reaction unit (1) comprises: at least one residuum hydrogenation reactor;
when a plurality of residual oil hydrogenation reactors are arranged, the residual oil hydrogenation reactors are sequentially communicated according to the flow direction of the residual oil, and the inlets of the residual oil hydrogenation reactors are communicated with the hydrogenation pipeline (10).
5. The treatment system according to claim 4, wherein the number of the residual hydrogenation reactors is 1-7.
6. A process for the hydrotreatment of a residual oil, characterized in that it uses a treatment system according to any one of claims 1 to 5, said treatment process comprising:
conveying residual oil into a residual oil hydrogenation reaction device (1), and conveying hydrogen into the residual oil hydrogenation reaction device (1) by using a hydrogenation pipeline (10) to react the residual oil to generate a first-stage hydrogenation product;
separating the first-stage hydrogenation product into a hot high-pressure separation gas and a hot high-pressure separation liquid by using a hot high-pressure separator (2);
separating the hot high-separation liquid into hot low-separation gas and hot low-separation liquid by using a hot low-pressure separator (3);
separating the hot low-fraction gas and the hot low-fraction liquid into primary naphtha, primary diesel oil, hydrogenated residual oil and gas by using a residual oil hydrogenation fractionation device (4);
heating the hot high-molecular gas, the primary naphtha and the primary diesel in the shell pass by using a heat exchange device (5), and cooling a secondary hydrogenation product which is from a hydrofining reaction device (6) and is positioned in the tube pass;
utilizing the hydrofining reaction device (6) and the hydrogenation pipeline (10) to convey hydrogen into the hydrofining reaction device (6), so that the heated hot high-molecular gas, the primary naphtha and the primary diesel oil react to generate a secondary hydrogenation product;
separating the cooled secondary hydrogenation product into cold high-pressure gas and cold high-pressure liquid by using a cold high-pressure separator (7);
separating the cold high-liquid into cold low-liquid and cold low-liquid by using a cold low-pressure separator (8);
the cold low fraction is fractionated into a naphtha product, a diesel product and a gas by means of a hydrorefining fractionator (9).
7. The processing method according to claim 6,
the operating pressure of the residual oil hydrogenation reaction device (1) is 17.5 MPag-18.5 MPag;
the operating pressure of the hot high-pressure separator (2) is 15.3 MPag-16.3 MPag, and the operating temperature is 330-350 ℃;
the operating pressure of the hot low-pressure separator (3) is 2.4 MPag-3.4 MPag, and the operating temperature is 330-360 ℃;
the operating pressure of the hydrofining reaction device (6) is 9.5 MPag-10.5 MPag, and the operating temperature is 330-350 ℃;
the operating pressure of the cold high-pressure separator (7) is 7.1 MPag-8.1 MPag, and the operating temperature is 40-60 ℃;
the operation pressure of the cold low-pressure separator (8) is 2.3 MPag-3.3 MPag, and the operation temperature is 40-60 ℃.
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| CN1098337C (en) * | 2000-11-02 | 2003-01-08 | 中国石油天然气股份有限公司 | Normal pressure suspension bed hydrogenation process adopting liquid multiple-metal catalyst |
| CN101376840B (en) * | 2007-08-27 | 2011-10-12 | 中国石油化工股份有限公司 | Heavy fraction oil hydrotreating method |
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| CN103436290B (en) * | 2013-09-13 | 2015-05-27 | 王树宽 | Method for producing naphthenic base refrigerating machine oil base oil by using coal tar oil |
| CN103965960B (en) * | 2014-03-03 | 2015-11-18 | 北京华石联合能源科技发展有限公司 | A kind of heavy-oil hydrogenation prepares the technique of diesel oil and petroleum naphtha |
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| CN104946306B (en) * | 2015-05-26 | 2017-06-16 | 中国石油大学(华东) | A kind of full fraction of coal tar floating bed hydrocracking and fixed bed hydrogenation modification combined method |
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