The present invention is concerned with a process for providing a homogeneous particle-containing slurry comprising the steps of: (a) providing a vessel comprising at least one impeller rotating around a vertical axis of the vessel, wherein a rotational speed n.sub.1 of the at least one impeller is higher than n.sub.min according to equation (1), the vessel further comprising an inlet and an outlet; (b) introducing a particle-containing slurry into the vessel or introducing components forming the particle-containing slurry into the vessel; (c) rotating the at least one impeller at least around the vertical axis for homogenizing and/or maintaining a homogeneous particle distribution within the slurry; (d) withdrawing the homogeneous particle-containing slurry via the outlet; (e) reducing the rotational speed n.sub.1 of the at least one impeller to a reduced rotational speed n.sub.red, whereas n.sub.red is lower than n.sub.1 and higher or equal gas inlet than n.sub.min according to equation (1):

[00001]$\begin{array}{cc}{n}_{\min }=\frac{S{v}^{0.1}{D_p^{0.2}\left(g\frac{\Delta \rho }{{\rho }_f}\right)}^{0.45}{B}^{0.13}}{D_a^{0.85}}& \left(1\right)\end{array}$

The present invention is concerned with a process for providing a homogeneous particle-containing slurry comprising the steps of: (a) providing a vessel comprising at least one impeller rotating around a vertical axis of the vessel, wherein a rotational speed n.sub.1 of the at least one impeller is higher than n.sub.min according to equation (1), the vessel further comprising an inlet and an outlet; (b) introducing a particle-containing slurry into the vessel or introducing components forming the particle-containing slurry into the vessel; (c) rotating the at least one impeller at least around the vertical axis for homogenizing and/or maintaining a homogeneous particle distribution within the slurry; (d) withdrawing the homogeneous particle-containing slurry via the outlet; (e) reducing the rotational speed n.sub.1 of the at least one impeller to a reduced rotational speed n.sub.red, whereas n.sub.red is lower than n.sub.1 and higher or equal gas inlet than n.sub.min according to equation (1):

[00001]$\begin{array}{cc}{n}_{\min }=\frac{S{v}^{0.1}{D_p^{0.2}\left(g\frac{\Delta \rho }{{\rho }_f}\right)}^{0.45}{B}^{0.13}}{D_a^{0.85}}& \left(1\right)\end{array}$

This disclosure relates to a processing that includes a first shell and a second shell disposed within the first shell. The second shell includes a first end, a second end, and a wall extending between the first end and the second end. The second shell also defines a cavity and a longitudinal axis extending between the first end and the second end. A cross section of the second shell transverse to the longitudinal axis includes a first arcuate inner wall portion having a first radius of curvature and a second arcuate inner wall portion having a second radius of curvature. The first radius of curvature is larger than the second radius of curvature.

This disclosure relates to a processing that includes a first shell and a second shell disposed within the first shell. The second shell includes a first end, a second end, and a wall extending between the first end and the second end. The second shell also defines a cavity and a longitudinal axis extending between the first end and the second end. A cross section of the second shell transverse to the longitudinal axis includes a first arcuate inner wall portion having a first radius of curvature and a second arcuate inner wall portion having a second radius of curvature. The first radius of curvature is larger than the second radius of curvature.

Methods for determining ethylene concentration in an ethylene oligomerization reactor using an ultrasonic flow meter are described, and these methods are integrated into ethylene oligomerization processes and related oligomerization reactor systems.

Methods for determining ethylene concentration in an ethylene oligomerization reactor using an ultrasonic flow meter are described, and these methods are integrated into ethylene oligomerization processes and related oligomerization reactor systems.

Provided herein are methods, devices and systems for processing of carbonaceous compositions. The processing may include the manufacture (or synthesis) of oxidized forms of carbonaceous compositions and/or the manufacture (or synthesis) of reduced forms of oxidized carbonaceous compositions. Some embodiments provide methods, devices and systems for the manufacture (or synthesis) of graphite oxide from graphite and/or for the manufacture (or synthesis) of reduced graphite oxide from graphite oxide.

Provided herein are methods, devices and systems for processing of carbonaceous compositions. The processing may include the manufacture (or synthesis) of oxidized forms of carbonaceous compositions and/or the manufacture (or synthesis) of reduced forms of oxidized carbonaceous compositions. Some embodiments provide methods, devices and systems for the manufacture (or synthesis) of graphite oxide from graphite and/or for the manufacture (or synthesis) of reduced graphite oxide from graphite oxide.

A method for producing polyphenylene ether amine includes following steps. In step (a), a hydrogenation reaction tank is provided; a guided gas stirrer is disposed in the hydrogenation reaction tank. In step (b), a reaction solution is placed in the hydrogenation reaction tank, and the reaction solution is nitro polyphenylene ether dissolved in a solvent. In step (c), a hydrogenation catalyst is added to the reaction solution. In step (d), a hydrogen gas is introduced into the hydrogenation reaction tank. In step (e), the guided gas stirrer is activated. In step (f), a hydrogenation reaction is carried out on the conditions that a reaction temperature is 50-200° C. and a reaction time is 1-20 hours, so as to hydrogenate the nitro polyphenylene ether in the reaction solution to polyphenylene ether amine. In step (g), the reaction solution is cooled down to a room temperature; the hydrogenation catalyst is removed.

A method for producing polyphenylene ether amine includes following steps. In step (a), a hydrogenation reaction tank is provided; a guided gas stirrer is disposed in the hydrogenation reaction tank. In step (b), a reaction solution is placed in the hydrogenation reaction tank, and the reaction solution is nitro polyphenylene ether dissolved in a solvent. In step (c), a hydrogenation catalyst is added to the reaction solution. In step (d), a hydrogen gas is introduced into the hydrogenation reaction tank. In step (e), the guided gas stirrer is activated. In step (f), a hydrogenation reaction is carried out on the conditions that a reaction temperature is 50-200° C. and a reaction time is 1-20 hours, so as to hydrogenate the nitro polyphenylene ether in the reaction solution to polyphenylene ether amine. In step (g), the reaction solution is cooled down to a room temperature; the hydrogenation catalyst is removed.