U.S. patent application number 11/814843 was filed with the patent office on 2008-06-19 for process for dehydrating glycerol to acrolein.
This patent application is currently assigned to Arkema France. Invention is credited to Jean-Luc Dubois, Christophe Duquenne, Wolfgang Holderich.
Application Number | 20080146852 11/814843 |
Document ID | / |
Family ID | 35170070 |
Filed Date | 2008-06-19 |
United States Patent
Application |
20080146852 |
Kind Code |
A1 |
Dubois; Jean-Luc ; et
al. |
June 19, 2008 |
Process For Dehydrating Glycerol To Acrolein
Abstract
The present invention relates to a process for manufacturing
acrolein by dehydration of glycerol in the presence of molecular
oxygen. The reaction is performed in the liquid phase or in the gas
phase in the presence of a solid catalyst. The addition of oxygen
makes it possible to obtain good glycerol conversion by inhibiting
the deactivation of the catalyst and the formation of
by-products.
Inventors: |
Dubois; Jean-Luc; (Millery,
FR) ; Duquenne; Christophe; (Chaussoy-Epagny, FR)
; Holderich; Wolfgang; (Frankenthal-Allemagne,
DE) |
Correspondence
Address: |
ARKEMA INC.;PATENT DEPARTMENT - 26TH FLOOR
2000 MARKET STREET
PHILADELPHIA
PA
19103-3222
US
|
Assignee: |
Arkema France
Colombes
FR
|
Family ID: |
35170070 |
Appl. No.: |
11/814843 |
Filed: |
January 6, 2006 |
PCT Filed: |
January 6, 2006 |
PCT NO: |
PCT/EP2006/000735 |
371 Date: |
July 26, 2007 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
|
|
60689395 |
Jun 10, 2005 |
|
|
|
Current U.S.
Class: |
568/449 |
Current CPC
Class: |
C07C 45/52 20130101;
C07C 45/52 20130101; C07C 47/22 20130101 |
Class at
Publication: |
568/449 |
International
Class: |
C07C 45/52 20060101
C07C045/52 |
Foreign Application Data
Date |
Code |
Application Number |
Feb 15, 2005 |
FR |
0501499 |
Claims
1. Process for manufacturing acrolein by dehydration of glycerol in
the presence of an amount of molecular oxygen chosen so as to be
outside the flammability range at any point in the process.
2. Process according to claim 1, characterized in that the
molecular oxygen is in the form of air or in the form of a mixture
of gases containing molecular oxygen.
3. Process according to claim 1, characterized in that the glycerol
is in the form of an aqueous solution with a concentration of
between 10% and 50% by weight in the reactor.
4. Process according to claim 1, characterized in that an acidic
solid catalyst with a Hammett acidity H.sub.0 of less than +2 is
used.
5. Process according to claim 4, characterized in that the catalyst
is selected from natural siliceous materials, synthetic siliceous
materials, acidic zeolites, mineral supports, oxides, mixed oxides,
or heteropolyacids.
6. Process according to claim 4, characterized in that the catalyst
is chosen from zeolites, composites based on sulfonic acid of
fluorinated polymers, chlorinated aluminas, phosphotungstic acids
and salts, silicotungstic acids and acid salts, and solids of metal
oxide.
7. Process according to claim 4, characterized in that the catalyst
is selected from sulfate zirconias, phosphate zirconias, tungsten
zirconias, siliceous zirconias, sulfate titanium oxides, sulfate
tin oxides, phosphate aluminas or phosphate silicas.
8. Process according to claim 1, characterized in that the
dehydration reaction is performed in the gas phase.
9. Process according to claim 8, characterized in that the reaction
is performed in a fixed-bed reactor, a fluidized-bed reactor or a
circulating fluidized-bed reactor.
10. Process according to claim 1, characterized in that it is
performed in a plate heat exchanger.
11. Process according to claim 1, characterized in that the
dehydration reaction is performed in the liquid phase.
12. Process according to claim 1, characterized in that the
glycerol is in the form of an aqueous solution with a concentration
of between 15% and 30% by weight in the reactor.
