Thermal integrated reactor with reaction rate control function and application thereof

Abstract

The application discloses a thermal comprehensive reactor with a reaction rate control function and application thereof. The thermal comprehensive reactor is a vertical reactor. The thermal comprehensive reactor comprises, from top to bottom, a tubular heat exchange reaction chamber I, a Venturi jet mixing chamber and a tubular heat exchange reaction chamber II which are sequentially communicated. The application realizes the original normal hydrogenation consecutive reaction rate distribution control by splitting the reaction chamber and feeding hydrogen in batches, improves the normal hydrogenation product yield, adopts the Venturi jet mixing mode to fully mix the raw materials, and realizes the self-use of reaction heat through the self-heat exchange of the raw materials and products, and improves the thermal energy utilization efficiency.

Description

Technical Field

[0001] This application relates to a thermal integrated reactor with reaction rate control function and its application, belonging to the field of chemical technology. Background Technology

[0002] C4 compounds are byproducts of processes such as naphtha cracking to ethylene and methanol-to-olefins production. Rich in C4 alkylene / olefins, they are important chemical raw materials. They can be used as fuel for production and daily life, and can also be purified to obtain high-purity n-butane, isobutane, n-butene, and isobutylene, among other chemical products. Isobutylene is mainly used in oil conditioning and the synthesis of methyl tert-butyl ether (MTBE) to produce butyl rubber, methacrylonitrile, and antioxidants, but market demand is limited. Developing new downstream derivative production processes for isobutylene is an urgent issue. n-Butane is an important chemical product obtained through purification of a byproduct during oil refining. It can be used directly as fuel and as an extraction solvent in subcritical biotechnology. In recent years, with the continuous expansion of n-butane thermal cracking to ethylene technology and the n-butane-to-maleic anhydride production technology, the demand for high-purity n-butane has been rising steadily. At the same time, the shortage of domestic n-butane resources has further driven up the n-butane market. Considering the corresponding market effects of isobutylene and n-butane, it is evident that researching and exploring the technology for producing n-butane by hydrogenation of isobutylene has significant scientific and economic implications.

[0003] Existing research on the production of n-butane from isobutene is very scarce, and there is even less attention paid to the specific design of the reactor and the control and improvement of the reaction process. It is necessary to conduct in-depth research on related issues. Summary of the Invention

[0004] To address the exothermic characteristics of the n-butane production reaction of isobutene n-hydrogenation and the influence of hydrogen on the control of different reactions in the series reaction, this invention provides a thermal integrated reactor with reaction rate control function. This reactor achieves inherent rate distribution control of the n-hydrogenation series reaction, improves the yield of n-hydrogenation products, and enhances thermal energy utilization efficiency.

[0005] One aspect of this application provides a thermal integrated reactor, which is a vertical reactor;

[0006] The thermal integrated reactor comprises, from top to bottom, a tubular heat exchange reaction chamber I, a Venturi jet mixing chamber, and a tubular heat exchange reaction chamber II, which are connected in sequence.

[0007] The tubular heat exchanger reaction chamber I is provided with a tube-side inlet I and a tube-side outlet I;

[0008] The Venturi jet mixing chamber is provided with an inlet section, a necking section and a diffusion section from top to bottom. The inlet section is provided with a first inlet and the diffusion section is provided with a first outlet. The first inlet is connected to the tube outlet I. The necking section of the Venturi jet mixing chamber is provided with a second inlet.

[0009] The tubular heat exchanger reaction chamber II is provided with a shell-side inlet II and a shell-side outlet II, and the shell-side inlet II is connected to the first outlet;

[0010] The tubular heat exchanger reaction chamber II is also equipped with a tube-side inlet II-1 and a tube-side outlet II-1;

[0011] The tube outlet II-1 is connected to the second inlet.

[0012] Optionally, the tubular heat exchanger reaction chamber I further includes a shell-side inlet I and a shell-side outlet I;

[0013] The shell-side outlet II is connected to the shell-side inlet I.

[0014] Optionally, the tubular heat exchanger reaction chamber II is further provided with a tube-side inlet II-2 and a tube-side outlet II-2.

[0015] Another aspect of this application provides a normal hydrogenation reactor, said normal hydrogenation reactor comprising the aforementioned thermal integrated reactor.

