CN109777504B - Refinery gas hydrogenation combination method - Google Patents
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Abstract
The invention discloses a refinery gas hydrogenation combination method, which comprises the following steps: (a) mixing the wax oil raw oil and the circulating oil with hydrogen in hydrogen dissolving equipment, and then entering a hydrogenation catalyst bed layer in a wax oil hydrogenation reactor to react under the condition of liquid-phase hydrogenation operation; (b) mixing the reactant flow obtained in the step (a) with refinery gas and hydrogen in a gas dissolving device, and then allowing the mixture to enter a hydrogenation catalyst bed layer in a supplementary hydrogenation reactor to react under the liquid-phase hydrogenation operation condition; (c) separating the hydrogenation reaction effluent in the step (b) into a gas phase and a liquid phase, continuously separating the gas phase obtained by separation after removing hydrogen sulfide to obtain hydrogen and hydrotreated refinery gas, fractionating the liquid phase obtained by separation to obtain naphtha, diesel oil and hydrogenated wax oil products, and returning part of the hydrogenation reaction effluent obtained in the step (a) and/or part of the hydrogenation reaction material flow obtained in the step (b) and/or part of the liquid phase obtained by separation of the high-pressure separator as circulating oil to hydrogen dissolving equipment. The method can simultaneously carry out hydrotreatment on refinery gas and produce hydrogenated wax oil.
Description
Technical Field
The invention belongs to a hydrogenation process of an oil refining technology, and relates to a refinery gas hydrogenation combination method, in particular to a hydrogenation combination method for refinery gas hydrotreating and hydrogenated wax oil production.
Background
Energy currently worldwide is derived primarily from fossil energy sources, with petroleum being the most prominent source of motor fuel. Petroleum belongs to non-renewable energy resources, resources are increasingly exhausted, the trend of heavy and poor petroleum is increased, the continuous development of world economy and the stricter environmental protection regulations require the production of a large amount of light clean fuel, and the improvement and improvement of the existing oil refining technology are required, and meanwhile, new petroleum substitutes are added, so that products meeting the requirements are produced at the lowest cost. Catalytic cracking is one of important means for the conversion of heavy oil into light oil, but with the deterioration and the heavy conversion of catalytic cracking processing raw materials, the operation conditions are more and more rigorous, the yield of light products and the properties of the products are poor, and the hydrotreating technology of the catalytic cracking raw materials can not only remove the contents of impurities such as sulfur, nitrogen, metals and the like, but also improve the cracking performance of feeding materials and reduce the severity of FCC operation; the product distribution is improved, and the selectivity of the target product is improved; the yield of dry gas and coke is reduced, and the economical efficiency of an FCC device is improved; the sulfur content of the target product is reduced; reduce the content of SOx and NOx in the regenerated flue gas, and the like.
The wax oil hydrogenation technology is the most important means for improving the quality of catalytic cracking products and realizing clean production, and the liquid phase wax oil hydrogenation technology can meet the requirement of clean diesel oil production under the condition of greatly reducing energy consumption. US6213835 and US6428686 disclose a hydrogenation process of pre-dissolved hydrogen, CN104560132A discloses a continuous liquid phase wax oil hydrotreating method, and CN104927902A discloses a wax oil hydrotreating method, which focuses more on dissolving hydrogen in the wax oil raw material, and these methods all dissolve hydrogen in the wax oil raw material to carry out hydrogenation reaction, and do not utilize the residual hydrogen, and directly treat it additionally after separation.
