Catalytic hydrogenation reactor for treating biomass raw material with high acid value and high iodine value

Abstract

The utility model discloses a catalytic hydrogenation reactor for treating a biomass raw material with a high acid value and a high iodine value, and belongs to the technical field of oil product hydrogenation. The catalytic hydrogenation reactor comprises a reactor pressure-bearing container, an inner cylinder, an ash discharge port, a feeding assembly, a reaction assembly and a discharging assembly, the inner cylinder is arranged in the reactor pressure-bearing container, the feeding assembly and the reaction assembly are arranged in the inner cylinder, the reaction assembly comprises a ceramic tube bundle internal part, the discharging assembly is arranged above the inner cylinder, and the discharging assembly is arranged above the inner cylinder. The ash discharge port is formed in the center of the bottom of the reactor pressure-bearing container. By arranging the ceramic tube bundle internal part in the catalytic hydrogenation reactor, on one hand, the ceramic tube bundle internal part serves as a reaction assembly and has certain acid corrosion resistance, and on the other hand, the ceramic tube bundle internal part serves as a solid catalyst carrier, selective hydrogenation of high-acid-value and high-iodine-value biomass raw materials is achieved, the iodine value is effectively reduced, and coking of the high-iodine-value biomass raw materials in the reaction process is avoided; in addition, the acid value is maintained as far as possible while the iodine value is reduced, and the solid catalyst and the catalytic hydrogenation reactor are not corroded, so that the stability of the solid catalyst and the yield of the product are improved.

Description

Technical Field

[0001] This application relates to a catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstocks, belonging to the field of oil hydrogenation technology. Background Technology

[0002] Biomass, as a renewable energy source, can replace petroleum resources in the production of liquid fuels and chemicals. Biomass oil is a liquid fuel obtained from biomass through rapid pyrolysis technology. Biomass oil contains a certain amount of unsaturated fatty acids and glycerides, and has a high oxygen content, resulting in poor thermal stability and low calorific value. It must undergo upgrading and modification to be converted into high-grade fuel. Catalytic hydrogenation is an excellent method for upgrading biomass oil. Through selective catalytic hydrogenation, the C=C double bonds in unsaturated fatty acid chains can be converted into C=C single bonds. The saturated oil is called hydrogenated oil or hardened oil. On the one hand, the hydrogenation process can improve the antioxidant capacity and thermal stability of oils, as well as improve their color and odor, alter their plasticity, and obtain suitable physicochemical properties, thus expanding their applications. On the other hand, hardened oils can be hydrolyzed to produce high-purity long-chain fatty acids, providing industrial raw materials for downstream applications. Therefore, oil hydrogenation is an effective means of oil modification and has high economic value.

[0003] Because high-iodine-value biomass raw material oils have a high number of C=C structures and a high degree of unsaturation, they have poor thermal stability and are prone to polymerization at high temperatures. If a conventional fixed-bed reactor is used, coking is likely to occur. Coking not only damages the raw material, but also increases heat consumption and shortens the equipment's operating cycle when it occurs inside the equipment. In severe cases, it can cause overheating damage to the equipment, making normal production difficult.

[0004] To address catalyst bed clogging issues, current technologies often favor fluidized bed reactors. However, high-iodine-value biomass feedstocks are more unsaturated and therefore more susceptible to oxidation and rancidity, resulting in higher acid values. Processing these high-acid-value, high-iodine-value biomass feedstocks places specific requirements on the process equipment and catalysts used, demanding resistance to acid corrosion.

[0005] Current conventional solid catalysts for catalytic hydrogenation mostly employ catalysts supported on alumina. However, these catalysts are unsuitable for biomass feedstocks with high acid and iodine values. When alumina is used as a support, it readily reacts with the high-acid-value biomass feedstock, leading to corrosion of the solid catalyst and affecting its stability. Existing technologies address the corrosive nature of high-acid-value and high-iodine-value biomass feedstocks by adding alkaline substances for neutralization to prevent corrosion of metal equipment and solid catalysts. However, the resulting carboxylates increase the cost of subsequent processing.

