CA2081853C

CA2081853C - Preparation of alkanolamines and use of the reaction product as a motor fuel or lubricant additive

Info

Publication number: CA2081853C
Application number: CA002081853A
Authority: CA
Inventors: Uwe Dingerdissen; Wolfgang Hoelderich; Juergen Mohr; Knut Oppenlaender; Juergen Thomas
Original assignee: BASF SE
Current assignee: BASF SE
Priority date: 1991-10-31
Filing date: 1992-10-30
Publication date: 1998-01-20
Anticipated expiration: 2012-10-30
Also published as: DE4135946A1; EP0539821A2; EP0539821A3; CA2081853A1

Abstract

Alkanolamines prepared from epoxides and amines using solid catalysts are useful as motor fuel and lubricant additives.

Description

c~ q~35 ~O-Z- 0050/~2787 Preparatio~ of alkanolamine~ and use of the reaction product as a motor fuel or lubricant additive The present invention concerns a process for preparing alkanolamines from epoxldes a~d the use of the reaction product as motor fuel and lubricant additive.
The addition of the~e alkanolamines to motor fuels for internal combu~tion engine~ and lubricant~ keep~ valve~
and carburetors clean.
The carburetor and inlet systems of gasoline engines but also fuel injection systems in ga~oline and diesel engines are increasingly subject to contamination due to dust particle~ from the air, unburnt hydrocarbon residues from the combustion space and the crankca~e ventilation gases pas~ed into the carburetor.
The contamination alters the composition of the fuel-air mixtuxe under idling and under low part-load operating conditions in ~uch a way that the mixture ~ecomes richer, combustion becomes less complete and again the proportion of unburnt or incompletely burnt hydrocarbons in the exhaust gases becomes larger and fuel consumption increa~es.
It i9 known that, to avoid theqe di~advantages, fuel additive~ are used for keeping valves and carbure-tors or injection sy~tem~ clean (cf. for example M. Rossenbeck in Katalysatoren, Tenside, Mineraloladdi-tive, ed-~. J. Falbe, U. Hasqerodt, p. ~23, G. Thieme Verlag, Stuttgart, 1978).
Today there are two generation~ of 3uch detergent additiveq, di~tingui~hed by their mode of action but al50 by their preferred ~ite of action.
The first generation of detergent additives could only prevent the formation of deposit~ in the inlet ~y~tem but could not remove deposit~ already pre~ent, wherea~ second generation additives c~n do both, keep clean and clean up, owing to their excellent thermal ~tability, including in particular in high temperature zone~, namely at the inlet valve3.

~r~ 3r3,~

- 2 - O.Z~ 0050/42787 At a molecular level, th~ struc-tural principle on which rnotor fu~l detergents are bas~d can be generalised as the ]inking of polar structures to usually relatively high molecular weight, apolar o~ lipophilic radicals.
Representatives of second generation additives are frequently products based on polyi~obutenes in the apolar part of the molecule. Ad~itives of the polyiso-butylamine type may be mentioned in particular. Polyiso-butylamines are obtained from polyisobutenes in essentially two ways. The first process involves a chlorination of the basic polymeric structure and subse-quent nucleophilic replacement by amino or preferably ammonia. The disadvantage of this method is the use of chlorine and the occurrence of chlorine- or chloride-containing products, which are certainly no longer wanted and should be avoided as far as possible (DE-A-21 29 461, DE-A-22 45 918).
In the ~econd process, a reactive polyisobutene is first carbonylated in an oxo process and then reductively aminated in the presence of ~mmonia (DE-A-36 11 230).
More favorable properties are obtained on using alkanolamines.
DE 40 30 16~, not published prior to the date of filing the present invention, discloses polyisobutyl-aminoalcohols obtained by epoxidation of the correspond-ing polyisobutenes and subsequent reaction with ammonia or amlnes. The synthQ~i~ of the epoxide i~ acco~plished by mean~ of known epoxidating agents (peracetic acid, m-ohloroperbenzoic acid, hydroperoxides).
Under the conditions of the homo~eneous catalysis de~cribed therein it is not entirely possible, in the presence Of ~2~~ to avoid the formation of diols as a result of hydrolysis of the epoxides. Moreover, the yields are not as yet fully satisfactory.
The use of chlorine-cont~; n; ng Lewis acids as homogeneous catalyst as described in DE-A-23 31 290 3r~ ~

- 3 - O.Z. 0050/42787 likewise has appreciable disadvant~ges~ The catalysts have corrosive properties, their workup must take place hydrolytically, and the salts formed theref rom have to be disposed of in an environmentally sound manner. In addi-tion, chlorinated hydrocarbons are formed a~ by-products.
It is an o~ject of the present invention to ma~e available an improved process for preparing alkanolamines in high purity.
We have found, surprisingly, that this object i~
achieved, and that the abovementioned disadvantages are avoided, by a proces~ for preparing alkanolamines of the formula I
Rl-- CH-- CH-- H2 R

l~ where R1 and R2 are each independently of the other hydro~en or an unsub~tituted or aryl-substituted saturated or un-saturated aliphatic radical of from 25 to 350 carbon atoms, with the proviso that at least one o~ the two radicals n' and R2 i9 said alkyl radical and the total numbex of carbon atoms in the radicals R~ and ~2 i~ from 25 to 350, and R3 and R~ are each independently of the other hydrogen or alkyl, hydroxyalkyl, aryl, aralkyl, alkaryl or aminoalkyl radical~ which may be additionally substituted by further hydroxyl- or amino-carrying alkyl radi~als, it being possible for R3 and R4 together to form a heterocyclic ring, which comprises reacting epoxides of the formula II
Rl - CH - CH - R2 II
o whe~e R1 and R2 are each as defined above, with NH3 or ~ ~ L. 35 ~3 - 4 - O.ZO 005~/42787 amines of the formula III

