SU727214A1 - Method of obtaining catalyst for cracking crude oil - Google Patents

Description

The invention relates to the manufacture of catalysts for the cracking of petroleum feedstocks. A known method for producing a catalyst for cracking petroleum, a raw material, is by mixing a zeolite with a co-precipitated aluminum silicate hydrogel, followed by the exchange of sodium ions for calcium, followed by impregnation of REE fl. The closest in technical essence is a method for producing a cracking catalyst for crude oil from a feedstock by mixing a modified type zeolite 3 1 calcium calcium silicate hydrogel and alumina produced by the alumina method 2. All three components are mechanically mixed in a ratio of 3: 1: 1, the gel is molded, dried and calcined. The result is a catalyst of the following composition, wt.%: Zeolite type NAZ20-25. Calcium silicate45-60 Alumina Else In the presence of this catalyst, the cracking of Grozny gas oil, 87O2, at a temperature of 45 ° C, a space velocity of 1 hour for a cycle time of 30 minutes, produces gasoline with a yield of 43.2 wt.%, And after steam treatment 52.6 wt.% . The disadvantage of the known method is the relatively low activity of the obtained catalyst. The aim of the invention is to obtain a catalyst with increased activity. This goal is achieved by mixing a modified N00 type zeolite with a calcium silicate hydrogel pretreated with 1-1.5N. an aqueous solution of aluminum sulfate, followed by molding, drying and calcining. The simplification of the method according to the invention is achieved in that instead of the three components (zeolite, Calcium silicate and alumina, obtained by aluminizing), two components are subjected to interaction (zeolite and calcium silicate treated with aluminum sulfate).

The resultant catalyst for the cracking of crude oil is gasoline yield of 48.5 wt.%, And after treatment of the catalyst with water vapor - 5b,.%.

Feed stock Liquid glass: Si02-26,41; MdgO-V.86; H ,, O -65,73; d 1.4190. Calcium chloride L1I, hydrophyllite, h. Solon-acid, d 1.14, 28%. Distilled water, .2.5% solution of a1 1miac. Zeolite YtsZ. Aluminum sulfate h.

PRI me R 1. 100 g of zeolite N on L with continuous stirring with a mechanical stirrer are subjected to four times treatment: once with 0.1 N. NH.C6 solution and three times with 0.1 n. rasSa ce2Pri temperature for 2 h each time.

The alumina-silicate silicate hydrogel is prepared by the method of co-precipitating liquid glass and hydrochloric acid acidified solution of CaSb salt (100 g of liquid glass + 400 ml 3.75 g of CACEjj + HCl + 300 ml at pH 9 treatment with 2.5% NH4OH (60O ml 2.5% per 1 kg of the body for 2 hours, subjected to stepwise activation with 1N aluminum sulphate solution () n for 5, 16, 5 hours and washed from SQi anions Then both components at the rate of 20% of the modified zeolite and 80% of alumino-silicate carrier the bodies are mechanically mixed. The gel is formed, dried and calcined at temperatures of 110, 250, 350, 450, with aging at each temperature for 6 hours. The resulting catalyst has a component composition,

Zeolite Tipo2O, 0

Calcium silicate 80.0. Moreover, the composition of the alumina-silicate component contains 19.0% of ASPO

The cracking capacity of the finished catalyst is determined by the cracking process of Grozny gasoline 620 O, 87 O 2 at a temperature of 45 ° C, the feed rate of the raw material is 1 hour and the cycle time is 30 minutes. To determine the stability indices, a fresh portion of the catalyst is subjected to water vapor treatment at a temperature of 65 ° C.

for which 50 cm of catalyst are treated with 30 cm of distilled water for 5 hours (50 cm of catalyst and 6 cm of water for 1 hour). Physico-chemical constants of the fresh sample (1 and after processing (2),

1. Poured weight 0.60 True beats. weight 2.3580

2. Poured weight0,65 True beats. weight 2.5433

Gasoline output with a CC of 48.5%. The gas yield of 19.7%, the output of coke 6.0 wt.%.

Stable activity: gasoline yield 56.8 wt.% Gas yield 15.6; coke yield 3.1% by weight.

Example 2. 100 g of zeolite Mo (

with continuous mixing with a mechanical stirrer, it is subjected to four-time processing; once 0.1 n. NNSE solution and three times O, 1 n. CaCB solution at a temperature of 8 ° C

5 for 2 h each time.

The hydrogel alu; "oxalicate silicate carrier is obtained, as in Example 1, by the method of co-precipitating liquid glass and Ca It solution, acidified

0 who has it (, pH 8).

The obtained calcium silicate hydrogel after washing from the Ct ions and treatment with an aqueous solution of 3% - «wow, is subjected to 1.5 n treatment. solution

5 aluminum sulphate and washed from SC ions. :

Then, both coYjunents from a calculation of 20% of modified zeolite and 80.% of alumino-silicate carrier mechanically

0 mixed, the gel is molded, dried and calcined. The catalyst has the same component composition as in the example of Ms 1, with the only difference that, when this is part of the apyum silicate carrier

45 contains 28, O% ASgO,

Physico-chemical constant of a fresh sample (1) of the obtained catalyst, and after steam processing (2), g / cm

1.Pouring weight 0.72

SO True beats. weight.2,4228

2. Bulk weight, 73 True beats. weight. 2.5715

Activity, No. of sample, wt.%: Gasoline45,4

55 Gas21.5

Coke6,5

Claims (2)

Stable activity after steam treatment, wt.%: Gasoline55.6 Gas, 17.9 Coke 3.4 Example 3. 100 g of Xc zeolite with continuous stirring with a mechanical stirrer are subjected to four-fold treatment: once with 0.1 N, - with a solution and three times 0.1 n. dissolve the temperature for two hours each time. The alumina-silicate silicate hydrogel is prepared by the method of co-precipitating liquid glass and hydrochloric acid acidified solution of the salt of SaCb / COOO g liquid glass 400 ml NdO, 3.75 SvSPa + 32 g HSE + ZOO ml tJj t-1 ph 9). I, -0 Calcium silicate hydro gel obtained after washing from C6 anions and treating with 2.5% NH4 OH (BOO ml 2.5% Mnfon per kg gel for 2 hours is subjected to step activation with 1 N, aluminum sulphate solution ( within 5, 16.5 hours) and washed away from unwanted anions SQj., Then both components at the rate of 25% of the 1st component and 75% of the 2nd component are mixed. The resulting catalyst has the following composition,, € (Zeolite Type A2525 Aluminum-silicate-silicate (3.0 Moreover, the composition of the alumina-silicate component contains 19.0 wt.% Agg Qj. Activity fresh sample, wt.%; Gasoline .44.7 Gas23.2 Coke6.4. Stable activity after steam treatment, wt.%: Gasoline, 55.9 Gas18.8 Cox3.8 Formula to invent and Method for producing catalyst for rewing petroleum feedstock, including mixing of a modified zeolite of NclO type with a calcium silicate hydrogel, orming, drying and calcination, starting with the fact that, in order to obtain a catalyst with increased acuity, the calcium hydrogel is pretreated with 1-1.5N. one solution of aluminum sulfate. Sources of information taken into account during the examination 1. Labor of GrozNII, Th. I.e. 92, 974, Grozny, i 2. The copyright certificate for number 233O424 / 04, cl. J 29 / O8, 976 (prototype).