U.S. patent application number 14/668235 was filed with the patent office on 2016-01-14 for catalytic dehydration of alcohols using phase pure, calcined single- and multi-site heterogeneous catalysts.
This patent application is currently assigned to SIGNA CHEMISTRY, INC.. The applicant listed for this patent is SIGNA CHEMISTRY, INC.. Invention is credited to Michael LEFENFELD, Alexander James PATERSON, Matthew Edward POTTER, Robert RAJA.
Application Number | 20160008798 14/668235 |
Document ID | / |
Family ID | 42356413 |
Filed Date | 2016-01-14 |
United States Patent
Application |
20160008798 |
Kind Code |
A1 |
LEFENFELD; Michael ; et
al. |
January 14, 2016 |
CATALYTIC DEHYDRATION OF ALCOHOLS USING PHASE PURE, CALCINED
SINGLE- AND MULTI-SITE HETEROGENEOUS CATALYSTS
Abstract
The disclosure describes a new class of isomorphously
metal-substituted aluminophosphate materials with high phase purity
that are capable of performing selective Bronsted acid catalyzed
chemical transformations, such as transforming alcohols to olefins,
with high conversions and selectivities using mild conditions.
Isomorphous substitutions of functional metal ions for both the
aluminum ions and the phosphorous ions were successful in various
AlPO structures, along with multiple metal substitutions into a
single aluminum site and/or a phosphorous site. This invention can
be used towards the catalytic conversion of hydroxylated compounds
of linear and/or branched moiety with the possibility of being
substituted to their respective hydrocarbon products, preferably
light olefins containing 2 to 10 carbon atoms, among other
chemistries.
Inventors: |
LEFENFELD; Michael; (New
York, NY) ; RAJA; Robert; (Hampshire, GB) ;
PATERSON; Alexander James; (Perth, GB) ; POTTER;
Matthew Edward; (Southampton, GB) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
SIGNA CHEMISTRY, INC. |
New York |
NY |
US |
|
|
Assignee: |
SIGNA CHEMISTRY, INC.
New York
NY
|
Family ID: |
42356413 |
Appl. No.: |
14/668235 |
Filed: |
March 25, 2015 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
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14275042 |
May 12, 2014 |
9012709 |
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14668235 |
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12692561 |
Jan 22, 2010 |
8759599 |
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14275042 |
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61146844 |
Jan 23, 2009 |
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Current U.S.
Class: |
423/704 |
Current CPC
Class: |
C07C 1/24 20130101; C07C
1/24 20130101; C01B 37/065 20130101; C07C 1/24 20130101; B01J 29/84
20130101; C01B 39/54 20130101; Y02P 20/52 20151101; C07C 1/24
20130101; C07C 11/06 20130101; C07C 11/04 20130101; C07C 15/46
20130101; B01J 35/1057 20130101; C07C 11/09 20130101; B01J 29/85
20130101; C07C 2529/84 20130101; C01B 37/08 20130101; C07C 1/24
20130101; C07C 2529/85 20130101 |
International
Class: |
B01J 29/84 20060101
B01J029/84; C01B 39/54 20060101 C01B039/54 |
Claims
1. A process for preparing a substantially phase pure, calcined
metal-substituted aluminophosphate, AlPO, wherein at least one
aluminum (Al.sup.III) site is substituted by a divalent metal ion
(M.sup.II) and/or at least one phosphorous (P.sup.V) site is
substituted by a tetravalent metal ion (M.sup.IV) comprising the
steps of: slowly heating an isomorphously, metal-substituted
aluminophosphate catalyst product containing a structure directing
agent within its crystalline structure under a flowing inert gas at
a calcination temperature ranging between about 200.degree. C. and
about 1000.degree. C., holding the isomorphously, metal-substituted
aluminophosphate catalyst product under the flowing inert gas at
the calcination temperature, calcining the isomorphously,
metal-substituted aluminophosphate catalyst product for a time of
at least about 3 to about 24 hours to form a substantially phase
pure, calcined metal-substituted aluminophosphate, and slowly
cooling the substantially phase pure, calcined metal-substituted
aluminophosphate to room temperature.
Description
CROSS-REFERENCE TO RELATED APPLICATIONS
[0001] This application claims priority to U.S. Provisional
Application 61/146,844, filed Jan. 23, 2009, and to U.S. patent
application Ser. No. 12/692,561, filed Jan. 22, 2010, and to U.S.
patent application Ser. No. 14/275,042, filed May 12, 2014, all of
which are incorporated herein by reference in their entirety.
FIELD OF THE INVENTION
[0002] This invention relates to new aluminophosphate (AlPO or
AlPO.sub.4) catalysts with isomorphous substitutions for the
aluminum (Al.sup.III) and/or the phosphorus (P.sup.V) ions to form
strong Bronsted acid sites within a single catalyst. Also, multiple
metal ion isomorphous substitutions can be made for both the
aluminum (Al.sup.III) and the phosphorus (P.sup.V) ions in the same
instance--generating no fewer than two different acid sites. The
catalysts can be used in acid-catalyzed reactions, such as the
dehydration of numerous oxygenated compounds to form their
respective olefin.
BACKGROUND OF THE INVENTION
[0003] Olefins and their substituted counterparts (defined herein
as, but not limited to, ethylene, propylene, butenes, and mixtures
thereof) serve as feedstocks for the production of numerous
chemicals and polymers. For example, ethylene is one of the largest
volume chemical intermediates in the world, being used as a raw
material in the production of, for example, polyethylene,
ethylbenzene-styrene, ethylene dichloride, ethylene oxide and
ethylene glycol. Most olefins are commercially produced by the
thermal or catalytic cracking of saturated hydrocarbons found in
petroleum and naphtha (See M. Ladisch et al., Science (1979) 205,
898). Due to the thermodynamic limitations of the reaction, thermal
cracking reactors operate at temperatures as high as 1,100.degree.
C. to maintain the desired levels of conversion--typical yields are
between 50 and 100% (See U.S. Patent Applications and Patents:
2006/0149109; U.S. Pat. Nos. 4,351,732; 4,556,460; 4,423,270; and
4,134,926). Information on production of ethylene by thermal
cracking is available in Kirk Othmer Encyclopedia of Chemical
Technology, 5.sup.th ed. Wiley (2004-2007) and Ullmann's
Encyclopedia of Industrial Chemistry, 6.sup.th ed. Wiley (2003),
both hereby incorporated by reference.
[0004] Finding new, more efficient, and environmentally friendly
pathways to produce olefins from renewable starting materials that
are not encumbered by the varying costs and tightening supply of
crude petroleum has been a challenging research area of the past
decade (See U.S. Patent Applications and Patents: 2006/0149109;
U.S. Pat. Nos. 4,351,732; 4,556,460; 4,423,270; and 4,134,926).
Catalytic oxidative dehydration of ethane was proposed as an
alternative method to produce ethylene at much lower temperatures,
but the yields and selectivity achieved to date have not been
encouraging (See S. Golay et al., Chem. Eng. Sci. (1999) 54,
3593).
[0005] Dehydration of oxygenates are conventionally carried out
using either concentrated sulfuric acid or concentrated phosphoric
acid, H.sub.3PO.sub.4. The mechanistic details for the dehydration
reaction can be summarized in Scheme 1 (below). The alcohol is
first protonated, followed by a loss of water to give a carbocation
(carbonium ion), which results in the subsequent abstraction of a
hydrogen ion from the carbocation. Apart from the acid's corrosive
nature, as a side reaction, the acid can oxidize the alcohol into
polluting carbon dioxide. Also, in the case of concentrated
H.sub.2SO.sub.4, large quantities of sulfur dioxide can be
produced. Both of these gases have to be removed from the product
olefin before it can be used in a later chemical process.
##STR00001##
[0006] Silicoaluminophosphates (SAPOs), such as SAPO-34 and its
analogues, possess strong Bronsted acid sites and are excellent
shape-selective catalysts for the conversion of methanol and other
alcohols to light olefins (See U.S. Pat. Nos. 4,499,327; 5,952,538;
6,046,673; 6,334,994; and 7,199,277; as well as WO 1993/024430).
However, SAPOs are composed of Si atoms tetrahedrally coordinated
to oxygen atoms making an integral part of the overall catalyst
framework. SAPO-34 is being commercially exploited (by UOP) for the
selective conversion of methanol to low-molecular weight olefins
(See WO 2007/032899). Further, the Bronsted acidity of a SAPO
varies greatly depending on its particular structure type and
architecture.
[0007] To vary the intensity and number of Bronsted acid sites in
aluminophosphates (AlPOs), one can isomorphously introduce ions to
replace a portion of the Al.sup.III ions with a single type of
divalent metal ion, such as Zn, Mg, Mn, Co, Ni, Cu, and Fe, among
others. In other words, a fraction of the
.ident.Al.sup.III--O--P.sup.V.ident. linkages is replaced by
.ident.M.sup.II--O(H)--P.sup.V.ident., the proton that is loosely
attached to the bridging oxygen being the locus of the Bronsted
acid center. The properties of the resulting Bronsted acid center
can be controlled by the appropriate choice of structure-directing
agents, transition-metal precursor, or gel composition, leading to
a wide range of solid-acid catalysts. However, by substituting only
the Al.sup.III ion or the P.sup.V ion in the framework, only
partial tuning of the acid strength occurs. See, for example,
EP0141662A2. Yet, phase purity must also be accomplished to get
significant selectivity towards the desired product of the
reaction.
[0008] Olefins, particularly light olefins, are the most desirable
products from oxygenate conversion and crude petroleum cracking. A
need exists to improve the performance of ethylene plants. To this
end, a number of catalytically mediated processes have been
proposed. The most chemically straightforward among these is
ethanol dehydration. This invention meets that need and provides
the full tuning of the AlPO acid strength via controlled,
judicious, and simultaneous substitution of both the Al.sup.III and
P.sup.V ions combined with substantial phase purity of the calcined
catalyst.
SUMMARY OF THE INVENTION
[0009] The invention relates to a new class of three-dimensional
crystalline isomorphously metal-substituted aluminophosphate
materials with high phase purity that are capable of performing
selective Bronsted acid catalyzed chemical transformations, such as
transforming alcohols to olefins, with high conversions and
selectivities using mild conditions. Isomorphous substitutions of
functional metal ions for both the aluminum ions and the
phosphorous ions were successful in various AlPO structures, along
with multiple metal substitutions into a single aluminum site
and/or a phosphorous site and with substantial phase purity of the
substituted AlPO after calcining. The AlPO compositions of this
invention can be used in the catalytic conversion of hydroxylated
compounds of linear and/or branched alkyl or aralkyl moiety with
the possibility of being substituted to their respective
hydrocarbon products, such as, for example, light olefins
containing 2 to 10 carbon atoms, among other chemistries.
