Isobutane normalizing production device

Abstract

The utility model discloses an isobutane normalizing production device which circulates isoalkane-containing light components treated by a separation unit to a second reactor as feed, so that the conversion rate of a normalizing reaction in the second reactor can be remarkably improved; the defect that the conversion rate is influenced due to the fact that materials are directly fed into the reactor II after reaction in the reactor I approach to reaction equilibrium is avoided, and compared with single-stage reaction, the raw material consumption and energy consumption are remarkably reduced by increasing the feeding amount and simple circulation.

Description

Technical Field

[0001] This utility model relates to the field of n-butane production technology, specifically to an isobutane n-assembly production apparatus. Background Technology

[0002] n-Butane, as a high-quality feedstock for the production of trienes from ethylene cracking, has the advantages of higher yield and less methane byproduct compared to isobutane. Furthermore, n-butane is also a feedstock for the oxidative process to produce maleic anhydride. However, there is a significant domestic shortage of n-butane, an important petrochemical feedstock. Therefore, the production of n-butane through the n-butane conversion of isobutane is an important measure to improve the efficiency of the petrochemical industry.

[0003] Existing isobutane n-assembly units generally employ a single reactor or two reactors directly connected in series. However, due to the influence of reaction equilibrium, the conversion rate is generally low, with a single reactor achieving a conversion rate of approximately 30%. If two reactors are directly connected in series, the fresh isobutane feed passes through a first-stage reactor, where the isobutane n-assembly conversion rate is around 30%. The product from the first-stage reactor continues into the second-stage reactor. Since the feed to the second-stage reactor already contains approximately 30% n-butane, the n-butane content in the product emanating from the second-stage reactor is limited by reaction equilibrium, resulting in an outlet product from the second-stage reactor containing approximately 35% n-butane. This means that the second-stage reactor only increases the single-pass conversion rate by 5%, far lower than that of the first-stage reactor. In summary, the single-pass conversion rates of the two current processing methods are not high. In order to ensure that all isobutane is converted into n-butane, a large amount of unreacted isobutane is circulated within the unit. When two reactors are directly connected in series, the amount of circulating isobutane in the reactor feed is about twice that of fresh isobutane. If a single reactor is used, the amount of circulating isobutane is about 2.3 times that of fresh isobutane. The production efficiency of n-butane is low, and the large amount of isobutane circulating also increases energy consumption.

[0004] Therefore, it is necessary to design an isobutane normalization production unit to solve the defects of low conversion rate and high energy consumption in the existing isobutane normalization production technology. Utility Model Content

[0005] The purpose of this invention is to provide an isobutane normalization production device to solve the defects of low conversion rate and high energy consumption in the existing isobutane normalization production technology.

[0006] To achieve the above objectives, the solution of this utility model is as follows:

[0007] An isobutane n-assembly production apparatus includes a reactor 1, a reactor 2, and a separation unit connected to both reactors. The separation unit includes a stabilization tower and a separation tower connected to each other. The reactor 1 and reactor 2 are used for the n-assembly reaction of hydrogen and isobutane. The upper part of the separation tower is provided with a circulation pipe connected to the feed end of reactor 2. The stabilization tower is used to remove non-condensable gases, and the separation tower is used to separate light components, n-butane, and heavy components.

[0008] Furthermore, the circulation pipe is connected to the feed end of reactor one.

[0009] Furthermore, the discharge end of reactor one is connected to the feed end of reactor two via a series pipe.

[0010] Furthermore, reactor one and reactor two are filled with a catalyst layer.

[0011] Furthermore, the reactor is equipped with a preheater at the feed end for preheating hydrogen and / or isobutane.

[0012] Furthermore, the circulation pipe is connected to a hydrogen pipe, and a preheater is installed at the feed inlet of reactor two.

[0013] Compared with the prior art, the beneficial effects of this utility model are as follows:

[0014] The production device of this invention recycles the light component containing isoalkanes after being processed by the separation unit to reactor two as feed, which can significantly improve the conversion rate of the ortho-alkation reaction in reactor two. This avoids the defect of directly feeding the material into reactor two after the reaction in reactor one, which affects the conversion rate due to the approaching reaction equilibrium. Compared with a single-stage reaction, which simply increases the amount of feed and recycles the material, this device significantly reduces the consumption of raw materials and energy. Attached Figure Description

[0015] Figure 1 This is a schematic diagram of an isobutane ortho-formation production apparatus provided by this utility model.

[0016] in:

[0017] E1, Preheater 1; E2, Preheater 2; K1, Valve 1; L1, Isobutane feed pipe; L2, Hydrogen pipe; L3, Circulation pipe; L4, Series pipe; P1, Pump 1; P2, Pump 2; R1, Reactor 1; R2, Reactor 2; T1, Stabilizer; T2, Separator; V1, Buffer tank. Detailed Implementation

[0018] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the protection scope of the present utility model.

[0019] It should be understood that the terms "upper", "lower", "top", "bottom", "inner", "outer", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this utility model 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 utility model.

