SU575127A1 - Catalyst for gasoline reforming - Google Patents

Description

(54) CATALYST FOR REFORMING BENZINS ©

one

The invention relates to the production of catalysts for the reforming of gasolines.

Catalysts for the reforming of gasolines containing platinum on alumina LlU are known.

1 Yev & Sgen is also a catalyst, which contains platinum injected on oxide al-emini (bayerite), promoted with halides, for example chlorine. The catalyst has an increased number of pores with a diameter of more than 100 A And}.

However, the known catalyst has a low stability (720O hour in the first period of work).

The chain of the invention — increasing the stability of the catalyst — is achieved by additionally adding titanium dioxide to the catalyst composition with the following content of components, wt.%:

1Ppatina0,2 - 1,0

Khpor0,1 - 3,0

Titanium dioxide O, 1 -1O, 0

Alumina Rest

Example. To obtain a catalyst, dried g-hydroxide of aluminum with a boehmite structure containing

0.05; 0.10 and 5, OO wt.% Titanium dioxide.

Aluminum hydroxide is prepared by the decomposition of alkoxyproducible aluminum with a carbon number of 6 to 18. These compounds are waste products of fatty alcohol production by catalytic polymerization of ethylene in the presence of oxygen with the participation of aluminum triethyl and titanium, which can be adjusted as before. hydrolysis, and after it. Grate alumina; Peptitized and molded in the form of puffs with a diameter of 1.5 mm and a diameter of 5 mm, dried at 15 ° C, annealed for 4 hours in a stream of air at and impregnated with a solution of hydrochloride, acetic acid (in cooTHOiiieHHB 1: 2) hydrochloric acid. The resulting catapant is dried 24

hour at

Catalysts are obtained with a content of 0.60} 0.25 or 1, OO wt% by weight of O, 35j O, 30 or O, 2O wt.% Of chior and ODL; O, O ip 5, OO Bes.% Of alumina dioxide (up to 1 OO wt.%) Respectively. The catalysts have a specific surface of 19 O m /, a micropore volume of 0.50 mp / g, a pore diameter of 10 and a mechanical strength when cutting Yun. : The catapiser is activated in the reforming unit in the atmosphere: hydrogen, containing 2% nitrogen and methane, rtpH heated to 4OOt at a rate of 35 C / hour. Circulating gas passes; through the dehumidification, filled with type 4A network cards. For activation, a gas containing 0, OO1 by volume is used. water, activation time 4 hours. Example 2. The testing of catalysts is carried out in an adiabatic installation of catalysts.

The tested catalysts are practically the same in activity and composition of the reformed products.

Example 3. Catalysts are prepared under {common conditions (see Table 2) and tested to feedstock 100: 1.

0.15

0.15 0.15

0.00

The time it takes for the initial activity of the catalyst, characterized by the octane number of the product, to be 100%, is determined. the research port 5 is reduced to an octane number of 90.

Calculate the material balance for the first 72 hours and analyze the average sample of the product during this time.

The results are shown in Table 3.

; rolled on the unit with the volume of the reactor YuOmp, using the same raw materials as in example 2, at a pressure of 15 kg / cm, temperature 5p5С, space velocity 2, and gas ratio

Table 2

Drying, actin behind the reactor

Also

HN

Burning out in a stream of air with the subsequent - activation - the same

Catalysts containing 0.2 wt.% ThOg or 0.2 wt.%, When reformed with the same feed, are comparable in activity to catalyst A and are superior to the catalyst. G.

As follows from the data given in table. Titanium dioxide cathode composition leads to an increase in catalyst stability. The duration of the catalyst in the first period is 1OOOOH. reforming with a catapic space of 100 mp. Volume ratio of three separate catalyst layers 1. 2 4. After the recovery of the catapacizers, a gasoline fraction of 100-170 ° C containing 7O% aliphatic, 20% naphthenic and 10% aromatic hydrocarbons is supplied. The activity of the catalysts is determined at a pressure of 35 kg / cm, a space velocity of Ii5 hour and a gas: feed ratio of 1500: 1. In tab. 1 shows the reforming results obtained at different inlet temperatures in the catalyst beds. Table 1

Claims (2)

1.Sukhanov V.P. Catalytic processes in oil refining, L. Khimi, 1973, p. 172. 2. Materials of the coordination center of the CMEA member countries on the problem Development of new industrial catalysts and improvement of the quality of catalysts used in industry, Novosibirsk, 1973 p. 126.