阅读说明：本技术 一种原油两级加氢生产汽油的装置及工艺 (Device and process for producing gasoline by crude oil two-stage hydrogenation ) 是由 邓宏达 昝大鑫 王鑫 吕云飞 刘哲 于 2020-07-03 设计创作，主要内容包括：本发明涉及一种原油两级加氢生产汽油的装置及工艺,其特征在于：原油蒸馏塔底端设置的原油蒸馏塔出料管与添加剂进料管、新氢进气管汇合并通过加压泵及第一预热器连接至一级反应器,一级反应器的顶端连接至分离器,分离器的底端设置有渣油出口,分离器顶端连接至二级反应器顶端,二级反应器底端通过第一冷却器连接至冷分离器,冷分离器连接至分馏塔,分馏塔的顶端通过第二冷却器连接至汽油收集罐,分馏塔的底端设置有余料回收管。本发明结构设计科学合理,工艺简单,汽油生产效率高,且能耗成本低,原油得以高效彻底分离。(The invention relates to a device and a process for producing gasoline by crude oil two-stage hydrogenation, which are characterized in that: the crude oil distillation tower discharging pipe and the additive inlet pipe that the crude oil distillation tower bottom set up, new hydrogen admission manifold and be connected to first order reactor through force (forcing) pump and first pre-heater, the top of first order reactor is connected to the separator, the bottom of separator is provided with the residual oil export, the separator top is connected to second order reactor top, second order reactor bottom is connected to cold separator through first cooler, cold separator is connected to the fractionating tower, the top of fractionating tower is connected to the petrol collection tank through the second cooler, the bottom of fractionating tower is provided with the clout recovery tube. The invention has scientific and reasonable structural design, simple process, high gasoline production efficiency and low energy consumption cost, and crude oil can be efficiently and thoroughly separated.)

1. A device for producing gasoline by crude oil two-stage hydrogenation is characterized in that: the system comprises a crude oil distillation tower, a primary reactor, a separator, a secondary reactor, a cold separator, a fractionating tower and a gasoline collecting tank, wherein a crude oil distillation tower discharge pipe arranged at the bottom end of the crude oil distillation tower, an additive feeding pipe and a fresh hydrogen inlet pipe are converged and connected to the primary reactor through a pressure pump and a first preheater, the top end of the primary reactor is connected to the separator, a residual oil outlet is arranged at the bottom end of the separator, the top end of the separator is connected to the top end of the secondary reactor, the bottom end of the secondary reactor is connected to the cold separator through a first cooler, the cold separator is connected to the fractionating tower, the top end of the fractionating tower is connected to the gasoline collecting tank through a second cooler, and a residual material recycling pipe is arranged at the bottom end of the fractionating tower.

2. The apparatus for producing gasoline by two-stage hydrogenation of crude oil according to claim 1, wherein: and a circulating hydrogen pipeline is arranged at the top end of the cold separator, and the circulating hydrogen pipeline is converged with the residual material recovery pipe, the gasoline and diesel oil fraction oil pipe arranged at the top end of the crude oil distillation tower and the fresh hydrogen supply pipe and is connected to the top end of the secondary reactor through a second preheater.

3. The apparatus for producing gasoline by two-stage hydrogenation of crude oil according to claim 2, wherein: and a circulating hydrogen pipeline at the top end of the cold separator is combined with a crude oil distillation tower discharge pipe, an additive feeding pipe and a fresh hydrogen inlet pipe and is connected to the primary reactor through a first preheater.

4. A process for producing gasoline by crude oil two-stage hydrogenation is characterized in that: the process flow comprises the following steps:

1) crude oil distillation: introducing crude oil into a crude oil distillation tower, and distilling 20-50% of gasoline and diesel oil components at the top of the tower and heavy oil components at the bottom of the tower at normal pressure through the crude oil distillation tower;

2) first-order reaction: bottom heavy oil fraction is produced by crude distillationHydrogen gas in a discharge pipe of a distillation tower and a fresh hydrogen inlet pipe is converged with an additive in an additive feeding pipe according to a hydrogen-oil ratio of 600-1300 liters/kg, is pressurized to 150-250 bar by a pressure pump and is introduced into a first preheater for preheating, and the preheating temperature is 350-500 ℃; the preheated mixed gas enters a primary reactor for reaction, and the volume airspeed is 0.3-0.8 h ^-1；

3) First-stage separation: the product in the first-stage reactor enters a separator through the top end, the pressure in the separator is 150-250 bar, the temperature is 350-500 ℃, and 3-5% of unconverted residual oil and added solid matters are separated from a residual oil outlet at the bottom end of the separator;

