The way the dimerization and codimerization of lower olefins

 

(57) Abstract:

The invention relates to petrochemistry. The process is carried out in the presence of a catalyst containing alkali metal on a solid inorganic carrier, modified by various forms of carbon in the reactor having a vertical cylindrical housing and containing a reaction zone with a stationary catalyst bed. The area is designed as a sealed cylindrical tank having spaced parallel to its vertical axis of the cylindrical channels. The reactor is equipped with gazoprovodsk pipes mounted with radial clearance in cylindrical channels. The reaction zone is installed coaxially with radial clearance relative to the reactor vessel with the ability to extract her from the reactor to replace the catalyst. Preferably the method is carried out in the presence of a catalyst containing 3.0 to 3.5 wt.% metallic sodium to the potassium modified by various forms of carbon in the amount of 1.0 to 3.0 wt. % at 100 - 200oC - pressure 8,0 - 10,0 MPa. 1 C.p. f-crystals, 1 Il., table 2.

The invention relates to the field of chemistry, in particular to a method of dimerization and codimerization of lower olefins.

In the process of dimerization and hundreds way of dimerization and codimerization of lower olefins [1] in which the process is carried out in a reactor with a vertical cylindrical casing, having a reaction zone with a stationary catalyst bed. The heat of reaction carried out by a system comprising heat exchanger, designed to be placed in the four plates hollow chambers located along the axis of the reactor and a cruciform cross-sectional area of the reactor. The heat of reaction divert the circulation of the temperature-controlled liquid propane in a closed loop.

The method uses a catalyst containing alkali metal on a solid inorganic carrier, various modified forms of carbon.

The disadvantages of this method are not high performance and duration of stable operation of the catalyst.

Closer to the proposed to the technical essence and the achieved effect is the way the dimerization and codimerization of lower olefins, which process is also carried out in a reactor with a vertical cylindrical housing having a reaction zone with a stationary catalyst bed [2]

The heat dissipation perform the same as the above except that the plate heat exchanger hollow chamber is divided into upper and lower polyamory, interconnected, resulting in more usovershenstvoval on a solid inorganic carrier, modified various forms of carbon, for example, 3,5 wt. sodium to the calcium carbonate containing 1.5 wt. graphite. When carrying out process at 150oC and a pressure of 9.0 MPa conversion of propylene is of 29.1 wt. for passage, the selectivity of the formation of 4-methylpentene-1 (4-MP-1) of 89.7 wt.

The method has the same drawbacks, namely poor performance and duration of stable operation of the catalyst. In addition, the complexity of replacing spent catalyst leads to the contact of the used catalyst with air, which in turn leads to a decrease in catalyst activity.

The purpose of the invention improving the performance of the catalyst, the duration of its stable operation.

This goal is achieved by the described method of dimerization and codimerization of lower olefins in the presence of a catalyst containing alkali metal on a solid inorganic carrier, modified by various forms of carbon at elevated temperature and pressure in the reactor having a vertical cylindrical housing and containing a reaction zone with a stationary catalyst bed, made in the form of a sealed cylindrical tank installed ENES hollow chamber, made in the form of cylindrical channels within which are mounted with radial clearance gazoprovoda pipe. The feedstock is served in the hollow chamber and then into the catalyst bed. The reaction zone is configured to retrieve her from the reactor to replace the catalytic Converter.

Preferably the process is carried out in the presence of a catalyst containing 3,0 3,5 wt. metallic sodium to the potassium modified by various forms of carbon in the amount of 1.0 to 3.0 wt. when 100 200oC and the pressure 8,0 10,0 MPa.

Distinctive features of the process involve the latest in a reactor having a reaction zone, is designed as a sealed cylindrical tank mounted coaxial with radial clearance relative to the reactor vessel with the ability to extract the last of the reactor to replace the catalyst and the hollow chamber, made in the form of cylindrical channels within which are mounted with radial clearance gazoprovoda pipe.

The drawing shows a schematic diagram of carrying out the described method.

The method is carried out in reactor 1 with a housing 2 containing a reaction zone, made in the form of a cylindrical tank 3 with the hospital the bone 3. The reactor is equipped with gazoprovodsk tubes 6, which are mounted with radial clearance in a cylindrical channel 5. The reaction zone is installed coaxially with radial clearance relative to the reactor vessel 2. The propylene feedstock on line 7 serves in gazoprovoda pipe 6. Next last submit in cylindrical channels, where propylene is heated by the heat of reaction. Heated propylene through a radial gap between the reactor vessel and the reaction zone and further along the line 8 serves to mix with the recirculating flow of propylene supplied through line 9 into the heat exchanger 10. The mixture in line 11 serves on the fixed catalyst bed 4. The reaction stream in line 12 is directed to the separation of the products obtained.

As a catalyst can be used alkali metals such as, for example, sodium, potassium, lithium solid inorganic carrier, for example, potassium carbonate (potash), aluminum oxide, etc.

To modify the catalyst is used such forms of carbon, as carbon black, graphite, charcoal.

Preferably the process is carried out in the presence of a catalyst containing 3,0 5,0 wt. metallic sodium on the potash. The amount of modifier is 1.0 to 3.0 wt. Bake from the reactor and connect directly to the site of regeneration of the catalyst (Fig. not shown) for the least contact of the catalyst with air.

In table. 1 shows conditions of the method according to examples 1 to 3, PL. 2 the results obtained here, as well as data by a known method.

From these tables it is seen that under the conditions described method, the conversion of propylene is 29,2 29,4 wt. the selectivity of the formation of 4-MP-1 - 89,8 90,1 wt. the performance of the catalyst 285 310 kg/kg, the duration of stable operation of the catalyst 830 875 hours

Thus, the described method can improve the performance of the catalyst and the duration of its stable operation. In addition, this method allows us to simplify the operation of loading and unloading of the used catalyst.

Literature.

1. Application France N 2633284, C 07 C 2/24, 1989.

2. Application France N 2633285, C 07 C 2/24, 1989.

1. The way the dimerization and codimerization of lower olefins in the presence of a catalyst containing alkali metal on a solid inorganic carrier, modified by various forms of carbon at elevated temperature and pressure in a vertical cylindrical reactor having a reaction zone with a stationary catalyst bed, in which the fact, that the reaction zone is designed as a sealed cylindrical tank mounted coaxial with radial clearance relative to the reactor vessel with the ability to extract the last of the reactor to replace the catalyst, and a hollow chamber in the form of cylindrical channels within which are mounted with radial clearance gazoprovoda pipe.

2. The method according to p. 1, wherein the process is carried out in the presence of a catalyst containing 3 to 5 wt. metallic sodium to the potassium modified by various forms of carbon number 1 to 3 wt. at a temperature of 100 200oC, a pressure of 8 to 10 MPa.

 

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2 cl, 6 ex, 2 tbl

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