Three-stage reaction kettle for continuously catalyzing oil plants by straws
By designing a three-stage reactor for straw continuous catalytic oil, using thermal conduction oil and agitator to accelerate thermal cracking, combined with electronic valve control of multi-stage reactors, the problem of low production efficiency of straw catalytic liquid fuel in the prior art is solved, and efficient and continuous straw liquid fuel production is achieved.
Patent Information
- Application Number
- CN202422308490.3
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-09-22
- Publication Date
- 2025-08-12
- Estimated Expiration
- 2034-09-22
AI Technical Summary
The primary reactor for the production of existing straw catalytic liquid fuel has complex structure, insufficient reaction, high energy consumption, low output rate, difficult discharge, unable to achieve continuous reaction, and low efficiency.
A three-stage reactor for straw continuous catalytic oil is designed, including a primary reactor, agitator, heater, filter, vacuum machine, a secondary reactor, a primary reactor, a condenser interface, a separator interface, a catalyst interface, an electronic valve and a conveyor pipe. The continuous reaction is achieved through the electronic valve control of the multi-stage reactor, and thermal cracking is accelerated by using thermal oil and catalyst to ensure uniform mixing of materials.
It realizes efficient production of straw liquid fuel, improves the continuous participation efficiency of the reactor, enhances oil output efficiency, simplifies the operation process, and reduces energy consumption.
Smart Images
Figure CN223214046U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of production of biomass liquid fuel, in particular to a three-stage reactor for continuous catalysis of oil by straw. Background Art
[0002] The existing primary reactor for straw-catalyzed liquid fuel production has no valve control problem and requires the participation of each link and the process of participation in the reaction. Its structure is complex and the reaction is not sufficient. At the same time, it is high in energy consumption, the output rate of biomass liquid fuel is low, the discharge is difficult, and the reaction and discharge cycle is slow. Therefore, there is an urgent need for a multi-stage reactor device that can continuously participate in the reaction and improve efficiency. Utility Model Content
[0003] In order to overcome the above-mentioned deficiencies in the prior art, the present invention provides a three-stage reactor for continuous catalytic conversion of straw into oil.
[0004] A three-stage reactor for continuous catalytic conversion of straw into oil comprises a primary reactor, an agitator, a heater, a filter, a vacuum machine, a secondary reactor, a primary reactor, a condenser interface, a separator interface, a catalyst interface, an electronic valve, a vacuum pumping pipe, and a delivery pipe; the primary reactor is connected to the primary reactor via a delivery pipe, the primary reactor is connected to the secondary reactor via a delivery pipe, and the filter is connected to the primary reactor via a vacuum pumping pipe, the filter is connected to the primary reactor via a vacuum pumping pipe, the filter is connected to the secondary reactor via a vacuum pumping pipe, the filter is connected to the vacuum machine, the vacuum pumping pipe is provided with an electronic valve, and the delivery pipe is provided with an electronic valve.
[0005] Working principle and process of the present invention:
[0006] Close the electronic valve R4, add the crushed straw raw material and catalyst into the primary reactor, add heat transfer oil into the primary reactor, start the agitator to mix thoroughly, open the electronic valve R1 at the same time, close the electronic valve R2 and the electronic valve R3, and start the vacuum machine to extract the air in the primary reactor, so that the primary reactor becomes a vacuum state, then turn on the heater to heat to 300 degrees Celsius, after being fully heated, the steam (including bio-oil) enters the condenser interface and then to the condenser for condensation, cooling and collecting the oil, and maintains a temperature of 300 degrees Celsius until no steam enters the condenser, then stops heating, and waits for the mixture in the primary reactor (straw powder residue and heat transfer oil, catalyst mixture) to cool naturally, opens the delivery pipe R4 and closes the delivery pipe R5, and uses the mixture in the primary reactor to flow into the primary reactor by gravity, and after all the mixture enters the primary reactor, closes the electronic valve R4 and closes the electronic valve at the same time. Doors R1-R3, and pressurize the interior of the primary reactor for minutes (at the same time, add the crushed straw raw material and catalyst into the primary reactor, then add heat transfer oil into the primary reactor, turn on the agitator to fully mix, and repeat the above process) open the delivery pipe R5, and the mixture flows into the secondary reactor by gravity. After the mixture has completely entered the secondary reactor, open the electronic valves R1 and R3 (at this time the primary reactor is in the vacuum stage), close the electronic valve R2, turn on the vacuum machine and heater, add to 500 degrees Celsius, and after sufficient heating, the steam (including bio-oil) enters the condenser interface and then to the condenser for condensation, cooling and collection of the oil, and continues to maintain a temperature of 500 degrees Celsius until no steam enters the condenser. At this time, stop heating (at this time the steam in the primary reactor enters the condenser together), the mixture in the primary reactor enters the primary reactor, and the mixture in the secondary reactor enters the separator through the separator interface.