[0016] Wherein, the tube inlet I is the inlet for the reaction raw materials;

[0017] The tube inlet II-1 is the H2 inlet;

[0018] The tube outlet II-1 is the H2 outlet;

[0019] The shell-side outlet II is the outlet of product I from the ortho-hydrogenation reaction.

[0020] Optionally, the shell-side outlet I is the outlet of the product II from the ortho-hydrogenation reaction;

[0021] The pipe inlet II-2 is the cooling water inlet.

[0022] Optionally, the tube side of the tubular heat exchanger reaction chamber II is cooled and heated by both cooling water and hydrogen gas.

[0023] In another aspect of this application, a method for an ortho-hydrogenation reaction is provided, the method employing the ortho-hydrogenation reactor described above;

[0024] The method includes:

[0025] The raw material containing hydrogen I and isobutylene is introduced into the tubular heat exchange reaction chamber I through the tube inlet I, and comes into contact with catalyst I to undergo a catalytic hydronormative reaction to obtain the hydronormative reaction product.

[0026] Hydrogen gas II is introduced from the tube inlet II-1, enters the Venturi injection mixing chamber through the second inlet, mixes with the product of the orthohydrogenation reaction, and enters the tubular heat exchange reaction chamber II through the first outlet, where it comes into contact with catalyst II to undergo a catalytic hydrogenation reaction and obtain the orthohydrogenation reaction product.

[0027] Optionally, the product of the n-type hydrogenation reaction enters the shell side of the tubular heat exchange reaction chamber I through the shell side outlet II and the shell side inlet I, exchanges heat with the raw material I, and is then discharged through the shell side outlet I.

[0028] Optionally, cooling water is introduced into the tubular heat exchange reaction chamber II via the tube-side inlet II-2, exchanges heat with hydrogen II, and is then discharged via the tube-side outlet II-2.

[0029] Optionally, the heat required for the catalytic hydronormative reaction is compensated by the reaction products flowing out of the tubular heat exchange reaction chamber II through shell-side heat exchange.

[0030] Optionally, the hydronormative reaction products flowing out of tubular heat exchanger reaction chamber I flow into the Venturi jet mixing chamber, where the flow velocity increases sharply at the constriction, generating a pressure drop, drawing in a large amount of hydrogen required for hydrogenation and mixing thoroughly, before entering the shell side of tubular heat exchanger reaction chamber II to undergo catalytic hydrogenation.

[0031] Optionally, the tube side of the tubular heat exchanger reaction chamber II removes the heat generated by the reaction through cooling water and hydrogen gas required for hydrogenation, controlling the temperature rise. The heated hydrogen gas is then thoroughly mixed with the product flowing out of the tubular heat exchanger reaction chamber I via a Venturi jet mixer. The high-temperature hydrogenation reaction product obtained from the shell side of the tubular heat exchanger reaction chamber II flows into the shell side of the first reaction chamber, and after compensating for the heat of the hydrogen-induced orthomeric reaction, it flows out of the reactor.

[0032] Optionally, in the raw materials, the molar ratio of hydrogen I to isobutylene is 0.5 to 2:1;

[0033] The molar ratio of hydrogen II to isobutylene is 0.5 to 3:1.

[0034] Optionally, the reaction temperature for the catalytic hydronormative reaction is 200–400 °C;

[0035] The reaction pressure for the catalytic hydronormative reaction is 0.5–5 MPaG.

[0036] Optionally, the molar ratio of hydrogen I to isobutylene is independently selected from any value among 0.5:1, 1:1, 1.5:1, 2:1 or a range between any two of the above points.

[0037] Optionally, the molar ratio of hydrogen II to isobutylene is independently selected from any value among 0.5:1, 1:1, 1.5:1, 2:1, 2.5:1, 3:1 or a range between any two of the above points.

[0038] Optionally, the reaction temperature of the catalytic hydronormative reaction is independently selected from any value among 200°C, 260°C, 300°C, 350°C, and 400°C, or a range between any two of the above.

[0039] Optionally, the reaction pressure of the catalytic hydronormative reaction is independently selected from any value of 0.5 MPaG, 1 MPaG, 2 MPaG, 2.4 MPaG, 3 MPaG, 4 MPaG, 5 MPaG, or a range between any two of the above values.

[0040] Optionally, after heat exchange I, the temperature difference between the cooling of the ortho-hydrogenation reaction product and the temperature difference is 3 to 10°C.