\ III
N-- H
R4~

where R3 and R4 are each a~ defined above, in the presence of solid catalysts.
Preferably, R3 and R4 are each independently of the other hydrogen, Cl-Cl0-alkyl, C5-C10-aryl, C7-C20-aral-kyl, Cl-C8 hydroxyalkyl, C7-C20-alkylaryl or an aminoalkyl radical of the formula IV

~ R5--NR6~ R7 IV
r~
wher~ R5 is C2-C5-alkylene and R6 and R7, which can be identical or dffferent, are each hydrogen, Cl-C6-alkyl, Cb-C10-aryl or Cl-ca-hydroxyalkyl~ and m i~ from 1 to 8, and where R3 and R~ may to~ether form a heterocyclic ring.
By using ~olid (heterogeneous) cat~ly3ts such as zeolites, SiO2 with a zeolite structure, phosphates (including pho~phateq with a zeolite structure), phos-phoric acid and/or boric acid on oxide~ of Al, Si, Ti, Zx, Nb, oxide~ of the elements Fe, Co, Ni, Si, Al, Ti, Zr, Nb, V, Mo, W, Cr or mixture~ thereof it i~ po3sible to prepare the desired alkanolc~nines in an advantageou~
manner.
If the epoxide mixture used ~till contains water in any proportion, then the use of zeolites and pho3-phate3 with a ~eolite structure ha~ an additional advantage. A~ well as acting catalytically they act a~
molecular sieves and can thu~ L~ ve water from the reaction mixture. The formation of additional diols i8 prevented. In thi~ ca~e the cataly~ts therefore al80 act as drier~.
In the alkanolamines of the formula I, Rl and R2 are each for example polymer chain~ of ethene/ propene, isobutene or styrene-butadiene copolymers, depending on 2~ $ ~

- 5 - o.~. 0050/42787 the epoxide II used. The number of carbon atoms in the radicals Rl ~nd R2 will fn each case vary from 25 to 350, preferably from 40 to 200, in particular from 50 to 100.
The total number of carbon atoms in the radicals R1 and R2 is within the range from 25 to 350, prefera~ly from 40 to 200, in particular from 50 to 100, since R1 and R2 may also be hydrogen. R3 and R~ are preferably each, depending on the amine used or if NH3 was used, hydrogen, alkyl radicals of from 1 to 10, in particular of from 1 to 6, carbon atoms (linear, branched, eg. butyl, propyl, i~obutyl), aryl of from 6 to 10 carbon atom~ (eg.
phenyl), aralkyl of from 7 to 20 carbon atoms ~eg.
benzyl), alkylaryl of ~rom 7 to 20, in particular of from 7 to 13, carbon atoms (eg. toluyl), aminoalkyl of the above-indicated formula IV (eg. diethylenetriamine radical, triethylenetetraamineethylene radical, poly-ethylene:imine radical), hydroxyalkyl of from 1 to 8 carbon atoms (eg. ethanol radical, ethanolamine radical, diethanolamine radical, aminoel;hylethanol~mine radical) or cyclic ~mine derivatives (eg. morpholine radical).
The solid catalysts u3ed for the process of the invention are for example zeolites, in particular acidic zeolitic cataly3ts. Zeolite~ are~crystalline aluminosili-cates which po~e~ a highly ordered ~tructure comprising a rigid three~ n~ional network of SiO4 and ~lO~ tetra-hedra joined together ~y common oxygen atoms. The ratio of the Si and A1 atoms to oxygen i8 1: 2 (~ee Ull ~nn~
Encyclopadie d. t~chn. ~hemie, 4th edition, Volume 24, page 575, 1983) a The electrovalence of the aluminum-cont~;n;ng tetrahedra is balanced by the inclu~ion in the crystal of cations, for example an alkali metal or hydro~en ion. Cation exchanqe i9 po~ible. The spaces between the tetrah~dra are occupied by water molecules prior to dehydration by drying or calcination Instead of aluminum ~he zeolite lattice may also contain other elements such a~ B, Ga, Fe, Cr, Ti, V, As, Sb, Bi or Be or mixture~ thereof, or the ~ilicon may be 2~ $~r3~

