An anionic surfactant of general formula (I) in which n and m are, independently of one another, numbers from 0 to 17 and 2<n+m<20, and X.sup.+ is a charge-balancing cation. The invention also relates to a production method by way of: the acid-catalysed reaction of 2,5-bis(hydroxymethyl) tetrahydrofuran with an alkene having 5 to 22 C atoms in equimolar amounts, at an increased temperature; subsequent sulphation with a sulphating agent; and optional neutralisation by a subsequent reaction with ##STR00001##
X.sup.+OH.sup.− or X.sup.+.sub.2 CO.sup.2−.sub.3, where X.sup.+ is an alkali metal cation or a group N.sup.+R.sup.1R.sup.2R.sup.3, in which R.sup.1, R.sup.2 and R.sup.3 are, independently of one another, hydrogen, an alkyl group with 1 to 6 C atoms, or a hydroxyalkyl group with 2 to 6 C atoms. Detergents or cleaning agents containing—the surfactant, and the use of same to improve the performance of the detergents or cleaning agents, are also disclosed.

The present application relates to a method for synthesizing nanozeolite Y crystals, nanozeolite Y crystals obtainable by said method, and the use of the synthesized nanozeolite Y crystals in cracking hydrocarbons, as molecular sieves or as ion-exchangers.

The present disclosure provides a catalyst represented by Formula (I)

##STR00001##

wherein the moiety X[(RO.sub.a)(QO.sub.b)] and the moiety Z are mechanically mixed; wherein the weight percentage of the moiety Z is about 1% to about 99% of the total weight of the catalyst. Furthermore, the present disclosure provides a tunable, low-temperature, energy-efficient process for hydrocracking plastics to form a fuel, a lubricant, or a mixture thereof.

The present disclosure is directed to a method of manufacture of faujasite zeolite including zeolite Y. A sol-gel formulation includes a water-soluble fraction of ODSO as an additional component. The resulting products include faujasite zeolite, and yields can be increased relative to comparable sol-gel formulations without ODSO.

The present invention addresses to a process for the production of aromatic compounds from streams containing linear chains with 5 to 18 carbon atoms, of fossil or renewable origin, and application in the field of catalytic cracking aiming at a regenerator operation at much lower temperature, between 480° C. and 620° C., preferably the temperature should be between 500° C. and 600° C. The coked catalyst generated by the cracking of light streams with low potential for delta coke generation can have the combustion effected at a lower temperature. The regeneration temperature must be at least 40° C. and at most 100° C. higher than the reaction temperature, keeping the catalyst circulation high to maintain the energy balance in the reaction section. The minimum regeneration temperature can be ensured by installing an air preheating furnace before entering the regenerator and passing through the air distributor inside the regenerator. The used catalyst must contain zeolite with pores of intermediate size. Such conditions greatly favor the production of aromatics and the octane rating of the produced naphtha.

A molecular sieve complex contains an oxide of aluminum, an oxide of an alkaline earth metal and a rare earth-modified molecular sieve. The rare earth-modified molecular sieve is a molecular sieve doped by a rare earth element. The percentage of the pore volume occupied by pores of 3 nm or less to the total pore volume in the molecular sieve complex is greater than or equal to 63.5%. The content of the rare earth element and the contents of the oxide of aluminum, the oxide of the alkaline earth metal and the molecular sieve satisfy a certain relationship. The composite material contains a molecular sieve complex and an auxiliary agent loaded on the molecular sieve complex, and the composite material may be applied to flue gas adsorption and desulfurization.

Methods use a catalytic composition built up from a ceramic material including a catalytic material and a first inorganic binder and a second inorganic binder and a catalytic structure made thereof. Preferably, the structure is made by a colloidal ceramic shaping technique. The structure is used for catalytic or ion exchange applications. The catalytic structures have excellent mechanical, physicochemical and catalytic properties.

A method for selectively chemically reducing CO.sub.2 to form CO includes providing a catalyst, and contacting H.sub.2 and CO.sub.2 with the catalyst to chemically reduce CO.sub.2 to form CO. The catalyst includes a metal oxide having a chemical formula of Fe.sub.xCo.sub.yMn(.sub.1-x-y)O.sub.z, in which 0.7≤x≤0.95, 0.01≤y≤0.25, and z is an oxidation coordination number.

The present specification discloses a membrane reactor comprising a reaction region; a permeate region; and a composite membrane disposed at a boundary of the reaction region and the permeate region, wherein the reaction region comprises a bed filled with a catalyst for dehydrogenation reaction, wherein the composite membrane comprises a support layer including a metal with a body-centered-cubic (BCC) crystal structure, and a catalyst layer including a palladium (Pd) or a palladium alloy formed onto the support layer, wherein ammonia (NH.sub.3) is supplied to the reaction region, the ammonia is converted into hydrogen (H.sub.2) by the dehydrogenation reaction in the presence of the catalyst for dehydrogenation reaction, and the hydrogen permeates the composite membrane and is emitted from the membrane reactor through the permeate region.

A process for preparing crystalline boehmite includes combining a stoichiometric amount of flash calcined gibbsite (AI.sub.2O.sub.3) and gibbsite (Al(OH).sub.3) in a pressurizable reaction vessel; heating the flash calcined gibbsite and gibbsite in the reaction vessel to a temperature of about 200° C. to about 280° C. and for a time sufficient to form crystalline boehmite. A crystalline boehmite exhibiting a crystallite from about 600 Å to about 850 Å when measured in the 120 direction of the crystallographic space group Cmcm.