13. Process according to claim 5, characterized in that said
mineral supports is selected from oxides, coated with mono-, di-,
tri- or polyacidic inorganic acids.
14. Process according to claim 6, characterized in that the solids
of metal oxide are selected from tantalum oxide Ta.sub.2O.sub.5,
niobium oxide Nb.sub.2O.sub.5, alumina Al.sub.2O.sub.3, titanium
oxide TiO.sub.2, zirconia ZrO.sub.2, tin oxide SnO.sub.2, silica
SiO.sub.2 or silico-aluminate SiO.sub.2--Al.sub.2O.sub.3.
15. Process according to claim 14, characterized in that the solids
of metal oxide are impregnated with acidic functions selected from
borate BO.sub.3, sulfate SO.sub.4, tungstate WO.sub.3, phosphate
PO.sub.4, silicate SiO.sub.2 or molybdate MoO.sub.3.
Description
[0001] The present invention relates to a process for manufacturing
acrolein by dehydration of glycerol in the presence of molecular
oxygen.
[0002] Acrolein is the simplest of the unsaturated aldehydes. It is
also known as 2-propenal, acrylaldehyde or acrylic aldehyde. As a
result of its structure, acrolein has high reactive power by virtue
of the presence of its two reactive functions, which are capable of
reacting individually or together. It is for this reason that
acrolein finds many applications, especially as a synthetic
intermediate. It is in particular a key intermediate for the
synthesis of methionine, a synthetic protein used as an animal feed
supplement, which has established itself as a substitute for
fishmeal. Acrolein is a non-isolated synthetic intermediate of
acrylic acid in the industrial production of acrylic acid by
catalytic oxidation of propylene in the gas phase. The importance
of the chemistry of acrylic acid and its derivatives is known.
Acrolein also leads, via reaction with methyl vinyl ether followed
by hydrolysis, to glutaraldehyde, which has many uses in leather
tanning, as a biocidal agent in oil well drilling and during the
processing of cutting oils, and as a chemical disinfectant and
sterilizing agent for hospital equipment.
[0003] Acrolein is usually used as a synthetic intermediate of
derivatives that are synthesized on the site of production to
minimize the transportation of acrolein from the manufacturer to
the client. The essential reason is linked to the toxicity of
acrolein, which leads industrials to avoid the storage and
transportation of this chemical product.
[0004] The most commonly used process for producing acrolein is
based on the gas-phase catalytic oxidation reaction of propylene
with atmospheric oxygen. The acrolein thus obtained may then be
incorporated directly into an acrylic acid manufacturing process.
When acrolein is used as starting material for the synthesis of
methionine or for fine chemistry reactions, a purification section
allows the removal of the reaction by-products, mainly carbon
oxides, acrylic acid, acetic acid and acetaldehyde.
[0005] The production of acrolein is thus highly dependent on the
propylene starting material obtained by steam cracking or catalytic
cracking of petroleum fractions. This starting material, of fossil
origin, furthermore contributes towards increasing the greenhouse
effect. It thus appears necessary to have available an acrolein
synthesis process that is not dependent on propylene as resource
and that uses another starting material, which is preferably
renewable. This process would be particularly advantageous for the
synthesis of methionine, which might then be said to be "obtained
from biomass". Specifically, during its use in animal feed,
methionine is rapidly metabolized and the carbon dioxide expelled
into the atmosphere contributes towards increasing the greenhouse
effect. If acrolein is obtained from a renewable starting material,
for example obtained from plant oil, the CO.sub.2 emissions no
longer enter into the process balance, since they compensate for
the carbon dioxide used by the biomass for its growth; there is
therefore no increase in the greenhouse effect. Such a process thus
satisfies the criteria associated with the new concept of "green
chemistry" within a more global context of durable development.
