CN202823383U - Butane oxidation reactor - Google Patents

Abstract

The utility model discloses a butane oxidation reactor which comprises a barrel body, a liquid inlet and a gas outlet are formed in the upper portion of the barrel body, a liquid outlet and a gas inelt are formed in the lower portion of the barrel body, a plurality of reactive tanks are respectively formed in the upper portion and the lower portion inside the barrel body, liquid downcommers are arranged between the reactive tanks and the barrel body lateral wall, the upper and lower adjacent liquid downcomers are arranged in a stagger mode, gas ascending channels and gas distributors are arranged on the reactive tanks, external circulating pipelines are connected outside the barrel body, and a cooler and a circulating pump are installed on the external circulating pipelines. Liquid material enters the barrel body through the liquid inlet, and flows through the reactive tanks in sequence from top to bottom through overflow of the liquid downcomers; gas enters the gas distributors through the gas ascending channels, is mixed with the liquid material inside the reactive tanks in a bubbling mode, and reacts with the liquid material; and reaction heat is cooled and removed through the cooler installed on the external pipelines. The butane oxidation reactor is suitable for being used in a liquid phase oxidation process with low rate of reaction, and continuous operation is achieved easily. The oxygen-containing gas flows through the reactor from bottom to top in one time, and therefore power consumption is saved.

Description

A butane oxidation reactor

technical field

The utility model relates to chemical reaction equipment, in particular to a butane oxidation reactor suitable for butane oxidation reaction.

Background technique

The butane oxidation reaction is a typical gas-liquid two-phase reaction, or a gas-liquid-solid three-phase catalytic reaction, and the oxidation reaction mainly occurs in the liquid phase itself. At present, the bubbling reactor with mechanical stirring is generally used to realize the oxidation reaction. This type of reactor can accelerate the gas-liquid mixing, reduce or eliminate the mass transfer resistance between the gas-liquid two phases, thereby speeding up the reaction speed. . However, this type of reactor requires high energy consumption for operation and high repair and maintenance costs. In addition, the pressure required for the butane oxidation reaction is high, and the mechanically stirred reactor is prone to leakage, posing potential safety hazards.

Chinese patent ZL200410000231.9 discloses a cyclohexane oxidation reactor, which adopts multi-stage feeding of a gas circulation compressor, and installs fillers in the reaction zone to reduce gas-liquid mass transfer resistance, speed up reaction rate, and operate intermittently. This type of reactor is obviously not suitable for the butane oxidation process, because butane oxidation is a reaction with a long induction period, the reaction rate is slow, the consumption of oxygen-containing gas per unit time is less, and the gas-liquid mass transfer resistance is not the main contradiction.

Utility model content

Based on the above technical problems, the utility model provides a butane oxidation reactor, which does not need a gas circulation compressor, saves power consumption, and is suitable for a liquid-phase oxidation reaction process with a relatively slow reaction rate.

Its technical solutions are:

A butane oxidation reactor, comprising a cylinder, a liquid inlet and a gas outlet are arranged on the upper part of the cylinder, a liquid outlet and a gas inlet are arranged on the lower part of the cylinder, a plurality of reaction tanks are sequentially arranged up and down in the cylinder, and the reaction tank and the cylinder The downcomer is arranged between the side walls of the body, and the upper and lower adjacent downcomers are arranged in a dislocation. The gas ascending channel and the gas distributor are arranged on the reaction tank, and the outer circulation pipeline is connected outside the cylinder, and the cooler and the circulation are installed on the outer circulation pipeline. Pump, the liquid material enters the cylinder through the liquid inlet, flows through the reaction tank from top to bottom through the overflow of the downcomer, and the gas enters the gas distributor through the gas ascending channel and reacts with the liquid material in the reaction tank by bubbling and mixing. Cooling and removal through the cooler on the external circulation pipeline.

Further, the above-mentioned liquid outlet is connected to the cooler through the outlet pipe, and part of the liquid cooled by the cooler is sent to the pipeline mixer through the liquid circulation pump to mix with the raw material liquid preheated by the preheater, and the pipeline mixer is connected through the inlet pipe Liquid import.

Furthermore, an external circulation liquid inlet and an external circulation liquid outlet connected to the external circulation pipeline are provided on the side wall of the cylinder.

The ratio of the height to the inner diameter of the cylinder body is not less than 8, preferably the height/diameter ratio is 30-50.

The number of the above-mentioned reaction tanks is not less than 6, and preferably the number of reaction tanks is 20-30.

The depth of the above-mentioned reaction tank is not less than 80mm, preferably the depth of the reaction tank is 80-120mm.

A tear hole is opened on the bottom plate of the reaction tank, and the diameter of the tear hole is 2-6mm.

The cross-sectional area of the above-mentioned downcomer accounts for more than 5% of the cross-sectional area of the cylinder, preferably 5%-10%.

