CN102268293B - Hydrogenation combined process - Google Patents
Hydrogenation combined process Download PDFInfo
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- CN102268293B CN102268293B CN201010197103.3A CN201010197103A CN102268293B CN 102268293 B CN102268293 B CN 102268293B CN 201010197103 A CN201010197103 A CN 201010197103A CN 102268293 B CN102268293 B CN 102268293B
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Abstract
The invention discloses a hydrogenation combined process. In the process, a reaction effluent from a middle-high pressure hydrogenation device with a pressure of more than 4.0MPa is subjected to gas-liquid separation in a high pressure separator, wherein the gas obtained by separation is used as circular hydrogen, and the liquid obtained by separation enters into a low pressure separator for further gas-liquid separation; and the liquid obtained by further separation is used as a product, and the gas obtained by further separation is used as hydrogen for a low pressure hydrogenation with an operation pressure of 2.0-3.0MPa. The reaction effluent is subjected to gas-liquid separation, the gas obtained by separation is discharged out of the device, and the liquid obtained by separation is the product.
Description
Technical field
The present invention relates to hydrocarbon oil refining field under hydrogen exists, particularly a kind of with the refining hydrocarbon ils combination process of hydrogen, relate to the hydrogen COMBINED PROCESS of hydrogenation unit.
Background technology
The sustainable development of world economy at present and the increasingly stringent of environmental regulation, need to produce a large amount of light clean fuels, and these all require existing oil Refining Technologies to improve, and with minimum cost, produce satisfactory product.Along with the worsening shortages of crude resources and heaviness, in poor quality development, distillate hydrogenation technique is applied widely in Clean Fuel Production.
Tradition hydrocarbon oil hydrogenation process reaction system needs a large amount of hydrogen to guarantee certain hydrogen dividing potential drop, and wherein small portion hydrogen falls by hydrogenation consumption of chemical reaction, and major part recycles after being boosted by circulating hydrogen compressor.
Conventional residual hydrogenation, hydrocracking, hydrotreatment, hydro-upgrading, high-pressure separator and light pressure separator are set in the mesohigh hydrogenation technique flow processs such as hydrofining, hydrogen and hydrogenation after cut oil at high-pressure separator specified temp with to carry out liquid phase under pressure separated, high-pressure separator gas phase is through the circulating hydrogen compressor Returning reacting system that boosts, high-pressure separator liquid phase discharges low minute gas after vacuum flashing under light pressure separator specified temp and pressure, in prior art, general this part low minute gas is delivered to PSA device as hydrogen-rich gas and is reclaimed hydrogen wherein, or using this part low minute gas as fuel, referring in July, 2000, petroleum industry press publishes, the woods generation ruler of great talent and bold vision compiles the petroleum refining engineering third edition, 423rd～436 pages.Hydrogen richness in low minute gas is generally about 70%, as fuel, uses and has wasted a large amount of hydrogen resources.
General mesohigh hydrogenation unit light pressure separator pressure design is at 1.2～3.0MPa (G), to guarantee that isolated low minute oily depended on pressure enters into separation column.
The device technique flow processs such as regular price gasoline hydrogenation, the pre-hydrogenation of petroleum naphtha, kerosene hydrogenation are more simple, and a gas-liquid separator is generally only set, and isolated hydrogen is through the circulating hydrogen compressor Returning reacting system that boosts.
In modern plant, the quantity of hydrogenation unit is more and more, the reaction conditions difference of different device is also very large, if can keep the hydrogen of traditional hydrogenation process to divide pressure request, can rationally utilize the hydrogen of each hydrogenation unit again, hydrogen recycle flow process is revised as to hydrogen and once passes through flow process, safe, efficient, the economical operation of greatly reducing investment outlay and reduce energy consumption ，Dui enterprise are brought to benefit.
Summary of the invention
In order to have overcome the defect of prior art, the present invention proposes a kind of hydrogenation combination technique by utilizing low minute gas of mesohigh hydrogenation unit, before entering PSA, low minute gas is introduced into low pressure hydrogenation unit, make full use of the pressure of this part hydrogen, cancel the circulating hydrogen compressor of low pressure hydrogenation unit, reduced investment and process cost.
A kind of hydrogenation combination technique of the present invention, comprises,
1) mesohigh hydrogenation unit reaction effluent carries out gas-liquid separation through mesohigh hydrogenation unit high-pressure separator, gas is as mesohigh hydrogenation unit recycle hydrogen, liquid is that mesohigh hydrogenation unit high score oil enters mesohigh hydrogenation unit light pressure separator and further carries out gas-liquid separation, low minute gas of mesohigh hydrogenation unit light pressure separator enters 2), liquid is as the charging of mesohigh hydrogenation unit separation column;
2) coming from 1) to enter working pressure with low-voltage hydrogenation material be to react in 2.0～3.0MPa low pressure hydrogenation unit reactor to low minute gas, reaction effluent carries out gas-liquid separation in low pressure hydrogenation unit gas-liquid separator, isolated gas enters PSA device, and liquid is as the charging of low pressure hydrogenation unit separation column.