Advantageously, the process of the invention may take place with
the hydroxylated compound in the liquid phase.
BRIEF DESCRIPTION OF THE DRAWINGS
[0010] FIG. 1 is an X-ray Diffraction Pattern of 3 different
isomorphously substituted mono-metallic AlPO-5s (Mg.sup.II,
Zn.sup.II, and Si.sup.IV) showing they are phase pure and
crystalline.
[0011] FIG. 2 is an X-ray Diffraction Pattern of 3 different
isomorphously multiply substituted bi-metallic AlPO-5s
(Zn.sup.IIMg.sup.II, Zn.sup.IISi.sup.IV, and Mg.sup.IISi.sup.IV)
showing they are phase pure and crystalline.
[0012] FIG. 3 is an X-ray Diffraction Pattern of an isomorphously
multiply substituted bi-metallic AlPO-5
(Mg.sup.IIZn.sup.IISi.sup.IV) showing it is phase pure and
crystalline.
[0013] FIG. 4 is the Celref analysis of the XRD traces in FIGS. 1-3
showing the correlation between observed and theoretically
calculated peaks are only different on average by less than
0.1000.degree..
[0014] FIG. 5 (A) is the published powder x-ray diffraction (XRD)
pattern generated for the AlPO-5 (AFI) from the IZA powder pattern
simulation, and (B) is the overlay of the substituted AlPO-5 from
EP0141662A2 Example 1 and the invented AlPO-5 Example 1 showing
that the XRD from EP0141662A2 is absent of crystal plane
reflections compared to FIG. 5 (A) and the pattern from the
invented AlPO-5 (indicated by arrows).
[0015] FIG. 6 is the kinetic plot showing ethanol conversion and
ethylene produced versus time for the Si.sup.IV substituted
mono-metallic AlPO-5 at 453 K.
[0016] FIG. 7 is the kinetic plot showing ethanol conversion and
ethylene produced versus time for the Mg.sup.II substituted
mono-metallic AlPO-5 at 463 K.
[0017] FIG. 8 is the kinetic plot showing ethanol conversion and
ethylene produced versus time for the Mg.sup.IISi.sup.IV
substituted bi-metallic AlPO-5 at 453 K.
[0018] FIG. 9 is the kinetic plot showing ethanol conversion and
ethylene produced versus time for the Mg.sup.IISi.sup.IV
substituted bi-metallic AlPO-5 at 483 K.
[0019] FIG. 10 is a flow diagram of the general synthesis of the
substituted AlPO framework in accordance with the claimed
invention.
DETAILED DESCRIPTION OF THE INVENTION
[0020] Processes for converting alcohols to olefins via dehydration
are known in the art. The invention relates to new catalysts and
their use in the dehydration of light alcohols (also described in
the art as hydroxylated compounds or oxygenates) to form their
respective light olefins. The process relates to making light
olefins containing 2 to 10 carbon atoms from oxygenates wherein
said process comprises contacting a feedstock containing an alcohol
(an oxygenate feedstock) with an isomorphously, metal-substituted
aluminophosphate (AlPO) catalyst of the invention comprising a
molecular framework of [AlO.sub.2.sup.-] and [PO.sub.2.sup.+]
tetrahedral units, at effective process conditions to produce such
light olefin products. As used herein, the isomorphously,
metal-substituted aluminophosphate (AlPO) catalysts of the
invention refer to a substantially phase-pure, calcined
aluminophosphate, AlPO.sub.4, where at least one aluminum
(Al.sup.III) site is isomorphously metal-substituted by a divalent
metal ion (M.sup.II) and/or at least one phosphorous (P.sup.V) site
is isomorphously metal-substituted by a tetravalent metal ion
(M.sup.IV).
[0021] The terms "light alcohols" or "light olefins" refers to
alcohols and olefins having two to ten carbon atoms, inclusive.
Although other hydrocarbon products are formed, the products of
particular interest herein are the light olefins and they are
preferably produced as the major hydrocarbon products i.e., over 50
mole percent of the hydrocarbon product is light olefins. The
ability of the isomorphously metal-substituted AlPO catalysts of
the invention to catalytically provide for the formation of light
olefins from alcohols in the liquid phase, preferably as the major
portion of the hydrocarbon product, has not heretofore been
reported or suggested. Examples of alcohol dehydration include:
conversion of lower alkanols to their corresponding olefins,
especially ethanol to ethylene, propanol to propylene, t-butyl
alcohol to isobutylene, and methyl benzyl alcohol to styrene.
Isomorphously Metal-Substituted Aluminophosphate (AlPO) Catalyst
Preparation and Composition
[0022] The invention relates to new aluminophosphate catalysts
(AlPO.sub.4 or AlPOs) with isomorphous substitutions for the
aluminum (Al.sup.III) and the phosphorus (P.sup.V) ions at both
atom positions at the same time, to form strong and tunable
Bronsted acid sites within a single catalyst. Also, isomorphous
substitutions for multiple metal atoms can be made for either the
aluminum or the phosphorus ions alone (incorporating as few as two
new and different strength acid sites) as well as for both
Al.sup.III and P.sup.V in the same instance. These
three-dimensional catalysts comprise a stable crystalline solid
framework enclosing cavities of multi-.ANG.ngstrom diameter. The
cavities form a well-defined system of cages with one-, two-,
and/or three-dimensional channels that can be connected to each
other. The pore diameter can be as small as 3 .ANG.ngstroms and as
large as 15 .ANG.ngstroms or more. Most of the chemical
transformations are believed to occur inside the solid framework.
Accordingly, the invention relates to isomorphously
metal-substituted aluminophosphates (AlPO's). Mono-substituted
AlPO's of the invention must be substantially phase pure and have
at least one aluminum, (Al.sup.II), site substituted by a divalent
metal ion (M.sup.II) or at least one phosphorous, (P.sup.V), site
substituted by a tetravalent metal ion (M.sup.IV). In the
mono-substituted AlPOs of the invention, the Al.sup.III or the
P.sup.V sites may each be multiply substituted with two or more
such metal ions. The invention also relates to substantially phase
pure bi-substituted AlPO's where at least one aluminum,
(Al.sup.III), site is substituted by a divalent metal ion
(M.sup.II) and at least one phosphorous, (P.sup.V), site is
substituted by a tetravalent metal ion (M.sup.IV). In the
bi-substituted AlPOs of the invention, the Al.sup.III and/or the
P.sup.V sites may each be multiply substituted with two or more
such metal ions.
[0023] AlPOs have a three-dimensional microporous crystalline
framework incorporating tetrahedral units with the designation
MO.sub.2.sup.n (where "M" is a metal or metal-like species and "n"
is the net electric charge), specifically AlO.sub.2.sup.- with
PO.sub.2.sup.+ for AlPOs, with or without metals or other
substituents in the complete structure. In the cases of
AlO.sub.2.sup.- and PO.sub.2.sup.+, the Al atom has a +3 charge
resulting in a net charge of -1 for the unit and the P atom has a
+5 charge resulting in a net charge of +1 for the unit. Of course,
as known to those familiar with the art, other "M" atoms may be
used and incorporated to form tetrahedral units of various net
oxidation states, for example SAPOs, which has been the only method
until now to encase a higher than +3 valence state.
[0024] Since the aluminophosphate (AlPO) framework is inherently
neutral in electric charge, the incorporation of silicon, or other
elemental, tetrahedral units into the framework through
substitution generates more active catalytic sites, specifically
acid sites and increased acidity, leading to enhanced
selectivities. In other words, the catalyst compositions of the
invention allow tuning of the Bronsted acid sites and activity
within the catalyst. Until now, the only known method to
incorporate silicon is through the generation of a SAPO by silicon
tetrahedral unit incorporation, where the gel composition is
representative of a SAPO and the primary framework is built around
the Si tetrahedral unit in a stoichiometric amount. Controlling the
quantity and location of silicon atoms and other elements is
important in determining the catalytic properties of a particular
AlPO catalyst.
[0025] Compared to mineral acids, the AlPO catalysts of the
invention have the advantage of reduced corrosion and have no need
to be separated from reaction products. Compared to Lewis and
Bronsted acids and ion exchange resins, they are stronger acids and
have better temperature stability than ion exchange resin and most
Lewis and Bronsted acids. They are also stronger acids than most
other heterogeneous acid catalysts.
[0026] Properly adjusted acid strength, acidity distribution, and
acid site density are the keys to forming a high oxygenate
conversion or petroleum cracking catalyst. This invention, for the
first time, describes how the P.sup.V ion may be exchanged for a
lower valence metal, like Si' among other metals with similar +4
valence states, combined with a substitution of the Al.sup.III ion
by a metal, like Mg.sup.II among other metals with a +2 valence
state. These new substituted ions are incorporated into the AlPO
framework through the isomorphous substitution of the Al.sup.III
and P.sup.V ion to tune the acid strength with precision.
[0027] Often, the Al.sup.III ion is substituted to incorporate
other metal ions to increase the active catalytic sites, such as
adding metals of a +2 valence to generate acid sites, within the
AlPO framework. The silicon ion has only been incorporated into
these three-dimensional frameworks via (i) the post-synthesis route
or (ii) through the art known to generate SAPOs, by adding a
stoichiometric amount of silicon tetrahedral units altering the
crystal structure of the starting AlPO.
[0028] In this invention, a new metal ion, which includes metals
and metalloids, of lower valence, M.sup.IV has been substituted
isomorphously into the AlPO framework by replacing the phosphorous
ion, P.sup.V with cations of +3 valence to generate Bronsted acid
sites simultaneously with the replacement of one or more Al.sup.III
sites with different cations of +2 valence. M.sup.IV includes, but
is not limited to, Si.sup.IV, Zr.sup.IV, Pt.sup.IV, Sn.sup.IV,
Ti.sup.IV, Ge.sup.IV, Pd.sub.IV, and mixtures thereof. The
substitution of the silicon into the P.sup.V site has never been
performed in conjunction with separate metal ion substitution for
the aluminum ion, Al.sup.III, with a new metal ion, which includes
metals and metalloids, of lower valence, M.sup.II. M.sup.II
includes, but is not limited to, Zn.sup.II, Mg.sup.II, Co.sup.II,
Ca.sup.II, Ni.sup.II, Pd.sup.II, and mixtures thereof. If a
M.sup.II is used that can be oxidized to a higher valence number
during preparation, the metal must be reduced under a reducing
environment to return the metal to a +2 valence forming the
Bronsted acid site. Lastly, multiple replacements of new metal ions
(M.sup.II and/or M.sup.IV) can be substituted for either, or both,
of the Al.sup.III or P.sup.V ions generating no fewer than 3
separate kinds of acid sites in close proximity. The molar amount
of M.sup.II substituted for Al.sup.III may range, for example, from
about 0.001 to about 0.99 moles M.sup.II, or further, for example,
from about 0.01 to about 0.09 moles M.sup.II, or further, for
example, from about 0.03 to about 0.07 moles M.sup.II. The molar
amount of M.sup.IV substituted for P.sup.V may range from about
0.01 to about 0.99 moles M.sup.IV, or further, for example, from
about 0.05 to about 0.20 moles M.sup.IV, or further, for example,
from about 0.08 to about 0.17 moles M.sup.IV.