Refinery gases generally include dry gases, liquefied gases, and the like, and have various paths for their use. The main application comprises that dry gas is hydrogenated and then used as a raw material for preparing ethylene by steam cracking, liquefied gas is hydrogenated and then used as a raw material for preparing ethylene by steam cracking, a raw material for synthesizing maleic anhydride, liquefied gas for vehicles and the like. In the existing refinery gas hydrogenation technology, CN201410271572.3 discloses a coking dry gas hydrogenation catalyst and a catalyst grading method. The method only solves the problem of controlling the reaction temperature during the hydrogenation of the coking dry gas, but the temperature rise in the reaction process is large. CN201010221244.4 discloses a method for preparing ethylene cracking material by hydrogenation of liquefied petroleum gas, which comprises two reactors, a cooling facility is arranged between the reactors, and CN201310628425.2 discloses a high-temperature hydrogenation purification process of liquefied petroleum gas, wherein olefin saturation and hydrogenation are performed by hydrogenation to remove impurities. As is well known, the hydrogenation reaction of unsaturated hydrocarbons such as olefin, diene, alkyne and the like is a strong exothermic reaction, the temperature rise in the gas hydrogenation process is very large, generally 100-200 ℃, the balance of the hydrogenation reaction is damaged along with the temperature rise, and the generation of carbon deposition is seriously increased, so that the service cycle of the catalyst is reduced.
CN201010221263.7 discloses a liquefied petroleum gas-coker gasoline hydrogenation combination process method, which is a combination method, but not a liquid phase hydrogenation method, the coker gasoline is firstly mixed with hydrogen to carry out fixed bed hydrogenation reaction, and a hydrogenation product and liquefied gas are mixed and enter another reactor, so that the problem of hydrogenation temperature rise of the liquefied gas is only solved.
In summary, in the prior art, the hydrotreating process of refinery gas is a gas phase reaction, the wax oil hydrogenation is a liquid phase reaction, and the reaction types of the two are completely different, so the combined method of the hydrotreating process of refinery gas and the liquid phase hydrogenation of wax oil has been reported.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a hydrogenation combination method. The method can simultaneously carry out hydrotreatment on refinery gas and produce hydrogenated wax oil. The utilization efficiency of hydrogen is improved on the premise of further improving the quality of wax oil products, the problem of temperature rise in the hydrotreating process of refinery gas is effectively solved, the equipment investment is reduced overall, and the operation energy consumption is reduced.
The refinery gas hydrogenation combination method comprises the following steps:
(a) mixing the wax oil raw oil and the circulating oil with hydrogen in hydrogen dissolving equipment, and then entering a hydrogenation catalyst bed layer in a wax oil hydrogenation reactor to react under the condition of liquid-phase hydrogenation operation;
(b) mixing the reactant flow obtained in the step (a) with refinery gas and hydrogen in a gas dissolving device, and then allowing the mixture to enter a hydrogenation catalyst bed layer in a supplementary hydrogenation reactor to react under the liquid-phase hydrogenation operation condition;
(c) separating the hydrogenation reaction effluent in the step (b) into a gas phase and a liquid phase, continuously separating the gas phase obtained by separation after removing hydrogen sulfide to obtain hydrogen and hydrotreated refinery gas, fractionating the liquid phase obtained by separation to obtain naphtha, diesel oil and wax oil products, and returning part of the hydrogenation reaction effluent obtained in the step (a) and/or part of the hydrogenation reaction material flow obtained in the step (b) and/or part of the liquid phase obtained by separation of the high-pressure separator as circulating oil to hydrogen dissolving equipment.
In the above method, the wax oil raw material oil used may include one or more of straight-run wax oil, coker wax oil, thermally cracked wax oil, visbreaker wax oil, synthetic wax oil, coal tar wax oil fraction, coal direct liquefaction wax oil, shale oil wax oil, and other wax oil fractions, or may be a portion of catalytically cracked light cycle oil, naphthenic straight-run diesel, coal tar diesel fraction, and other inferior diesel fractions mixed in the wax oil raw material oil.
In the method, the hydrogenation operation condition is generally 3.0MPa to 20.0MPa of reaction pressure, and the volume space velocity of the wax oil raw material oil is 0.2h-1~8.0h-1The average reaction temperature is 180-450 ℃, and the ratio of the circulating oil to the wax oil raw oil is 0.5: 1-10: 1; the preferable operation conditions are that the reaction pressure is 4.0 MPa-18.0 MPa, and the volume space velocity of the wax oil raw material oil is 0.5h-1~6.0h-1The average reaction temperature is 200-440 ℃, and the ratio of the circulating oil to the wax oil raw oil is 0.6: 1-8: 1.