[0006] Therefore, due to their unique properties such as high acid value and high iodine value, high acid value and high degree of unsaturation, the catalytic hydrogenation of such biomass feedstocks places higher demands on equipment and catalysts. How to achieve catalytic hydrogenation of high acid value and high iodine value biomass feedstocks and broaden the source of raw materials for biomass hydrogenation to manufacture green products has always been the focus of technical research in the industry. Utility Model Content

[0007] To address the aforementioned issues, this application proposes a catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstocks. By incorporating ceramic tube bundles as internal components within the reactor, the ceramic tube bundles serve two purposes: firstly, they act as reaction components, exhibiting a certain degree of acid corrosion resistance; secondly, they also function as carriers for the solid catalyst. Under the action of the solid catalyst, selective hydrogenation of the high-acid-value and high-iodine-value biomass feedstocks is achieved, effectively reducing the iodine value and preventing coking of the high-iodine-value biomass feedstocks during the reaction. Furthermore, this application reduces the iodine value while maintaining the acid value as much as possible, without corroding the solid catalyst and the catalytic hydrogenation reactor, thereby improving the stability of the solid catalyst and the product yield.

[0008] According to one aspect of this application, a catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock is provided, comprising a reactor pressure vessel, an inner cylinder, an ash discharge port, a feed assembly, a reaction assembly, and a discharge assembly. The inner cylinder is disposed inside the reactor pressure vessel, the feed assembly and the reaction assembly are disposed within the inner cylinder, the reaction assembly includes ceramic tube bundle internals, the discharge assembly is disposed above the inner cylinder, and the ash discharge port is disposed at the center of the bottom of the reactor pressure vessel.

[0009] Optionally, the ceramic tube bundle internal component has a frustum-shaped structure, and the ceramic tube bundle internal component is provided with a plurality of channels, the channels penetrating the ceramic tube bundle internal component.

[0010] Optionally, the ceramic tube bundle internals are provided with a flow guiding channel in the center, and the two ends of the flow guiding channel are provided with flow guiding plates.

[0011] Optionally, the feeding assembly includes a feed inlet, an annular feed injector, and a pre-rectifier; the feed inlet is located at the bottom of the reactor pressure vessel, and the annular feed injector is located at the bottom of the inner cylinder.

[0012] Optionally, the feed inlet is connected to the annular feed injector; the pre-rectifier is connected to the inner wall of the inner cylinder, and the pre-rectifier is located above the annular feed injector to form a plunger flow pattern through mixing and equalization.

[0013] Optionally, the discharge assembly includes a combined baffle plate, a post-rectifier, a scale inhibitor bed, and a discharge port; the post-rectifier and the scale inhibitor bed are connected to the inner wall of the reactor pressure vessel; the scale inhibitor bed is located above the post-rectifier, and the post-rectifier is located above the combined baffle plate.

[0014] Optionally, the height-to-diameter ratio of the reactor pressure vessel is greater than 10:1, and the reactor pressure vessel is coaxially arranged with the inner cylinder.

[0015] Optionally, both the pre-rectifier and the post-rectifier are disc structures, and both the pre-rectifier and the post-rectifier are provided with a plurality of first through holes for material flow; both the pre-rectifier and the post-rectifier are provided with a second through hole in the center for ash and heavy impurities to settle and fall.

[0016] Optionally, the scale inhibitor bed is a packing layer with dense, narrow, tortuous channels to adsorb ash and heavy impurities, preventing them from flowing out of the reactor with the outlet material.

[0017] Optionally, the annular feed injector is connected to the feed inlet via a pipe; the annular feed injector is provided with a plurality of injection ports.

[0018] The beneficial effects that this application may produce include, but are not limited to:

[0019] 1. The catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock provided in this application incorporates ceramic tube bundle internals. On one hand, the ceramic tube bundle internals serve as reaction components, exhibiting a certain degree of acid corrosion resistance. On the other hand, the ceramic tube bundle internals can also act as a carrier for the solid catalyst. Under the action of the solid catalyst, selective hydrogenation of the high-acid-value and high-iodine-value biomass feedstock is achieved, effectively reducing the iodine value and preventing coking of the high-iodine-value biomass feedstock during the reaction process. Furthermore, this application reduces the iodine value while maintaining the acid value as much as possible, without corroding the solid catalyst and the catalytic hydrogenation reactor, thereby improving the stability of the solid catalyst and the product yield.

