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Selective hydrogenation method for C3 fraction

A selective hydrogenation and fractionation technology, applied in hydrocarbons, chemical instruments and methods, purification/separation of hydrocarbons, etc., can solve problems such as long distances in industrial applications, and achieve excellent anti-coking performance and operational flexibility Good, no ethylene loss effect

Inactive Publication Date: 2018-07-06
PETROCHINA CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0009] To sum up, the selective hydrogenation of C3 fractions currently mainly uses noble metal catalysts. Although a lot of work has been done on the research and development of non-noble metal catalysts, there is still a long way to go before industrial application.

Method used

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  • Selective hydrogenation method for C3 fraction
  • Selective hydrogenation method for C3 fraction
  • Selective hydrogenation method for C3 fraction

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0070] Weigh a clover-shaped alumina carrier of Φ4.5×4.5mm. Take ferric nitrate, dissolve it in 60ml of deionized water by heating, adjust the pH value to 2.5, impregnate the equal volume on the surface of the carrier at the temperature of 50°C, flip the carrier quickly for 6 minutes, let it stand still for 30 minutes until the adsorption equilibrium, and age at 60°C for 30 minutes, then in In the oven follow the procedure: Dry the catalyst, and then use the temperature programming method to activate the catalyst. The activation procedure: Weigh cobalt nitrate and impregnate according to the above preparation steps. The physical properties of the carrier and catalyst and the content of each component of the catalyst are shown in Table 1.

[0071] Before the catalyst is used, it is reduced with 40% hydrogen + 60% nitrogen in a reduction furnace, the reduction temperature is 420° C., the pressure is 0.5 MPa, and the reduction time is 4 hours. Catalyst XRD analysis after r...

Embodiment 2

[0074] At 50°C, the NaAlO 2 solution and ZrCl 4 The solution was stirred and mixed, then neutralized with nitric acid solution, stirred for 10 hours, and uniform Al-Zr particles were formed by co-precipitation. The resultant was filtered and the Na in it was washed with deionized water + and Cl - Ions, and then add polyvinyl alcohol with a mass concentration of 15% as a pore-forming agent, kneading and molding. Dry at 130°C for 2h, and calcined at 650°C for 4h to obtain a Zr-Al composite support. The mass ratio of alumina to zirconia in the carrier is 4:1.

[0075]The catalyst was prepared with alumina-zirconia composite carrier. Take ferric chloride and cobalt chloride, heat and dissolve them in deionized water, adjust the pH value to 2.0, impregnate the excess on the carrier at a temperature of 80°C, shake the beaker for 10 minutes, filter off the excess impregnating liquid, and place the catalyst in a water bath at 60°C Medium aging for 50min, then follow the procedur...

Embodiment 3

[0081] Weigh 100ml of a Φ1.5mm spherical α-alumina carrier. Dissolve ferric nitrate in 40ml of deionized water, adjust the pH value to 3.0, soak the liquid at 40°C, spray it on the carrier with a watering can, load it in the drum for 10 minutes to make the active components evenly loaded, and control the loading process in 6 minutes to complete, and then In the oven follow the procedure: Dry the catalyst, move the catalyst into an evaporating dish, and activate the catalyst in a muffle furnace using a temperature-programmed method. Activation procedure: room temperature Obtain a catalyst dip.

[0082] Using the same method as the first step, take cobalt nitrate, dissolve it, spray it on the surface of the catalyst, dry it, and roast it to obtain the final catalyst. Drying procedure: Roasting procedure:

[0083] The physical properties of the carrier and catalyst and the content of each component of the catalyst are shown in Table 1.

[0084] Before the catalyst i...

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Abstract

The invention relates to a selective hydrogenation method for a C3 fraction. The C3 fraction used as a hydrogenation raw material undergoes hydrogen distribution, and is selectively hydrogenated by anFe-Co catalyst to convert methylacetylene (MA) and propadiene (PD) in the material into propylene. The carrier of the catalyst is a high temperature-resistant inorganic oxide, the active components of the catalyst at least contain Fe and Co, and 100 mass% of the catalyst contains 9-15 mass% of Fe and 3-4 mass% of Co; and the specific surface area of the catalyst is 10-300 m<2> / g, and the pore volume is 0.2-0.65 ml / g, wherein Fe and Co are loaded on the carrier in an impregnating manner, and the Fe and Co supported carrier is calcined, and is reduced in a hydrogen atmosphere to prepare the catalyst. Reaction conditions are as follows: the inlet temperature is 30-50 DEG C, the pressure is 1.5-3.5 MPa, the liquid space velocity is 15-120 h<-1>, and a ratio of hydrogen / MAPD is 1-10. The catalyst has the advantages of good hydrogenation activity, excellent olefin selectivity, high olefin increment and good long-period running performance, and has a lower cost than a precious metal Pd catalyst.

Description

technical field [0001] The present invention relates to a method for selective hydrogenation of C3 cuts, in particular to a method for selectively hydrogenating propyne (MA) and propadiene (PD) contained in C3 cuts into propylene using Fe-Co catalysts . Background technique [0002] Propylene is one of the most important basic raw materials in the petrochemical industry and an important monomer for the synthesis of various polymers. have to. The propylene-based C obtained by this method 3 In the fraction, the content of propylene is 70-90% (mol), propane is 5-10% (mol), and propyne (PD)+propadiene (MA) is 1.5-8.0% (mol). The existence of MAPD will affect the quality of the polymerization product. At present, the method of selective hydrogenation is generally used in the petrochemical industry to remove it. The usual process conditions for hydrogenation reaction are: reactor inlet temperature 20-50°C, reaction pressure 2.2-3.0MPa, liquid volume space velocity 15-120h -1 ...

Claims

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Application Information

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IPC IPC(8): C07C7/167C07C7/163C07C11/06B01J23/75B01J35/10
CPCC07C7/163C07C7/167B01J23/002B01J23/75B01J35/613B01J35/615B01J35/635B01J35/633C07C11/06Y02P20/52
Inventor 张峰苟尕莲钱颖韩伟谷丽芬车春霞潘曦竹梁玉龙景喜林杨珊珊王斌郭珺景丽
Owner PETROCHINA CO LTD
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