Described mesohigh hydrogenation unit at least contains the hydrogenation unit that a working pressure is 4.0～20.0MPa.
Described mesohigh hydrogenation unit high-pressure separator working pressure is 4.0～20.0MPa.
Described mesohigh hydrogenation unit is one or more device in hydrotreatment, hydrocracking, hydro-refining unit.
Described a kind of hydrogenation combination technique, is further characterized in that: low pressure hydrogenation unit adopts hydrogen once to pass through flow process.
Described a kind of hydrogenation combination technique, is further characterized in that: after low minute gas of mesohigh hydrogenation unit should remove hydrogen sulfide, enter low pressure hydrogenation unit, to meet the needs of low pressure hydrogenation unit reaction.
Described a kind of hydrogenation combination technique, the pressure rating of mesohigh hydrogenation unit reactor, mesohigh hydrogenation unit high-pressure separator, mesohigh hydrogenation unit light pressure separator, low pressure hydrogenation unit reactor, low pressure hydrogenation unit gas-liquid separator equipment is successively decreased successively, to guarantee that low pressure hydrogenation unit gas-liquid separator gas can enter into PSA device and return receipts hydrogen.
Described a kind of hydrogenation combination technique, is further characterized in that: low pressure hydrogenation unit gas-liquid separator gas and the grid-connected merging of reformation hydrogen, enter into PSA device recover hydrogen.
Described a kind of hydrogenation combination technique, is further characterized in that: the partial liquefaction gas that low minute gas of mesohigh hydrogenation unit carries can be recovered in low pressure hydrogenation unit gas-liquid separator.
Mesohigh hydrogenation unit of the present invention is the hydrogenation unit that working pressure is greater than 4.0MPa, as: hydrotreatment, hydrocracking, hydro-upgrading and hydrofining.
Low minute of the present invention gas refers to the light pressure separator flash gas of mesohigh hydrogenation unit, also comprises the waste discharge hydrogen release venting of reactive system.
Low pressure hydrogenation unit of the present invention is that the reaction pressures such as gasoline hydrogenation, the pre-hydrogenation of petroleum naphtha, kerosene hydrogenation are at the hydrogenation unit of 2.0～3.0MPa.
Hydrogenation combination technique of the present invention makes full use of the pressure of low minute gas of light pressure separator of mesohigh hydrogenation unit and hydrogen wherein, and the hydrogen using it as low pressure hydrogenation unit, is all utilized the pressure of low minute gas and hydrogen, has overcome the shortcoming of prior art.
Hydrogenation combination technique of the present invention has following advantage:
1) lower investment;
2) lower process cost;
3) recyclable partial liquefaction gas;
4) make full use of the pressure of low minute gas, reduce energy expenditure
5) low minute gas is when low-voltage hydrogenation, and hydrogen once passes through, and has reduced H
2the accumulation of S;
5) larger flexibility of operation;
Accompanying drawing explanation
Fig. 1 is hydrogenation combination technique schematic flow sheet of the present invention.
1. mesohigh hydrogenation unit fresh feed is oily, 2. the new hydrogen of mesohigh hydrogenation unit, 3. mesohigh hydrogenation unit mixing hydrogen, 4. mesohigh hydrogenation unit parallel feeding, 5. mesohigh hydrogenation unit reactor, 6. mesohigh hydrogenation unit reaction effluent, 7. mesohigh hydrogenation unit high-pressure separator, 8. mesohigh hydrogenation unit recycle hydrogen, 9. mesohigh hydrogenation unit high score is oily, 10. mesohigh hydrogenation unit light pressure separator, 11. mesohigh hydrogenation unit separation column chargings, 12. low minute of mesohigh hydrogenation unit gas, 13. low pressure hydrogenation unit fresh feed oil, 14. low pressure hydrogenation unit parallel feedings, 15. low pressure hydrogenation unit reactors, 16. low pressure hydrogenation unit reaction product, 17. low pressure hydrogenation unit gas-liquid separators, 18. low pressure hydrogenation unit separation column chargings, 19. low pressure hydrogenation unit gas-liquid separator gases, 20.PSA device, 21. high-purity hydrogens.
Embodiment
As shown in Figure 1, hydrogenation combination technique is comprised of mesohigh hydrogenation unit reactor 5, mesohigh hydrogenation unit high-pressure separator 7, mesohigh hydrogenation unit light pressure separator 10, low pressure hydrogenation unit reactor 15, low pressure hydrogenation unit gas-liquid separator 17 and PSA device 20.