[0029] The general method for preparing AlPO catalysts of the
invention is shown in Scheme 2 as shown in FIG. 10. To synthesize
these AlPO frameworks with generated Bronsted acid sites, a known
quantity of a phosphorous source (PO.sub.2.sup.+), including
phosphoric acid, organic phosphates such as triethyl phosphate, and
aluminophosphates, can be added to a known amount of water and be
left to stir. Next, a known amount of an aluminum source
(AlO.sub.2.sup.-), including aluminum alkoxides such as aluminum
isopropoxide, aluminum phosphates, aluminum hydroxide, sodium
aluminate, and pseudoboehmite, must be added slowly to the reaction
mixture to stop its solidification. The entire solution is stirred
vigorously. A desired amount of substituting metal source (M.sup.II
and M.sup.IV) is mixed in water. When it has fully suspended or
dissolved, slowly add the solvated metal source into the above
reaction mixture to isomorphously replace the Al.sup.III and/or
P.sup.V. The mixture is then stirred vigorously to homogenize for
several minutes before adding a further quantity of water. Next, a
measured quantity of structure directing agent (SDA) is slowly
added into the stirring reaction mixture before adding a final
amount of water and aging the resulting mixture, for example for
about 1 minute to about 2 hours.
[0030] Once the synthesis reaction is complete, stirring should be
terminated and the reaction contents should be transferred into a
high pressure autoclave unit with resistant liners. The autoclave
should be sealed and heated with the product for up to about 6
hours, such as, for example, between 1 and 3 hours, at a
temperature ranging between 23.degree. C. and 500.degree. C., such
as, for example, between 100.degree. C. and 300.degree. C. After
the heating step is complete, the autoclave should be removed from
the oven and quenched in cold water/ice for at least between 0 and
5 hours, such as, for example, between 10 minutes and 2 hours,
before opening and filtering the catalyst product, using water to
wash it. The catalyst product from the autoclave is an
isomorphously, metal-substituted aluminophosphate (AlPO) catalyst
product which still contains the SDA within its crystalline
structure. Once the product has been dried, it is transferred to a
furnace and slowly heated (approximately 3-5.degree. C./minute) in
an inert gas (e.g. nitrogen) at a calcination temperature ranging
between 200.degree. C. and 1000.degree. C., such as, for example,
between 400.degree. C. and 700.degree. C. and then calcined in air
or another oxygen-containing gas for at least between 3 and 24
hours, such as, for example, between 8 hours and 16 hours, to
calcine the catalyst. Prior to calcining in air, the product may be
held at temperature under the flow of inert gas for about 5 minutes
to about 3 hours, such as, for example for about 1 to about 2
hours. After calcining, the product is slowly cooled (approximately
3-5.degree. C./minute) to room temperature. As used herein, the
phrase "heated at" a certain temperature or variations thereof
means that the oven, furnace, or other heating device is set at the
specified temperature.
[0031] Preferred sources of Metal Precursors 1 and 2 being M.sup.II
and M.sup.IV include, but are not limited to, magnesium (II)
acetate, zinc (II) acetate, silica (fumed), and titanium (IV)
isopropoxide, germanium (IV) methoxide, nickel (II) acetate
tetrahydrate, tin chloride (IV) pentahydrate, zirconium (IV)
acetate hydroxide, manganese (II) acetate, cobalt (II) acetate
tetrahydrate, and copper (II) acetate monohydrate.
[0032] Preferred SDA's include, but are not limited to,
tetramethylammonium (TMAOH), tetraethylammonium (TEAOH),
tetrapropylammonium (TPAOH), or tetrabutylammonium ions;
di-n-propylamine; tripropylamine (TPA); triethylamine (TEA);
triethanolamine; piperidine; cyclohexylamine; 2-methylpyridine;
N,N-dimethylbenzylamine; N,N-diethylethanolamine;
dicyclohexylamine; N,N-dimethylethanolamine; choline; morpholine
(MOR); N,N'-dimethylpiperazine; 1,4-diazabicyclo(2,2,2) octane;
N-methyldiethanolamine, N-methylethanolamine; diisopropylethylamine
(DIPE); N-methylpiperidine; 3-methylpiperidine;
N-methylcyclohexylamine; 3-methylpyridine; 4-methylpyridine;
quinuclidine; N,N'-dimethyl-1,4-diazabicyclo(2,2,2)octane ion;
di-n-butylamine, neopentylamine; di-n-pentylamine; isopropylamine;
t-butylamine; ethyldicyclohexylamine (EDCHA);
methyldicyclohexylamine (MDCHA); ethylenediamine; pyrrolidine; and
2-imidazolidone. As will be readily apparent from the illustrative
examples set forth hereinafter, not every template will produce
every AlPO composition although a single template can, with proper
selection of the reaction conditions, be used in the formation of
different isomorphously, metal-substituted aluminophosphate (AlPO)
catalysts of the invention, and a given AlPO composition can be
made using different templates. As known in the art, these
templates lead to various pore sizes and orientations in the
framework of the specific AlPO being synthesized, which is
designated by a number at the end of the AlPO name (i.e.,
AlPO-5).
[0033] The AlPOs of the invention display many catalytic advantages
in acid-catalyzed transformations. Not least among these advantages
are the catalysts' high internal surface area, which becomes
accessible to reactant molecules of certain size and shape, and
from which those products of appropriate dimension can diffuse.
Some example AlPOs and their surface area measurement are shown
below in Table 1 along with their metal content which was measured
using Inductively Coupled Plasma spectroscopy (ICP). Other
advantages include: (a) the ability for small quantities of
isolated transition metal ions (M) to be incorporated into the AlPO
frameworks; (b) relative ease of preparation, using appropriately
chosen structure-directing organic templates, resulting in a
considerable range of MAlPO structures differing in their micropore
and cage characteristics (e.g., pore diameters, extent of pore
intersection); and (c) good thermal stability. An added bonus is
that, detailed quantitative knowledge about the local structure of
metal-ion-centered active sites in these microporous catalysts is
readily retrievable from the application of in situ techniques,
such as X-ray absorption spectroscopy and FTIR.
TABLE-US-00001 TABLE 1 BET ICP Metal content Surface Substituted by
weight/% Area AlPO Empirical formula Mg Zn Si (m.sup.2/g) MgAlPO-5
Mg.sub.0.04Al.sub.0.96P.sub.1.00O.sub.4.00H.sub.0.04 0.81 -- --
193.32 ZnAlPO-5
Zn.sub.0.04Al.sub.0.96P.sub.1.00O.sub.4.00H.sub.0.04 -- 2.18 --
165.41 SiAlPO-5
Si.sub.0.12Al.sub.1.00P.sub.0.88O.sub.4.00H.sub.0.12 -- -- 2.66
181.87 MgSiAlPO-5
Mg.sub.0.03Si.sub.0.08Al.sub.0.97P.sub.0.92O.sub.4.00H.sub.0.11
0.58 -- 1.93 167.58 ZnSiAlPO-5
Zn.sub.0.03Si.sub.0.04Al.sub.0.97P.sub.0.96O.sub.4.00H.sub.0.08 --
1.76 1.18 236.21 MgZnAlP0-5
Mg.sub.0.04Zn.sub.0.03Al.sub.0.93P.sub.1.00O.sub.4.00H.sub.0.07
0.69 1.84 -- 283.78 MgZnSiAlPO-5
Mg.sub.0.03Zn.sub.0.03Si.sub.0.17Al.sub.0.94P.sub.0.83O.sub.4.00H.sub.0.2-
3 0.65 1.60 3.87 101.53
[0034] AlPO-5 has hexagonal symmetry with a=1.372 nm and c=0.847 nm
and contains one-dimensional channels oriented parallel to the c
axis that are fused by 12-membered rings composed of alternating
AlO.sub.4 and PO.sub.4 tetrahedra. The overall framework is neutral
(unlike zeolites) and the structure has distinct channels (as
opposed to cages with sodalite or AlPO-18). It can be easily
synthesized using a range of SDA's (e.g., triethylamine,
tripropylamine, etc), as the large one-dimensional cylindrical pore
system imposes fewer constraints on the template fit. This material
belongs to the AFI framework type (as classified by the
International Zeolite Association). The pores in this structure are
formed by the alternation of squares and hexagons and have a
diameter of 7.3 {acute over (.ANG.)} and are only 1 dimensional,
thus are actually channels.
[0035] AlPO-18 is a microporous crystalline molecular sieve with a
chabazite-like structure with a framework topology characterized by
a three-dimensional pore system (pear-shaped) possessing 8-membered
intersecting channels. The framework density (14.8 T/1000 A.sup.o)
of the AEI topology is among the lowest in the family of
aluminophosphate microporous materials. AlPO-18 is typically formed
using N,N-diisopropylethyl amine as the SDA and the un-substituted
framework has a neutral charge.
[0036] The main difference between the AlPO-18 and AlPO-34
structures is the way in which the double six ring units are
oriented. The structures are also different crystallographically,
but they essentially possess a similar cage-type structure with
pore openings consisting of 8-membered rings resulting in pore
entry sizes of ca. 3.8 .DELTA.. While AlPO-34 belongs to the CHA
framework type, AlPO-18 has an AEI-type framework.
[0037] Phase purity of the catalyst, defined herein as having only
one crystalline phase, maintained through temperature and addition
control, was monitored before and after calcination by a
combination of powder X-ray diffraction and Reitveld analysis. The
precise stoichiometry (an error of ca..+-.3.times.10.sup.-3) was
determined by ICP (metal) analysis. Substantial phase purity is
defined as the presence or absence of certain peaks (or
reflections) in the X-ray powder diffraction pattern, which permits
the determination of the lattice type. Nearly all crystalline
solids have a unique powder diffraction pattern in terms of the
angles of reflection and their intensities. Where mixtures of
compounds, or where phase impurities are present, each phase
contributes to the powder diffraction pattern through its own set
of reflection angles and intensities. By using the Reitveld method
one can fit a calculated diffraction pattern with an experimental
trace to get quantitative insights on atomic positions, which in
turn provide a superior measure of the phase purity of the
sample.
