Continuous reaction device and method for preparing aldehyde through hydroformylation reaction

Abstract

The invention discloses a continuous reaction device for preparing aldehyde through a hydroformylation reaction. The reaction device comprises a reaction unit, a separation unit and a circulation unit; the circulation unit is located between the reaction unit and the separation unit; the reaction unit is connected with the separation unit; and a catalyst is circulated between the reaction unit andthe separation unit through the circulation unit. The invention further discloses a method for preparing the aldehyde by adopting the reaction device. According to the method and device provided by the invention, the catalyst can be uninterruptedly and continuously recycled without being separated by external equipment, continuous production of the aldehyde can be realized, reaction heat can be rapidly removed, the progress of the hydroformylation reaction is facilitated, the conversion rate of raw materials is high, the yield of the target products is high, and the ratio of a n-configurationproduct to an iso-configuration product is high.

Description

Technical field

[0001] The present application relates to a continuous reaction device for preparing aldehydes through hydroformylation reaction and a method for preparing aldehydes using the device, and belongs to the fields of chemical engineering and chemical synthesis. Background technique

[0002] The hydroformylation reaction is a reaction between olefins and synthesis gas (CO and H 2 ) is a reaction process that produces one molecule more aldehyde or alcohol than the original olefin under the action of a transition metal complex catalyst. The aldehydes, alcohols, and their derivatives produced are widely used as plasticizers, fabric additives, surfactants, solvents, and fragrances. This type of reaction was first discovered by O. Roelen in Fischer-Tropsch synthesis at the Ruhr Chemical Company in Germany in 1938. Propanaldehyde and ethylenedione were obtained from synthesis gas and ethylene, and were soon applied to propylene. Process for producing butanol. However...

Examples

Embodiment 1

[0122] use figure 1 As shown in the process flow, the process conditions are as follows:

[0123] The catalyst aqueous solution adopts the proportioning composition of Example 1 in the published patent number CN101462932A.

[0124] Reaction temperature: 80°C, reaction pressure is 2.5MPa (A);

[0125] Reactor inlet conditions:

[0126] Feed flow of catalyst aqueous solution: 10m 3 / Hour;

[0127] Ethylene feed flow: 25Nm 3 / Hour;

[0128] CO+H 2 Feed flow: 50Nm 3 / Hour;

[0129] CO:H 2 = 1:1 (molar ratio);

[0130] The discharge results at the discharge port 3:

[0131] Ethylene conversion rate: 98%;

[0132] Propionaldehyde yield: 98%.

[0133] In this example, the production process of preparing propionaldehyde by hydroformylation of ethylene olefin is realized with a high ethylene conversion rate of 98% and a high propionaldehyde selectivity of 98%.

Embodiment 2

[0135] use figure 1 As shown in the process flow, the process conditions are as follows:

[0136] The catalyst aqueous solution adopts the proportioning composition of Example 5 in the published patent number CN101462932A.

[0137] Reaction temperature: 110°C, reaction pressure 2.5MPa (A);

[0138] Reactor inlet conditions:

[0139] Feed flow of catalyst aqueous solution: 10m 3 / Hour;

[0140] Propylene feed flow: 50kg / hour;

[0141] CO+H 2 Feed flow: 50Nm 3 / Hour;

[0142] CO:H 2 = 1:1 (molar ratio);

[0143] The discharge results at the discharge port 3:

[0144] Propylene conversion rate: 98%;

[0145] n-Butyraldehyde yield: 97%;

[0146] n-Butyraldehyde:Isobutyraldehyde=40:1 (molar ratio).

[0147] In this example, the production process of preparing n-butyraldehyde by hydroformylation of propene olefin is realized with a high propylene conversion rate of 98% and a high n-butyraldehyde selectivity of 97%.

Embodiment 3

[0149] use figure 1 As shown in the process flow, the process conditions are as follows:

[0150] The catalyst aqueous solution adopts the proportioning composition of Example 10 in the published patent number CN101462932A.

[0151] Reaction temperature: 120°C, reaction pressure is 3.0MPa (A);

[0152] Reactor inlet conditions:

[0153] Feed flow of catalyst aqueous solution: 10m 3 / Hour;

[0154] 1-Butene feed flow: 60kg / hour;

[0155] CO+H 2 Feed flow: 50Nm 3 / Hour;

[0156] CO:H 2 = 1:1 (molar ratio);

[0157] The discharge results at the discharge port 3:

[0158] 1-Butene conversion rate: 97%;

[0159] n-valeraldehyde yield: 97%;

[0160] n-valeraldehyde:isovaleraldehyde = 60:1 (molar ratio).