- 6 - O.Z. 0050/42787 repl~ced by a tetravalent element such a~ Ge~ Ti, Zr or Hf .
According to their structure, zeolites are divided into different groups (see Ullmanns Encyclopadie S d. tech. Chemie, 4th edition, Volume 24, page 575, 1983). For instance, in the mordenite group the zeolite structure is made up of chains and in the chabasite group it is made up of layers of te-trahedra, whereas in the faujasite group the tetrahedra are arranged in the form of polyhedra, for example in the form o~ a cubooctahedron composed of 4- or 6-membered rings. Depending on the manner of linking of the cubooctahedron, which results in voids and pores of different sizes, zeolites are classi-fied as type A, L, X or Y.
Catalysts suitable for the process of the inven-tion are zeolites of the mordenite group or narrow-pored zeolites of the erionite or chabasite type or zeolite of the faujasite type, eg. X-, Y- or L-zeolite3, and also Beta zeolite. This group of zeolite~ also includes the so-called "ultrastable" zeolitles of the faujasite type, ie. dealuminated zeolites. Processes for preparing such zeolites are desc~lbed for example in US Patent 4,512,961.
Of particular advantage are zeoliteQ of the pentasil type (MFI structu3-e; G.T~ Kokotailo and W.M. Meier, Spec. Publ. Chem. Soc. 33 (1980), 133). Their common feature i~ the basic building block comprising a five-membered ring composed of SiO~ tetrahedra. They ar~
characterized by a high SiO2/Al2O3 ratio and al~o by a pcre size between that of the zeolites of type A and those of type X or Y (cf. Ull ~nn~ Encyclopadie d. techn.
Chem., loc. cit.).
These 2eolites can have different chemical compositions. The zeolites in question are aluminum ~ilicate, boron silicate, iron silica~e, beryllium silicate, gallium silicate/ chromium silicate, arsenic silicate, antimony silicate and bismuth silicate zeolites s~
_ 7 . o.z. Q050/42787 or mixtures thereof and also aluminum germanate, boron germanate, gallium germanate and iron germanate ~eolites or mixtures thereof or titanium silicate zeolite~ such as TS-l, ETS 4 and ETS 10.
Of particular suitability for the proce~s of the invention are the aluminum silicate, boron silicate, gallium ~ilicate and iron qilicate zeolites of the pentasil type~
The aluminum silicate zeolike i9 prepared for example from an aluminum compound, preferably Al(0~)3 or Al~(S04)3, and a silicon component, preferably finely divided silicon dioxide, in an aqueous amine ~olution, in particular in polyamines such as 1,6-hexanediamine or 1,3-propanediamine or t~iethylen~tetraamine solution, lS with or i.n particular without the addition of an alkali or alkaline e~rth metal at from 100 to 220~C under autogenous preqsure. Thi3 includes the iqotactic zeoliteq of EP 34 727 and EP 46 504. The aluminoqilicate zeolites ! obtained have an SiO2/Al203 rat:io of from 10 to 40,000 d~pending on the choice of starting m~terials. Such aluminosilicate zeolites can al.so be ~ynthesized in an ethereal medium such as diethyleme glycol dimethyl ether, in an alcoholic medium such as methanol or 1,4-butanediol or in water.
The boro~ilicate zeolite i9 synthesized for example at from 90 to 200~C under autogenous preqsure by r~acting a bo~on compound, eg. H3B03, with a silicon compound, preferably finely divided silicon dîoxide, in an aqueouR amine solution, in particular in 1~6-hexane-~i~mine or 1,3-propane~;~ ;ne or triethylenetetraamine ~olution, with and in particular without the addition of an alkall or alkaline earth metal. Thi~ al30 includes the isotactic zeoliteR of EP 34 727 and EP 46 5040 Such borosilicate zeolite~ can likewi~e he prepared by carry-ing out the reaction not in aqueou~ amine sollltion but in an ethereal solution, for example in diethylene glycol dimethyl ether, or in an alcoholic ~olution, for example 2~
- 8 ~ O.Z. 0050/~2~87 in 1,6-hexanediol.
The gallium ~ilicate zeolite of the penta8il type is synthesized for example at from 90 to 200~C under autogenous p~-essure hy reactinq a gallium compound for ex~mple an alkali metal gallate, preferably sodium gallate, or a gallium oxide or gallium halide or othér suitable gallium ~alts, with the silicon compound, for example alkali metal silicates, silica s015, silicic esters or preferably finely divided silicon dioxide, in an aqueous amine solution, for example primary, secondary or tertiary amines or quaternary alkylammonium compounds, in which case one or more amine functions can ~e pre~ent in the molecule, ~or example in 1,6-diaminohexane 301u-tion or in particular tetrapropylammonium hydroxide solution, with or without the addition of an alkali or alkaline earth metal. The preparation of zeolites in the presence of the~e amine~ i~ described for example in US-A-3 702 886 and DE-B-30 06 471.
~I The iron ~ilicate zeolite is obtained for example ~' 20 from an iron compound, preferab:ly Fe2( S04 ) 3, and a ~ilicon compound, preferably finely divided silicon oxide, in an aqueous amine ~olution, in particular 1,6-hexanediamine, with or without the addition of an alkali or alkaline earth metal at from 100 to 220~C under autogenous pres~ure.
The usable high-~ilicon 2eolites ( SiO2/A1203 2 10 ) al~o include the so-called ~SM type~, zeolite Beta, ferrierite, ~U-1, NU-l and sio~ with a zeolite tructure (~ilicalite, a molecular ~ieve, a ~o called ~ilica polymorph), ie. 5iO2 pha~e~ with a pentasil structure whose parameter~ and a process for the preparation thereof are de~cribe~ for example in US 4 061 724 and al~o in EP-A-64 37~, EP-A~93 476 and EP-A-123 060.
The process of the invention can also be carried out with so-called ultrastable zeolite~, for example of the faujasite type or mordenite typeJ ie. dealuminated Y-zeolite.~ or dealuminated mordenitel the preparation ~ r? ~ ~ r-- - g - o.z.~5d~ 7 thereof is described for example in US-A-4 S12 961 and also in H.~. Beyer and s. selenykajy~ Stud. Surf. sc.