In the method, the supplementary hydrogenation operation condition is generally 3.0MPa to 20.0MPa of reaction pressure, and the volume space velocity of the wax oil raw material oil is 0.3h-1~40.0h-1The average reaction temperature is 180-450 ℃; the preferable operation conditions are that the reaction pressure is 4.0 MPa-18.0 MPa, and the volume space velocity of the wax oil raw material oil is 0.5h-1~30.0h-1The average reaction temperature is 200-440 ℃.
In the method, the hydrogenation active component in the hydrogenation catalyst is one or more of Co, Mo, W and Ni, the weight content of the hydrogenation active component is 5-70% by weight calculated by oxide, the carrier of the hydrogenation catalyst is generally alumina, amorphous silicon aluminum, silicon oxide, titanium oxide and the like, and other auxiliary agents such as P, Si, B, Ti, Zr and the like can be simultaneously contained. The catalyst may be used commercially or may be prepared by methods known in the art. The hydrogenation active component is a catalyst in an oxidation state, and is subjected to conventional vulcanization treatment before use, so that the hydrogenation active component is converted into a vulcanization state. The commercial hydrogenation catalysts mainly include hydrogenation catalysts such as 3926, 3936, CH-20, FF-14, FF-18, FF-24, FF-26, FF-36, FF-46, FF-56, FH-98, FH-UDS and FZC-41 developed by the Fushu petrochemical research institute (FRIPP), hydrogenation catalysts such as HR-406, HR-416 and HR-448 of IFP company, hydrogenation catalysts such as ICR154, ICR174, ICR178 and ICR179 of CLG company, hydrogenation catalysts such as HC-P, HC-K UF-210/220 newly developed by UOP company, hydrogenation catalysts such as TK-525, TK-555 and TK-557 of Topsor company, KF-752, KF-756, KF-757, KF-840, KF-848, KF-901, KF-907 and the like hydrogenation catalysts of AKZO corporation.
In the method, the catalyst bed layers of the hydrogenation reactor in the step (a) are arranged into a plurality of layers, preferably 2-8 layers, and a gas dissolving device is arranged between the adjacent catalyst bed layers; the introduced hydrogen is mixed with the reactant flow in the gas dissolving device and then enters the next catalyst bed layer for reaction.
In the above method, one or more catalyst beds, preferably 2 to 8 catalyst beds, may be provided in the make-up hydrogenation reactor. If only one catalyst bed layer is arranged in the supplementary hydrogenation reactor, the liquid-phase hydrogenation reaction material flow is mixed with the refinery gas in the gas dissolver and then enters the top of the supplementary hydrogenation reactor and passes through the catalyst bed layer; if a plurality of catalyst beds are arranged in the supplementary hydrogenation reactor, a gas dissolving device is arranged between the beds, refinery gas and hydrogen are mixed and then enter any gas dissolving device arranged between adjacent catalyst beds, and are mixed with reactant flow from the previous catalyst bed and then enter the next catalyst bed for reaction.
A preferred embodiment is as follows: the catalyst bed layers of the wax oil hydrogenation reactor are arranged into three layers, the catalyst bed layer of the supplementary hydrogenation reactor is arranged into two layers, hydrogen is introduced between the second catalyst and the third catalyst bed layer of the wax oil hydrogenation reactor, and hydrogen and refinery gas are introduced between the catalyst bed layers of the supplementary hydrogenation reactor.
In the method, the wax oil raw oil and the circulating oil are mixed and then enter from the top of the wax oil hydrogenation reactor, the mixed material flow with dissolved hydrogen can pass through the catalyst bed layer from top to bottom in a downward mode, the wax oil raw oil and the circulating oil can also enter from the bottom of the hydrogenation reactor after being mixed, and the mixed material flow with dissolved hydrogen can pass through the catalyst bed layer from bottom to top in an upward mode.