[0038] To ensure that a high degree of phase purity and
crystallinity is achieved, the synthesis procedure, the formation
of the gel, and its subsequent aging and crystallization are all
carried out in Teflon vessels. The Teflon provides an inert surface
with appropriate heat transfer and helps avoid the incorporation of
contaminants and undesired metals, like iron, into the AlPO
structure. Also, the order of material addition contributes to
synthesizing superior phase pure material as at first the Al--O--P
linkages, the primary and secondary building units of the AlPO, are
formed followed by the isomorphous substitution of the desired
metal ions into the framework. The reaction mixture must be kept
homogenous and is therefore stirred at high speeds, ranging from
500 to 5,000 rpm, such as, for example, from 750 to 2,500, and
further such as, for example from 1,000 to 1,500 rpm. The selection
of the SDA is carried out to give a high specificity towards the
desired AlPO product, for example MDCHA is a structure directing
agent for AlPO-5. The choice of the appropriate SDA is critical to
avoiding the co-crystallization of mixture phases or heavy phases,
such as chabazite. Lastly, the amount of water used in the
synthesis procedure should be sufficient to facilitate molecular
homogeneity throughout the synthesis procedure, particularly of the
substituting metal sources and the SDA, thereby minimizing the
formation of co-crystallization of impure phases and facilitating
the removal of any dense phases. Too much water may affect the
crystallization of the mixture.
[0039] The calcination procedure is also significant in ensuring
phase purity. The initial flow of an inert gas, such as nitrogen,
during the heat ramp loosens the SDA from the tetrahedral-atom
sites prior to it being removed during calcinations, which prevents
any breakdown of the AlPO phase structure. The sample may also be
held for a time at temperature under a flow of the inert gas. The
sample is then heated under a flow of dry air gently to calcine the
sample removing the SDA and any remaining water to prevent the
disruption to the phase structure and crystallinity. The sample is
also cooled slowly to prevent disruption to the structure.
[0040] Accordingly, the invention also relates to a process for
preparing a substantially phase pure, calcined metal-substitituted
aluminophosphate, AlPO, wherein at least one aluminum (Al.sup.III)
site is substituted by a divalent metal ion (M.sup.II) and/or at
least one phosphorous (P.sup.V) site is substituted by a
tetravalent metal ion (M.sup.IV). The process comprises the steps
of:
[0041] adding a phosphorous source, such as, for example,
phosphoric acid, to water to form an aqueous mixture,
[0042] stirring the aqueous mixture,
[0043] adding an aluminum source, such as, for example, aluminum
hydroxide, to the stirred aqueous mixture to form a first reaction
mixture,
[0044] adding at least one aqueous solution or suspension of a
M.sup.II metal source, a M.sup.IV metal source, or both to the
stirred first reaction mixture,
[0045] stirring the first reaction mixture containing the metal
source for a time sufficient to form a homogenized mixture,
[0046] optionally adding a further quantity of water to the stirred
homogenized mixture,
[0047] adding a SDA to the stirred homogenized mixture to form a
second reaction mixture, optionally adding water,
[0048] stirring the second reaction mixture until the reaction is
complete to form a substituted AlPO reaction product mixture,
[0049] aging the substituted AlPO reaction product mixture,
[0050] autoclaving the aged substituted AlPO reaction product
mixture in a high pressure autoclave unit equipped with resistant
liners to a temperature ranging between about 23.degree. C. and
about 500.degree. C. for up to about 6 hours,
[0051] quenching the autoclave,
[0052] filtering the autoclaved substituted AlPO reaction product
mixture to recover a solid catalyst product, which is an
isomorphously, metal-substituted aluminophosphate (AlPO) catalyst
product which still contains the SDA within its crystalline
structure,
[0053] washing the solid catalyst product with water,
[0054] drying the solid catalyst product,
[0055] slowly heating the dried catalyst product under a flowing
inert gas at a calcination temperature ranging between about
200.degree. C. and about 1000.degree. C.,
[0056] holding the dried catalyst product under the flowing inert
gas at the calcination temperature,
[0057] calcining the dried catalyst product for a time of at least
about 3 to about 24 hours to form a substantially phase pure,
calcined metal-substitituted aluminophosphate, and
[0058] slowly cooling the substantially phase pure, calcined
metal-substitituted aluminophosphate to room temperature.
[0059] The invention also relates to a process for preparing a
substantially phase pure, calcined metal-substitituted
aluminophosphate, AlPO, wherein at least one aluminum (Al.sup.III)
site is substituted by a divalent metal ion (M.sup.II) and/or at
least one phosphorous (P.sup.V) site is substituted by a
tetravalent metal ion (M.sup.IV) comprising the steps of:
[0060] slowly heating an isomorphously, metal-substituted
aluminophosphate catalyst product containing a SDA within its
crystalline structure under a flowing inert gas at a calcination
temperature ranging between about 200.degree. C. and about
1000.degree. C.,
[0061] holding the isomorphously, metal-substituted
aluminophosphate catalyst product under the flowing inert gas at
the calcination temperature,
[0062] calcining the isomorphously, metal-substituted
aluminophosphate catalyst product for a time of at least about 3 to
about 24 hours to form a substantially phase pure, calcined
metal-substitituted aluminophosphate, and
[0063] slowly cooling the substantially phase pure, calcined
metal-substitituted aluminophosphate to room temperature.
[0064] Phase purity and the crystallinity of the catalyst is an
important and integral feature of this invention. It is known in
the prior art that the substitution of the Al.sup.III site with a
transition metal may lead to the generation of a catalyst with a
potential for high phase purity, but this was seldom obtained. The
invention achieves the simultaneous substitution of the Al.sup.III
site and/or the P.sup.V site with Bronsted acid sites, transition
metals in the +2 and +4 valence states, respectively, and yielding
catalysts with high levels of phase purity and crystallinity.
Catalysts with inferior levels of crystallinity, or those
containing mixed phases such as chabazite and trydimite, lead to
inferior catalytic performance and, more importantly, to decreased
levels of selectivity for the desired olefins.
[0065] Typical XRD patterns and Reitveld analysis of substituted
AlPO catalysts of the invention demonstrate the catalyst's
phase-purity, crystallinity, and unit cell dimension. These XRD
patterns (shown in FIGS. 1-3) show that a high level of structural
phase purity and good crystallinity were obtained in all cases.
Celref analysis (shown in FIG. 4) of the XRD data show an
acceptable correlation between observed and theoretically
calculated peaks. In most cases, a difference in the 2theta
(2.theta.) angle of less than 0.1000.degree. was observed. FIG. 4
shows that despite the isomorphous substitution of metals to the
AlPO, the X-ray signature of the chosen AlPO is retained. This high
phase purity and high degree of crystallinity drive the catalyst's
exceptional ability to perform the olefin conversion while the
alcohol is in the liquid phase.
[0066] As a further demonstration of the phase purity of the AlPO
compositions of the invention, FIG. 5 shows a comparison of a
substituted MgZnAlPO-5 of the invention (Example 1) and a prior art
substituted CoAlPO-5 from EP0141662A2, Example 1. FIG. 5 (A) is the
published powder x-ray diffraction (XRD) pattern generated for the
phase pure AlPO-5 (AFI) from the IZA powder pattern simulation
(http://izasc.ethz.ch/fmi/xsl/IZA-SC/mat_xrd.xsl?-db=crystal_data&-lay=we-
b&-recid=8&-find=, Jan. 21, 2009). The XRD pattern of a
phase pure AlPO-5 structure includes two peaks at 24.7 and 36.9
.degree.2.theta.. FIG. 5 (B) overlays of the peak positions
(vertical lines) reported for the substituted CoAlPO-5 from
EP0141662A2, Example 1 and the XRD pattern for the substituted
MgZnAlPO-5 of Example 2 of the invention. EP0141662A2, Example 1
lists thirteen XRD peaks each for its precalcined and calcined
compositions. The XRD pattern reported for the calcined composition
in EP0141662A2, Example 1 lacks two peaks at 24.7 and 36.9
.degree.2.theta. of a phase pure AlPO-5 structure (FIG. 5 (A)).
Those two peaks are either missing or substantially shifted
indicating a significant change in crystalline phase or the
introduction of other phases. In contrast, the XRD pattern of the
substituted MgZnAlPO-5 of the invention (as indicated by the
arrows) displays those two peaks, matching the XRD pattern of an
AlPO-5 structure and demonstrating its phase purity.
Isomorphously Metal-Substituted Aluminophosphate (AlPO) Catalyst
Uses
[0067] Metal-substituted AlPO catalysts of the invention desirably
have a kinetic pore diameter such that the selectivity to the
desired reaction product is greater than 50 mole percent and which
permits the easy diffusion of both the reactant and the desired
product. As is known in the art, the AlPO type and its
corresponding pore size are determined by the SDA. The selection of
the isomorphously metal-substituted AlPO catalyst for the process
is preferably related, in part, to the desired product mixture
sought. It is believed that the kinetic diameter of the pores of
the selected metal-substituted AlPO catalyst is related to the
products formed. In carrying out the dehydration of alcohols to
form light olefins according to the invention, the isomorphously
metal-substituted AlPO catalysts may be admixed (blended) or
provided sequential to other materials which may provide some
property which is beneficial under process conditions, such as
improved temperature resistance or improved catalyst life by
minimization of coking or which is simply inert under process
conditions. Such materials may include synthetic or naturally
occurring substances as well as inorganic material such as clays,
silicas, aluminas, crystalline aluminosilicate zeolites, metal
oxides and mixtures thereof. The relative proportions of the above
materials and the isomorphously metal-substituted AlPO catalysts
may vary widely ranging between about 1 and about 99 percent by
weight of the composite.
[0068] In addition to the dehydration of alcohols (oxygenates) to
form light olefins, discussed above, the substituted AlPO catalysts
of the invention may be used for any reaction known to be catalyzed
by strong acids, that include, but are not limited to, mineral
acids (sulphuric acid, phosphoric acid, etc.), Lewis or Bronsted
acids (aluminum chloride, etc.), ion exchange resins, as well as
other heterogeneous acids. See for example, Geissman, T. A.,
Principles of Organic Chemistry, 4.sup.th ed, W.H. Freeman &
Co. San Francisco, (1977), Morrison and Boyd, Organic Chemistry,
3.sup.rd Ed., Allyn & Bacon (1973) and Allinger, N. L., et al.
