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
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[0046] Example 1
[0047] One-stage reaction composite catalyst preparation:
[0048] Weigh 15g SAPO-34 molecular sieve and disperse it in 200ml deionized water, add 3.75ml PdCl 2 The solution (metal Pd content 20mg / ml) was slowly added dropwise to the molecular sieve, exchanged in a water bath at 60°C for 8 hours, and then filtered and washed with suction, dried at 120°C, and roasted at 520°C for 6 hours to obtain 0.5% Pd / SAPO -34. The catalyst Cu-ZnO-Al 2 O 3 (Cu-Zn-Al) and 0.5%Pd / SAPO-34, respectively compressed into tablets, broken into 20-40 mesh. Take 0.8g (1ml) mixed catalyst and mix the particles with Cu-Zn-Al:0.5%Pd / SAPO-34=1:3 mass ratio, H 2 Reduced at 250℃ for 5h under atmosphere, H 2 The flow rate is 10ml / min. The temperature is increased to 325°C, and the synthesis gas (H 2 +CO+4% volume concentration of N 2 ), the pressure is increased to 2.0MPa, the total gas flow rate is 1000ml / h, H 2 / CO=2. The CO conversion rate is 77%, and the hydrocarbon composition in the p...
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[0054] Example 2
[0055] In one stage of the process, the synthesis gas to low-carbon alkanes reaction was carried out according to the conditions given in Example 1, the CO conversion rate was 77%, and the hydrocarbon composition in the first stage reaction product was:
[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 of the second stage is 0.35. Table 2 shows the test results of thermal cracking of low-carbon alkanes to low-carbon olefins at different cracking temperatures.
[0058] Table 2 The influence of the same dilution steam ratio at different temperatures
[0059]
Example Embodiment
[0060] Example 3
[0061] In one stage of the process, the synthesis gas to low-carbon alkanes reaction was carried out according to the conditions given in Example 1, the CO conversion rate was 77%, and the hydrocarbon composition in the first stage reaction product was:
[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 obtained 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 the feed gas to the second stage is 2. Table 3 shows the test results of thermal cracking of low-carbon alkanes to low-carbon olefins at different cracking temperatures.
[0064] Table 3 Same N at different temperatures 2 Influence of dilution ratio
[0065]
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