In the method, the mixed material flow of the wax oil hydrogenation reaction effluent dissolved with the refinery gas enters from the top of the supplementary hydrogenation reactor, the mixed material flow dissolved with the refinery gas can pass through the catalyst bed layer from top to bottom, the mixed material flow of the wax oil hydrogenation reaction effluent dissolved with the refinery gas can also enter from the bottom of the supplementary hydrogenation reactor, and the mixed material flow dissolved with the refinery gas can pass through the catalyst bed layer from bottom to top.
In the above method, the previous catalyst bed or the next catalyst bed is based on the flowing direction of the reactant flow, and whether the hydrogenation reaction is an upflow type or a downflow type, the bed in the adjacent beds which is contacted with the reactant flow first is an upper bed and then is a lower bed.
In the method, the refinery gas may comprise one or more of dry gas, liquefied gas and the like. The source of the gas can be one or more of coking, catalytic cracking, thermal cracking, visbreaking and the like.
In the method, if hydrogen and refinery gas are introduced simultaneously in any process, the volume ratio of the introduced hydrogen to the refinery gas is 1: 1-100: 1, preferably 1: 1-50: 1.
In the method, the hydrogenation reaction effluent is separated by a high-pressure separator and/or a low-pressure separator. The high-pressure separator is a conventional gas-liquid separator. The hydrogenation reaction flow is separated in a high-pressure separator to obtain gas and liquid. The low-pressure separator is a conventional gas-liquid separator. The liquid obtained by separation in the high-pressure separator is separated in the high-low pressure separator to obtain gas and liquid.
In the method, the fractionating system used for fractionating comprises a stripping tower and/or a fractionating tower. And the liquid obtained by separation in the low-pressure separator is subjected to steam stripping and/or fractionation in a fractionation system to obtain a naphtha product, a diesel oil product and a hydrogenated wax oil product.
In the above method, the gas separator used for gas separation is a conventional separator. The gas obtained by separation in the high-pressure separator and the gas obtained by separation in the low-pressure separator are mixed, hydrogen sulfide is removed, then hydrogen, dry gas, liquefied gas and the like are obtained by separation in the gas separator, and if liquid products exist, the gas directly enters a stripping tower and/or a fractionating tower.
In the process of gas hydrogenation, the temperature rise of a catalyst bed layer is large due to large reaction heat release, so that the temperature range of the hydrogenation reaction is large, the effect of the hydrogenation reaction is influenced, the generation of carbon deposition of the catalyst is accelerated, and the service cycle of the catalyst is shortened. In the wax oil liquid phase hydrogenation process, hydrogenation reaction is realized through hydrogen dissolved in oil, and the aim of producing clean wax oil products is achieved, but the dissolved hydrogen is excessive and cannot be completely reacted, and the hydrogen dissolved in the hydrogenated oil after the reaction is finished can usually remain 20% -70% of the dissolved hydrogen, so that the hydrogen is ineffectively used, namely, the energy consumption is increased.
According to the invention, by fully utilizing the characteristic that a large amount of hydrogen is still dissolved in oil generated by a wax oil liquid phase circulation hydrogenation process, a supplementary hydrogenation reactor is arranged in the subsequent stage of the wax oil hydrogenation reactor, the refinery gas raw material is dissolved in the wax oil hydrogenation reaction material flow and enters the catalyst bed layer of the supplementary hydrogenation reactor, and the hydrogenation reaction of the gas is completed by utilizing the dissolved hydrogen and the catalyst atmosphere, so that the problem of large gas hydrogenation temperature rise is solved, and the hydrogen dissolved in the wax oil is used for the gas hydrogenation reaction, thereby reducing the hydrogen consumption; or a plurality of catalyst beds are arranged in a further supplementary hydrogenation reactor, part of dry gas or all dry gas raw materials in the mixed gas and wax oil hydrogenation generated oil are mixed to enter the first catalyst bed, and the rest gas and/or hydrogen mixed mixture enters the subsequent catalyst bed. The combination method is generally characterized in that the gas hydrogenation process is completed on the premise of not influencing the quality of the wax oil product or further improving the quality of the wax oil product to obtain the wax oil product and the gas product, and the two technologies are optimally combined, so that the hydrogen dissolved in the wax oil product is reduced, namely, the hydrogen consumption and the energy consumption are reduced, the equipment investment is saved, and the operation cost is reduced.