Organic Chemistry, Worth, (1971), which are incorporated herein by
reference.
[0069] Preferred reactions include dehydration of alcohols to
olefins, hydrolysis of olefins to alcohols, esterification,
transesterification and ester hydrolysis, aldol condensation, and
alkylation. Examples of alcohol dehydration include, for example:
conversion of lower alkanols to their corresponding olefins,
especially ethanol to ethylene, propanol to propylene, t-butyl
alcohol to isobutylene and methyl benzyl alcohol to styrene.
Examples of olefin hydrolysis include, for example, ethylene to
ethanol and propylene to propanol.
[0070] Esterifications include, for example, the reaction of light
alcohols with acids to make the corresponding esters. Examples
include reaction of methanol and ethanol, respectively with acetic
acid to make methyl and ethyl acetates respectively; reaction of
acrylic and methacrylic acids with lower alcohols like methanol and
butanol to make methyl acrylate, methyl methacrylate, and butyl
methacrylate; and the reaction of 2-ethyl hexanol with phthalic
anhydride to make dioctyl phthalate. An ester hydrolysis of
interest includes the hydrolysis of methyl acetate to methanol and
acetic acid. Transesterifications include, for example, conversion
of methyl methacrylate to butyl methacrylate and conversion of
alkyl glycerates to methyl esters (biodiesel) and glycerin.
[0071] Aldol condensations include, for example, reactions of
aldehydes and ketones with functional aromatic compounds, including
the reaction of phenol with acetone to make bisphenol A or the
reaction of formaldehyde with aniline to make methylene dianiline
as well as the classical self condensation of acetone to yield
diacetone alcohol, mesitylene, and isophorone.
[0072] Alkylations include, for example, reactions of olefins with
aromatic compounds including ethylene and benzene to ethylbenzene
and propylene and benzene to cumene.
[0073] An especially preferred use for the substituted ALPO
catalysts of the invention is the conversion of alcohols to
olefins, such as ethanol to ethylene, where there are currently
known alternative catalysts with lesser performance. In one
embodiment then, the invention relates to a process for the
dehydration of alcohols to form olefins. In that process, a
feedstock containing an alcohol is contacted with an isomorphously
metal-substituted aluminophosphate of the invention under
conditions sufficient to convert the alcohol to an olefin. The
alcohol is preferably a light alcohol, e.g., a C.sub.2-C.sub.10
alcohol. Examples of light chain alcohols include, but are not
limited to, ethanol, propanol, butanol, pentanol, hexanol,
heptanol, octanaol, nonanol, and decanol. Those having three or
more carbons may be straight chains or branched, alkyl or aralkyl
moiety, e.g., iso-propanol, tert-butanol, etc. The hydroxyl group
may be on any carbon in the chain. The light chain alcohols may
contain other substituents which do not unduly prevent or slow the
dehydration reaction or poison the catalyst.
[0074] It has been discovered that by use of the newly invented
metal-substituted ALPO catalysts for the conversion of such a
feedstock that, in general, higher feedstock conversions and
selectivities to light olefin products may be obtained as compared
to that obtained by the use of the prior art unsubstituted, or
monosubstituted, AlPOs and SAPOs as well as aluminosilicate
zeolites as catalysts. It has also been discovered that by use of
specific metal-substituted AlPO catalysts that the selectivity to
C.sub.2 to C.sub.10 olefin products (e.g., ethylene, propylene,
butenes, etc.) of at least about 25 mole percent, based on the
total hydrocarbon products formed, may be obtained, such as, for
example, in excess of 50 mole percent. Further, the selectivity to
such olefin products may be in excess of 95 mole percent when
specific metal-substituted AlPO catalysts of the invention are
employed. In addition, it has been observed that the formation, if
any, of aromatic hydrocarbons is below that which is detectable by
standard vapor phase chromatographic techniques (GC). An additional
bonus is that certain metal-substituted AlPO catalysts as employed
in the process are believed to have increased catalyst life with
respect to the conversion of the feedstock to light olefin products
as compared with the crystalline aluminosilicates (ZSM-type) and
unsubstituted, or monosubstituted, aluminophosphate and
silicoaluminophosphate catalysts.
[0075] An alcohol to olefin conversion process of the invention can
be carried out in a either a two or three phase process with the
alcohol, such as ethanol, in either the liquid or vapor phase.
Preferably, the reaction is carried out with the alcohol, like
ethanol, in the liquid phase, such that it is contacted in a
reaction zone with a solid metal-substituted aluminophosphate
catalyst at effective process conditions such as to produce light
olefins in the gas phase, i.e., an effective temperature, pressure,
Weight Hourly Space Velocity (WHSV), and, optionally, an effective
amount of diluent, correlated to produce light olefins. Maximum
yield and selectivity can be achieved whether the reaction is
conducted in the liquid or vapor phase making the invented
catalysts superior to those known in the prior art.
[0076] The temperature that may be employed in an alcohol to olefin
conversion process of the invention may vary over a wide range
depending, at least in part, on the selected metal-substituted AlPO
catalyst and whether the reaction is performed in the liquid or
vapor phase. In general, the process can be conducted at an
effective temperature ranging between about 23.degree. C. and about
700.degree. C. (liquid and vapor phase), such as, for example,
between 50.degree. C. and 250.degree. C. (liquid phase) and about
250.degree. C. and about 600.degree. C. (vapor phase), and further
such as, for example, between about 100.degree. C. and 240.degree.
C. (liquid phase) and 300.degree. C. and about 500.degree. C.
(vapor phase). Temperatures outside the stated range are not
excluded from the scope of this invention, although such do not
fall within certain desirable embodiments of the invention. At the
lower end of the temperature ranges and, thus, generally at the
lower rate of reaction, the formation of the desired light olefin
products may become markedly slow. Notwithstanding these factors,
the reaction will still occur and the feedstock, at least in part,
can be converted to the desired light olefin products at
temperatures outside the ranges stated above for a process of the
invention.
[0077] An alcohol to olefin conversion process of the invention is
effectively carried out over a wide range of pressures including
autogenous pressures. At pressures ranging between about 0.10
atmospheres and about 500 atmospheres, such as, for example,
between about 1 atmosphere and about 100 atmospheres, and further
such as, for example, between about 1 atmosphere and about 30
atmospheres, the formation of light olefin products will be
affected although the optimum amount of product will not
necessarily form at all pressures. The pressures referred to herein
for the process are exclusive of the inert diluent, if any is
present, and refer to the partial pressure of the feedstock as it
relates to oxygenates or mixtures thereof. Pressures outside the
stated range are not excluded from the scope of this invention,
although such do not fall within certain desirable embodiments of
the invention. At the lower and upper end of the pressure range,
and beyond, the selectivities, conversions and/or rates to light
olefin products may not occur at the optimum although light olefin
products can be formed
[0078] An alcohol to olefin conversion process of the invention is
affected for a period of time sufficient to produce the desired
light olefin products. In general, the residence time employed to
produce the desired product can vary from seconds to a number of
hours. It will be readily appreciated by one skilled in the art
that the residence time will be determined to a significant extent
by the reaction temperature, the isomorphously metal-substituted
AlPO selected, the WHSV, the phase (liquid or vapor) selected, and,
perhaps, selected process design characteristics.
[0079] An alcohol to olefin conversion process of the invention may
be carried out under process conditions comprising a temperature
ranging between about 100.degree. C. and about 240.degree. C.
(liquid phase) and 300.degree. C. and about 500.degree. C. (vapor
phase) using a pressure ranging between about 1 atmosphere to about
30 atmospheres (liquid and vapor phase). The temperature, pressure,
and WHSV are each selected such that the effective process
conditions, i.e. the effective temperature, pressure, and WHSV, are
employed in conjunction, i.e., correlated, with the selected
metal-substituted AlPO catalyst and selected oxygenate feedstock
such that light olefin products are produced.
[0080] The oxygenate feedstock is selected based on the olefin to
be produced. Generally speaking, the feedstock is the corresponding
alcohol (linear, branched, substituted, etc.), e.g., ethanol to
produce ethylene, propanols to produce propylenes, butanols to
butenes, etc. The preparation of the oxygenate feedstock is known
in the art. Ideally, the feedstock should be `dry`, but especially
when the reaction is carried out in the liquid phase, under
conditions where the product is a gas, may contain substantial
amounts of water but, of course, not so much as to adversely impact
the catalytic dehydration. In addition to the presence of alcohols
(e.g., ethanol, propanol, butanols, etc.), or mixtures thereof in
the feedstock, a diluent may be present in the feedstock in an
amount ranging between about 1 and about 99 mole percent, based on
the total number of moles of all feed components fed to the
reaction zone (or catalyst). Typical of the diluents which may be
employed in the process are, for example, helium, argon, nitrogen,
carbon monoxide, carbon dioxide, hydrogen, water (steam),
paraffins, hydrocarbons (such as methane and the like), aromatics
(such as benzene, toluene, xylenes and the like), mixtures thereof,
and the like. Various feedstocks and their preparation as well as
processes using them are described, for example, in U.S. Pat. No.
7,626,067 and published PCT applications WO 03/000412 and WO
03/000413. It has been discovered that the addition of a diluent to
the feedstock prior to such being employed in the process is
generally beneficial, although not required.
[0081] An alcohol to olefin conversion process of the invention may
be carried out in a batch, semi-continuous, or continuous fashion.
The process can be conducted in a single reaction zone or a number
of reaction zones arranged in series or in parallel, or it may be
conducted intermittently or continuously in an elongated tubular
zone or a number of such zones. When multiple reaction zones are
employed, it may be advantageous to employ one or more of such
metal-substituted AlPO catalysts in series to provide for a desired
product mixture. Owing to the nature of the process, it may be
desirable to carry out the process by use of the catalyst in a
dynamic (e.g., fluidized or moving) bed system or any system of a
variety of transport beds rather than in a fixed bed system. Such
systems would readily provide for any regeneration (if required) of
the catalyst after a given period of time. If regeneration is
required, the catalyst can be continuously introduced as a moving
bed to a regeneration zone where it can be regenerated, such as for
example by removing carbonaceous materials by oxidation in an
oxygen-containing atmosphere In the preferred practice of the
invention, if coking occurs, the catalyst will be subject to a
regeneration step by burning off carbonaceous deposits accumulated
during reactions.
