Method of production of light olefins in catalytic cracking units with energy deficiency

a technology of light olefins and catalytic cracking, which is applied in the direction of cracking process, catalytic cracking, petroleum industry, etc., can solve the problems of increasing the thermal demand in the reactor, aggravate the problem of meeting the thermal demand, and difficult to meet the energy demand, so as to minimize the energy deficiency of catalytic cracking in petrochemical operations with light hydrocarbons

Inactive Publication Date: 2011-11-03
PETROLEO BRASILEIRO SA (PETROBRAS)
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Benefits of technology

[0012]In the present invention, light olefins are produced, such as ethylene and propylene, and moreover an appreciable amount of coke is deposited on the catalyst. Gains are observed in selectivity for light olefins, and at the same time the energy def

Problems solved by technology

The cracking reactions for production of light olefins are highly endothermic, drastically increasing the thermal demand in the reactor, which makes it difficult to meet the energy demand.
The problem of meeting the thermal demand is aggravated if the streams used as feed are formed by light hydrocarbons, such as diesel or naphtha, which usually deposit smaller amounts of coke on the catalyst compared with the heavier feeds such as vacuum gas oils or atmospheric residues.
Nevertheless, besides the increase in the heat of reaction, the thermal demand is not met for three main reasons:1) the actual feed used is not a good precursor for formation of coke, having low Ramsbottom carbon residue,2) light hydrocarbons are more refractory to cracking, requiring higher reaction temperatures;3) conventional zeolites ZSM-5 do not produce much deposition of coke on the catalyst and the amount that must be used in the catalytic system is very large.
The regenerator bed must be heated

Method used

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Examples

Experimental program
Comparison scheme
Effect test

example 1

[0043]After the hydrothermal treatment, an amount of equilibrium catalyst E1, obtained from a commercial unit, equivalent to a weight ratio of 8% to 92% of E1, was mixed with each sample investigated. Catalytic tests were carried out using feed C1 at a temperature of 535° C.

[0044]Table 3 presents the most important results of the catalytic tests.

TABLE 3Catalytic tests performed in the ACE unit with feed C1Condition (mixture 92% E1 + 8% catalyst)12345CatalystR1ABCDConditions:Reaction temperature (° C.)535535535535535Catalyst / feed ratio (w / w)5.05.05.05.05.0Balance relative to the feed:FG—Fuel gas (% w / w)3.03.13.73.43.4LPG—Liquefied gas (% w / w)19.219.619.519.318.7Gasoline: C5 −220° C. (% w / w)33.832.632.632.533.1+220° C. (% w / w)39.839.638.638.839.7Coke (% w / w)4.25.15.66.05.1Coke relative to catalyst R1—+22%+32% +43%+22%Total (% w / w)100.0100.0100.0100.0100.0Light olefins relative to thefeed:Propylene (% w / w)7.67.97.97.77.7Ethylene (% w / w)1.141.311.61.31.41Ethylene relative to catalyst R1...

example 2

[0046]After the hydrothermal treatment, an amount of equilibrium catalyst E2, obtained from a commercial unit, equivalent to a weight ratio of 80% to 20% of E2, was mixed with the sample investigated. It should be pointed out that in this example catalytic tests were carried out at 600° C., a higher reaction temperature within the range of reaction temperature employed for production of light olefins, and feed C2, typical of middle distillates with low coke forming potential.

[0047]The results are shown in Table 4.

TABLE 4Catalytic tests performed in the ACE unit with feed C2Condition (mixture 80% catalyst + 20% E2)(6)(7)CatalystR2DConditions:Reaction temperature (° C.)600600Catalyst / feed ratio (w / w)5.05.0Balance relative to the feed:FG—Fuel gas (% w / w)8.4011.24LPG—liquefied gas (% w / w)22.717.4Gasoline: C5 −220° C. (% w / w)25.628.0>220° C. (% w / w)39.539.0Coke (% w / w)3.774.36Coke relative to catalyst R2—+16%Total (% w / w)100.0100.0Light olefins relative to the feed:Ethylene (% w / w)5.296....

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Abstract

The present invention relates to a method of production of light olefins, with the objective of maximizing the production of propylene and in particular ethylene by the use of a special catalyst containing high-silica zeolite, whose composition also includes a dehydrogenating metal, so as to generate light olefins and appreciable deposition of coke on the catalyst. Gains in selectivity for light olefins are observed, and at the same time the energy deficiency of catalytic cracking in petrochemical operations with light hydrocarbons is minimized, avoiding problems due to the need to burn heating oil in the catalyst regenerating section to make up for the energy deficit of the converter.

Description

FIELD OF THE INVENTION[0001]The present invention relates to the field of processes for the production of light olefins, more particularly ethylene and propylene, in circulating fluidized-bed reactors by means of catalytic conversion with solid acids, being applicable to a feed comprising light hydrocarbons. The method described in the present invention teaches the use of a special catalyst for producing light olefins and depositing an appreciable amount of coke on the catalyst. Besides increasing the selectivity for light olefins and maximizing the production of propylene and, in particular, ethylene, at the same time use of the method minimizes the energy deficiency of catalytic cracking in petrochemical operations with light hydrocarbons.BACKGROUND OF THE INVENTION[0002]In the fluidized-bed catalytic cracking process, the cracking reactions of hydrocarbons take place by contact of a feed with a catalyst in conditions of dynamic flow, in a tubular reactor in ascending flow, also k...

Claims

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Application Information

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IPC IPC(8): C10G11/04C10G11/00
CPCC10G11/02C10G11/18C10G11/05
Inventor PINHO, ANDREA DE REZENDELAU, LAM YIU
Owner PETROLEO BRASILEIRO SA (PETROBRAS)
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