Catal. 5 (lg80) 203-209 and also in I.M. Newsam, science, ~31 (1986), 1094.
SIt is similarly po~sible to use titanium sili-cates with a pentasil ~tructure, for example TS-1, described for example by B. Kraushaar and I.H.C. von Haaff in Catalysis Letters 1 (1988), 81-89.
Similarly, the ETS molecular sieves such as ETS-4 and 10ETS-10 (US-A-4 853 202) can be used.
The preparation of the zeolite BETA i~ effected according to US 4 391 4sa, ~pecifically according to Examples 1 and 2 thereof.
The resulting aluminum silicate, gallium sili-15cate, boron silicate, titanium silicate and iron silicate zeolites or silicalites, after they have been isolated, dried at f~om 100 to 160~C, preferably at 110~C, and calcined at from 450 to 550~C, preferably at 500~C, can be molded with a binder in a ratio of from 90:10 to 2040:60% by weight into extrudates or tablet~. Suitable binders are various aluminum oxides, preferably ~oehmite, amorphous aluminum silicate~ having an SiO2/Al203 ratio of from 25:75 to 95:5, preferably 75:25, silicon dioxide, preferably finely divided Al2O3, Tio2, ZrO2 and also clay.
25After molding, the extrudates or pellets are dried at 110~C over 16 h and calcined at 500~C for 16 h.
Advantageous cataly~t~ are also obtained on molding the isolated zeolite~ such as the aluminum silicate zeolite and the boron silicate zeolite directly 30after drying and not subjecting it to a calcination until after molding. For instance, the a~-prepared aluminosili-cata and borosilicate zeolites can al~o be u~ed in the pure form, without binder, a~ extrudate~ or tablet~ t in which case the extru~ion or peptization aids used being 35for example ethylcellulo~e, ~tearic acid, potato starch, fo~mic acid, oxalic acid, acetic acid, nitric acid, ammonia, amines, silicoe~ter~ and graphite or mixtures 2~ J~
- lO - O.Z. 0050/42787 thereof.
If the zeolite, on account of it~ manner of preparation, is present not in the acidic H-form but, for example in the Na-form, it can be completely or partially S converted into the desired H-form by ion exchange, for example with ammonium ion~, and sub-~equent calcination, or by treatment with acids.
Should the zeolitic catalyst used according to the invention undergo deactivation due to coking, it is advisable to regenerate the zeolite by burning off the coke deposi-t with air or with an air-N2 mixture at from 400 to 550~C, preferably at 500~C. Thi~ re~tores the initial activity level of the zeolite.
By partial precoking it is possible to optimize the selectivity of the catalyst in respect of the desired reaction product.
To obtain the higheRt possible selectivity, a high conversion and al~o long times on stream, it is q advantageous to modify the zeolites. A ~uitable method o~
modifying the catalys-ts comprises for example doping the molded or unmolded zeolite with metal salts by ion exchange or impregnation. The metal~ u~ed are alkali metals such as Li, C~ or K, alkaline earth metals such as Mg, Ca or Sr, metals o~ main groups 3, 4 and 5 such as Al, Ga, Ge, Sn~ Pb or Bi, trans:ition metals of ~ubgroup~
1 ~ 8 comprising Ti, Zr, V, Nb, Cr, Mo, W, Mn, Re, Fe, Ru, O~, Co, Rh, Sx, Ni, Pd and Pt, or transition metals Ruch as La, Ce, Pr, Nd, Fr, Yb and U.
Advantageously, the doping i-~ carried out by introducing for example the molded zeolite into a riser pipe and pa~sLng an aqueou~ or ammoniacal solution of a halide or nitrate of one of the ab~v~ -ntioned metal~
through it at from 20 to 100~C. Such an ion exchange can take place for example with the hydrogen r an~onium or alkali metal form of the zeolite. Another way of applying metal to the zeolite compri~e~ impregnating the zeolitic material with, for example, a halide, nitrate or oxide of r~
~ ll - O.Z. 0050/42787 one of the abovementioned metals in aqueou~, alcoholic or ammoniacal solution. sOth ion exchange and impregnation ~re followed by ~ least a drying operation, alterna-tively by another calcination.
A possible embodiment compri~es for example clissolvinq Cu(NO3)2 x 3 ~2~ or Ni(NO3)z x 6 H2O or Ce(NO3)3 x 6 H2O or La(NO3)2 x 6 ~2~ or Cs2CO3 in water and impreg-nating the molded or unmolded zeolite with the solution for a certain period, for example 30 minute~. Any super-natant solution is stripped of water in a rotary evapora-tor. The impregnated zeolite is then dried at about 150~C
and calcined at about 550~C. This impregna-ting ~tep can be carried out several times in succession until the desired metal content is obtained.
It is also possible to prepare, for ~xample, an aqueous Ni(NO3)2 solution or an ammoniacal Pd(NO3)2 solu-tion and to suspend the pure ~ulverulent zeolite therein at from 40 to 100~C by ~tirring for about 24 hours. After filtration, drying at about 150~C and calcination at about 500~C, the zeolitic material thus obtained can be further processed with or withlout binders into extru-dates, pellet~ or fluidizable material.
An ion exchange on the zeolite pre~ent in the H-form or ammonium form or allcali metal form can be carxied out by introducin~ the zeolite in extruded or pellet fonm into a column and for example pa~ing an aqueous Ni(NO3)2 ~olution or an ammoniacal Pd(NO3)2 ~olu-tion through it at from 30 to 80~C in a recycle loop for from 15 to 20 hour~. This i~ followed by washing out with water, drying at about 150~C and calcination at about 550~C. With some metal-doped zeolite~, for example Pd-, Cu- or Ni-doped zeolite~ an aftertreatment with hydrogen i8 advantageou~.
A further method of modifying the zeolite com-prise~ treating the zeolitic material, which may be in molded or unmolded form, with an acid ~uch a~ hydro chloric acid, hydrofluoric acid or phosphoric acid and/or s~ 3r~