4) and (3) secondary reaction: feeding the material separated from the top of the separator into a secondary reactor with a catalyst (containing nickel, molybdenum, cobalt and other conventional hydrocracking and hydrofining catalysts), wherein the reaction pressure is 150-250 bar and the temperature is 350-400 ℃;

5) secondary separation: the reaction product at the bottom end of the secondary reactor enters a cold separator through a first cooler, and the product separated from the bottom end of the cold separator enters a fractionating tower and is fractionated into gasoline fraction with the distillation range of the top of the tower being less than 180 ℃ and diesel oil and wax oil components with the distillation range of the bottom of the tower being more than 180 ℃ through the fractionating tower;

6) and (3) cyclic reaction: the bottom of the fractionating tower is mixed with straight-run gasoline and diesel oil components distilled from a gasoline and diesel oil fractionating oil pipe arranged at the top end of the crude oil distillation tower through a residual material recovery pipe, fresh hydrogen in a fresh hydrogen supply pipe and circulating hydrogen in a circulating hydrogen pipeline, the mixture is heated by a second preheater, the preheated mixture and materials separated from the top end of the separator are introduced into a secondary reactor according to the hydrogen-oil ratio of 1000-2000 standard liters/kg of oil, and the airspeed is 0.8-1.5 h ^-1(ii) a Meanwhile, a circulating hydrogen pipeline is combined with a crude oil distillation tower discharging pipe, an additive feeding pipe and a fresh hydrogen inlet pipe and is connected to the primary reactor through a first preheater.

7) And (3) gasoline collection: the gasoline fraction is cooled by a second cooler and then collected by a gasoline collecting tank.

5. The process for producing gasoline by two-stage hydrogenation of crude oil according to claim 4, wherein: the components of the additive in the step 2) are activated carbon and ferric sulfate, the mass fraction of the activated carbon is 0.5-3% of the total feeding of the first reactor, and the mass fraction of the ferric sulfide is 5-20% of the total amount of the additive.

Technical Field

The invention belongs to the technical field of crude oil hydrogenation, relates to a device for producing gasoline by crude oil hydrogenation, and particularly relates to a device for producing gasoline by crude oil two-stage hydrogenation.

Background

The existing crude oil processing technology, especially in the aspect of processing heavy oil with high boiling point, generally adopts a hydrogenation method, firstly hydrogenation reaction is carried out in a suspension bed reactor, then a reaction product is distilled, a product with low boiling point is extracted, heavy components are recycled to the reactor for continuous reaction, the process is circulated all the time until the heavy oil with high boiling point is fully converted into light middle distillate oil to be distilled out; in the light product distilled out, secondary hydrofining and hydrocracking are required to produce qualified gasoline and diesel, and the secondary hydrogenation reaction generally adopts a fixed bed reactor mode.

Attempts have been made to obtain light oil products with low boiling points by one-step hydrogenation in a fixed bed reactor, but a number of examples reveal the fact that the catalyst activity decreases more rapidly. Catalyst life can only be guaranteed at lower pressures and catalyst activity is greatly attenuated with increasing feed carbon residue and heavy metals. It is only possible to ensure the catalyst activity with frequent replacement of the catalyst, which makes the operation of the hydrogenation unit very costly.

Disclosure of Invention

The invention aims to provide a device for producing gasoline by crude oil two-stage hydrogenation, which aims at overcoming the defects and shortcomings of the prior art and has the advantages of simple process, high gasoline production efficiency and low energy consumption cost.

The technical problem to be solved by the invention is realized by the following technical scheme:

a device for producing gasoline by crude oil two-stage hydrogenation is characterized in that: the system comprises a crude oil distillation tower, a primary reactor, a separator, a secondary reactor, a cold separator, a fractionating tower and a gasoline collecting tank, wherein a crude oil distillation tower discharge pipe arranged at the bottom end of the crude oil distillation tower, an additive feeding pipe and a fresh hydrogen inlet pipe are converged and connected to the primary reactor through a pressure pump and a first preheater, the top end of the primary reactor is connected to the separator, a residual oil outlet is arranged at the bottom end of the separator, the top end of the separator is connected to the top end of the secondary reactor, the bottom end of the secondary reactor is connected to the cold separator through a first cooler, the cold separator is connected to the fractionating tower, the top end of the fractionating tower is connected to the gasoline collecting tank through a second cooler, and a residual material recycling pipe is arranged at the bottom end of the fractionating tower.

And a circulating hydrogen pipeline is arranged at the top end of the cold separator, and the circulating hydrogen pipeline is converged with a residual material recovery pipe, a gasoline and diesel oil fraction oil pipe arranged at the top end of the crude oil distillation tower and a fresh hydrogen supply pipe and is connected to the top end of the secondary reactor through a second preheater.

