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Method for production of low carbon olefins from synthetic gas via low carbon alkanes

A technology for the production of low-carbon olefins and carbon alkanes, which is applied in the field of low-carbon olefins, can solve the problems of relatively large influence of olefin prices and low selectivity of low-carbon olefins, and achieve the effects of reducing equipment investment, less by-products, and reducing operating costs

Inactive Publication Date: 2014-06-18
DALIAN INST OF CHEM PHYSICS CHINESE ACAD OF SCI
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The indirect method is mature and has entered industrialization. The catalyst is modified ZSM-5 or SAPO-34 molecular sieve. The conversion rate of methanol can reach 100%, the selectivity of ethylene and propylene is 85%-90%, and there is no C 5 + The above products, but the price of olefins is greatly affected by the fluctuation of methanol price
In the Fischer-Tropsch synthesis process, limited by the distribution of ASF, the selectivity of light olefins is low

Method used

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  • Method for production of low carbon olefins from synthetic gas via low carbon alkanes
  • Method for production of low carbon olefins from synthetic gas via low carbon alkanes
  • Method for production of low carbon olefins from synthetic gas via low carbon alkanes

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0047] One-stage reaction composite catalyst preparation:

[0048] Weigh 15g SAPO-34 molecular sieve and disperse it in 200ml deionized water, dissolve 3.75ml of PdCl 2 The solution (metal Pd content 20mg / ml) was slowly added dropwise onto the molecular sieve, exchanged in a water bath at 60°C for 8h, then filtered and washed, dried at 120°C, and roasted at 520°C for 6h to obtain 0.5%Pd / SAPO -34. Catalyst Cu-ZnO-Al 2 o 3 (Cu-Zn-Al) and 0.5%Pd / SAPO-34, respectively pressed into tablets, broken into 20-40 mesh. Get 0.8g (1ml) mixed catalyst, carry out particle mixing with Cu-Zn-Al:0.5%Pd / SAPO-34=1:3 mass ratio, H 2 Reduction at 250°C for 5h under atmosphere, H 2 The flow rate is 10ml / min. The temperature is raised to 325°C, and synthesis gas (H 2 + CO + 4% N by volume 2 ), pressurized to 2.0MPa, total gas flow rate 1000ml / h, H 2 / CO=2. The CO conversion rate is 77%, and the hydrocarbon composition in the product after the first stage of reaction is:

[0049] CH 4 5....

Embodiment 2

[0055] One-stage process is carried out according to the conditions given in Example 1 to produce low-carbon alkanes from syngas, the CO conversion rate is 77%, and the hydrocarbon composition in the one-stage reaction product is:

[0056] CH 4 5.2%, C 2 h 6 23.6%, C 3 h 8 49.9%, C 4 h 10 16.1%, C 5 +5.2%.

[0057] The obtained product is directly introduced into the second-stage reactor for steam thermal cracking reaction. The volume ratio of the dilution steam to the feed gas in the second stage is 0.35. Table 2 shows the test results of pyrolysis of light alkanes to light olefins at different cracking temperatures.

[0058] Table 2 Effect of the same dilution steam ratio at different temperatures

[0059]

Embodiment 3

[0061] One-stage process is carried out according to the conditions given in Example 1 to produce low-carbon alkanes from syngas, the CO conversion rate is 77%, and the hydrocarbon composition in the one-stage reaction product is:

[0062] CH 4 5.2%, C 2 h 6 23.6%, C 3 h 8 49.9%, C 4 h 10 16.1%, C 5 +5.2%.

[0063] The resulting product is directly introduced into the second-stage reactor for thermal cracking reaction. The dilution steam of the second stage process is changed to N 2 , diluted N 2 The volume ratio of raw material gas to the second stage is 2. Table 3 shows the test results of the thermal cracking of light alkanes to light olefins at different cracking temperatures.

[0064] Table 3 The same N at different temperatures 2 Effect of Dilution Ratio

[0065]

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Abstract

The invention relates to a method for production of low carbon olefins from a synthetic gas via low carbon alkanes. The low carbon olefins are produced by adopting a two stage reactor in series way. A first stage reactor is filled with a multifunctional composite catalyst, in the reaction conditions of the temperature of 260-450 DEG C, the space velocity of 500-5000h <-1>, the pressure of 1.0-5.0MPa, the H2 / CO molar ratio of 0.5-5.0, the synthesis gas reacts on the multifunctional composite catalyst to produce a hydrocarbon product mainly comprising low carbon alkanes. The product directly enters without separation into a second stage reactor to produce low carbon olefins mainly comprising ethylene by a thermal cracking way; also the product can be divided into two parts, one part of the product mainly comprising methane and ethane produces the ethylene by the thermal cracking way, and the other part of the product mainly comprising propane and butane produces the low carbon olefins mainly comprising propylene and butylenes by catalytic dehydrogenation and other ways.

Description

technical field [0001] The invention relates to a method for preparing low-carbon olefins from syngas, in particular to a method for producing low-carbon olefins from syngas through light alkanes. Background technique [0002] Low-carbon olefins represented by ethylene and propylene are basic organic chemical raw materials with wide application and great demand. At present, the production of low-carbon olefins mainly adopts the petrochemical route of cracking light hydrocarbons (ethane, naphtha, light diesel oil), which is heavily dependent on petroleum resources. Due to the increasing shortage of global oil resources and the long-term high price of crude oil, the tube furnace cracking process for the production of light olefins from petroleum light hydrocarbons will encounter more and more raw material problems. Therefore, the production process and raw materials of low-carbon olefins must be Diversification. Nowadays, the route of producing syngas from coal, natural gas,...

Claims

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Application Information

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IPC IPC(8): C07C11/04C07C11/02C07C4/04C07C5/333C07C5/327C07C1/04C07C9/02
Inventor 葛庆杰方传艳徐恒泳马现刚侯守福李卫力
Owner DALIAN INST OF CHEM PHYSICS CHINESE ACAD OF SCI
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