[0006] It has been known for a long time that glycerol can lead to
the production of acrolein. Glycerol (also known as glycerine) is
derived from the methanolysis of plant oils at the same time as the
methyl esters, which are themselves used especially as fuels or
combustibles in diesel and domestic fuel oil. It is a natural
product that has an "environmentally friendly" image, is available
in large amount and may be stored and transported without
difficulty. Many studies have been devoted to the financial
upgrading of glycerol according to its degree of purity, and the
dehydration of glycerol to acrolein is one of the routes
envisaged.
[0007] The reaction involved for obtaining acrolein from glycerol
is:
CH.sub.2OH--CHOH--CH.sub.2OH ? CH.sub.2=CH--CHO+2H.sub.2O
[0008] As a general rule, the hydration reaction is favoured at low
temperatures, and the dehydration reaction is favoured at high
temperatures. To obtain acrolein, it is thus necessary to use a
sufficient temperature, and/or partial vacuum to shift the
reaction. The reaction may be performed in the liquid phase or in
the gas phase. This type of reaction is known to be catalysed by
acids.
[0009] According to patent FR 695 931, acrolein is obtained by
passing glycerol vapours at a sufficiently high temperature over
salts of acids containing at least three acid functions, for
instance phosphoric acid salts. The yields indicated are greater
than 75% after fractional distillation.
[0010] In U.S. Pat. No. 2,558,520, the dehydration reaction is
performed in the gas/liquid phase in the presence of diatomaceous
earths impregnated with phosphoric acid salts, suspended in an
aromatic solvent. A degree of conversion of the glycerol into
acrolein of 72.3% is obtained under these conditions.
[0011] The process described in patent application WO 99/05085 is
based on a complex homogeneous catalysis, under a CO/H.sub.2
atmosphere at a pressure of 20/40 bar and in the presence of a
solvent such as an aqueous solution of sulfolane.
[0012] Chinese patent application CN 1 394 839 relates to a process
for preparing 3-hydroxypropanaldehyde from glycerol. The acrolein
produced as reaction intermediate is obtained by passing vaporized
pure glycerol over a catalyst of potassium sulfate or magnesium
sulfate type. The reaction yields are not given.
[0013] U.S. Pat. No 5,387,720 describes a process for producing
acrolein by dehydration of glycerol, in the liquid phase or in the
gas phase over acidic solid catalysts defined by their Hammett
acidity. The catalysts must have a Hammett acidity of less than +2
and preferably less than -3. These catalysts correspond, for
example, to natural or synthetic siliceous materials, for instance
mordenite, montmorillonite, acidic zeolites; supports, such as
oxides or siliceous materials, for example alumina
(Al.sub.2O.sub.3), titanium oxide (TiO.sub.2), coated with mono-,
di- or triacidic inorganic acids; oxides or mixed oxides such as
gamma-alumina, the mixed oxide ZnO-Al.sub.2O.sub.3, or
alternatively heteropolyacids. According to the said patent, an
aqueous solution comprising from 10% to 40% of glycerol is used,
and the process is performed at temperatures of between 180.degree.
C. and 340.degree. C. in the liquid phase, and between 250.degree.
C. and 340.degree. C. in the gas phase. According to the authors of
the said patent, the gas-phase reaction is preferable since it
enables a degree of conversion of the glycerol of close to 100% to
be obtained, which leads to an aqueous acrolein solution containing
side products. A proportion of about 10% of the glycerol is
converted into hydroxypropanone, which is present as the major
by-product in the acrolein solution. The acrolein is recovered and
purified by fractional condensation or distillation. For a
liquid-phase reaction, a conversion limited to 15-25% is desired,
to avoid excessive loss of selectivity. U.S. Pat. No. 5,426,249
describes the same gas-phase process for the dehydration of
glycerol to acrolein, but followed by a hydration of the acrolein
and a hydrogenation to lead to 1,2- and 1,3-propanediol.
