Fluidized bed hydrogenated reactor and fluidized bed hydrogenating method

Abstract

The invention belongs to the technical field of hydrogenation, and particularly relates to a fluidized bed hydrogenated reactor and a fluidized bed hydrogenating method. The fluidized bed hydrogenatedreactor comprises a shell, wherein a catalyst adding opening and a gas outlet are formed in the top of the shell; a three-phase separator is arranged on the upper portion of the inside of the shell and comprises two concentric barrels with different inner diameters, namely an inner barrel and an outer barrel; a flow guiding body is arranged below an opening of the lower end of the outer barrel; the shape of the flow guiding body is in the shape of a spindle with the small upper and lower ends and the large middle; a distributing plate is arranged on the lower portion of the inside of the shell; and a material inlet and a catalyst discharging opening are formed in the bottom of the shell. While the capacity utilization ratio of the reactor is improved, a catalyst lean-phase zone is reducedor cancelled, the hydrogenation reaction effect is improved, and the problem that the reaction effect is affected due to uneven distribution of catalysts caused by earth rotation is solved.

Description

technical field [0001] The invention belongs to the technical field of hydrogenation, and in particular relates to an ebullated bed hydrogenation reactor and an ebullated bed hydrogenation method. Background technique [0002] Ebullated bed hydrogenation reaction refers to the process of hydrogenation reaction of feedstock oil (mainly in liquid phase) and hydrogen (gas phase) on catalyst (solid phase). Hydrogenation reaction mainly occurs in hydrodesulfurization, hydrodenitrogenation and hydrodeoxygenation , hydrogenation saturation, hydrocracking, etc. The reactor operates in the boiling state of gas, liquid and solid. The catalyst is in a boiling state driven by the raw material oil and hydrogen entering from the bottom of the reactor, which is in a completely different fluid state from the fixed bed reactor. The ebullating bed hydrogenation reaction can process low-quality feed oil with high metal and high asphaltene content. The reaction has the characteristics of small...

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Problems solved by technology

[0003] There are currently two main types of ebullating hydrogenation technology, one is the oil phase circulation method, such as the ebullating bed process described in USRe25,770, the disadvantage of this process in practical application is: in order to maintain the liquid-solid separation effect, The amount of catalyst in the reactor should not be too much, and the utilization rate of the reactor is low. The utilization rate of the industrial ebullating bed reactor is generally only about 40% (the utilization rate generally refers to the percentage of the catalyst loading to the reactor volume (excluding the head space). The utilization rate of the reactor is generally above 90%); the reactor has a large space so that the residence time of the liquid material is too long without catalytic conditions, there is no hydrogenation reaction in this part, and the material is easy to react and coke at high temperature

Another kind is to arrange three-phase separator in the reactor, carry out gas-liquid-solid separation in the upper part of the reactor, as the ebullating bed reactor that CN02109404.7 introduces, by arranging built-in three-phase separator according to this scheme, can Increase the amount of catalyst, that is, increase the utilization space of the reactor, but in actual use, the increase in the amount of catalyst is limited. If the amount of catalyst increases, the separation effect of the three-phase separator will drop rapidly, and it is actually more efficient than the first type of ebullating bed reactor. The improvement of the efficiency is limited; CN200710012680.9 has further improved the above-mentioned technology. A guide structure is set at the lower part of the three-phase separator, and the guide structure is used to increase the operating flexibility of the three-phase separator, ensure the efficient separation of the three-phase separator, and reduce the catalyst. The amount of carry-over can increase the amount of catalyst storage and the utilization rate of the reactor, but when in use, it is still necessary to set a catalyst dilute phase zone in a certain area at the lower part of the three-phase separator (as shown in the attached figure, the amount of catalyst in this area is very small, basically hydrogenation reaction does not occur), otherwise the separation effect of the three-phase separator still cannot meet the requirements, and the existence of the dilute phase zone affects the further improvement of the reactor utilization rate (although it is pointed out in the specification that the catalyst loading in the reactor shell can be 40% to 70% of the reactor volume, but generally only about 50% of the situation can be stable), which also affects the hydrogenation reaction effect, and after the scale of the reactor is enlarged, it is more difficult to increase the catalyst loading, and it is difficult to achieve The effect of the experimental setup

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