This application claims foreign priority to Chinese Patent Application No. 201911175767.7, filed Nov. 26, 2019, the disclosure of which is incorporated herein in its entirety by reference.

TECHNICAL FIELD

The present disclosure relates to the chemical field, in particular to a differential hydrogenation reaction apparatus.

BACKGROUND

The scale of chemical enterprises becomes larger and the yield of a single machine becomes increased caused by scale benefit of the chemical industry. By taking the most commonly used reacting kettles in the chemical enterprises as examples, the volume is increased to 10 m3-100 m3from past 1000 L-5000 L, and reported that the volume of a foreign fermentation reaction tank achieves 3200 m3. With continuous increase of the reactor, the problem, must to be solved, of reduction in reaction quality caused by the unbalanced reaction phenomenon in the reactor occurs. For example, for a large-capacity reactor, differences of heat transport, quality transport and momentum transport occur between materials at different positions in the reactor, which causes unbalanced reaction of unstable quality of a product. However, the non-equilibrium of such reaction is in proportion to the volume of the reactor, and thus the larger the reactor is, the more serious the non-equilibrium phenomenon is. In order to eliminate non-equilibrium of the reactor and momentum transport, energy transport, quality transport and reaction engineering of acceleration, the chemical reactor is generally arranged as a stirring reactor. However, stirring reaction is limited by the capacity of the reactor, and for a large or ultra-large reactor, a mode of directly arranging a stirring paddle is infeasible. Hence, the large scale requirement of the reactor and the non-equilibrium phenomenon caused by large scale of the reactor severely form a pair of contradictions in the chemical reaction.

Hydrogenation reaction is one of the most common reactions in industry and widely exists in industries such as the refining industry, the chemical industry, the pharmaceutical industry, the food industry and the agricultural industry. As hydrogen is very light and energy of a hydrogen bond is high, hydrogenation reaction has two common points that A, all processes adopt high-pressure hydrogenation, the very light hydrogen is pressurized into a liquid phase material to participate to reaction, and a generally used hydrogen pressure range is 5 MPa-50 MPa; and B, in all the processes, the hydrogen always participates to material reaction in a very high ratio, and a ratio of a general hydrogen standard volume to a material volume is 500-1000.

To sum up, the large or ultra-large hydrogenation reactor must have the following problems of

A, safety problem: high pressure or ultra-high pressure hydrogenation reactor has the danger of having leakage and then causing explosion, and the hydrogen may generate strong effects of hydrogen attack and hydrogen embrittlement to a metal wall face of the reactor, such that the reactor has a tiny breaking point to cause leakage. In order to prevent leakage of the reactor, a high-intensity material and a thickness of thickened metal wall face must be adopted, for example, specifications of a fixed-bed high-pressure hydrogenation reactor manufactured in China in 1999 are as follows:

inside diameter: 4000 mm; inside circumference: 23016 mm; wall thickness: 176.5 mm;

gross weight: 366T; pressure: 19.95 MPa; temperature: 435° C.

Therefore, the thickness of the wall face of a reactor of only 20 MPa approaches 20 cm. Thus, the first question brought by large or ultra-large high-pressure hydrogenation reactor is the safety problem, and in other words, for running safety of the reactor, high investment must be required to obtain a reactor made of a high-quality material and having ultra thickness of a wall;

B, unbalanced reaction problem: known by tests from micromolecular aspect, the time required for breakage and rebonding of molecular bonds is only from a few microseconds to tens of microseconds, but as for the large or ultra-large reactor, a residence time (of about 1 h generally) of a material in the reactor must be prolonged for balanced reaction. Theoretically, reaction is completely balanced only when the residence time of the material is infinitely large; and however, prolonging of the residence time means reduction in productivity.

Based on the above reasons, it is necessary to provide a novel hydrogenation reaction process to overcome the high pressure unsafety problem and the unbalanced reaction problem generally existing in the hydrogenation reaction process.

SUMMARY

A primary objective of the present disclosure is to provide a differential hydrogenation reaction apparatus to solve the high pressure unsafety problem and the unbalanced reaction problem generally existing in the hydrogenation reaction process in the prior art.

In order to accomplish the above object, according to one aspect of the present disclosure, provided is a differential hydrogenation reaction apparatus which includes mixing vessel with reaction product inlets, a plurality of microreactors used as hydrogenation reaction places of a liquid phase reaction raw material and a raw material conveying device; each microreactor is provided with a liquid phase reaction raw material inlet and a reaction product outlet, each reaction product outlet is connected with the corresponding reaction product inlet, the plurality of microreactors are divided into one group or a plurality of groups which are arranged in parallel, and each group includes at least one microreactor arranged in parallel; each microreactor in each group is a pressurized microreactor with a volume smaller than or equal to 0.025m3 and an inside diameter smaller than 0.1 m, or an atmospheric microreactor with a volume smaller than or equal to 0.1 m3 and an inside diameter smaller than 0.1 m; and a raw material conveying device is arranged on a feeding pipeline of the liquid phase reaction raw material inlet and is used for conveying the liquid phase reaction raw material into the microreactors.