[0020] 2. The catalytic hydrogenation reactor for processing high acid value and high iodine value biomass feedstock provided in this application guides and equalizes the flow of biomass feedstock entering the catalytic hydrogenation reactor by setting up a feed inlet, an annular feed injector and a pre-rectifier, so as to ensure that the biomass feedstock enters the interior of the ceramic tube bundle uniformly and reacts fully with the solid catalyst.

[0021] 3. The catalytic hydrogenation reactor for processing high acid value and high iodine value biomass feedstock provided in this application has several channels inside the ceramic tube bundle internals to ensure that the biomass feedstock is in full contact with the solid catalyst to carry out the hydrogenation reaction, thereby increasing the saturation of double bonds and reducing the iodine value of the biomass feedstock.

[0022] 4. The catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock provided in this application uses a combination of baffles to guide and divert the biomass feedstock released from the inner cylinder. Most of the material returns to the lower part of the inner cylinder through the channel between the inner cylinder and the pressure vessel of the reactor, achieving backmixing and extending the residence time of the material in the reactor to continue the previously unfinished chemical reaction. The other part of the material guided by the combination of baffles becomes the outlet material through the gaps between the combination of baffles, continues to move upward, passes through the post-rectifier and scale inhibitor bed, and becomes a relatively clean pre-treated material, which flows out from the outlet. Attached Figure Description

[0023] The accompanying drawings, which are included to provide a further understanding of this application and form part of this application, illustrate exemplary embodiments and are used to explain this application, but do not constitute an undue limitation of this application. In the drawings:

[0024] Figure 1 This is a front view cross-sectional schematic diagram of a catalytic hydrogenation reactor for processing high acid value and high iodine value biomass feedstock, according to an embodiment of this application.

[0025] Figure 2 This is a front view cross-sectional schematic diagram of a catalytic hydrogenation reactor for processing high acid value and high iodine value biomass feedstock, according to another embodiment of this application.

[0026] List of components and reference numerals:

[0027] 1. Reactor pressure vessel; 2. Inner cylinder; 3. Ash discharge port; 4. Ceramic tube bundle internals; 5. Channel; 6. Flow guide channel; 7. Flow guide plate; 8. Feed inlet; 9. Annular feed injector; 10. Pre-rectifier; 11. Combined baffle plate; 12. Post-rectifier; 13. Scale inhibitor bed; 14. Discharge port. Detailed Implementation

[0028] To more clearly illustrate the overall concept of this application, a detailed explanation is provided below with reference to the accompanying drawings.

[0029] To better understand the above-mentioned objectives, features, and advantages of this application, the application will be further described in detail below with reference to the accompanying drawings and specific embodiments. It should be noted that, unless otherwise specified, the embodiments and features described in these embodiments can be combined with each other.

[0030] Many specific details are set forth in the following description in order to provide a full understanding of this application. However, this application may also be implemented in other ways different from those described herein. Therefore, the scope of protection of this application is not limited to the specific embodiments disclosed below.

[0031] Furthermore, it should be understood in the description of this application that the terms "center," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "axial," "radial," and "circumferential" indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this application.

[0032] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this application, "a plurality of" means two or more, unless otherwise explicitly specified.

[0033] In this application, unless otherwise expressly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection, an electrical connection, or a communication connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. Those skilled in the art can understand the specific meaning of the above terms in this application according to the specific circumstances.

[0034] In this application, unless otherwise expressly specified and limited, the "above" or "below" of the second feature can mean that the first and second features are in direct contact, or that the first and second features are in indirect contact through an intermediate medium. In the description of this specification, references to terms such as "an embodiment," "some embodiments," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of this application. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described can be combined in any suitable manner in one or more embodiments or examples.