[0161] In this example, the production process of preparing n-valeraldehyde by hydroformylation of 1-butene is realized with a high 1-butene conversion rate of 97% and a high n-valeraldehyde selectivity of 97%.

Technical field

[0001] The present application relates to a continuous reaction device for preparing aldehydes through hydroformylation reaction and a method for preparing aldehydes using the device, and belongs to the fields of chemical engineering and chemical synthesis. Background technique

[0002] The hydroformylation reaction is a reaction between olefins and synthesis gas (CO and H 2 ) is a reaction process that produces one molecule more aldehyde or alcohol than the original olefin under the action of a transition metal complex catalyst. The aldehydes, alcohols, and their derivatives produced are widely used as plasticizers, fabric additives, surfactants, solvents, and fragrances. This type of reaction was first discovered by O. Roelen in Fischer-Tropsch synthesis at the Ruhr Chemical Company in Germany in 1938. Propanaldehyde and ethylenedione were obtained from synthesis gas and ethylene, and were soon applied to propylene. Process for producing butanol. However...

Examples

Embodiment 1

[0122] use figure 1 As shown in the process flow, the process conditions are as follows:

[0123] The catalyst aqueous solution adopts the proportioning composition of Example 1 in the published patent number CN101462932A.

[0124] Reaction temperature: 80°C, reaction pressure is 2.5MPa (A);

[0125] Reactor inlet conditions:

[0126] Feed flow of catalyst aqueous solution: 10m 3 / Hour;

[0127] Ethylene feed flow: 25Nm 3 / Hour;

[0128] CO+H 2 Feed flow: 50Nm 3 / Hour;

[0129] CO:H 2 = 1:1 (molar ratio);

[0130] The discharge results at the discharge port 3:

[0131] Ethylene conversion rate: 98%;

[0132] Propionaldehyde yield: 98%.

[0133] In this example, the production process of preparing propionaldehyde by hydroformylation of ethylene olefin is realized with a high ethylene conversion rate of 98% and a high propionaldehyde selectivity of 98%.

Embodiment 2

[0135] use figure 1 As shown in the process flow, the process conditions are as follows:

[0136] The catalyst aqueous solution adopts the proportioning composition of Example 5 in the published patent number CN101462932A.

[0137] Reaction temperature: 110°C, reaction pressure 2.5MPa (A);

[0138] Reactor inlet conditions:

[0139] Feed flow of catalyst aqueous solution: 10m 3 / Hour;

[0140] Propylene feed flow: 50kg / hour;

[0141] CO+H 2 Feed flow: 50Nm 3 / Hour;

[0142] CO:H 2 = 1:1 (molar ratio);

[0143] The discharge results at the discharge port 3:

[0144] Propylene conversion rate: 98%;

[0145] n-Butyraldehyde yield: 97%;

[0146] n-Butyraldehyde:Isobutyraldehyde=40:1 (molar ratio).

[0147] In this example, the production process of preparing n-butyraldehyde by hydroformylation of propene olefin is realized with a high propylene conversion rate of 98% and a high n-butyraldehyde selectivity of 97%.

Embodiment 3

[0149] use figure 1 As shown in the process flow, the process conditions are as follows:

[0150] The catalyst aqueous solution adopts the proportioning composition of Example 10 in the published patent number CN101462932A.

[0151] Reaction temperature: 120°C, reaction pressure is 3.0MPa (A);

[0152] Reactor inlet conditions:

[0153] Feed flow of catalyst aqueous solution: 10m 3 / Hour;

[0154] 1-Butene feed flow: 60kg / hour;

[0155] CO+H 2 Feed flow: 50Nm 3 / Hour;

[0156] CO:H 2 = 1:1 (molar ratio);

[0157] The discharge results at the discharge port 3:

[0158] 1-Butene conversion rate: 97%;

[0159] n-valeraldehyde yield: 97%;

[0160] n-valeraldehyde:isovaleraldehyde = 60:1 (molar ratio).

[0161] In this example, the production process of preparing n-valeraldehyde by hydroformylation of 1-butene is realized with a high 1-butene conversion rate of 97% and a high n-valeraldehyde selectivity of 97%.

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