- 12 - O.Z. 0050t42787 steam, advantageously, for example, by treating the zeolite in pulverulent form with 1 N phosphoric acid at 80~C for l hour and then washing with water, drying at 110~C for 16 hours and ~alcining at 500~C for 20 hours.
S Alternatively, before or a~ter being molded together with the binder, the zeolite is treated for examplP at from 60 to 80~C with from 3 to 25% by weigh-t, in particular from 12 to 20% by weight, aqueous hydro~hloric acid for from 1 to 3 hours. A~terwards, the zeolite thus treated is washed with water, dried and calcined at ~rom 400~C to 500~C.
In a special embodiment, the acid treatment comprises treating the zeolitic material, before it is molded, with hydrofluoric acid, generally in the fo~m of from 0.001 N to 2 N, preferably from 0.05 N to 0.5 N, hydrofluoric acid, at elevated temperatures, for example by heating under re~lux for, in general, from 0.5 to 5, preferably from 1 to 3, hours. After the zeolitic mater-ial has ~een isolated, for example by filtering and washing, it is advantageously dried, for example at from 100 to 160~C, and calcined, in general at from 450~C to 600~C. In a further preferred form of the acid treatment, the zeolitic material, a~ter it has been molded tog~ther with a binder, i8 treated at elevated temperatures, advantageously at from 50 to ~O'IC, preferably at from 60 to 80~C, for from O.S to 5 hours with, preferably, from 12 to 20~ by weight of hydrochloric acid. The zeolitic material is, in general, sub~equently washed, expediently dri.ed at from 100 to 160~C and calcined at, in general, from 450 to 600~C. An ~F treatment may also be followed by an ~Cl treatment.
Alternatively zeolites can be modified by appli-cation of pho~phoru~ compounds, such a~ trimethyl phos-phate, trimethylphosphine or primary, secondary or tertiary sodium phosphate. Of particular advantage is the treatment with primary sodium phosphate. It comprises impregnating the zeolite~ in extrudate, tablet or - 13 - O.Z. 0050/~2787 fluidizable form with an aqueous NaH2P04 solution, drying at 110~C and calcining ~t 500~C.
Further catalysts for the process of the inven-tion are phosphates, in particul~r aluminum phosphate, S silicon ~luminum phosphates, cerium phosphate, zirconium phospha-tes, boron phosphate, iron phosphate or mixtures thereof.
The ~luminum phosphate and silicon aluminum phosphate catalysts used for the process of the invention are in particular hydrothermally ~ynthesized substituted and unsubstituted aluminum phosphates and silicon alumin~lm phosphates.
The aluminum phosphate catalysts, structurally related to the zeolites, are synthesized for the process of the invention in particular un~er hydrothermal condi-tions. They are silicon aluminum phosphates (SAPOs) or aluminum phosphates (AlP04). The~e crystalline solids have defined void and pore ~tructures and are structurally related to the zeolites.
The preparation, properties and classification of these solids on the basis of structure and chemical composition are described in cletail in Pure and App.
Chem. 58 (1986), 1317-22, 1351-58.
The cry~tal structure~ known to date and the numerous elemental modification~ now make up some 700 different combinations. The aluminopho~phate9 are desig-nated by the ~ollowing acronyms: AlP04, SAP0, MeAP0, MeAPS0, ElAP0 or ElAPS0. Here A or Al i8 ~luminum, S is silicon, P is phosphorus and 0 i9 oxygen. Me is a metal from Fe, Mg, Mn, Co and Zn and E1 denotes elements ~uch as Be, Ga, Ge, Ti, As, B or Li. A hyphenated num~rical ~uffix denotes the cry~tal ~tructure of the phase in que~tio~.
The hydrothermally synthesized alumlnum phos-phates are for example AlP0-5, AlP0-9, AlP0-11, AlP0 12, AlP0-14, AlP0-21, AlP0-25, AlP0-31, AlP0-33, AlP0-34, AlP0-37 and AlP0-54. Syntheses of these compounds are Z ~ $ 'L . ~
- 14 - O.Z. 0050/~2787 de~cribed in EP 132 709, US 4 310 440 and US 4 473 663.
For instance, AlPO~-S (APO-5) is synthesized by homogeneously mixing orthophosphoric acid with pseudo-boehmite (Catapal ss~) in wat~r, adding tetrapropyl-ammonium hydroxide and reactinq at about 150~C under autogenous pressure in an autoclave for from 20 to 60 h.
The AlPO4 i~ filtered off, dried at from 100 to 160~C and calcined at from 450 to 550~C.
AlPO4-9 (APO-9) is likewise synthesized from 1 n orthophosphoric acid and pseudoboehmite, but in aqueou~
DABCO solution (1,4-diazabicyclo[2.2.2]octane) at about 200~C under autogenous pressure for from 200 to ~00 h.
The synthesis of AlPO4~21 (AP0-21) take~ place from orthophosphoric acid and pseudoboehmite in aqueous pyrrolidone solution at from 150 to 200~C under autogen-ous pres~ure for from 50 to 200 h.
Synthese3 for MeAPOs are described in US-A-4 544 143, EP-A-132 70~ and US-A-4 567 029 and for ElAPO in US-A-4 500 651 and EP-A-2 158 976.
Preference for the proces~ of the invention is given in particular to the silicon-containing alumino-phosphateR (SAPO, MeAPSO or E~lAPSO) such a~ SAPO-ll, SAP0-5, SAP0-20, SAPO-34, SAPO-37, SAPO-41 or SAPO-46~
Synthe~es of silicon aluminopho~phates are described inter alia for SAPO in US-A 4 440 871 and EP-A-103 117, for MeAPSO in ~P-A-158 348, EP-A-158 975 and EP-A-161 491, and for ElAPSO in EP-A-159 624.
SAP08 are prepared by cry~tallization from aqueous mixture at from 100 to 250~C under autogenous pressure in the course of from 2 h to 2 weeks, the reaction mixture comprising a silicon, an aluminum and a pho~phoru~ component being reacted in aqueous organoamine solution~ .
Suitable silicon aluminum phosphates are for example ZYT-5, ZYT-6, ZYT-7, ZYT-9, ZYT-11 and ZYT-12 (J 5 9217-619).
SAP0-5 i~ o~tained for example by mixing SiO