[0082] The ability to carry out a three phase reaction is often
advantageous. This is particularly so with reactions being carried
out at conditions where the equilibrium conversion is less than
100%. It is particularly preferred to carry out the dehydration of
light alcohols in a three phase system. Another group of reactions
that can benefit from being practiced in a three phase system are
esterifications, ester hydrolysis and transesterifications. In all
of these systems the advantage of three phase operation lies in the
ability to drive otherwise equilibrium limited reactions by
volatilizing one or more of the products.
[0083] Three phase reactions may be carried out in any type of
convenient equipment: a simple boiling reactor with the invented
AlPO in the slurry phase, a trickle bed reactor (either massive or
with the AlPO catalyst deployed in tubes) or even a distillation
column. In the latter case, the AlPO may function as the
distillation packing or may be present in discrete reaction zones
within the distillation and be applied in combination with trays or
other distillation packing
EXAMPLES
[0084] Specific examples of the preparation of metal-substituted
AlPO catalysts of the invention were done using the method
described above. Examples 1-31 describe the reagents and conditions
used to prepare the specific catalyst. RMM is defined as the sum of
all relative atomic masses of the atoms in the molecule described.
Examples 33 and 34 describe the catalytic dehydration of ethanol
and propanol using those catalysts.
Example 1
Procedure for Making a Mono-Metallic Substituted AlPO
[0085] Synthesis of Mg.sup.IIZn.sup.IIAlPO-5.
[0086] Phosphoric acid (9.601 g, 85 wt % aqueous solution, Aldrich)
was diluted with H.sub.2O (10 g) in a Teflon beaker and stirred for
5 minutes. Teflon was used because the reaction vessel should be
inert to the leaching of undesired metals, such as iron, into the
AlPO structure. Aluminium hydroxide (4.071 g, 52.225 mmol,
Al(OH).sub.3.H.sub.2O, Aldrich) was added slowly to the beaker and
stirred at high speed (between 1000 and 1,200 rpm) for 10 minutes.
Magnesium acetate tetrahydrate (0.357 g, 1.668 mmol,
Mg(C.sub.2H.sub.3OO).sub.2.4H.sub.2O, Aldrich, 99%) and zinc
acetate (0.306 g, 1.667 mmol, Zn(C.sub.2H.sub.3OO).sub.2, Aldrich,
99%) were measured into separate glass beakers and dissolved in 10
g of H.sub.2O each. The diluted metal precursors were then added
dropwise simultaneously to the Teflon beaker. The mixture was
allowed to stir at high speed (between 1000 and 1200 rpm) for 30
minutes before the SDA, methyldicyclohexylamine (MDCHA), (8.682 g,
44.443 mmol, Aldrich) was added dropwise to the mixture. The
remaining water (18.17 g) was then added achieving a total 50 moles
of water, maintaining substantial phase purity to avoid heavy, or
dense, phase impurity formation, like chabazite. The composition of
the gel was 0.94Al:1.5P:0.03Zn:0.03Mg:0.8SDA:50H.sub.2O. The
resulting gel was aged for 25 minutes before being transferred to
Teflon-lined tubes inside stainless steel autoclaves. Teflon lined
autoclaves are important for phase purity as glass or metal
autoclaves with no lining lead to phase impurity formation. The
sealed autoclaves were heated under autogenous pressure under
static conditions in a conventional oven at 180.degree. C. for 2
hours. The autoclaves were quenched with cold water and the
resulting product was filtered, washed with water, and dried gently
at 90.degree. C.
[0087] Calcination was carried out in a tube furnace (Lenton)
heated at 3.degree. C./minute under a steady nitrogen flow until
the temperature reached 550.degree. C. The sample was then held
under the nitrogen flow for 2 hours. After 2 hours the gas was
changed to dry air and the sample was held under a constant gentle
flow of air for 12 hours at 550.degree. C. before being allowed to
cool gently at a rate of approximately 5.degree. C./minute to room
temperature.
Example 2
Procedure for Making a Bi-Metallic Substituted AlPO
[0088] Synthesis of Mg.sup.IIZn.sup.IISi.sup.IVAlPO-5.
[0089] Phosphoric acid (5.441 g, 85 wt % aqueous solution, Aldrich)
was diluted with H.sub.2O (10 g) in a Teflon beaker and stirred for
5 minutes. Teflon was used because the reaction vessel should be
inert to the leaching of undesired metals, such as iron, into the
AlPO structure. Aluminium hydroxide (4.331 g, 55.56 mmol,
Al(OH).sub.3.H.sub.2O, Aldrich) was added slowly to the beaker and
stirred at high speed (between 1,000 and 1,200 rpm) for 10 minutes.
Magnesium acetate tetrahydrate (0.357 g, 1.668 mmol,
Mg(C.sub.2H.sub.3OO).sub.2.4H.sub.2O, Aldrich, 99%) and zinc
acetate (0.306 g, 1.668 mmol, Zn(C.sub.2H.sub.3OO).sub.2, Aldrich,
99%) were measured into separate glass beakers and dissolved in 10
g of H.sub.2O each. The diluted metal precursors were then added
dropwise simultaneously with dry fumed silica (0.677 g, 11.117
mmol, Aldrich) to the Teflon beaker. The mixture was allowed to
stir at high speed (between 1000 and 1200 rpm) for 30 minutes
before the SDA, methyldicyclohexylamine (MDCHA), (8.682 g, 44.443
mmol, Aldrich) was added dropwise to the mixture. The remaining
water (38.92 g) was then added achieving a total 70 moles of water,
maintaining substantial phase purity to avoid heavy, or dense,
phase impurity formation, like chabazite. The composition of the
gel was 1.00Al:0.85P:0.03Zn:0.03Mg:0.20Si:0.8SDA:70H.sub.2O. The
resulting gel was aged for 25 minutes before being transferred to
Teflon-lined tubes inside stainless steel autoclaves. Teflon lined
autoclaves are important for phase purity as glass or metal
autoclaves with no lining lead to phase impurity formation. The
sealed autoclaves were heated under autogenous pressure under
static conditions in a conventional oven at 180.degree. C. for 2
hours. The autoclaves were quenched with cold water and the
resulting product was filtered, washed with water, and dried gently
at 90.degree. C.
[0090] Calcination was carried out in a tube furnace (Lenton)
heated at 3.degree. C./minute under a steady nitrogen flow until
the temperature reached 550.degree. C. The sample was then held
under the nitrogen flow for 2 hours. After 2 hours the gas was
changed to dry air and the sample was held under a constant gentle
flow of air for 12 hours at 550.degree. C. before being allowed to
cool gently at a rate of approximately 5.degree. C./minute to room
temperature.
Example 3
Zn.sup.IIAlPO-5
TABLE-US-00002 [0091] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.321 77.95 0.0554 1.000 0.0292 0
H.sub.3PO.sub.4 (85%) 7.234 97.93 0.0627 1.133 2.9% 0 190 Silica 0
60.09 0 0.000 Mg acetate.cndot.4H.sub.2O 0 214.46 0 0.000 Zn
Acetate 0.306 183.46 0.0016 0.030 MDCHA 8.5 195.35 0.0435 0.785
H.sub.2O 70 18 3.8888 70.155
Example 4
Mg.sup.IIAlPO-5
TABLE-US-00003 [0092] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.321 77.95 0.0554 1.000 0.0291 0
H.sub.3PO.sub.4 (85%) 7.112 97.93 0.0617 1.114 2.9% 0 200 Silica 0
60.09 0 0.000 Mg acetate.cndot.4H.sub.2O 0.357 214.46 0.0016 0.030
Zn Acetate 0 183.46 0 0.000 Cyclohexylamine 8.7495 99.17 0.0882
1.592 H.sub.2O 68 18 3.7777 68.150
Example 5
Si.sup.IVAlPO-5
TABLE-US-00004 [0093] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.321 77.95 0.0554 1.000 0 0.194024
H.sub.3PO.sub.4 (85%) 5.392 97.93 0.0468 0.844 0% 19% 180 Silica
0.677 60.09 0.0112 0.203 Mg acetate.cndot.4H.sub.2O 0 214.46 0
0.000 Zn Acetate 0 183.46 0 0.000 MDCHA 8.7495 195.35 0.0447 0.808
H.sub.2O 76 18 4.2222 76.168
Example 6
Zn.sup.IIMg.sup.IIAlPO-5
TABLE-US-00005 [0094] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.321 77.95 0.0554 1.000 0.0567 0
H.sub.3PO.sub.4 (85%) 7.423 97.93 0.0644 1.162 5.7% 0 190 Silica 0
60.09 0 0.000 Mg acetate.cndot.4H.sub.2O 0.357 214.46 0.0016 0.030
Zn Acetate 0.306 183.46 0.0016 0.030 TPAOH 8.7495 203.36 0.0430
0.776 H.sub.2O 57 18 3.1666 57.126
Example 7
Mg.sup.IISi.sup.IVAlPO-5
TABLE-US-00006 [0095] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.321 77.95 0.0554 1.000 0.02915
0.194024 H.sub.3PO.sub.4 (85%) 5.392 97.93 0.0468 0.844 2.9% 19.4%
180 Silica 0.677 60.09 0.0112 0.203 Mg acetate.cndot.4H.sub.2O
0.357 214.46 0.0016 0.030 Zn Acetate 0 183.46 0 0.000 MDCHA 8.7495
195.35 0.0447 0.808 H.sub.2O 65 18 3.6111 65.144
Example 8
Zn.sup.IISi.sup.IVAlPO-5
TABLE-US-00007 [0096] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.321 77.95 0.0554 1.000 0.0292
0.175455 H.sub.3PO.sub.4 (85%) 6.1 97.93 0.0529 0.955 2.9% 17.5%
180 Silica 0.677 60.09 0.0112 0.203 Mg acetate.cndot.4H.sub.2O 0
214.46 0 0.000 Zn Acetate 0.306 183.46 0.0016 0.030 MDCHA 8.7495
195.35 0.0447 0.808 H.sub.2O 50 18 2.7777 50.111
Example 9
Mg.sup.IITi.sup.IIAlPO-5
TABLE-US-00008 [0097] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.321 77.95 0.0554 1.000 0.0567 0
H.sub.3PO.sub.4 (85%) 7.423 97.93 0.0644 1.162 5.7% 0% 200 Silica 0
60.09 0.0000 0.000 Mg acetate.cndot.4H.sub.2O 0.357 214.46 0.0017
0.030 Ti isopropoxide 0.474 284.26 0.0017 0.030 TPAOH 8.7495 203.36
0.0430 0.776 H.sub.2O 57 18 3.1667 57.126
Example 10
Zn.sup.IIMg.sup.IISi.sup.IVAlPO-5
TABLE-US-00009 [0098] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.321 77.95 0.0554 1.000 0.0567