[0041] After heat exchange II, the temperature of hydrogen II is 170-370°C, and the temperature difference is controlled within 20°C.

[0042] Optionally, the catalyst I is located within the tube side of the tubular heat exchanger reaction chamber I;

[0043] The catalyst II is located in the shell side of the tubular heat exchanger reaction chamber II.

[0044] As one specific implementation, the thermal integrated reactor with reaction rate control function includes:

[0045] A thermal integrated reactor with reaction rate control function includes a first reaction chamber, a Venturi jet mixing chamber, and a second reaction chamber connected sequentially from top to bottom. The first reaction chamber is a tubular heat exchange reactor with catalyst packed in the tubes, and its inlet is connected to the shell-side outlet of the second reaction chamber. The Venturi jet mixing chamber has two inlets: one inlet is connected to the tube-side outlet of the first reaction chamber, and the second inlet is located at the neck and connected to the hydrogen tube-side outlet of the second reaction chamber. The second reaction chamber is also a tubular heat exchange reactor with catalyst packed in the shell, and its tube-side is cooled and cooled by both cooling water and hydrogen gas. The hydrogen tube-side outlet is connected to the second inlet of the Venturi jet mixing chamber.

[0046] The beneficial effects that this application can produce include:

[0047] (1) This application achieves the original rate distribution control of the n-type hydrogenation series reaction by dividing the reaction chamber and feeding hydrogen in batches, thereby improving the yield of n-type hydrogenation products and reducing the selectivity of by-products.

[0048] (2) This application uses a Venturi jet mixing method to ensure that the raw materials are fully mixed.

[0049] (3) This application realizes the self-utilization of reaction heat through the self-heating of raw materials and products, thereby improving the efficiency of heat energy utilization. Attached Figure Description

[0050] Figure 1 This is the thermal integrated reactor with reaction rate control function in Embodiment 1 of this application.

[0051] in:

[0052] 1. First reaction chamber; 2. Venturi jet mixing chamber; 3. Second reaction chamber. Detailed Implementation

[0053] The present application is described in detail below with reference to the embodiments, but the present application is not limited to these embodiments.

[0054] Unless otherwise specified, the raw materials and catalysts used in the embodiments of this application were all purchased commercially.

[0055] Example 1

[0056] like Figure 1 As shown, a thermal integrated reactor with reaction rate control function includes a first reaction chamber 1, a Venturi jet mixing chamber 2, and a second reaction chamber 3 connected sequentially from top to bottom. The first reaction chamber is a tubular heat exchange reactor with catalyst packed in the tubes, and its inlet is connected to the shell-side outlet of the second reaction chamber 3. The Venturi jet mixing chamber 2 has two inlets: one inlet is connected to the tube-side outlet of the first reaction chamber 1, and the second inlet is located at the neck and connected to the hydrogen tube-side outlet of the second reaction chamber 3. The second reaction chamber is also a tubular heat exchange reactor with catalyst packed in the shell, and its tube-side is cooled and cooled by both cooling water and hydrogen. The hydrogen tube-side outlet is connected to the second inlet of the Venturi jet mixing chamber.

[0057] Example 2

[0058] Using the thermal reactor obtained in Example 1, the reactants, hydrogen and isobutylene in a 1:1 molar ratio, enter the first reaction chamber 1 from the top of the reactor at 260°C. A catalytic hydronormative reaction occurs in the tube side at a pressure of 2.4 MPaG. The heat required for the reaction is compensated by heat exchange in the shell side by the reaction products flowing out of the second reaction chamber 3, keeping the temperature rise below 15°C. The hydronormative reaction products flowing out of the first reaction chamber 1 flow into the Venturi jet mixing chamber 2, where the flow velocity increases sharply at the constriction, creating a pressure drop. The hydrogen required for hydrogenation is drawn in and thoroughly mixed before entering the shell side of the second reaction chamber 3 for catalytic hydrogenation. The molar ratio of newly added hydrogen at the inlet of the second reaction chamber 3 to isobutylene at the inlet of the first reaction chamber 1 is 1.5:1. The heat generated by the reaction is removed from the tube side of the second reaction chamber 3 through cooling water and the hydrogen required for hydrogenation, keeping the temperature rise below 20°C. The heated hydrogen is then thoroughly mixed with the products flowing out of the first reaction chamber 1 via the Venturi jet mixing chamber 2. The high-temperature hydrogenation reaction product obtained from the shell side of the second reaction chamber 3 flows into the shell side of the first reaction chamber 1, and flows out of the reactor after compensating for the heat of the hydrogen ortho-reaction.