- 15 - O. ~ . OQSO/42787 suspended in aqueou~ tetrapropylammonium hydroxide solution with an aqueous ~u~pension of pseudohoe~mite and orthophosphoric acid and subsequent reaction at from 150 ! to 200~C for from 20 to 200 h under autogenous pressure - 5 in a stirred autoclave. The powder i8 filtered off, dried at from 110 to 160~C and calcined at from 450 to 550~C.
As phosphate cataly~ts it is also pos~ible to use in the process precipitated al~minum phosphate~. Such an aluminum phosphate i~ prepared for exampls by dissolving 92 g of diammonium hydrogenphosphate in 700 ml of water.
To this solution are added 260 g of Al(NO3)3 x H20 in 700 mi of water dropwise over 2 h. At the same time the pH is maintained at 8 by the simultaneous addition of 25%
streng-th NH3 solution. The resulting precipitate is subsequently stirred for 12 h, and then filtered o~f with suction and washed. It is dried at 60~C for 16 h.
~oron pho~phates for the proce~s of the invention can be prepared ~or example by mixing and kneading concentrated boric acid and phosphoric acid and subse-; 20 quent drying and calcination of the mixture in an inert gas, air or steam atmosphere at from 250 to 650~C, preferably at from 300 to 500~C.
CePO4 is obtained by precipitation of 5Z g of Ce~NO3)3 x 6 H20 and 56 g o~ NaH2]?0~ x 6 ~2~- After filtra-tion, the material i3 extruded, dried at 120~C and calcined at 450~C. The catalyst contains 47.1% by weight of Ce and 12.7~ by weight of P.
Suitable zirconium phosphates are commercially available zirconium pho~phates, for example CSZ 100, zirconium phosphate ~ilicates and zirconium phosphates which will adsorb or have ad~orbed N~3.
Phosphoric a~id is applied for example to SiO2, AlqO3r Tio2, ZrO2, Nb205 or pumice carrier~ by Lmpregnating or spraying. A phosphoric acid-contA;ning catalyst can be obtain~d for example by impregnating SiOz with ~3PO4 or NaH2~PO4 or NazHPO4 solution and ~ubsequent drying or calcination. However, phosphoric acid can also be sprayed 2.~ ..$ ~.'3 - 16 - O.z. 0050/427~7 tog~ther with silica gel in-to a prill tower, followed by drying ~nd usually a calcination~ Pho~phoric acid c~n also be sprayed onto the carrier material in an imprey-nating mill.
Suitable untreated catalysts also include for example metal oxides, in particular acidic oxide~ of the elements Ti, Zr, Si, Al, Fe, Co, Ni, V, W, Mo, Nb and Cr.
They are titanium dioxide, zirconium dioxide, vanadium oxides, niobium oxide~, chromium oxide~, molybdenum oxides, tungsten oxides, etc. or mixtures thereof. Using these catalysts the process of the invention will like-wise give the desired products.
The catalysts described herein are alternatively usable in the form of from 2 to 4 mm extrudates or as tablets from 3 to 5 mm in diameter or as chips having particle sizes of from 0.1 to 0.5 mm, or in a fluidizable form. As solid catalysts they have the additional advan-tage of being simple to separate from the reaction mixture Eor reu3e.
The preferred polyisobutenes used have a mole-cular weight of about 400 - 5000, preferably of from 800 to lS00. They are obtained in a conventional manner by cationic polymer.ization of isobutene.
The epoxide~ II are prepared by mean~ of known epoxidating agents (see DE 40 30 164~.
The reaction temperatures for the process of the invention are in general from ~0~C to 600~C, preferably from 50 to 500~C, in particular from 100 to 350~C.
The reaction timas can range from 30 min to 100 hourq~
It is preferred to car~y out the reaction in the li~uid pha~e~ in particular by the suspension, downward-flow or upward-flow proceduxe, at from 50 to 300~C, preferably at from 100 to ~50~C, under a weight hourly space velocity (W~SV) of from 100 h-~ to 0.5 h-1, prefer-ably of from 60 h-' to 10 h-1.
Usable sol~ents are in general inert solvents, - 17 - O. Z . 0050/427~3~
for example cyclohexane, toluene or petroleum e-ther. The reaction autoclave i~ made for example of noncorrodable stainless steel. The amount of catalyst used is in general from 0.01 to 20% by weiqht, based on the epoxide used.
Th~ proces~ i~ in general carried out at atmos-pheric pressure or under superatmospheric pressure, ie.
at from 1 to 800 bar, preferably at from 50 to 500 bar, in particular at from 150 to 350 bar. It can be carried out sontinuously or batchwise.
Sparingly volatile or ~olid starting material~
are u~ed in dissolved form, for example in THF, toluene, cyclohexane or petroleum ether solutionO Generally, dilution of the starting mixture with such ~olvents or with an inert gas such as N2 or Ar is possible.
The invention will now be more particularly described by way of example~