[0035] refer to Figure 1 and Figure 2The embodiments of this application disclose a catalytic hydrogenation reactor for processing high acid value and high iodine value biomass raw materials, including a reactor pressure vessel 1, an inner cylinder 2, an ash discharge port 3, a feed assembly, a reaction assembly, and a discharge assembly. The inner cylinder 2 is located inside the reactor pressure vessel 1, and the feed assembly and the reaction assembly are located in the inner cylinder 2. The reaction assembly includes a ceramic tube bundle inner part 4, the discharge assembly is located above the inner cylinder 2, and the ash discharge port 3 is located at the center of the bottom of the reactor pressure vessel 1.

[0036] Specifically, by incorporating ceramic tube bundle internals 4 into the catalytic hydrogenation reactor, the ceramic tube bundle internals 4 serve two purposes: firstly, as a reaction component, they possess a certain degree of acid corrosion resistance; secondly, they can also act as a carrier for the solid catalyst, enabling selective hydrogenation of high-acid-value and high-iodine-value biomass feedstocks under the action of the solid catalyst, effectively reducing the iodine value and preventing coking of the high-iodine-value biomass feedstocks during the reaction process; furthermore, this application aims to reduce the iodine value while maintaining the acid value as much as possible, without corroding the solid catalyst and the catalytic hydrogenation reactor, thereby improving the stability of the solid catalyst and the product yield.

[0037] In one embodiment, the ceramic tube bundle inner component 4 has a frustum-shaped structure, and the ceramic tube bundle inner component 4 is provided with a plurality of channels 5, which penetrate the ceramic tube bundle inner component 4.

[0038] Specifically, this application does not limit the number or size of channels 5, and those skilled in the art can choose according to the actual situation.

[0039] In one embodiment, the ceramic tube bundle internal component 4 is provided with a flow guide channel 6 in the center, and flow guide plates 7 are provided at both ends of the flow guide channel 6.

[0040] Specifically, under the combined action of the flow channel 6 and the flow plate 7, the biomass raw material is encouraged to enter the channel 5 of the ceramic tube bundle internals 4 so as to fully contact the solid catalyst and make the reaction complete.

[0041] As another implementation, the ceramic tube bundle internal component 4 can also serve as a carrier for the solid catalyst. That is, an active metal material is coated on the inner wall of the ceramic tube bundle internal component 4 to form a solid catalyst. On the one hand, as part of the solid catalyst, the ceramic tube bundle internal component 4 helps to maintain the unobstructed flow of the channel 5 of the ceramic tube bundle internal component 4 and avoid problems such as blockage. On the other hand, due to the acid and corrosion resistant properties of the ceramic tube bundle internal component 4, it also serves as the reaction site for the hydrogenation reaction. This helps to maintain the acid value as much as possible while reducing the iodine value, so as not to corrode the solid catalyst and the catalytic hydrogenation reactor, thereby improving the stability of the solid catalyst and the yield of the product.

[0042] In one embodiment, the feeding assembly includes a feed inlet 8, an annular feed injector 9, and a pre-rectifier 10; the feed inlet 8 is located at the bottom of the reactor pressure vessel 1, and the annular feed injector 9 is located at the bottom of the inner cylinder 2.

[0043] Specifically, this application does not limit the size of the feed inlet 8, and those skilled in the art can choose according to the actual situation.

[0044] In one implementation, the feed inlet 8 is connected to the annular feed injector 9; the pre-rectifier 10 is connected to the inner wall of the inner cylinder 2, and the pre-rectifier 10 is located above the annular feed injector 9 to form a plunger flow pattern through mixing and equalization.

[0045] Specifically, by setting up the feed inlet 8, the annular feed injector 9, and the pre-rectifier 10, the biomass feedstock entering the catalytic hydrogenation reactor is guided and shaped to ensure that the biomass feedstock enters the interior of the ceramic tube bundle 4 evenly and reacts fully with the solid catalyst.