Drawings
FIG. 1 is a flow diagram of a hydrogenation combination process of the present invention.
Wherein: 1-raw oil, 2-raw oil pump, 3-cycle oil, 4-hydrogen dissolver, 5-new hydrogen, 6-refinery gas raw material, 7-wax oil hydrogenation reactor, 8-vent valve, 9-wax oil hydrogenation reaction stream, 10-high pressure separator, 11-low pressure separator, 12-stripping/fractionating system, 13-stripping gas, 14-naphtha, 15-diesel, 16-hydrogenation wax oil, 17-high pressure separator gas, 18-low pressure separator gas, 19-gas separator, 20-hydrogen, 21-dry gas, 22-liquefied gas, 23-gas dissolver, 24-make-up hydrogenation reactor, 25-make-up hydrogenation reaction stream.
Detailed Description
The flow and effect of the hydrogenation combination method of the present invention will be further illustrated with reference to the following examples, which should not be construed as limiting the process of the present invention.
The specific implementation mode of the hydrogenation combination method is as follows: raw oil 1 and cycle oil 3 are mixed, the mixed material and hydrogen are mixed in a hydrogen dissolver 4 and then enter a wax oil hydrogenation reactor 7, a wax oil hydrogenation reaction material flow 9 and refinery gas raw materials are mixed in a gas dissolver 23 and then enter a supplementary hydrogenation reactor 24, supplementary hydrogenation reaction effluent 25 enters a high-pressure separator 10 and is separated in the high-pressure separator 10 to obtain high-pressure separator gas 17 and liquid, the liquid enters a low-pressure separator 11 and is separated in the low-pressure separator 11 to obtain low-pressure separator gas 18 and liquid, the liquid and liquid component separated in a gas separator 19 are mixed and then enter a stripping/fractionating system 12, and are fractionated in the fractionating system under the action of stripping gas 13 to obtain naphtha 14, diesel 15 and hydrogenation wax oil 16, the high-pressure separator gas 17 and the low-pressure separator gas 18 are mixed and then enter the gas separator 19, and are separated in the gas separator 19 to obtain hydrogen, Dry gas and liquefied gas products. The cycle oil 3 can be obtained directly from the wax oil hydrogenation reaction material flow 9, and can also be obtained from the liquid obtained by the separation in the high-pressure separator 10.
The following examples further illustrate specific aspects of the present invention. Experimental studies were conducted using FF-24 catalyst developed and produced by FRIPP.