[0059] The above description is merely a few embodiments of this application and is not intended to limit this application in any way. Although this application discloses preferred embodiments as described above, it is not intended to limit this application. Any changes or modifications made by those skilled in the art without departing from the scope of the technical solution of this application using the disclosed technical content are equivalent to equivalent implementation cases and fall within the scope of the technical solution.

Claims

1. A thermal integrated reactor, characterized in that, The thermal reactor is a vertical reactor; The thermal integrated reactor comprises, from top to bottom, a tubular heat exchange reaction chamber I, a Venturi jet mixing chamber, and a tubular heat exchange reaction chamber II, which are connected in sequence. The tubular heat exchanger reaction chamber I is provided with a tube-side inlet I and a tube-side outlet I; The Venturi jet mixing chamber is provided with an inlet section, a necking section and a diffusion section from top to bottom. The inlet section is provided with a first inlet and the diffusion section is provided with a first outlet. The first inlet is connected to the tube outlet I. The necking section of the Venturi jet mixing chamber is provided with a second inlet. The tubular heat exchanger reaction chamber II is provided with a shell-side inlet II and a shell-side outlet II, and the shell-side inlet II is connected to the first outlet; The tubular heat exchanger reaction chamber II is also equipped with a tube-side inlet II-1 and a tube-side outlet II-1; The tube outlet II-1 is connected to the second inlet; The tubular heat exchanger reaction chamber I also includes a shell-side inlet I and a shell-side outlet I; The shell-side outlet II is connected to the shell-side inlet I; The tubular heat exchanger reaction chamber II is also equipped with a tube-side inlet II-2 and a tube-side outlet II-2.

2. A normal hydrogenation reactor, characterized in that, The ortho-hydrogenation reactor includes the thermal integrated reactor as described in claim 1. Wherein, the tube inlet I is the inlet for the reaction raw materials; The tube inlet II-1 is the H2 inlet; The tube outlet II-1 is the H2 outlet; The shell-side outlet II is the outlet of product I from the ortho-hydrogenation reaction.

3. The ortho-hydrogenation reactor according to claim 2, characterized in that, The shell-side outlet I is the outlet of product II from the ortho-hydrogenation reaction; The pipe inlet II-2 is the cooling water inlet.

4. A method for an ortho-hydrogenation reaction, characterized in that, The method employs the ortho-hydrogenation reactor as described in any one of claims 2 to 3; The method includes: The raw material containing hydrogen I and isobutylene is introduced into the tubular heat exchange reaction chamber I through the tube inlet I, and comes into contact with catalyst I to undergo a catalytic hydronormative reaction to obtain the hydronormative reaction product. Hydrogen gas II is introduced from the tube inlet II-1, enters the Venturi injection mixing chamber through the second inlet, mixes with the product of the orthohydrogenation reaction, and enters the tubular heat exchange reaction chamber II through the first outlet, where it comes into contact with catalyst II to undergo a catalytic hydrogenation reaction and obtain the orthohydrogenation reaction product.

5. The method according to claim 4, characterized in that, The product of the n-type hydrogenation reaction enters the shell side of the tubular heat exchange reaction chamber I through the shell side outlet II and the shell side inlet I, and after exchanging heat with the raw material I, it is discharged through the shell side outlet I. Cooling water is introduced into the tubular heat exchange reaction chamber II through the tube inlet II-2, exchanges heat with hydrogen II, and is then discharged through the tube outlet II-2.

6. The method according to claim 4, characterized in that, In the raw materials, the molar ratio of hydrogen I to isobutylene is 0.5~2:1; The molar ratio of hydrogen II to isobutylene is 0.5~3:1; The reaction temperature for the catalytic hydronormative reaction is 200~400℃; The reaction pressure for the catalytic hydronormative reaction is 0.5~5 MPaG.

7. The method according to claim 5, characterized in that, After heat exchange I, the temperature difference between the cooling of the normal reaction products is 3~10℃; After heat exchange II, the temperature of hydrogen II is 170~370℃.

8. The method according to claim 4, characterized in that, The catalyst I is located within the tube side of the tubular heat exchanger reaction chamber I; The catalyst II is located in the shell side of the tubular heat exchanger reaction chamber II.

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