And the circulating hydrogen pipeline at the top end of the cold separator is combined with a crude oil distillation tower discharging pipe, an additive feeding pipe and a fresh hydrogen inlet pipe and is connected to the primary reactor through a first preheater.

A process for producing gasoline by crude oil two-stage hydrogenation is characterized in that: the process flow comprises the following steps:

1) crude oil distillation: introducing crude oil into a crude oil distillation tower, and distilling 20-50% of gasoline and diesel oil components at the top of the tower and heavy oil components at the bottom of the tower at normal pressure through the crude oil distillation tower;

2) first-order reaction: heavy oil components at the tower bottom are merged with the additive of an additive feeding pipe through hydrogen gas of a discharging pipe and a new hydrogen inlet pipe of a crude oil distillation tower according to the hydrogen-oil ratio of 600-1300 liters/kg, are pressurized to 150-250 bar through a pressure pump and are introduced into a first preheater for preheating, and the preheating temperature is 350-500 ℃; the preheated mixed gas enters a primary reactor for reaction, and the volume airspeed is 0.3-0.8 h ^-1；

3) First-stage separation: the product in the first-stage reactor enters a separator through the top end, the pressure in the separator is 150-250 bar, the temperature is 350-500 ℃, and 3-5% of unconverted residual oil and added solid matters are separated from a residual oil outlet at the bottom end of the separator;

4) and (3) secondary reaction: feeding the material separated from the top end of the separator into a secondary reactor with a catalyst, wherein the reaction pressure is 150-250 bar, and the temperature is 350-400 ℃;

5) secondary separation: the reaction product at the bottom end of the secondary reactor enters a cold separator through a first cooler, and the product separated from the bottom end of the cold separator enters a fractionating tower and is fractionated into gasoline fraction with the distillation range of the top of the tower being less than 180 ℃ and diesel oil and wax oil components with the distillation range of the bottom of the tower being more than 180 ℃ through the fractionating tower;

6) and (3) cyclic reaction: the bottom of the fractionating tower is mixed with straight-run gasoline and diesel oil components distilled from a gasoline and diesel oil fractionating oil pipe arranged at the top end of the crude oil distillation tower through a residual material recovery pipe, fresh hydrogen in a fresh hydrogen supply pipe and circulating hydrogen in a circulating hydrogen pipeline, the mixture is heated by a second preheater, the preheated mixture and materials separated from the top end of the separator are introduced into a secondary reactor according to the hydrogen-oil ratio of 1000-2000 standard liters/kg of oil, and the airspeed is 0.8-1.5 h ^-1(ii) a Meanwhile, a circulating hydrogen pipeline is combined with a crude oil distillation tower discharging pipe, an additive feeding pipe and a fresh hydrogen inlet pipe and is connected to the primary reactor through a first preheater.

7) And (3) gasoline collection: the gasoline fraction is cooled by a second cooler and then collected by a gasoline collecting tank.

And in the step 2), the components of the additive are activated carbon and ferric sulfate, the mass fraction of the activated carbon is 0.5-3% of the total feed of the first reactor, and the mass fraction of the ferric sulfide is 5-20% of the total amount of the additive.

The invention has the advantages and beneficial effects that:

1. the device for producing the gasoline by the two-stage hydrogenation of the crude oil can convert the crude oil from the heavy oil into the light oil and then from the light oil into the gasoline by the two-stage hydrogenation of the first-stage reactor and the second-stage reactor, can efficiently and thoroughly separate the crude oil, and has high gasoline yield.

2. The process for producing the gasoline by the two-stage hydrogenation of the crude oil has simple process steps and low energy consumption cost, and the recycle hydrogen and part of intermediate products can be recycled, thereby improving the conversion rate of the crude oil and the yield of the gasoline.

3. The invention has scientific and reasonable design, simple process, high gasoline production efficiency and low energy consumption cost, and the crude oil can be efficiently and thoroughly separated.

Drawings

FIG. 1 is a process flow diagram of the present invention.

Description of the reference numerals

The system comprises a 1-gasoline and diesel oil fraction oil pipe, a 2-crude oil distillation tower, a 3-crude oil distillation tower discharge pipe, a 4-additive feed pipe, a 5-pressure pump, a 6-fresh hydrogen inlet pipe, a 7-first preheater, an 8-first-stage reactor, a 9-separator, a 10-residual oil outlet, an 11-second preheater, a 12-second-stage reactor, a 13-first cooler, a 14-circulating hydrogen pipeline, a 15-cold separator, a 16-second cooler, a 17-fractionating tower, an 18-gasoline collecting tank, a 19-residual material recovery pipe and a 20-fresh hydrogen supply pipe.