TABLE 1 wax oil feedstock Primary Properties
| Wax oil feedstock | Raw oil 1 | Raw oil 2 |
| Density, g/cm3 | 0.923 | 0.945 |
| Range of distillation range, deg.C | 345~540 | 300~600 |
| Sulfur content, wt.% | 1.5 | 2.3 |
TABLE 2 refinery gas feedstock key properties
| Refinery gas feedstock | Dry gas | Liquefied gas | Mixed gas |
| Gas composition | |||
| H2 | 7.0 | 0 | 3.5 |
| CH4 | 12.6 | 0 | 2.9 |
| C2H6 | 55.3 | 0 | 27.1 |
| C2H4 | 5.6 | 0.1 | 4.6 |
| C3 H8 | 10.8 | 16.0 | 13.6 |
| C3 H6 | 2.7 | 6.5 | 4.5 |
| C3 H4 | 0 | 0 | 0 |
| C4 H10 | 5.3 | 34.5 | 20.5 |
| C4 H8 | 0.5 | 33.1 | 19.1 |
| C4 H6 | 0 | 1.2 | 0.5 |
| C5 + | 0.1 | 8.6 | 3.6 |
| CO | 0.005 | 0 | 0.002 |
| CO2 | 0.01 | 0 | 0.008 |
Table 3 examples process conditions and main product properties
| Process conditions | Example 1 | Example 2 | Example 3 | Example 4 | Example 5 |
| Hydrogenation reactor operating conditions | |||||
| Raw oil | Raw oil 1 | Raw oil 1 | Raw oil 1 | Raw oil 2 | Raw oil 2 |
| Operating conditions of wax oil hydrogenation reactor | |||||
| Reaction pressure, MPa | 12.0 | 8.0 | 8.0 | 10.0 | 16.0 |
| Average reaction temperature,. degree.C | 370 | 360 | 360 | 375 | 385 |
| Volume space velocity of fresh raw oil, h-1 | 2.0 | 1.0 | 1.0 | 0.8 | 1.5 |
| Circulation ratio | 3:1 | 2.5:1 | 2.5:1 | 4:1 | 3:1 |
| Make-up of hydrogenation reactor operating conditions | |||||
| Refinery gas feedstock at reactor inlet | Dry gas | Mixed gas | Dry gas | Liquefied gas | Mixed gas |
| Reaction pressure, MPa | 12.0 | 8.0 | 8.0 | 10.0 | 16.0 |
| Average reaction temperature,. degree.C | 370 | 360 | 360 | 375 | 385 |
| Volume space velocity of fresh raw oil, h-1 | 20.0 | 15.0 | 15.0 | 25.0 | 18.0 |
| Two-bed inlet refinery gas raw material | — | — | Liquefied gas | — | — |
| Volume ratio of hydrogen dissolved in inlet of two-bed layer to raw material of refinery gas | — | — | 95:5 | — | — |
| Dry gas product | |||||
| Olefin content, v% | 0 | 0 | 0 | 0 | 0 |
| Liquefied gas product | |||||
| Olefin content, v% | 0 | 0 | 0 | 0 | 0 |
| CO+CO2，µg/g | 0 | 0 | 0 | 0 | 0 |
| Naphtha product | |||||
| Sulphur content, μ g/g | 0.3 | 0.4 | 0.3 | 0.3 | 0.4 |
| Diesel oil product | |||||
| Density, g/cm3 | 0.864 | 0.867 | 0.867 | 0.886 | 0.873 |
| Sulphur content, μ g/g | 145 | 235 | 227 | 380 | 120 |
| Wax oil product | |||||
| Density, g/cm3 | 0.885 | 0.889 | 0.889 | 0.912 | 0.899 |
| Sulphur content, μ g/g | 390 | 1450 | 1420 | 1950 | 290 |
It can be seen from the examples that wax oil feedstock and refinery gas feedstock can be directly used to produce hydrogenated wax oil products and clean gas products by the hydrogenation combination process of the present technology.