Preparation of alkanolamines ~XAMPLES 1 TO 2 5 The reaction~ were carried out in the liquid phase in an HC autoclave (300 ml) under isothermal conditions. In detail the procedure adopted was a~
follows. 1 part by volume (50 g~ of polyisobutene epoxide (molecular weight about 1000) was di~solved in 50 ml of cyclohexane at room temperature and 1 g of solid ca-talyst (see Table I) waB added; then the amount of NH3 shown in Table I was injected and the reaction mixture was raised to the temperature shown in Table I under autogenous condition~. The autogenou~ pressure~ and al~o the reac-tion times and yields of al~anolamines (GlA~I are also shown in Table I. The reaction products were charac-terized by dete ; n; ~q the usual numbers (hydrogenation iodine number in accordance with DIN 53 241 Part 2 or Ind. Chim. Belge 32 l1967), 134; amine number in accor-dance with DIN 16 945 or DAB9 (see also ASTM D 2073-66);
epoxides in accordance with DIN 16 945 or DAB9, cf~ also Hofmann and Stark: The Determination of ~poxide ~roups, ~' ~ ~L ~3r3~3 - 18 - O.Z. 0050/427~7 Per~c~non Press, Oxford, London, 1969; hydroxyl number in accordanc~ with DIN 16 945 or DAB9, see also DIN 53 240 or AST~I D 2849-69).
TA~3LE I
S
Examples 1-25 Run Cat. Ratio Temp. Pres- Time Yield No. epoxide/ [~t'] ~ure ~h~ [%]
NH3 [bar~ Gl~A based on epoxide 2 A 1~4 200 300 60 76 4 s 1/2 50 20 20 31 s 1/2 100 56 20 31 6 s 1/2 150 110 20 35 7 s 1/2 200 155 20 52 C 1~2 200 155 20 53 13 ~ 1/2 50 15 20 21 14 E 1/4 200 2-l0 60 59 F 1/2 50 lt) 20 25 19 ~ 1/6 200 5~14 60 59 24 J 1/4 ~00 238 80 57 - O. z . ooso/a~27~7 The reactions were carrfed out in the liquid pha~e under iF~othermal conditions in a stirred kettle ( 250 ml ) as describ~d in Example~ 1-25 . The reaction 5 products were ch~r~cteri2ed by determining the number~
m~ntioned. The starting material~ are polyisobutene epoxide (molecular weight about 1000) and morpholine, which are reacted to give the corresponding alcohol amine (GlAAm) (see Table II).
TABLE II
Run Cat. Ratio T~mp. Pres- Time Yield No. epoxideJ [~CJ sure [ h~ [%]
morpholine [barJ GlAAm*
26 A 1/4 102 1 10 14.4 27 A 1/4 102 1 60 57.2 28 A 1/4 102 1 72 71.5 * ba~ed on epoxide used The catalysts used in the Examples were prepared as follows:
Catalvst A
An alum:inosilicate zeolite of the pe.ntasil type was prepared from 65 g o~ finely divided SiOz and 203 9 of Al2(SO~)3 x 18 ~2~ in 10 kg of an aqueou~ 1,6-hexane-diamine solution (mixture 50:51J% by weight) in a stirred autoclave under hydrothermal condition3 at 150~C and autogenou~ pressure. After the crystalline reaction pro~uct had been filtered off and washed, it wa~ dried at 110~C for 24 h and calcined at 500~C for 24 h. Thi~
aluminosilicate zeolite contained 92.8~ by weight of SiO2 and 4O2% by weight of Al2O3. This material i~ molded with a molding aid into 2-mm extrudat~s, which are dried at 110~C fox 16 h and calcined at 500~C for 24 h.
Catalyst B
Catalyst ~ was prepared by molding a commercial Na-Y ~eolite into 2-mm extrudates which were dried at - ~0 - O.Z. 0050/~787 110~C for 16 h and calcined at 500~C for 16 h.
The extrudates were ion exchanged at 80~C with 20% stren~th NH4Cl solution (mass ratio 1:15). This was followed by wa hing until chloride-free, drying at 110~C
and a 5 h calcination at 500~C. The Na content was 0.07~O.
Catalyst C
Catalyst C wa~ prepared by molding a commercial Na-Y zeolite in powder form with pyrogenic silica (weight ratio 80:20~ into 2-mm extrudate~, which were driPd at 110~C for 16 h and calcined at 500~C for 16 h.
The extrudates were ion exchanged at 80~C with 20% strength NH4Cl solution (mass ratio 1:15). This wa~
followed by washing until chloride-free, drying at 110~C
and a 5 h calcination at 500~C. The Na content was 0.07%.
Catalyst D
Catalyct D wa~ prepared by molding pseudoboehmite with 2% ~f HCOO~ into 2-mm extrudate~, which were dried at 110~C for 16 h and calcined at 500~C for 16 h.
Catal~st E
Commercial Tio2 (from Degussa) Catalyst F
Commercial ZrO2 ~from Mel) Catalvst G
~-A12O3 (BASF catalyst K 10) Catal~st H
Cataly~t H was obtained by treating the extrud-ates of ca-talyst A with 0.1 N ~F for 1 h, filtering, wa~hing neutral, drying at 130~C' for 2 h and calcining at 540~C for 2 h~
Cakalyst I
Catalyst I wa~ prepared by molding catalyst A
with pyrogenic silica ~weight ratio 80:20) into 2-mm extrudates which were dried at 110~C for 16 h and calcined at 500~C ~or 16 h.
The extrudates were ion exchanged at 80~C with 20% strength NH4Cl ~olution (mass ratio 1:15~. This was ~ollowed hy washing until chloride-free, drying at 110~C