[0014] The dehydration reaction of glycerol to acrolein is thus
generally accompanied by side reactions leading to the formation of
by-products such as hydroxypropanone, propanaldehyde, acetaldehyde,
acetone, adducts of acrolein with glycerol, glycerol
polycondensation products, cyclic glycerol ethers, etc., but also
phenol and polyaromatic compounds, which are the cause of the
formation of coke on the catalyst. This results, firstly, in a
reduction in the yield of and the selectivity towards acrolein, and
secondly in deactivation of the catalyst. The presence of
by-products in the acrolein, such as hydroxypropanone or
propanaldehyde, some of which are moreover difficult to isolate,
necessitates separation and purification steps, which lead to high
recovery costs for the purified acrolein. Moreover, it is necessary
to regenerate the catalyst very regularly in order to regain
satisfactory catalytic activity.
[0015] The Applicant Company has sought to solve these problems and
has found many advantages in using molecular oxygen during the
reaction for the dehydration of glycerol to acrolein. It has been
observed, surprisingly, that supplying oxygen reduces the formation
of aromatic compounds such as phenol, and of by-products
originating from a hydrogenation of dehydrated products, for
instance propanaldehyde and acetone, but also from
hydroxypropanone. The formation of coke on the catalyst is reduced.
This results in inhibition of the deactivation of the catalyst and
continuous regeneration of the catalyst. Certain by-products are
found to be present in markedly lower amount, which facilitates the
subsequent purification steps.
[0016] One subject of the present invention is thus a process for
manufacturing acrolein by dehydration of glycerol in the presence
of molecular oxygen. The molecular oxygen may be present in the
form of air or in the form of a mixture of gases containing
molecular oxygen. The amount of oxygen is chosen so as to be
outside the flammability range at any point in the plant. From FIG.
4 of U.S. patent application 2004/15012, the maximum oxygen
content, in an acrolein/O.sub.2/N.sub.2 mixture is about 7% by
volume in order to be entirely outside the flammability range. The
oxygen content in the process according to the invention will
generally be chosen so as not to exceed 7% relative to the mixture
of gases entering the reaction (mixture of
glycerol/H.sub.2O/oxygen/inert gases). Preferably, the oxygen
content is less than 7% relative to the dry gas mixture leaving the
reactor (mixture of acrolein/oxygen/inert gases).
[0017] The dehydration reaction is performed on acidic solid
catalysts. The catalysts that are suitable are homogeneous or
multi-phase materials, which are insoluble in the reaction medium,
and which have a Hammett acidity, noted H.sub.0, of less than +2.
As indicated in U.S. Pat. No 5,387,720, which refers to the article
by K. Tanabe et al. in "Studies in Surface Science and Catalysis",
Vol. 51, 1989, chap. 1 and 2, the Hammett acidity is determined by
amine titration using indicators or by adsorption of a base in the
gas phase. The catalysts satisfying the acidity criterion H.sub.0
less than +2 may be chosen from natural or synthetic siliceous
materials or acidic zeolites; mineral supports, such as oxides,
coated with mono-, di-, tri- or polyacidic inorganic acids; oxides
or mixed oxides, or alternatively heteropolyacids.
[0018] The catalysts are advantageously chosen from zeolites,
Nafion.RTM. composites (based on sulfonic acid of fluorinated
polymers), chlorinated aluminas, phosphotungstic and/or
silicotungstic acids and acid salts, and various solids of metal
oxide type such as tantalum oxide Ta.sub.2O.sub.5, niobium oxide
Nb.sub.2O.sub.5, alumina Al.sub.2O.sub.3, titanium oxide TiO.sub.2,
zirconia ZrO.sub.2, tin oxide SnO.sub.2, silica SiO.sub.2 or
silico-aluminate SiO.sub.2-Al.sub.2O.sub.3, impregnated with acidic
functions such as borate BO.sub.3, sulfate SO.sub.4, tungstate
WO.sub.3, phosphate PO.sub.4, silicate SiO.sub.2 or molybdate
MoO.sub.3. According to the literature data, these catalysts all
have a Hammett acidity H.sub.0 of less than +2.
[0019] The preferred catalysts are sulfate zirconias, phosphate
zirconias, tungsten zirconias, siliceous zirconias, sulfate
titanium or tin oxides, and phosphate aluminas or silicas.