Claims (8)
1. The refinery gas hydrogenation combination method is characterized in that: the method comprises the following steps:
(a) mixing the wax oil raw oil and the circulating oil with hydrogen in hydrogen dissolving equipment, and then entering a hydrogenation catalyst bed layer in a wax oil hydrogenation reactor to react under the condition of liquid-phase hydrogenation operation;
(b) mixing the reactant flow obtained in the step (a) with refinery gas and hydrogen in a gas dissolving device, and then allowing the mixture to enter a hydrogenation catalyst bed layer in a supplementary hydrogenation reactor to react under the liquid-phase hydrogenation operation condition;
(c) separating the hydrogenation reaction effluent in the step (b) into a gas phase and a liquid phase, continuously separating the gas phase obtained by separation after removing hydrogen sulfide to obtain hydrogen and refinery gas after hydrogenation treatment, fractionating the liquid phase obtained by separation to obtain naphtha, diesel oil and wax oil products, returning part of the hydrogenation reaction effluent obtained in the step (a) and/or part of the hydrogenation reaction material flow obtained in the step (b) and/or part of the liquid phase obtained by separation of a high-pressure separator as circulating oil to hydrogen dissolving equipment,
wherein, three catalyst beds are arranged in the wax oil hydrogenation reactor, two catalyst beds are arranged in the supplementary hydrogenation reactor, gas dissolving equipment is arranged between the beds, hydrogen enters the gas dissolving equipment between the beds of the wax oil hydrogenation reactor, and hydrogen and refinery gas enter the gas dissolving equipment between the beds of the supplementary hydrogenation reactor; when hydrogen and refinery gas are introduced simultaneously, the volume ratio of the introduced hydrogen to the refinery gas is 1: 1-100: 1.
2. The method of claim 1, wherein: the wax oil raw material oil is one or more of straight-run wax oil, coked wax oil, thermal cracking wax oil, synthetic wax oil, coal tar wax oil fraction, coal direct liquefaction wax oil and shale oil wax oil, or at least one of part of catalytic cracking light cycle oil, naphthenic straight-run diesel oil and coal tar diesel oil fraction is mixed in the wax oil raw material oil.
3. The method of claim 1, wherein: the wax oil hydrogenation operation conditions are that the reaction pressure is 3.0MPa to 20.0MPa, and the volume space velocity of the wax oil raw material oil is 0.2h-1~8.0h-1The average reaction temperature is 180-450 ℃, and the ratio of the circulating oil to the wax oil raw oil is 0.5: 1-10: 1.
4. The method of claim 3, wherein: the wax oil hydrogenation operation conditions are that the reaction pressure is 4.0MPa to 18.0MPa, and the volume space velocity of the wax oil raw material oil is 0.5h-1~6.0h-1The average reaction temperature is 200-440 ℃, and the ratio of the circulating oil to the wax oil raw oil is 0.6: 1-8: 1.
5. The method of claim 1, wherein: the supplementary hydrogenation operation conditions are that the reaction pressure is 3.0MPa to 20.0MPa, and the volume airspeed of the wax oil raw material oil is 0.3h-1~40.0h-1The average reaction temperature is 180-450 ℃.
6. The method of claim 5, wherein: the supplementary hydrogenation operation conditions are that the reaction pressure is 4.0MPa to 18.0MPa, and the volume airspeed of the wax oil raw material oil is 0.5h-1~30.0h-1The average reaction temperature is 200-440 ℃.
7. The method of claim 1, wherein: the hydrogenation active components of the hydrogenation catalyst used in the wax oil hydrogenation reactor and the hydrogenation active components of the hydrogenation catalyst used in the supplementary hydrogenation reactor are one or more of Co, Mo, W and Ni, the weight content of the hydrogenation active components is 5-70 percent calculated by oxides, and the carrier of the hydrogenation catalyst is one or more of alumina, amorphous silicon aluminum, silicon oxide and titanium oxide.
8. The method of claim 1, wherein: the refinery gas is one or more of dry gas and liquefied gas, and the gas is one or more of coking, catalytic cracking and thermal cracking reaction.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101880549A (en) * | 2009-05-06 | 2010-11-10 | 中国石油化工股份有限公司 | Hydrogenation method for liquefied gas fraction |
| CN102268293A (en) * | 2010-06-07 | 2011-12-07 | 中国石油化工集团公司 | Hydrogenation combined process |
| 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 |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101880549A (en) * | 2009-05-06 | 2010-11-10 | 中国石油化工股份有限公司 | Hydrogenation method for liquefied gas fraction |
| CN102268293A (en) * | 2010-06-07 | 2011-12-07 | 中国石油化工集团公司 | Hydrogenation combined process |
| 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 |
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Effective date of registration: 20230908 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |
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