2~ 3~3 i - 21 ~ O. ~ . 0050/~2787 and a 5 h c~lcination at 500~C.
Cataly~-t J
Commercial ZSM-5 zeolite (CBM 3020, from Cont:eka ) .
Catalyst K
Cataly3t K wa~ prepared by moldin~ catalyst ~
with pyrogenic silica into 2-mm extrudates which were dried at 110~C for 16 h and calcined at 500~C for 16 h.
The extrudates were ion exchanged at 80~C with 20% strength NH4Cl ~olution (ma~ ratio 1~ his was followed ~y washing until chloride-free, drying at 110~C
and a 5 h calcinaticn at 500~C.
Appllcation testinq The respective additive was added to the motor . uel in a proportion of 800 ppm. The test was carried out on two valve~ at a time of an Opel Kadett engine in accordance with the CEC-F-02-T~79 standard. The additive quality was as3e~sed by weighing the valve tappets. The weight increase corre~pond6 to the amount of coke deposi-B 20 ted at the valve inlet. The re~ultq are ~hown in Table III.
TABLE III

Weight increase (mg) Valve l Valve 2 Untreated fuel 440 564 Additive of run 3 86 15 Additive of run 1 35 15 Additive of run 18 13 35

Claims

1. A process for preparing alkanolamines of the formula I

I

where R1 and R2 are each independently of the other hydrogen or an unsubstituted or aryl-substituted saturated or un-saturated aliphatic radical of from 25 to 350 carbon atoms, with the proviso that at least one of the two radicals R1 and R2 is said alkyl radical and the total number of carbon atoms in the radicals R1 and R2 is from 25 to 350, and R3 and R4 are each independently of the other hydrogen or alkyl, hydroxyalkyl, aryl, aralkyl, alkaryl or aminoalkyl radicals which may be additionally substituted by further hydroxyl- or amino-carrying alkyl radicals, it being possible for R3 and R4 together to form a heterocyclic ring, which comprises reacting epoxides of the formula II

where R1 and R2 are each as defined above, with NH3 or amines of the formula III

III

where R3 and R4 are each as defined above, in the presence of solid catalysts.

2. A process as claimed in claim 1, wherein the catalysts used are zeolites, SiO2 with a zeolite structure, phosphates, phosphoric acid and/or boric acid on oxides of Al, Si, Ti, Zr, Nb, oxides of the elements Fe, Co, Ni, Si, Al, Ti, Zr, Nb, V, Mo, W, Cr or mixtures thereof.

3. A process as claimed in claim 1, wherein R3 and R4 are each independently of the other: hydrogen, C1-C10-alkyl, C6-C10-aryl, C7-C20-aralkyl, C1-C8-hydroxyalkyl, C7-C20-alkylaryl or an aminoalkyl radical of the formula IV
IV

where R5 is C2-C5-alkylene and R6 and R7, which can be identical or different, are each hydrogen, C1-C6-alkyl, C6-C10-aryl or C1-C8-hydroxyalkyl, and m is from 1 to 8, and where R3 and R4 may together form a heterocyclic ring.

4. A process as claimed in claim 1, wherein the starting epoxide (II) is polyisobutyl epoxide.

5. A process as claimed in claim 2, wherein the solid catalysts used are zeolites of the pentasil type.

6. A process as claimed in claim 2, wherein the solid catalysts used have been doped with transition metals, alkaline earth metals and alkali metals.

7. A process as claimed in claim 2, wherein acid-treated solid catalysts are used.

8. A process as claimed in claim 1, wherein the reaction is carried out at from 20°C to 600°C and at 1-800 bar, in particular in the liquid phase.

9. Use of the reaction mixture prepared by the process of claim 1 and separated from the solid catalyst as a motor fuel or lubricant additive.

10. Use as claimed in claim 9, wherein the reaction mixture, if necessary after removal of solvents, is added as additive to the motor fuel in an amount of 10-5000 ppm or to the lubricant in an amount of from 0.6 to 6% by weight.