The present invention is in concrete implementation process, the new hydrogen 2 of mesohigh hydrogenation unit recycle hydrogen 8 and mesohigh hydrogenation unit is mixed into High-pressure Hydrogenation Unit and mixes hydrogen 3, mesohigh hydrogenation unit fresh feed oil 1 mixes hydrogen 3 and is mixed into mesohigh hydrogenation unit parallel feeding 4 with High-pressure Hydrogenation Unit, mesohigh hydrogenation unit parallel feeding 4 enters into mesohigh hydrogenation unit reactor 5, carry out mesohigh hydrogenation reaction, therefrom High-pressure Hydrogenation Unit reactor 5 mesohigh hydrogenation unit reaction effluent 6 out enters into mesohigh hydrogenation unit high-pressure separator 7 and carries out high-pressure gas-liquid separation, obtain mesohigh hydrogenation unit recycle hydrogen 8 and mesohigh hydrogenation unit high score oil 9, mesohigh hydrogenation unit recycle hydrogen 8 recycles, mesohigh hydrogenation unit high score oil 9 enters and in mesohigh hydrogenation unit light pressure separator 10, further carries out gas-liquid separation, be separated into the charging 11 of mesohigh hydrogenation unit separation column and low minute gas 12 of mesohigh hydrogenation unit, the follow-up product that is fractionated into all size is carried out in mesohigh hydrogenation unit separation column charging 11, low minute gas of mesohigh hydrogenation unit 12 and low pressure hydrogenation unit fresh feed oil 13 are mixed into low pressure hydrogenation unit parallel feeding 14 and enter into low pressure hydrogenation unit reactor 15 and carry out hydrogenation reaction, from low pressure hydrogenation unit reactor 15 low pressure hydrogenation unit reaction product 16 out, enter into low pressure hydrogenation unit gas-liquid separator 17, in low pressure hydrogenation unit gas-liquid separator 17, isolate low pressure hydrogenation unit separation column charging 18 and low pressure hydrogenation unit gas-liquid separator gas 19, low pressure hydrogenation unit separation column charging 18 is carried out separation column and is obtained desired product, low pressure hydrogenation unit gas-liquid separator gas 19 enters and in PSA device 20, carries out pressure-variable adsorption and obtain high-purity hydrogen 21.
Claims (5)
1. a hydrogenation combination technique, is characterised in that, the steps include:
1) mesohigh hydrogenation unit reaction effluent carries out gas-liquid separation through mesohigh hydrogenation unit high-pressure separator, gas is as mesohigh hydrogenation unit recycle hydrogen, liquid is that mesohigh hydrogenation unit high score oil enters mesohigh hydrogenation unit light pressure separator and further carries out gas-liquid separation, low minute gas of mesohigh hydrogenation unit light pressure separator enters 2), liquid is as the charging of mesohigh hydrogenation unit separation column;
2) come from 1) qi exhaustion in low minute except entering working pressure with low-voltage hydrogenation material after hydrogen sulfide, be to react in 2.0～3.0MPa low pressure hydrogenation unit reactor, reaction effluent carries out gas-liquid separation in low pressure hydrogenation unit gas-liquid separator, isolated gas send hydrogen recovery unit or directly send hydrogen pipe network, and liquid is as the charging of low pressure hydrogenation unit separation column.
2. according to a kind of hydrogenation combination technique claimed in claim 1, it is characterized in that: it is 4.0～20.0MPa hydrogenation unit that described mesohigh hydrogenation unit at least contains a working pressure.
3. according to a kind of hydrogenation combination technique claimed in claim 1, it is characterized in that: described mesohigh hydrogenation unit high-pressure separator working pressure is 4.0～20.0MPa.
4. according to a kind of hydrogenation combination technique claimed in claim 1, it is characterized in that: described mesohigh hydrogenation unit is one or more device in hydrotreater, hydroeracking unit, hydro-upgrading unit and hydro-refining unit.
5. according to a kind of hydrogenation combination technique claimed in claim 1, it is characterized in that: working pressure be 2.0～3.0MPa low pressure hydrogenation unit at least one for gasoline hydrofinishing, petroleum naphtha hydrogenation are refining, kerosene hydrogenation is refining, mineral spirit platreating device.
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| CN201010197103.3A CN102268293B (en) | 2010-06-07 | 2010-06-07 | Hydrogenation combined process |
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| CN201010197103.3A CN102268293B (en) | 2010-06-07 | 2010-06-07 | Hydrogenation combined process |
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Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant after: China Petrochemical Group Corp. Co-applicant after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant before: China Petrochemical Group Corp. Co-applicant before: Luoyang Petrochemical Engineering Co., China Petrochemical Group |
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