Flow process for synthesizing C3 to C13 high hydrocarbons by methane through non-synthetic gas method

A technology of methane and process, which is applied in the field of preparation of high-carbon hydrocarbons from C3 to C13, and can solve problems such as the danger of large-scale use

Active Publication Date: 2007-09-26
MICROVAST POWER SYST CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The above processes all involve the use of elemental bromine and require additional steps to regenerate elemental bromine, and it is dangerous to use and store elemental bromine in large quantities

Method used

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  • Flow process for synthesizing C3 to C13 high hydrocarbons by methane through non-synthetic gas method
  • Flow process for synthesizing C3 to C13 high hydrocarbons by methane through non-synthetic gas method

Examples

Experimental program
Comparison scheme
Effect test

example 1 to example 23

[0012] Example 1 to Example 23, the bromine oxidation reaction of alkanes

[0013] The catalyst is made of silica (10 g specific surface 1.70m 2 / g), RuCl 3 The solution (0.00080 g Ru / ml) and the corresponding metal nitrate solution (0.10 M) were mixed according to the mol composition of the catalyst in Table 1, stirred at room temperature for half an hour, dried at 110°C for 4 hours, and finally fired at 450°C Catalyst Examples 1 to 23 in Table 1 were obtained after 12 hours.

[0014] The catalytic reaction is carried out in a quartz tube reactor with an internal diameter of 0.80 cm and a length of 60 cm. The reaction temperature is listed in Table 1. The methane flow is 5.0 ml / min, the oxygen flow is 5.0 ml / min, and 40 wt% HBr / H 2 O aqueous solution flow rate is 4.0 milliliters (liquid) / hour, catalyst 1.0000 grams. Both ends of the catalyst are filled with quartz sand. The reaction products were analyzed by gas chromatography, and the results are listed in Table 1, as in...

example 24

[0018] The catalyst is made of silica (10 g specific surface 0.50m 2 / g), RuCl 3 solution (0.0008 g Ru / ml), La(NO 3 ) 3 (0.10M), Ba(NO 3 ) 2 (0.10M), Ni(NO 3 ) 2 (0.10M) by 2.5% La, 2.5% Ba, 0.5% Ni, 0.1% Ru and 94.4% SiO 2 Mix the mol composition, stir at room temperature for half an hour, dry at 110°C for 4 hours, and finally burn at 450°C for 12 hours to get the composition La2.5%Ba2.5%Ni0.5%Ru0.1% / SiO 2 catalyst.

[0019] The catalytic reaction is carried out in a quartz tube reactor with an inner diameter of 1.50 cm and a length of 60 cm. The reaction temperature is 660° C., the methane flow rate is 15.0 ml / min, the oxygen flow rate is 5.0 ml / min, and 40 wt% HBr / H 2 O aqueous solution flow rate is 6.0 milliliters (liquid) / hour, catalyst 5.000 grams. Both ends of the catalyst are filled with quartz sand. The reaction product is analyzed on gas chromatography, and the result is: methane conversion rate 32.0%, CH 3 The selectivity of Br is 80.8%, CH 2 Br 2 The s...

example 25 to example 38

[0020] Example 25 to Example 38, brominated hydrocarbons are converted into higher carbon hydrocarbons

[0021] Preparation of ZnO / HZSM-5 and MgO / HZSM-5 Catalysts

[0022] Catalysts C1 to C14 of examples 25 to 38 in table 2 are made of molecular sieve HZSM-5 (Si / Al=360,283m 2 / g), water and Zn(NO 3 ) 2 ·6H 2 O(or Mg(NO 3 ) 2 ·6H 2 O) Mix and stir according to the amount in Table 2, soak at room temperature for 12 hours, dry at 120°C for 4 hours, burn at 450°C for 8 hours, press at 100 atmospheres, crush and sieve to 40 to 60 mesh to obtain Catalysts in Table 2.

[0023] example

[0024] The catalysts of Examples 25 to 38 were used for CH 3 Br is converted into the reaction of high-carbon hydrocarbons, the reaction is carried out in a glass reaction tube with an inner diameter of 1.5 cm, the catalyst consumption is 8.0 grams, the reaction temperature is 240 ° C, CH 3 Br flow rate is 6.8ml / min, reaction product is analyzed on gas chromatography, CH 3 The con...

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Abstract

The invention discloses a new flow path to make C3-C13 hydrocarbonate at the beginning with methane, which is characterized by the following: transmitting methane into CH3Br and CH2Br2 acted by oxygen and HBr / H2O; reacting CH3Br and CH2Br2 in the second reactor to make C3-C13 hydrocarbonate and HBr; adopting HBr as circulated reacting dielectric in the making course of CH3Br and CH2Br2; making the transmitting rate of methane to 32.0% and the selectivity of CH3Br to 80-0% and the selectivity of CH2Br2 to 0.67%; entering the product in the first reactor and residual reacting material into the second reactor directly; making the transmitting rate of methane in the first reactor to 30.0% and total selectivity of CH3Br and CH2Br2 to 88% in the first reactor and the transmitting rate of CH3Br and CH2Br2 to 100% in the second reactor.

Description

technical field [0001] The present invention relates to a new process for preparing C3-C13 high-carbon hydrocarbons from methane, which is an extension of the Chinese invention patent with application number 200410022850.8 and involves further research results. Background technique [0002] The main component of natural gas is methane, with small amounts of ethane, propane, water vapor and carbon dioxide. Natural gas is the most abundant hydrocarbon fossil resource after coal. Compared with coal, natural gas is a cleaner hydrocarbon raw material. It can be directly used as fuel, and theoretically it can also be used as chemical raw material to produce other chemicals; but because gaseous natural gas is difficult to compress and transport, it is usually produced far away from the place of use. In other regions, the actual application cost is relatively high, and since the main component of natural gas is methane, the C-H bond in it is very stable, and it is difficult to conv...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C2/00C07C9/02C07C9/14
CPCB01J23/8946B01J23/63B01J29/46B01J21/08B01J37/0201B01J23/6482B01J23/58B01J37/0009B01J23/6525B01J23/462B01J29/405C07C17/154B01J2229/18B01J23/464B01J29/40B01J29/48B01J29/44C07C19/075
Inventor 李文生黄莉任艳群周小平
Owner MICROVAST POWER SYST CO LTD
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