There is a gap for liquid to pass between the bottom of the above-mentioned downcomer and the bottom plate of the adjacent reaction tank below, and there is a gas space between the bottom plate of the above-mentioned reaction tank and the top of the adjacent downcomer below, wherein the bottom plate of the reaction tank and the bottom adjacent downcomer The height of the reserved gas space between the tops of the liquid pipes is preferably 40-60 mm.

The cylinder body and components such as the reaction tank and the downcomer inside the cylinder body are all made of stainless steel.

The beneficial technical effect of the utility model is:

1. A plurality of reaction tanks are set in the reactor of the utility model, and in each reaction tank, the liquid material is mixed with the oxygen-containing gas bubbling from bottom to top to fully react; the reactor is suitable for a long induction period, and the reaction The rate is relatively slow, and the reaction that consumes less oxygen-containing gas per unit time is especially suitable for the oxidation reaction of butane, with high production efficiency and easy continuous operation;

2. The reactor of the utility model is externally connected to a circulation pipeline, and equipment such as a cooler and a liquid circulation pump are installed on the circulation pipeline, and the control of the reaction temperature is realized through one or more sections of liquid external circulation cooling and heat exchange;

3. In the reactor of the present invention, there is a gap or gas space with a suitable distance between the bottom plate of the reaction tank and the bottom end of the adjacent downcomer above and between the bottom plate of the reaction tank and the top end of the adjacent downcomer below. On the one hand, it is convenient for the liquid material in the reaction tank to overflow smoothly to the next reaction tank through the downcomer; The liquid in the reactor flows and mixes, and the update of the liquid surface is accelerated, which promotes the mass transfer between the liquid surface and the gas, continues the reaction to consume the oxygen in the gas, and makes the oxidation reaction more complete. At the same time, the oxygen content in the tail gas flowing out of the reactor is further reduced, improving To ensure the safety of oxidation reaction;

4. In the reactor of the present utility model, the ratio of the cross-sectional area of the downcomer to the cross-sectional area of the cylinder is not less than 5%, ensuring that there is always a liquid seal in the downcomer; 6mm tear hole, used to release the liquid material in the cylinder after the reactor is stopped;

5. The utility model reactor has no mechanical stirring facilities, which eliminates safety hazards such as leakage and reduces operating costs, and the oxygen-containing gas flows through the reactor from bottom to top without the need for a gas cycle compressor, saving power consumption.

Description of drawings

Fig. 1 is the structural schematic diagram of oxidation reactor among the embodiment 1;

Fig. 2 is the layout drawing of gas distributor in embodiment 1;

Fig. 3 is the structural schematic diagram of gas distributor in embodiment 2;

FIG. 4 is a layout diagram of the gas distributor in Embodiment 2.

In the figure: 1- cylinder, a liquid inlet, b gas inlet, c gas outlet, d liquid outlet, 2- reaction tank, 3- gas ascending channel, 4- gas distributor, 5- gas return channel, 6- tears Hole, 7-downcomer, 8-cooler, 9-liquid circulation pump, 10-pipeline mixer, 11-preheater, 21-27 pipelines.

Detailed ways

Example 1

As shown in Figure 1, a butane oxidation reactor includes a cylinder 1, the ratio of the height of the cylinder 1 to the inner diameter is 40, a liquid inlet a and a gas outlet c are arranged on the upper part of the cylinder 1, and a gas outlet c is arranged on the lower part of the cylinder 1 A liquid outlet d and a gas inlet b are set, and 20 reaction tanks 2 are arranged up and down in the cylinder 1 in sequence. The reaction tank 2 is surrounded by the bottom plate, the side plate and the side wall of the cylinder. The depth of the reaction tank 2 is H=120mm. A gas ascending channel 3 is installed on the bottom plate of the reaction tank 2. The shape of the gas ascending channel 3 is cylindrical , a gas distributor 4 is arranged on the outside of the gas ascending channel 3, the gas distributor 4 is a bubble cap type, as shown in Figure 2, a gas return channel 5 is formed between the gas ascending channel 3 and the gas distributor 4, and the gas passes through the gas The ascending channel 3 rises to the top, then enters the reaction tank through the gas return channel 5, and mixes with the liquid in the reaction tank by bubbling. A tear hole 6 with a diameter of 2 mm is also provided on the bottom plate of the reaction tank 2 . A downcomer 7 is arranged between the reaction tank 2 and the side wall of the cylinder, and the upper and lower adjacent downcomers are arranged in a dislocation, and the cross-sectional area of the downcomer 7 accounts for 7% of the cross-sectional area of the cylinder. A gas space is left between the bottom plate of the reaction tank 2 and the top of the adjacent downcomer below, the height of the gas space is h=50mm, and a gap is left between the bottom plate of the reaction tank and the bottom end of the adjacent downcomer above for liquid to pass through .

The liquid outlet d is connected to the cooler 8 through the pipeline 21, and part of the liquid cooled by the cooler 8 is transported to the pipeline mixer 10 through the liquid circulation pump 9 and the pipeline 22 to mix with the raw material liquid preheated by the preheater 11, and the cooler 8 The rest of the cooled liquid is sent to the downstream device through the circulating pump 9 and the pipeline 23, and the pipeline mixer 10 is connected to the liquid inlet a through the pipeline 24. The preheater is connected to the pipeline 25 for conveying fresh liquid material.