[0020] It should also be noted that, unless otherwise explicitly specified and limited, terms such as "installation," "connection," "joining," "fixing," and "setting" 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 or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication between two components or the interaction between two components. For those skilled in the art, the specific meaning of the above terms in this utility model can be understood according to the specific circumstances.

[0021] In one embodiment, such as Figure 1 As shown, an isobutane n-assembly production apparatus is proposed, comprising reactor one R1, reactor two R2, and separation units respectively connected to both; wherein:

[0022] The feed end of reactor one R1 is connected to isobutane feed pipe L1 and hydrogen pipe L2; the feed end of reactor two R2 is connected to hydrogen pipe L2. Both reactor one R1 and reactor two R2 are used for the normalization reaction of hydrogen and isobutane.

[0023] The separation unit includes a stabilizing tower T1 and a separating tower T2; the upper part of the separating tower T2 is provided with a circulation pipe L3 connected to the feed end of reactor R2; the stabilizing tower T1 is used to remove non-condensable gases, and the separating tower T2 is used to separate light components, n-butane and heavy components.

[0024] In the above embodiments, fresh isobutane and hydrogen enter reactor R1 for a first-stage normalization reaction. After non-condensable gases are removed by stabilization tower T1 and n-butane products and heavy components are removed by separation tower T2, the light component containing isobutane at the top of the towers enters reactor R2 via circulation pipe L3, where it mixes with hydrogen for a second-stage reaction. Recycling the light component containing isobutane, after being processed by the separation unit, into reactor R2 as feed significantly improves the conversion rate of the normalization reaction in reactor R2. This avoids the drawback of directly feeding the product from reactor R1 into reactor R2, which affects the conversion rate due to approaching reaction equilibrium. Furthermore, compared to a single-stage reaction with increased feed volume and simple isobutane recycling, this significantly reduces raw material consumption and energy consumption.

[0025] In a preferred embodiment, in order to further improve the utilization rate of isoalkanes in the separated light components, the circulation pipe L3 is connected to the feed end of reactor R1.

[0026] In a preferred embodiment, the discharge end of reactor R1 is connected to the feed end of reactor R2 via a series pipe L4, and valve K1 is installed on the series pipe L4. When fresh isobutane feedstock is insufficient, or when a single reactor malfunctions, valve K1 can be opened to achieve single-reactor production using the series bypass line of reactor R1 and reactor R2, and the reaction process can be flexibly adjusted.

[0027] It is understood that reactors R1 and R2 are filled with catalysts, including but not limited to at least one of the common Pt / HBeta molecular sieve catalysts, Pt-HM / Al2O3 or Pt-Al2O3 / HM catalysts.

[0028] In a preferred embodiment, a preheater E1 is provided at the feed end of reactor R1; the circulation pipe L3 is connected to a hydrogen pipe L2, and a preheater E2 is provided at the feed inlet of reactor R2 on the circulation pipe L3. Preheaters E1 and E2 are used to preheat the incoming hydrogen and isobutane to achieve a suitable reaction temperature.

[0029] In a preferred embodiment, the isobutane feed pipe L1 is connected to the buffer tank V1, and isobutane is transferred and fed through pump P1. The circulation pipe L3 is connected to the separation tower T2 through pump P2 to improve the feeding efficiency and stability.

[0030] It is understood that the production equipment also includes instruments, meters or valves installed in each unit or pipeline. Instruments and meters are used to monitor the status parameters of materials or unit devices, valves are used to control the start and stop or flow of materials, and power pumps are used to provide power for material transfer. All of these are within the design scope of this solution and will not be elaborated here.

[0031] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made to these embodiments without departing from the principles and spirit of the present invention, the scope of which is defined by the appended claims and their equivalents.

Claims

1. An isobutane n-assembly production apparatus, characterized in that, The system includes reactor 1 (R1) and reactor 2 (R2), and separation units connected to both of them. The separation units include a stabilizing tower (T1) and a separation tower (T2) connected to each other. Reactors 1 (R1) and 2 (R2) are used for the n-assembly reaction of hydrogen and isobutane. The upper part of the separation tower (T2) is provided with a circulation pipe (L3) connected to the feed end of reactor 2 (R2). The stabilizing tower (T1) is used to remove non-condensable gases, and the separation tower (T2) is used to separate light components, n-butane, and heavy components.

2. The production apparatus according to claim 1, characterized in that, The circulation pipe (L3) is connected to the feed end of reactor one (R1).

3. The production apparatus according to claim 1, characterized in that, The discharge end of reactor one (R1) is connected to the feed end of reactor two (R2) via a series pipe (L4).

4. The production apparatus according to claim 1, characterized in that, The reactors 1 (R1) and 2 (R2) are filled with catalyst layers.

5. The production apparatus according to claim 1, characterized in that, The reactor (R1) is equipped with a preheater (E1) at the feed end for preheating hydrogen and / or isobutane.

6. The production apparatus according to claim 1, characterized in that, The circulation pipe (L3) is connected to the hydrogen pipe (L2), and the circulation pipe (L3) is located at the feed inlet of reactor two (R2) and is equipped with preheater two (E2).

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