Detailed Description

The present invention is further illustrated by the following specific examples, which are intended to be illustrative, not limiting and are not intended to limit the scope of the invention.

The device for producing gasoline by crude oil two-stage hydrogenation is characterized in that: the system comprises a crude oil distillation tower 2, a primary reactor 8, a separator 9, a secondary reactor 12, a cold separator 15, a fractionating tower 17 and a gasoline collecting tank 18, wherein a crude oil distillation tower discharge pipe 3 arranged at the bottom end of the crude oil distillation tower is converged with an additive feed pipe 4 and a fresh hydrogen inlet pipe 6 and is connected to the primary reactor through a booster pump 5 and a first preheater 7, the top end of the primary reactor is connected to the separator, a residual oil outlet 10 is arranged at the bottom end of the separator, the top end of the separator is connected to the top end of the secondary reactor, the bottom end of the secondary reactor is connected to the cold separator through a first cooler 13, the cold separator is connected to the fractionating tower, the top end of the fractionating tower is connected to the gasoline collecting tank through a second cooler 16, and a residual material recycling pipe 19 is arranged at the bottom end of the fractionating tower.

And a circulating hydrogen pipeline 14 is arranged at the top end of the cold separator, and the circulating hydrogen pipeline is converged with the residual material recovery pipe, the gasoline and diesel oil fraction oil pipe 1 arranged at the top end of the crude oil distillation tower and the fresh hydrogen supply pipe 20 and is connected to the top end of the secondary reactor through a second preheater 11.

And a circulating hydrogen pipeline at the top end of the cold separator is combined with a crude oil distillation tower discharge pipe, an additive feeding pipe and a fresh hydrogen inlet pipe and is connected to the primary reactor through a first preheater.

The process for producing gasoline by crude oil two-stage hydrogenation is characterized by comprising the following steps of: the process flow comprises the following steps:

1) crude oil distillation: introducing crude oil into a crude oil distillation tower, and distilling 20-50% of gasoline and diesel oil components at the top of the tower and heavy oil components at the bottom of the tower at normal pressure through the crude oil distillation tower;

2) first-order reaction: heavy oil components at the tower bottom are merged with hydrogen in a new hydrogen inlet pipe and an additive in an additive inlet pipe according to a hydrogen-oil ratio of 600-1300 standard liters/kg through a discharge pipe of a crude oil distillation tower, are pressurized to 150-250 bar through a pressure pump and are introduced into a first preheater for preheating, the preheating temperature is 350-500 ℃, the components of the additive are activated carbon and ferric sulfate, the mass fraction of the activated carbon is 0.5-3% of the total feed of the first reactor, and the mass fraction of the ferric sulfide is 5-20% of the total amount of the additive; the preheated mixed gas enters a primary reactor for reaction, and the volume airspeed is 0.3-0.8 h ^-1；

3) First-stage separation: the product in the first-stage reactor enters a separator through the top end, the pressure in the separator is 150-250 bar, the temperature is 350-500 ℃, and 3-5% of unconverted residual oil and added solid matters are separated from a residual oil outlet at the bottom end of the separator;

4) and (3) secondary reaction: feeding the material separated from the top of the separator into a secondary reactor with a catalyst, wherein the catalyst is a traditional hydrocracking and hydrofining catalyst containing nickel, molybdenum, cobalt and the like, the reaction pressure is 150-250 bar, and the temperature is 350-400 ℃;

5) secondary separation: the reaction product at the bottom end of the secondary reactor enters a cold separator through a first cooler, and the product separated from the bottom end of the cold separator enters a fractionating tower and is fractionated into gasoline fraction with the distillation range of the top of the tower being less than 180 ℃ and diesel oil and wax oil components with the distillation range of the bottom of the tower being more than 180 ℃ through the fractionating tower;

6) and (3) cyclic reaction: the bottom of the fractionating tower is mixed with straight-run gasoline and diesel oil components distilled from a gasoline and diesel oil fractionating oil pipe arranged at the top end of the crude oil distillation tower through a residual material recovery pipe, fresh hydrogen in a fresh hydrogen supply pipe and circulating hydrogen in a circulating hydrogen pipeline, the mixture is heated by a second preheater, the preheated mixture and materials separated from the top end of the separator are introduced into a secondary reactor according to the hydrogen-oil ratio of 1000-2000 standard liters/kg of oil, and the airspeed is 0.8-1.5 h ^-1(ii) a A circulating hydrogen pipeline and a crude oil distillation tower discharging pipe at the same time,The additive feed line and the fresh hydrogen inlet line were combined and connected to the primary reactor through a first preheater.

7) And (3) gasoline collection: the gasoline fraction is cooled by a second cooler and then collected by a gasoline collecting tank.