0.177884 H.sub.3PO.sub.4 (85%) 5.999 97.93 0.0520 0.939 5.7% 17.8%
200 Silica 0.677 60.09 0.0112 0.203 Mg acetate.cndot.4H.sub.2O
0.357 214.46 0.0016 0.030 Zn Acetate 0.306 183.46 0.0016 0.030
MDCHA 8.7495 195.35 0.0447 0.808 H.sub.2O 60 18 3.3333 60.133
Example 11
Zn.sup.IIAlPO-18
TABLE-US-00010 [0099] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.22 77.95 0.0541 1.000 0.03130 0.0
H.sub.3PO.sub.4 (85%) 6.35 97.93 0.0551 1.018 3.1% 0.0% 160 Silica
0 60.09 0 0.000 Mg acetate.cndot.4H.sub.2O 0 214.46 0 0.000 Zn
Acetate 0.321 183.46 0.0017 0.032 DIPE 8.5 129.25 0.0657 1.215
H.sub.2O 65 18 3.6111 66.703
Example 12
Mg.sup.IIAlPO-18
TABLE-US-00011 [0100] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.123 77.95 0.0528 1.000 0.0239 0
H.sub.3PO.sub.4 (85%) 6.432 97.93 0.0558 1.055 2.4% 0 150 Silica 0
60.09 0 0.000 Mg acetate.cndot.4H.sub.2O 3.572 214.46 0.0166 0.315
Zn Acetate 0 183.46 0 0.000 DIPE 8.7495 129.25 0.0676 1.280
H.sub.2O 70 18 3.8888 73.524
Example 13
Si.sup.IVAlPO-18
TABLE-US-00012 [0101] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.753 77.95 0.0609 1.000 0 0.202144
H.sub.3PO.sub.4 (85%) 6.213 97.93 0.0539 0.884 0% 20.2% 170 Silica
0.821 60.09 0.0136 0.224 Mg acetate.cndot.4H.sub.2O 0 214.46 0
0.000 Zn Acetate 0 183.46 0 0.000 DIPE 8.7495 129.25 0.0676 1.110
H.sub.2O 65 18 3.6111 59.223
Example 14
Zn.sup.IIMg.sup.IIAlPO-18
TABLE-US-00013 [0102] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.652 77.95 0.0596 1.000 0.0586 0
H.sub.3PO.sub.4 (85%) 7.345 97.93 0.0637 1.068 5.9% 0 165 Silica 0
60.09 0 0.000 Mg acetate.cndot.4H.sub.2O 0.356 214.46 0.0016 0.028
Zn Acetate 0.378 183.46 0.0020 0.035 TEA 8.7495 101.07 0.0865 1.451
H.sub.2O 75 18 4.1666 69.818
Example 15
Mg.sup.IISi.sup.IVAlPO-18
TABLE-US-00014 [0103] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.329 77.95 0.0555 1.000 0.0255
0.145633 H.sub.3PO.sub.4 (85%) 7.345 97.93 0.0637 1.148 2.6% 14.6%
170 Silica 0.653 60.09 0.0108 0.196 Mg acetate.cndot.4H.sub.2O
0.312 214.46 0.0014 0.026 Zn Acetate 0 183.46 0 0.000 DIPE 8.7495
129.25 0.0676 1.219 H.sub.2O 66 18 3.6666 66.024
Example 16
Zn.sup.IISi.sup.IVAlPO-18
TABLE-US-00015 [0104] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.229 77.95 0.0542 1.000 0.03724
0.193605 H.sub.3PO.sub.4 (85%) 5.678 97.93 0.0492 0.908 3.7% 19.4%
170 Silica 0.711 60.09 0.0118 0.218 Mg acetate.cndot.4H.sub.2O 0
214.46 0 0.000 Zn Acetate 0.385 183.46 0.0020 0.039 TEA 8.7495
101.07 0.0865 1.596 H.sub.2O 68 18 3.7777 69.633
Example 17
Zn.sup.IIMg.sup.IISi.sup.IVAlPO-18
TABLE-US-00016 [0105] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.231 77.95 0.0542 1.000 0.0579
0.172101 H.sub.3PO.sub.4 (85%) 6.567 97.93 0.0569 1.050 5.8% 17.2%
165 Silica 0.712 60.09 0.0118 0.218 Mg acetate.cndot.4H.sub.2O
0.367 214.46 0.0017 0.032 Zn Acetate 0.299 183.46 0.0016 0.030 DIPE
8.7495 129.25 0.0676 1.247 H.sub.2O 50 18 2.7777 51.177
Example 18
Zn.sup.IIAlPO-34
TABLE-US-00017 [0106] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.111 77.95 0.0527 1.000 0.0377 0.0
H.sub.3PO.sub.4 (85%) 6.935 97.93 0.0601 1.141 3.7% 0.0% 170 Silica
0 60.09 0 0.000 Mg acetate.cndot.4H.sub.2O 0 214.46 0 0.000 Zn
Acetate 0.38 183.46 0.0020 0.039 TEA 8.5 101.07 0.0841 1.595
H.sub.2O 40 18 2.2222 42.136
Example 19
Mg.sup.IIAlPO-34
TABLE-US-00018 [0107] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.222 77.95 0.0541 1.000 0.0315 0
H.sub.3PO.sub.4 (85%) 7.113 97.93 0.0617 1.140 3.2% 0 170 Silica 0
60.09 0 0.000 Mg acetate.cndot.4H.sub.2O 0.378 214.46 0.0017 0.033
Zn Acetate 0 183.46 0 0.000 TEA 8.7495 101.07 0.0865 1.598 H.sub.2O
45 18 2.5 46.157
Example 20
Si.sup.IVAlPO-34
TABLE-US-00019 [0108] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.234 77.95 0.0543 1.000 0 0.211847
H.sub.3PO.sub.4 (85%) 5.892 97.93 0.0511 0.942 0% 21.2% 160 Silica
0.826 60.09 0.0137 0.253 Mg acetate.cndot.4H.sub.2O 0 214.46 0
0.000 Zn Acetate 0 183.46 0 0.000 MOR 8.7495 87.12 0.1004 1.849
H.sub.2O 35 18 1.9444 35.798
Example 21
Zn.sup.IIMg.sup.IIAlPO-34
TABLE-US-00020 [0109] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 3.911 77.95 0.0501 1.000 0.0691 0
H.sub.3PO.sub.4 (85%) 5.974 97.93 0.0518 1.033 6.9% 0 180 Silica 0
60.09 0 0.000 Mg acetate.cndot.4H.sub.2O 0.345 214.46 0.0016 0.032
Zn Acetate 0.389 183.46 0.0021 0.042 TEA 8.7495 101.07 0.0865 1.725
H.sub.2O 45 18 2.5 49.827
Example 22
Mg.sup.IISi.sup.IVAlPO-34
TABLE-US-00021 [0110] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.012 77.95 0.0514 1.000 0.0303
0.201621 H.sub.3PO.sub.4 (85%) 5.231 97.93 0.0454 0.882 3.0% 20.2%
170 Silica 0.689 60.09 0.0114 0.223 Mg acetate.cndot.4H.sub.2O
0.345 214.46 0.0016 0.031 Zn Acetate 0 183.46 0 0.000 MOR 8.7495
87.12 0.1004 1.951 H.sub.2O 56 18 3.1111 60.446
Example 23
Zn.sup.IISi.sup.IVAlPO-34
TABLE-US-00022 [0111] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 3.92 77.95 0.0502 1.000 0.0327
0.208683 H.sub.3PO.sub.4 (85%) 5.351 97.93 0.0464 0.924 3.3% 20.9%
160 Silica 0.736 60.09 0.0122 0.244 Mg acetate.cndot.4H.sub.2O 0
214.46 0 0.000 Zn Acetate 0.312 183.46 0.0017 0.034 TEAOH 8.7495
147.27 0.0594 1.181 H.sub.2O 60 18 3.3333 66.284
Example 24
Zn.sup.IIMg.sup.IISi.sup.IVAlPO-34
TABLE-US-00023 [0112] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.502 77.95 0.0577 1.000 0.0460
0.177342 H.sub.3PO.sub.4 (85%) 5.541 97.93 0.0480 0.833 4.6% 17.7%
160 Silica 0.623 60.09 0.0103 0.180 Mg acetate.cndot.4H.sub.2O
0.299 214.46 0.0013 0.024 Zn Acetate 0.256 183.46 0.0013 0.024 MOR
8.7495 87.12 0.1004 1.739 H.sub.2O 60 18 3.3333 57.715
Example 25
Zn.sup.IIAlPO-36
TABLE-US-00024 [0113] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.322 77.95 0.0554 1.000 0.0368 0.0
H.sub.3PO.sub.4 (85%) 5.472 97.93 0.0474 0.857 3.7% 0.0% 190 Silica
0 60.09 0 0.000 Mg acetate.cndot.4H.sub.2O 0 214.46 0 0.000 Zn
Acetate 0.389 183.46 0.0021 0.038 EDCHA 8.5 209.37 0.0405 0.732
H.sub.2O 50 18 2.7777 50.099
Example 26
Mg.sup.IIAlPO-36
TABLE-US-00025 [0114] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.444 77.95 0.0570 1.000 0.0311 0
H.sub.3PO.sub.4 (85%) 6.689 97.93 0.0580 1.018 3.1% 0 200 Silica 0
60.09 0 0.000 Mg acetate.cndot.4H.sub.2O 0.393 214.46 0.0018 0.032
Zn Acetate 0 183.46 0 0.000 EDCHA 8.7495 209.37 0.0417 0.733
H.sub.2O 56 18 3.1111 54.570
Example 27
Si.sup.IVAlPO-36
TABLE-US-00026 [0115] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.201 77.95 0.0538 1.000 0 0.243034
H.sub.3PO.sub.4 (85%) 5.5 97.93 0.0477 0.886 0% 24.3% 180 Silica
0.921 60.09 0.0153 0.284 Mg acetate.cndot.4H.sub.2O 0 214.46 0
0.000 Zn Acetate 0 183.46 0 0.000 EDCHA 8.7495 209.37 0.0417 0.775
H.sub.2O 80 18 4.4444 82.467
Example 28
Zn.sup.IIMg.sup.IIAlPO-36
TABLE-US-00027 [0116] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 3.901 77.95 0.0500 1.000 0.0637 0
H.sub.3PO.sub.4 (85%) 7.543 97.93 0.0654 1.308 6.4% 0 190 Silica 0
60.09 0 0.000 Mg acetate.cndot.4H.sub.2O 0.367 214.46 0.0017 0.034
Zn Acetate 0.311 183.46 0.0016 0.034 EDCHA 8.7495 209.37 0.0417
0.835 H.sub.2O 70 18 3.8888 77.708
Example 29
Mg.sup.IISi.sup.IVAlPO-36
TABLE-US-00028 [0117] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.342 77.95 0.0557 1.000 0.0246
0.138867 H.sub.3PO.sub.4 (85%) 6.456 97.93 0.0560 1.006 2.5% 13.9%
190 Silica 0.543 60.09 0.0090 0.162 Mg acetate.cndot.4H.sub.2O
0.302 214.46 0.0014 0.025 Zn Acetate 0 183.46 0 0.000 TPA 8.7495
143.27 0.0610 1.096 H.sub.2O 65 18 3.6111 64.829
Example 30
Zn.sup.IISi.sup.IVAlPO-36
TABLE-US-00029 [0118] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.321 77.95 0.0554 1.000 0.0284
0.1549723 H.sub.3PO.sub.4 (85%) 6.231 97.93 0.0540 0.976 2.8% 15.5%
200 Silica 0.596 60.09 0.0099 0.179 Mg acetate.cndot.4H.sub.2O 0
214.46 0 0.000 Zn Acetate 0.298 183.46 0.0016 0.029 TPA 8.7495
143.27 0.0610 1.102 H.sub.2O 70 18 3.8888 70.155
Example 31
Zn.sup.iiMg.sup.IISi.sup.IVAlPO-36
TABLE-US-00030 [0119] Mass RMM Moles Ratio M Loading Silica Loading
Temp (.degree. C.) Al(OH).sub.3 4.229 77.95 0.0542 1.000 0.0617
0.1411797 H.sub.3PO.sub.4 (85%) 5.925 97.93 0.0514 0.948 6.2% 14.1%
190 Silica 0.508 60.09 0.0084 0.156 Mg acetate.cndot.4H.sub.2O
0.311 214.46 0.0014 0.027 Zn Acetate 0.389 183.46 0.0021 0.039
EDCHA 8.7495 209.37 0.0417 0.770 H.sub.2O 57 18 3.1666 58.369
Example 32
Phase Purity
[0120] In FIGS. 1 through 3, the XRD patterns of the mono- and
bi-metallic substituted AlPOs of this invention are shown,
respectively. The patterns were compared with the AFI reported
powder pattern from the IZA website (FIG. 5(A)) and various
published reports. The FIGS. 1 through 3 show that a very high
level of AFI structure phase purity and crystallinity is achieved
even after metal substitution. The Celref analysis in FIG. 4 also
shows an almost perfect correlation between observed and
theoretically calculated peaks. In most cases, a difference in
2theta of less than 0.1000.degree. was observed. Similar analysis
was performed on the Mg.sup.IIZn.sup.IISi.sup.IV, AlPO-5 catalysts
also showing a strong correlation between the calculated and
observed peaks. Again, in almost all cases, differences of 2theta
were smaller than 0.1000.degree. as shown below in Table 2.