[0020] These catalysts all have a Hammett acidity H.sub.0 of less
than +2; the acidity H.sub.0 may then vary within a wide range, up
to values that may reach -20 in the scale of reference with the
Hammett indicators. The table given on page 71 of the publication
on acid-base catalysis (C. Marcilly) Vol. 1, published by Technip
(ISBN No. 2-7108-0841-2) illustrates examples of solid catalysts in
this acidity range. The content of molecular oxygen introduced into
the reaction medium may depend on the nature of the catalyst used,
its acidity and its capacity to form coke.
[0021] The reaction according to the invention may be performed in
the gas phase or in the liquid phase, preferably in the gas phase.
When the reaction is performed in the gas phase, various process
technologies may be used, i.e. a fixed-bed process, a fluidized-bed
process or a circulating fluidized-bed process. In the last two
processes, in a fixed bed or a fluidized bed, the regeneration of
the catalyst may be separate from the reaction. It may take place
ex situ, for example by extraction of the catalyst and combustion
in air or with a gaseous mixture containing molecular oxygen. In
this case, the temperature and pressure at which the regeneration
is performed do not need to be the same as those at which the
reaction is performed. According to the process of the invention,
it may take place continuously in situ, at the same time as the
reaction, given the presence of a small amount of molecular oxygen
or of a gas containing molecular oxygen in the reactor. In this
case, the regeneration is likened to an inhibition of deactivation
and takes place at the reaction temperature and pressure.
[0022] In the circulating fluidized-bed process, the catalyst
circulates in two containers, a reactor and a regenerator. It is
known that the dehydration reaction is endothermic, and energy must
therefore be supplied to the first container, whereas the
regeneration consisting of the combustion of coke is exothermic,
and heat must therefore be taken away from the second container. In
the case of the circulating fluidized bed, the two systems may
compensate each other: according to the process of the invention,
the regeneration of the catalyst under a flow of oxygen by
combustion leads to heating of the catalyst and consequently
supplies the energy required for the dehydration reaction when the
heated catalyst returns into the reactor. The residence time in
each container depends on the rate of deactivation of the catalyst
and on the level of coke formed on the catalyst. Specifically, a
minimum level of coke is desirable in order to be able to bring the
solid to the correct temperature, and a maximum level of coke is
necessary in order to prevent the solid from degrading by sintering
during combustion.
[0023] The selection of the optimum process is made as a function
of various criteria. The fixed-bed process has the advantage of
simplicity. The fluidized-bed processes make it possible to
continuously discharge the spent catalyst and to permanently
recharge fresh catalyst without stopping the production, with the
possibility of being isothermic. The circulating fluidized-bed
process has the advantage of optimizing the reaction selectivity by
permanently returning freshly regenerated catalyst into the
reactor, while at the same time compensating for the energy
exchange between the reactor and the regenerator.
[0024] According to one particular embodiment of the invention, the
process is performed in a reactor of the plate heat exchanger type.
This reactor consists of plates forming between themselves
circulation channels that can contain a catalyst. This technology
has many advantages in terms of heat exchange, associated with high
heat exchange capacity. Thus, this type of reactor is particularly
suitable for removing heat easily in the case of exothermic
reactions, or for supplying heat in the start-up phases of
reactions or in the case of endothermic reactions. More
particularly, this reactor makes it possible either to heat or to
cool the catalyst. The heat exchange is particularly efficient with
the circulation of a heat-exchange fluid in the system. The plates
may be assembled in modules, which gives greater flexibility,
whether as regards the size of the reactor, its maintenance or the
replacement of the catalyst. Systems that may be suitable for the
process of the invention are, for example, the reactors described
in documents EP 995 491 or EP 1 147 807, the content of which is
incorporated by reference. These reactors are particularly suitable
for the catalytic conversion of reaction media, specifically
gaseous reaction media, such as those used in the present
invention. The plate heat exchanger used for the preparation of
(meth)acrolein or (meth)acrylic acid via catalytic oxidation of C3
or C4 precursors, described in document US 2005/0020851, may also
be suitable for the manufacture of acrolein via dehydration of
glycerol, which is the subject of the present invention.
