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Method for preparing ethylene and propylene through catalytic cracking of light hydrocarbons

A technology for catalytic cracking and light hydrocarbons, applied in catalytic cracking, hydrocarbon cracking, hydrocarbon production, cracking, etc., can solve the problems of low yields of ethylene and propylene, difficulty in high-temperature cracking of light hydrocarbons, etc., and achieve good technical effects

Active Publication Date: 2012-10-24
CHINA PETROLEUM & CHEM CORP +1
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  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0010] The technical problem to be solved by the present invention is that it is difficult to realize the high-temperature cracking of light hydrocarbons in the process of catalytic cracking of light hydrocarbons in the prior art, and the yield of ethylene and propylene is low, and a new method for producing ethylene and propylene by catalytic cracking of light hydrocarbons is provided

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  • Method for preparing ethylene and propylene through catalytic cracking of light hydrocarbons
  • Method for preparing ethylene and propylene through catalytic cracking of light hydrocarbons
  • Method for preparing ethylene and propylene through catalytic cracking of light hydrocarbons

Examples

Experimental program
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Effect test

Embodiment 1

[0029] exist figure 1 On the shown device, 4 groups of experiments were carried out, and the reaction raw materials, catalysts, reaction conditions and results are shown in Table 1.

[0030] The content of butene in the mixed C4 is 73.8% by weight, and the content of n-butane is 26.2% by weight; the naphtha is mainly C 5 ~C 8 Alkanes, the contents are respectively 12.62 wt%, 25.54 wt%, 25.25 wt%, 17.86 wt%; catalytic cracking light gasoline (FCC light gasoline) is mainly pentene and hexene, the contents are respectively 36.4 wt% and 34.1 wt%.

[0031] The catalyst used in the experiment was prepared by a semi-synthetic method, that is, the molecular sieve, the carrier and the binder were mechanically mixed, and an appropriate amount of water, HCl and H 3 PO 4 (Not added when preparing SAPO-34 catalyst), control the pH value to not less than 3, stir the slurry evenly and spray it at 500°C. In the ZSM-5 catalyst used, the mass ratio of HZSM-5 molecular sieve and matrix is ​​...

Embodiment 2

[0039] Adopt the built-in type riser device basically identical with embodiment 1, but two feed nozzles are set on the built-in riser, two nozzles are 0.3 meters apart, enter and mix C4 and FCC light gasoline respectively from bottom to top, reaction raw material , reaction conditions, catalyst and reaction results are shown in Table 3. The composition of the raw materials used and the preparation process of the catalyst are shown in Example 1.

[0040] table 3

[0041]

Embodiment 3～7

[0043] exist figure 2 Five groups of experiments were carried out on the shown device, and the reaction raw materials, reaction conditions, catalysts and reaction results are shown in Table 4. The composition of the raw materials used and the preparation process of the catalyst are shown in Example 1.

[0044] The propane content in the liquefied gas was 7.5% by weight, the propylene content was 2.5% by weight, the butene content was 33.8% by weight, and the butane content was 56.2% by weight. The density of light diesel oil is 0.72 g / cm 3 , the H content was 15.2% by weight, the saturated content was 91.37% by weight, and the aromatic content was 8.63% by weight. Diesel has a density of 0.78 g / cm 3 , the H content is 14.7% by weight, the saturated content is 89.29% by weight, and the aromatic content is 10.71% by weight. Catalytically cracked gasoline (FCC gasoline) is mainly C 5 ~C 10 Hydrocarbons, olefins, alkanes, cycloalkanes, and aromatics are 36.4% by weight and ...

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Abstract

The invention relates to a method for preparing ethylene and propylene through the catalytic cracking of light hydrocarbons to mainly solve problems of difficult realization of the light hydrocarbon high temperature cracking, and low ethylene and propylene yields in the light carbon catalytic cracking process in the prior art. The method which allows the light hydrocarbon catalytic cracking to be carried out through a parallel type or coaxial type internal riser cycle reaction-regeneration device mainly comprises the following steps: 1, allowing a preheated light hydrocarbon raw material to enter an internal riser reactor, and reacting through contacting with a catalyst at 570-720DEG C to generate low carbon olefin-containing products and simultaneously form a carbon deposition catalyst; and 2, regenerating the carbon deposition catalyst through allowing it to enter a regenerator, and returning the regenerated catalyst to the riser reactor, wherein the active component of the catalyst is selected from at least one of a silicon-aluminum molecular sieve, an aluminum-phosphorous molecular sieve, a silicon-phosphorous-aluminum molecular sieve or a composite molecular sieve thereof, and the molecular sieve has a bore diameter of 0.4-0.65nm. The method well solves the problems through above technical scheme, and can be applied to the industrial production of ethylene and propylene.

Description

technical field [0001] The invention relates to a method for producing ethylene and propylene by catalytic cracking of light hydrocarbons. Background technique [0002] Ethylene and propylene are important basic raw materials for organic synthesis. In recent years, driven by the demand for downstream derivatives, the global market demand for ethylene and propylene has continued to grow. At present, the production of ethylene and propylene mainly relies on steam thermal cracking. About 90% by weight of ethylene and 61% by weight of propylene come from the steam thermal cracking process. Although this process has been widely used in the world, there are still unsatisfactory aspects, especially the reaction requires high temperature (800 ~ 1000 ℃) , high energy consumption, high yield of dry gas with low added value. If a catalyst is introduced and the method of catalytic cracking is adopted, the reaction temperature can be reduced by 50-200°C, energy consumption and dry gas ...

Claims

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Application Information

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IPC IPC(8): C10G11/18C10G11/05C07C11/06C07C11/04C07C4/06
CPCY02P20/52Y02P20/584
Inventor 李晓红钟思青王洪涛王莉
Owner CHINA PETROLEUM & CHEM CORP
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