Furthermore, the mixing vessel is further provided with a mixed material outlet, the differential hydrogenation reaction apparatus further includes a forced circulation apparatus, and the forced circulation apparatus includes: a circulation pipeline, an inlet of which is connected with the mixed material outlet and an outlet of which is connected with a liquid phase reaction raw material inlet; and a forced circulation pump, arranged on the circulation pipeline.

Furthermore, the mixing vessel is provided with a cavity, the cavity is internally provided with a non-submersed impinging stream assembly, the non-submersed impinging stream assembly is used for further performing non-submersed impinging, cavitation and shearing on a hydrogenation reaction product which enters from the reaction product inlet and goes out from the microreactors.

Furthermore, the non-submersed impinging stream assembly includes a cylinder, an inner cavity of the cylinder is used for providing a non-submersed impinging place, a wall of the cylinder is provided with a plurality of first hole structures, and an included angle is arranged between an axial direction of each first hole structure and an axial direction of the cylinder.

Furthermore, the cylinder is provided with inlets at the two ends, the mixing vessel is provided with two groups of reaction product inlets, each group of which includes at least one reaction product inlet, and the two groups of the reaction product inlets are arranged on the two sides of the mixing vessel respectively, wherein a part of the reaction product outlets are connected with one group of the reaction product inlets respectively, the other part of the reaction product outlets are connected with the other group of the reaction product inlets respectively, and the hydrogenation reaction products entering from the two groups of reaction product inlets enter the cylinder from the inlets at the two ends of the cylinder in a manner of an ejection fluid and are subjected to non-submersed impinging.

Furthermore, an inlet is formed in one end of the cylinder, and an impinging bottom plate is arranged at the other end of the cylinder; or an inlet is formed in one end of the cylinder, a radial sectional area of the cylinder is gradually reduced in a direction far away from the inlet end, and the other end of the cylinder is closed, wherein the reaction product inlets are all connected with the inlet end of the cylinder to be used for enabling the hydrogenation reaction products to enter the cylinder in the manner of the ejection fluid and are subjected to non-submersed impinging.

Furthermore, the non-submersed impinging stream assembly is arranged at the position, close to the top end, of the cavity of the mixing vessel.

Furthermore, each microreactor is of a tubular structure with a length-diameter ratio of (10-20) to 1.

Furthermore, each microreactor is further internally provided with a plurality of pipeline cavitation plates, each of which is provided with a plurality of second hole structures.

Furthermore, the pipeline cavitation plates are vertically or obliquely arranged in the corresponding microreactors in an axial direction.

Furthermore, two adjacent pipeline cavitation plates are the same or opposite in an oblique direction in each microreactor.

Furthermore, the differential hydrogenation reaction apparatus further includes a heating apparatus, and the heating apparatus is used for heating the microreactors and the mixing vessel.

Furthermore, the forced circulation apparatus further includes pipeline type heating furnaces, and the pipeline type heating furnaces are used for heating the circulation pipeline.

Furthermore, the circulation pipeline is further provided with hydrogen inlets to be used for introducing hydrogen into the circulation pipeline.

Furthermore, a gaseous product outlet is further formed in the top of the mixing vessel, the differential hydrogenation reaction apparatus further includes a condenser, the condenser is provided with a gaseous product inlet, a condensate outlet and a tail gas outlet, and the gaseous product inlet is connected with the gaseous product outlet.

Furthermore, the tail gas outlet is connected with the hydrogen inlets.

Furthermore, each microreactor is filled with a hydrogenation catalyst, and/or is added with a high electric field component and/or is added with a photocatalysis component.

The present disclosure provides a differential hydrogenation reaction apparatus which includes mixing vessel, a plurality of microreactors and a raw material conveying device; the mixing vessel is provided with reaction product inlets; each microreactor is used as a hydrogenation reaction place of a liquid phase reaction raw material and is provided with a liquid phase reaction raw material inlet and a reaction product outlet, each reaction product outlet is connected with the corresponding reaction product inlet, the plurality of microreactors are divided into one group or a plurality of groups which are arranged in parallel, and each group includes at least one microreactor arranged in parallel; each microreactor in each group is a pressurized microreactor with a volume smaller than or equal to 0.025 m3 and an inside diameter smaller than 0.1 m, or an atmospheric microreactor with a volume smaller than or equal to 0.1 m3 and an inside diameter smaller than 0.1 m; and the raw material conveying device is arranged on a feeding pipeline of the liquid phase reaction raw material inlet and is used for conveying a liquid phase reaction raw material into the microreactors. The problems of unsafety and non-equilibrium of high pressure generally existing in the hydrogenation reaction process at present can be effectively solved by adopting the reaction apparatus of the present disclosure. Simultaneously, the investment of the differential hydrogenation reaction apparatus would be greatly lower than that of a large or ultra-large high-pressure hydrogenation reactor; the safety of the differential hydrogenation reaction apparatus is greatly higher than that of the large or ultra-large high-pressure hydrogenation reactor; and overhaul and maintenance of the differential hydrogenation reaction apparatus may be implemented under the condition without stopping running of equipment, the economic benefit and the running flexibility of the differential hydrogenation reaction apparatus is also larger than those of an existing large high-pressure hydrogenation reactor, and safe and economic social requirements are implemented on the premise of invariability in production efficiency and reaction effect.