[0046] In one embodiment, the discharge assembly includes a combined baffle plate 11, a post-rectifier 12, a scale inhibitor bed 13, and a discharge port 14; the post-rectifier 12 and the scale inhibitor bed 13 are connected to the inner wall of the reactor pressure vessel 1; the scale inhibitor bed 13 is located above the post-rectifier 12, and the post-rectifier 12 is located above the combined baffle plate 11.

[0047] Specifically, by setting up combined baffles 11, the biomass raw materials released from the inner cylinder 2 are guided and diverted. Most of the material returns to the lower part of the inner cylinder 2 through the channel between the inner cylinder 2 and the reactor pressure vessel 1, achieving backmixing, so as to prolong the residence time of the material in the reactor and continue the previously unfinished chemical reaction. The other part of the material guided by the combined baffles 11 becomes the outlet material through the gaps between the combined baffles 11, continues to move upward, and becomes a relatively clean pre-treated material after passing through the post-rectifier 12 and the scale inhibitor bed 13, and flows out from the discharge port 14.

[0048] In one implementation, the height-to-diameter ratio of the reactor pressure vessel 1 is greater than 10:1, and the reactor pressure vessel 1 and the inner cylinder 2 are arranged coaxially.

[0049] Specifically, this application makes specific limitations on the height-to-diameter ratio of the reactor pressure vessel 1, which is beneficial to the full reaction of biomass feedstock in the catalytic hydrogenation reactor.

[0050] In one embodiment, both the pre-rectifier 10 and the post-rectifier 12 are disc structures. Both the pre-rectifier 10 and the post-rectifier 12 are provided with a plurality of first through holes to allow material to flow through. Both the pre-rectifier 10 and the post-rectifier 12 are provided with a second through hole in the center to allow ash and heavy impurities to settle and fall.

[0051] Specifically, this application does not impose specific limitations on the number and size of the first and second through holes, and those skilled in the art can make selections based on the actual situation.

[0052] Specifically, the diameter of the second through hole is larger than the diameter of the first through hole.

[0053] In one implementation, the scale inhibitor bed 13 is a packing layer with dense, narrow, tortuous channels, used to adsorb ash and heavy impurities, preventing them from flowing out of the reactor with the outlet material.

[0054] In one implementation, the annular feed injector 9 is connected to the feed inlet 8 via a pipe; the annular feed injector 9 is provided with several injection ports.

[0055] The working process of the catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock provided in this application is as follows:

[0056] High-acid-value and high-iodine-value feedstock oil, after being separated from mechanical impurities and free water, is mixed with hydrogen to become hydrogen-mixed feedstock oil. This is then heated and injected with a liquid catalyst to obtain feed oil. The feed oil enters the catalytic hydrogenation reactor through the inlet 8 at the bottom. The feed oil then passes through an annular feed injector 9 installed at the bottom of the reactor's inner cylinder 2, being sprayed upwards into the inner cylinder 2. The sprayed feed oil moves upwards and, after being mixed and homogenized by the pre-rectifier 10, enters the ceramic reactor in a relatively ideal plunger flow pattern. In the various channels 5 within the inner tube bundle 4, the feed oil reacts under the action of the solid catalyst, transforming into a material with a low iodine value. This material then exits the ceramic inner tube bundle 4 and enters the upper middle part of the reactor inner cylinder 2. Due to the considerable volume of the inner cylinder 2, the material flows slowly in the upper middle part of the inner cylinder 2 and remains there for a relatively long time. Under the action of the liquid catalyst, the material in the inner cylinder 2 continuously undergoes a series of chemical reactions such as hydrogenation, demetallization, and degumming to remove impurities from the raw material and saturate some double bonds. Afterwards, the material flows out from the upper opening of the inner cylinder 2. Under the guidance and diversion effect of the combined baffle 11, most of the material returns to the lower part of the inner cylinder 2 through the channel between the inner cylinder 2 and the reactor pressure vessel 1, where it is back-mixed with the fresh feed oil injected by the annular feed jet pipe. Under the entrainment of the feed jet from the annular feed injector 9, a circulating flow is formed throughout the reactor to prolong the residence time of the material in the reactor and continue the previously unfinished chemical reaction. The other part of the material guided by the combined baffle 11 becomes the outlet material through the gaps between the combined baffle 11 and continues to move upward. The effluent first passes through the post-rectifier 12, and under its flow equalization effect, it then passes through the scale inhibitor bed 13. Through its blocking effect, the solid impurities carried in the effluent are filtered out, becoming a relatively clean pre-treated material. Finally, it flows out from the discharge port 14 at the top of the reactor, becoming the raw material for the subsequent refining process. The solid ash and other non-ideal components such as heavy oil produced by the hydrogenolysis reaction in the reactor will be deposited at the bottom of the reactor under the blocking effect of the scale inhibitor bed 13 and gravity settling. Through operation control, the above components can be continuously or intermittently discharged from the reactor through the ash discharge port 3 at the bottom of the reactor.