The concrete work process of the present utility model is described below:

The fresh butane material is pumped into the preheater 11 through the pipeline 25 at a flow rate of 960.0ml/h to be preheated to 110° C. 1:1) into the pipeline mixer 10 to mix and send into the reactor through the inlet pipe 24 and the liquid inlet a, and flow through each reaction tank and downcomer in turn under the action of gravity until the bottom of the reactor, and then through the liquid outlet d flows out, enters the cooler 8 for cooling, then enters the liquid circulation pump 9, part of it is circulated back to the reactor through the pipeline 22, and the rest is sent to the downstream device through the pipeline 23, and the controlled reaction pressure is 3.2MPa. Oxygen-enriched air enters the reactor through gas inlet b, and then passes through the gas ascending channel and gas distributor of each reaction tank from bottom to top to contact with the liquid material in the reaction tank by bubbling, and reaches the top of the reactor. The tail gas is discharged through the gas outlet c. After chromatographic analysis of the reaction product, the conversion rate of isobutane is 24.6%, and the selectivity of product tert-butanol is 82.7%, realizing the purpose of the present invention.

Example 2

The structure of the butane oxidation reactor is basically the same as in Example 1, the difference being that two sections of external circulation pipelines 26, 27 are added outside the cylinder, and a cooler 8 and a liquid circulation pump 9 are installed on the external circulation pipelines 26, 27, so as to Better remove the heat of oxidation reaction, as shown in Figure 3; the depth of the reaction tank H=80mm, the number of reaction tanks is 30; the gas distributor adopts a distribution ring, as shown in Figure 4, so that the gas and the reaction tank Better mixing of medium liquids; remaining structural dimensions unchanged.

In the specific working process, the ratio of the flow rate of the externally circulated material to the flow rate of the fresh feed is 0.5:1, and the rest of the process conditions are the same as in Example 1. The reaction product is analyzed by chromatography, and the conversion rate of isobutane reaches 41.8%, and the selectivity of the product tert-butanol is 82.3%, realizing the purpose of the present invention.

The external circulation pipeline in the above-mentioned embodiment 2 can also be added at corresponding positions as required, so as to better realize the control of the reaction temperature in the reactor.

It should be noted that under the teaching of this specification, any equivalent replacement or obvious modification made by those skilled in the art shall fall within the protection scope of the present utility model.

Claims (10)

1. A butane oxidation reactor, comprising a cylinder, is characterized in that: a liquid inlet and a gas outlet are arranged at the cylinder top, a liquid outlet and a gas inlet are arranged at the cylinder bottom, and a plurality of reaction tanks are sequentially arranged up and down in the cylinder , a downcomer is set between the reaction tank and the side wall of the cylinder, and the upper and lower adjacent downcomers are dislocated, and the gas ascending channel and gas distributor are set on the reaction tank, and the external circulation pipeline is connected outside the cylinder, and the external circulation pipeline A cooler and a circulation pump are installed on the top, the liquid material enters the cylinder through the liquid inlet, flows through the reaction tank from top to bottom through the overflow of the downcomer, and the gas enters the gas distributor and the liquid material drum in the reaction tank through the gas ascending channel. Bubble mixing reaction, the heat of reaction is removed by the cooler on the external circulation pipeline. 2. A butane oxidation reactor according to claim 1, characterized in that: the liquid outlet is connected to a cooler through an outlet pipe, and part of the liquid cooled by the cooler is delivered to the pipeline mixer through a circulating pump and preheated. The preheated raw material liquid is mixed, and the pipeline mixer is connected to the liquid inlet through the inlet pipe. 3. A butane oxidation reactor according to claim 2, characterized in that: an external circulation liquid inlet and an external circulation liquid outlet connected to the external circulation pipeline are arranged on the side wall of the cylinder. 4. A butane oxidation reactor according to claim 1, characterized in that: the ratio of the height to the inner diameter of the cylinder is not less than 8. 5. A butane oxidation reactor according to claim 1, characterized in that: the number of said reaction tanks is not less than 6. 6. A butane oxidation reactor according to claim 1, characterized in that: the depth of the reaction tank is not less than 80mm. 7. A butane oxidation reactor according to claim 1, characterized in that: tear holes are opened on the bottom plate of the reaction tank, and the diameter of the tear holes is 2-6mm. 8. A butane oxidation reactor according to claim 1, characterized in that: the cross-sectional area of the downcomer accounts for more than 5% of the cross-sectional area of the cylinder. 9. A butane oxidation reactor according to claim 1, characterized in that: there is a gap for liquid to pass between the bottom of the downcomer and the bottom of the adjacent reaction tank below, A gas space is left between adjacent downcomer tips. 10. A butane oxidation reactor according to claim 1, characterized in that: the cylinder, the reaction tank and the downcomer inside the cylinder are all made of stainless steel.

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