[0007] Preferably, the catalyst interface (Q) is connected to the catalyst storage tank, the first condenser interface (H) is connected to the condenser, the upper end of the secondary reactor (F) is connected to the condenser through the first condenser interface (H), and the lower end of the secondary reactor (F) is connected to the separator through the separator interface (L), and the primary reactor is provided with a second condenser interface (Y), and the second condenser interface (Y) is connected to the condenser.
[0008] Preferably, the primary reactor (A) is provided with an agitator (B) inside and a first heater (C) at the bottom, and the secondary reactor (F) is provided with a second heater (C1) at the bottom.
[0009] The beneficial effects of the present invention are:
[0010] 1. Heat transfer oil participates in the primary reaction of straw powder, so that the materials in the primary reactor are evenly heated and have good fluidity. At the same time, adding sulfide catalyst can accelerate the thermal cracking rate.
[0011] 2. The setting of the agitator can make the materials in the pre-reactor mixed evenly and prevent the accumulation of materials. It can also speed up the cracking speed and improve the production efficiency.
[0012] 3. Multiple electronic valves facilitate the continuous reaction of multi-stage reactors and improve oil output efficiency. BRIEF DESCRIPTION OF THE DRAWINGS
[0013] Figure 1 It is a structural diagram of the present utility model.
[0014] A: primary reactor, B: agitator, C: first heater, C1: second heater, D: filter, E: vacuum machine, F: secondary reactor, G: first reactor, H: first condenser interface, L: separator interface, Q: catalyst interface, Y: second condenser interface, R1-R5: electronic valve, t1-t3: vacuum pumping pipe, t4-t5: delivery pipe; DETAILED DESCRIPTION
[0015] The following will clearly and completely describe the technical solutions in the embodiments of the present invention in conjunction with the accompanying drawings. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of the present invention.
[0016] It should be noted that, in this article, relational terms such as first and second, etc. are only used to distinguish one entity or operation from another entity or operation, and do not necessarily require or imply any actual relationship or order between these entities or operations. Moreover, the terms "include", "comprises" or any other variations thereof are intended to cover non-exclusive inclusion, so that a process, method, article or device that includes a series of elements includes not only those elements, but also other elements not explicitly listed, or also includes elements inherent to such process, method, article or device. In the absence of further restrictions, the elements defined by the sentence "including a..." do not exclude the existence of other identical elements in the process, method, article or device that includes the elements; for example, xx phase is not a fixed word, but a state of matter, such as the liquid phase of a metal, which is the molten state of the metal, and does not specifically refer to a fixed object. For example, the "slag phase" in this application is the filter residue after the target fuel is filtered out after the straw powder and catalyst are treated with heat transfer oil, or a mixture of the filter residue and heat transfer oil. If the two liquid phases are mixed but not miscible, they are divided into oil phase and water phase by density stratification. The water phase is not water in the noun sense, but a pictographic expression made to distinguish the liquid after extraction. It may also be alcohol or vinegar, the purpose of which is to distinguish the two liquid mixtures in terms of expression.
[0017] like Figure 1 As shown, a three-stage reactor for continuous catalytic production of straw oil is characterized by comprising: a primary reactor A, an agitator B, a first heater C, a second first heater C1, a filter D, a vacuum machine E, a secondary reactor F, a primary reactor G, a first condenser interface H, a separator interface L, a catalyst interface Q, electronic valves R1-R5, vacuum exhaust pipes t1-t3, and delivery pipes t4-t5; the primary reactor A is connected to the primary reactor G via a delivery pipe t4, and the primary reactor G is connected to the secondary reactor F via a delivery pipe t5. At the same time, the filter D is connected to the primary reactor (A) through a vacuum exhaust pipe t1, the filter D is connected to the first reactor G through a vacuum exhaust pipe t2, the filter D is connected to the second reactor F through a vacuum exhaust pipe t3, the filter D is connected to the vacuum machine E, the vacuum exhaust pipe t1 is provided with an electronic valve R1, the vacuum exhaust pipe t2 is provided with an electronic valve R2, the vacuum exhaust pipe t3 is provided with an electronic valve R3, the delivery pipe t4 is provided with an electronic valve R4, and the delivery pipe t5 is provided with an electronic valve R5.
[0018] Furthermore, the catalyst interface Q is connected to the catalyst storage tank, the first condenser interface H is connected to the condenser, the upper end of the secondary reactor F is connected to the condenser through the first condenser interface H, and the lower end of the secondary reactor F is connected to the separator through the separator interface L. The primary reactor is provided with a second condenser interface Y, and the second condenser interface Y is connected to the condenser.