[0025] The dehydration of glycerol may also be performed in the
liquid phase in a standard reactor for liquid-phase reaction on a
solid catalyst, but also in a reactor of catalytic distillation
type. Given the large difference between the boiling points of
glycerol (280.degree. C.) and acrolein (53.degree. C.), a
liquid-phase process at a relatively low temperature that allows
continuous distillation of the acrolein produced may also be
envisaged. The reaction is permanently shifted, thus limiting the
consecutive reactions on the acrolein in an equilibrium-shifted
continuous reactor.
[0026] The experimental conditions of the gas-phase reaction are
preferably a temperature of between 250.degree. C. and 350.degree.
C. and a pressure of between 1 and 5 bar. In the liquid phase, the
reaction is preferably performed at a temperature of between
150.degree. C. and 350.degree. C. and a pressure that may range
from 3 to 70 bar. It has been observed that a lower temperature
leads to a reduction in the degree of conversion of glycerol, but,
at the same time, the acrolein selectivity is increased. To avoid
consecutive reactions and the formation of unwanted products, it is
important to limit the residence time in the reactor; moreover, by
increasing the residence time, it is also possible to have higher
conversions. It is especially desirable to increase the contact
time (residence time) of the reagents in the region of the catalyst
in order to compensate for a decrease in the degree of conversion
when a lower reaction temperature is used.
[0027] Glycerol is available inexpensively in the form of aqueous
solutions. Advantageously, an aqueous glycerol solution with a
concentration of between 10% and 50% and preferably between 15% and
30% by weight is used in the reactor. The concentration should not
be too high, so as to avoid spurious reactions such as the
formation of glycerol ethers or reactions between the acrolein
produced and the glycerol. Moreover, the glycerol solution should
not be too dilute on account of the energy cost involved in the
evaporation of the aqueous glycerol solution. In any case, the
concentration of the glycerol solution may be adjusted by recycling
the water produced by the reaction. In order to reduce the glycerol
transportation and storage costs, the reactor may be fed with
concentrated solution of 40% to 100% by weight, dilution to the
optimum content being performed by recycling some of the steam
produced by the reaction and of the dilution water. Similarly, the
recovery of heat at the reactor outlet may also allow the glycerol
solution feeding the reactor to be vaporized.
[0028] Glycerol derived from the methanolysis of plant oils in
basic medium may contain certain impurities such as sodium chloride
or sulfate, non-glycerol organic matter, and methanol. The presence
of sodium salts is in particular detrimental to the catalytic
dehydration reaction since these salts are capable of poisoning the
acidic sites. A pretreatment of the glycerol by ion exchange may be
envisaged.
[0029] Compared with the conventional process for preparing
acrolein by selective oxidation of propylene, the acrolein produced
according to the process of the invention may contain impurities of
different nature or in different amount. According to the envisaged
use, synthesis of acrylic acid, synthesis of methionine or fine
chemistry reactions, it may be envisaged to purify the acrolein
according to the techniques known to those skilled in the art. More
particularly, the by-products may be recovered and incinerated,
thus producing vapour or energy. The energetic upgrading of the
by-products of the glycerol dehydration reaction furthermore makes
it possible to greatly reduce the greenhouse-gas emissions of the
process, compared with the conventional process, for which the
CO.sub.2 produced is derived from fossil carbon during the
incineration of the by-products.
[0030] The examples that follow illustrate the present invention
without, however, limiting its scope.