[0057] The various embodiments in this specification are described in a progressive manner. Similar or identical parts between embodiments can be referred to interchangeably. Each embodiment focuses on describing the differences from other embodiments. In particular, the system embodiments are basically similar to the method embodiments, so the description is relatively simple; relevant parts can be referred to the descriptions in the method embodiments.

[0058] The above description is merely an embodiment of this application and is not intended to limit the scope of this application. Various modifications and variations can be made to this application by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of this application should be included within the scope of the claims of this application.

Claims

1. A catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock, characterized in that, The reactor includes a pressure vessel, an inner cylinder, an ash discharge port, a feeding assembly, a reaction assembly, and a discharge assembly. The inner cylinder is located inside the pressure vessel, the feeding assembly and the reaction assembly are located in the inner cylinder, the reaction assembly includes ceramic tube bundle internals, the discharge assembly is located above the inner cylinder, and the ash discharge port is located at the center of the bottom of the pressure vessel.

2. The catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock according to claim 1, characterized in that, The ceramic tube bundle internal component has a frustum-shaped structure, and the ceramic tube bundle internal component is provided with several channels that penetrate through the ceramic tube bundle internal component.

3. The catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock according to claim 2, characterized in that, The ceramic tube bundle internals are provided with a flow guiding channel in the center, and the two ends of the flow guiding channel are provided with flow guiding plates.

4. The catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock according to claim 2, characterized in that, The feeding assembly includes a feed inlet, an annular feed injector, and a pre-rectifier; the feed inlet is located at the bottom of the reactor pressure vessel, and the annular feed injector is located at the bottom of the inner cylinder.

5. The catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock according to claim 4, characterized in that, The feed inlet is connected to the annular feed injector; the pre-rectifier is connected to the inner wall of the inner cylinder and is located above the annular feed injector to form a plunger flow pattern through mixing and equalization.

6. The catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock according to claim 4, characterized in that, The discharge assembly includes a combined baffle plate, a post-rectifier, a scale inhibitor bed, and a discharge port; the post-rectifier and the scale inhibitor bed are connected to the inner wall of the reactor pressure vessel; the scale inhibitor bed is located above the post-rectifier, and the post-rectifier is located above the combined baffle plate.

7. The catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock according to claim 1, characterized in that, The height-to-diameter ratio of the reactor pressure vessel is greater than 10:1, and the reactor pressure vessel is coaxially arranged with the inner cylinder.

8. The catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock according to claim 6, characterized in that, Both the pre-rectifier and the post-rectifier are disc structures. Each of the pre-rectifier and the post-rectifier has several first through holes to allow material to flow through. Each of the pre-rectifier and the post-rectifier has a second through hole in the center to allow ash and heavy impurities to settle and fall.

9. The catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock according to claim 6, characterized in that, The scale inhibitor bed is a packing layer with dense, narrow, and tortuous channels, used to adsorb ash and heavy impurities, preventing them from flowing out of the reactor with the outlet material.

10. The catalytic hydrogenation reactor for processing high-acid-value and high-iodine-value biomass feedstock according to claim 4, characterized in that, The annular feed injector is connected to the feed inlet via a pipe; the annular feed injector is provided with several injection ports.

Images