TABLE-US-00031 TABLE 2 Refined Final Values for
Mg.sup.IIZn.sup.IISi.sup.IVAlPO-5 Lambda a b c alpha beta gamma
volume 1.54000 13.6900 13.6900 8.4730 90.00 90.00 120.00 1375.22 h
k l 2Theta (observed) 2Theta (calculated) Difference 0 1 0 7.54
7.4476 0.0924 1 1 0 12.98 12.9179 0.0621 0 2 0 14.94 14.9269 0.0131
1 2 0 19.84 19.7888 0.0512 0 3 0 22.52 22.4708 0.0492 1 1 2 24.76
24.7342 0.0258 2 2 0 25.98 26.0037 -0.0237 1 3 1 29.14 29.0953
0.0447 0 4 0 30.08 30.1149 -0.0349 2 2 2 33.78 33.6833 0.0967 1 4 0
34.54 34.6298 -0.0898 0 4 2 37.04 36.9699 0.0701 0 5 0 37.86
37.8989 -0.0389 2 4 1 41.68 41.6456 0.0344 1 5 0 42.36 42.3980
-0.0380 0 1 4 43.24 43.3407 -0.1007 1 5 1 43.90 43.7833 0.1167 2 5
0 47.80 47.8565 -0.0565 1 6 1 51.64 51.6307 0.0093 2 5 2 52.80
52.7769 0.0231 2 6 0 55.70 55.8529 -0.1529
Example 33
[0121] Metal-substituted catalysts of the invention prepared
according to the general procedure described above, as exemplified
in Examples 1 through 31, were evaluated as follows in the liquid
phase:
[0122] The catalytic reactions were carried out in a
stainless-steel high-pressure 0.1 liter Parr 4590 catalytic reactor
lined with Poly Ether Ether Ketone (PEEK) that uses a 4843 Parr
controller. The substrate (typically 10 g), a suitable internal
standard (tetralin; 50 mg), and the isomorphously metal-substituted
AlPO catalyst (0.2 g, calcined at 823 K for 8 h prior to the
catalytic tests), were introduced into the reactor, which was
subsequently sealed. The reactor and the inlet and outlet ports
were purged three times with dry nitrogen prior to reaction. The
contents were stirred at 1200 rpm and the reactor was heated to the
desired temperature under autogeneous pressure (N2). Optionally,
the contents of the reactor can be pressurized to several bar of N2
(<60 bar), in order to keep the contents in the liquid-phase and
minimize gas-phase reactions.
[0123] At the end of the reaction, the heating was turned off and
the contents of the reactor were cooled (quenched) to 290 K. A
mass-balance calculation was performed at this stage to check for
handling and mass losses. Where kinetic and rate effects were
studied, a mini-robot liquid sampling valve was employed to remove
small aliquots (0.1 .mu.l) of the sample during the course of the
reaction. These data are displayed in the kinetic traces of FIGS. 5
through 8. The products were analyzed either online (using a
robotically-controlled unit with an online computer-controlled
system which is linked to a GC and/or LCMS) or offline by a Varian
Star 3400CX gas chromatograph employing a HP-1 capillary column
cross-linked with methylsiloxane (30 m.times.0.32 mm.times.1 .mu.m
film thickness) and a flame ionization detector using a variable
ramp temperature program (from 40.degree. C. to 200.degree. C.).
The identities of the products were confirmed using authenticated
standards and their individual response factors were determined
using the internal standard calibration method. The overall yields
were normalized with respect to the (GC) response factors obtained
as above and the conversions and selectivities were determined by
the following equations:
Conv. %=[(moles of initial substrate-moles of residual
substrate)/(moles of initial substrate)].times.100
Sel. %=[(moles of individual product)/(moles of total
products)].times.100
[0124] For the internal standard GC method, the response factor
(RF) and mol % of individual products were calculated using the
following equations:
RF=(mol Product/mol Standard).times.(Area Standard/Area
Product)
Mol % Product=RF.times.Mol Standard.times.(Area Product/Area
Standard).times.100/Mol Sample
TABLE-US-00032 TABLE 3 Efficacy of Multi-Substituted Bronsted-Acid
Sites for the Catalytic Dehydration of Ethanol Total Ethylene
Temperature TOF Conversion Conv. Catalyst (K) (h.sup.-1) (mol. %)
(mol. %) Mg.sup.IISi.sup.IVAlPO-5 453 656 78.5 88
Zn.sup.IISi.sup.IVAlPO-18 463 575 72.8 92 Zn.sup.IISi.sup.IVAlPO-5
453 680 80.7 89 Zn.sup.IITi.sup.IVAlPO-18 453 466 61.2 88
Mg.sup.IISi.sup.IVAlPO-5 423 700 75.7 98 Mg.sup.IITi.sup.IVAlPO-36
433 415 51.2 82 Mg.sup.IISi.sup.IVAlPO-18 443 578 78.8 91
Mg.sup.IITi.sup.IVAlPO-5 453 527 60.0 85 Zn.sup.IISi.sup.IVAlPO-5
353 65 9.5 99+ Zn.sup.IITi.sup.IVAlPO-36 443 500 61.2 88
Mg.sup.IISi.sup.IVAlPO-34 433 691 81.3 93 Mg.sup.IISi.sup.IVAlPO-18
353 38 5.0 98 Mg.sup.IISi.sup.IVAlPO-5 423 712 70.0 96
TABLE-US-00033 TABLE 4 Efficacy of Single-Substituted Bronsted-Acid
Sites for the Catalytic Dehydration of Ethanol Total Ethylene
Temperature TOF Conversion Conv. Catalyst (K) (h.sup.-1) (mol.%)
(mol.%) Si.sup.IVAlPO-5 453 420 48.0 92 Ti.sup.IVAlPO-36 433 305
41.2 76 Ti.sup.IVAlPO-5 453 345 40.0 75 Si.sup.IVAlPO-34 453 480
53.7 96 Si.sup.IVAlPO-18 463 545 58.8 97 Ti.sup.IVAlPO-36 443 290
35.3 65 Si.sup.IVAlPO-5 353 51 8.0 99+ Si.sup.IVAlPO-18 353 35 4.2
97 Ti.sup.IVAlPO-18 453 310 41.2 68 Ti.sup.IVAlPO-34 443 345 45.0
66 Si.sup.IVAlPO-5 453 413 55.7 91 Si.sup.IVAlPO-18 443 480 51.8 98
Si.sup.IVAlPO-36 453 486 59.5 90 Mg.sup.IIAlPO-5 463 466 61.5 96
Zn.sup.IIAlPO-18 473 515 63.2 99+ Mg.sup.IIAlPO-36 473 385 68.2 95
Mg.sup.IIAlPO-34 353 21 3.3 92 Zn.sup.IIAlPO-5 483 500 70.7 94
Mg.sup.IIAlPO-34 453 491 66.3 99+ Zn.sup.IIAlPO-36 463 566 61.7 95
Mg.sup.IIAlPO-18 443 499 58.8 99+ Mg.sup.IIAlPO-5 353 56 6.5
99+
Example 34
[0125] Metal-substituted catalysts of the invention prepared
according to the general procedure described above, as exemplified
in Examples 8, were evaluated by the general procedure above, as
exemplified in Example 33, in the liquid phase:
TABLE-US-00034 TABLE 5 Efficacy of Multi-Substituted Bronsted-Acid
Sites for the Catalytic Dehydration of Propanol Total Propylene
Temperature Conversion Conv. Catalyst (K) (mol. %) (mol. %)
Mg.sup.IISi.sup.IVZn.sup.IIAlPO-5 423 74.0 93
* * * * *
References