[0019] Furthermore, the primary reactor A is provided with an agitator B inside and a first heater C at the bottom, and the secondary reactor F is provided with a second first heater C1 at the bottom.
[0020] The working principle and process of this utility model:
[0021] Close the electronic valve R4, add the crushed straw raw material and catalyst into the primary reactor A, then add heat transfer oil into the primary reactor A, start the stirrer B to mix thoroughly, open the electronic valve R1 at the same time, close the electronic valve R2 and the electronic valve R3, and start the vacuum machine E to extract the air in the primary reactor A, so that the primary reactor A becomes a vacuum state, then turn on the first heater C to heat to 300 degrees Celsius, after being fully heated, the steam (including bio-oil) enters the first condenser interface H and then to the condenser for condensation, cooling and collection of the oil, and continues to maintain a temperature of 300 degrees Celsius until no steam enters the condenser, then stop heating, wait for the mixture in the primary reactor A (straw powder residue and heat transfer oil, catalyst mixture) to cool naturally, open the delivery pipe R4 and close the delivery pipe R5, and use the mixture in the primary reactor A to flow into the primary reactor G by gravity, wait until all the mixture enters the primary reactor G, close the electronic valve R4, and close the electronic valve R1 at the same time. -R3, and pressurize the interior of the first reactor G for minutes (at the same time, add the crushed straw raw material and catalyst into the primary reactor A, then add heat transfer oil into the primary reactor A, turn on the stirrer B to fully mix, and repeat the above process) open the delivery pipe R5, and the mixture flows into the secondary reactor F by gravity. After the mixture has all entered the secondary reactor F, open the electronic valves R1 and R3 (at this time the primary reactor A is in the vacuum stage), close the electronic valve R2, turn on the vacuum machine E and the first heater C, add to 500 degrees Celsius, and after fully heated, the steam (including bio-oil) enters the first condenser interface H and then to the condenser for condensation, cooling and collection of the oil, and continues to maintain a temperature of 500 degrees Celsius until no steam enters the condenser. At this time, stop heating (at this time the steam in the primary reactor A enters the condenser together), the mixture in the primary reactor A enters the first reactor G, and the mixture in the secondary reactor F enters the separator through the separator interface L. The above is merely illustrative and serves to illustrate some of the features of the present invention. The appended claims are intended to claim the broadest possible scope that can be imagined, and the embodiments presented herein are merely illustrative of selected implementations according to all possible combinations of embodiments. Therefore, the applicant intends that the appended claims are not limited by the selection of examples that illustrate the features of the present invention. Moreover, advances in technology will form possible equivalents or sub-alternatives that are not currently considered due to inaccuracies in the language, and these changes should also be interpreted as being covered by the appended claims where possible.
Claims
1. A three-stage reactor for continuous catalytic conversion of straw into oil, characterized by: The invention comprises a primary reactor (A), an agitator (B), a first heater (C), a second heater (C1), a filter (D), a vacuum machine (E), a secondary reactor (F), a primary reactor (G), a first condenser interface (H), a separator interface (L), a catalyst interface (Q), an electronic valve (R1-R5), a vacuum pumping pipe (t1-t3), and a delivery pipe (t4-t5); the primary reactor (A) is connected to the primary reactor (G) through a delivery pipe (t4), the primary reactor (G) is connected to the secondary reactor (F) through a delivery pipe (t5), and the filter (D) is connected to the primary reactor (A). The reactor (A) is connected via a vacuum pumping pipe (t1), the filter (D) is connected to the primary reactor (G) via a vacuum pumping pipe (t2), the filter (D) is connected to the secondary reactor (F) via a vacuum pumping pipe (t3), the filter (D) is connected to a vacuum machine (E), the vacuum pumping pipe (t1) is provided with an electronic valve (R1), the vacuum pumping pipe (t2) is provided with an electronic valve (R2), the vacuum pumping pipe (t3) is provided with an electronic valve (R3), the delivery pipe (t4) is provided with an electronic valve (R4), and the delivery pipe (t5) is provided with an electronic valve (R5).
2. The three-stage reactor for continuous catalytic conversion of straw into oil according to claim 1, characterized in that: The catalyst interface (Q) is connected to the catalyst storage tank, the first condenser interface (H) is connected to the condenser, the upper end of the secondary reactor (F) is connected to the condenser through the first condenser interface (H), and the lower end of the secondary reactor (F) is connected to the separator through the separator interface (L). The primary reactor is provided with a second condenser interface (Y), and the second condenser interface (Y) is connected to the condenser.
3. The three-stage reactor for continuous catalytic conversion of straw into oil according to claim 1, characterized in that: The primary reactor (A) is provided with an agitator (B) inside and a first heater (C) at the bottom. The secondary reactor (F) is provided with a second heater (C1) at the bottom.