EXAMPLES
[0031] In the examples, a tubular reactor consisting of a tube 85
cm long and with an inside diameter of 6 mm is used to perform the
glycerol dehydration reaction in the gas phase at atmospheric
pressure. This reactor is placed in a heated chamber maintained at
the reaction temperature, which is 300.degree. C., unless otherwise
indicated. The catalysts used are ground and/or pelletized to
obtain particles of 0.5 to 1.0 mm. 10 ml of catalyst are loaded
into the reactor to form a catalytic bed 35 cm long. This bed is
maintained at the reaction temperature for 5 to 10 minutes before
introducing the reagents. The reactor is fed with an aqueous
solution containing 20% by weight of glycerol at a mean feed flow
rate of 12 ml/h, and with a flow rate of 0.8 l/h of molecular
oxygen for the examples according to the invention. In this case,
the O.sub.2/vaporized glycerol/steam relative proportion is
6/4.5/89.5. The aqueous glycerol solution is vaporized in the
heated chamber, and then passes over the catalyst. The calculated
contact time is about 2.9 sec. The duration of a catalyst test is
about 7 hours, which corresponds to about 80 ml of aqueous glycerol
solution passed over the catalyst. After reaction, the products are
condensed in a trap refrigerated with crushed ice.
[0032] Samples of the effluents are collected periodically. For
each sample collection, the flow is interrupted and a gentle flow
of nitrogen is passed through the reactor to purge it. The trap at
the reactor outlet is then replaced, the nitrogen flow is stopped
and the reactor is returned under a flow of reagent. The test is
continued until appreciable deactivation of the catalyst is
noted.
[0033] For each experiment, the total mass of products entering and
leaving is measured, which allows a mass balance to be determined.
Similarly, the products formed are analysed by chromatography. Two
types of analysis are performed: [0034] an analysis by
chromatography on a filled column (FFAP column 2 m*1/8'') on a
Carlo Erba chromatograph equipped with a TCD detector. The
quantitative analysis is performed with an external standard
(2-butanone); [0035] an analysis by chromatography on a capillary
column (FFAP column 50 m*0.25 mm) on an HP6890 chromatograph
equipped with an FID detector with the same samples stored at
-15.degree. C.
[0036] The first method is particularly suitable for rapid analysis
of the products, and especially the yield of acrolein. The second
method is used to have a more precise analysis of all the reaction
by-products. Moreover, analyses by GC-MS or by chromatography after
silylation were performed to confirm these results.
[0037] The products thus quantified are the unreacted glycerol, the
acrolein formed, and the by-products such as hydroxypropanone,
acetaldehyde, propanaldehyde, acetone and phenol.
In the examples that follow, the glycerol conversion, the acrolein
selectivity and the yields of the various products are defined as
follows: [0038] glycerol conversion (%)=100-number of moles of
glycerol remaining/number of moles of glycerol introduced; [0039]
acrolein yield (%)=number of moles of acrolein produced/number of
moles of glycerol introduced; [0040] acrolein selectivity
(%)=100*number of moles of acrolein produced/number of moles of
glycerol reacted.
[0041] The acetone or hydroxypropanone yield is calculated as for
the acrolein yield: [0042] acetaldehyde yield (%)=2/3 *number of
moles of acetaldehyde produced/number of moles of glycerol
introduced. [0043] phenol yield (%)=2*number of moles of phenol
produced/number of moles of glycerol introduced.
[0044] All the results are expressed as molar percentages relative
to the glycerol introduced.
Example 1
Comparative and According to the Invention
[0045] The catalyst used is a zeolite HZSM5 (Zeocat PZ--2/54 H 15%
Aerosil--Ueticon). 10 ml, representing a mass of 6.41 g, were
loaded into the reactor. The results are given in Table 1
below:
TABLE-US-00001 TABLE 1 Cumulative glycerol introduced (g) 15 17 8
16 24 Addition of oxygen no no yes yes yes Glycerol conversion 79
64 96 88 83 Acrolein yield 39.1 24.3 40.6 40.9 37.5 Acrolein
selectivity 49 38 42 46 45 Hydroxypropanone yield 5.6 3.7 1.5 2.2
2.4 Acetaldehyde yield 1.2 0.6 2.2 1.8 1.7 Propanaldehyde yield 1.5
0.0 1.6 0.9 0.8 Acetone yield 0.1 0.5 0.0 0.2 0.1 Phenol yield 1.0
0.0 0.0 0.0 0.0 Material balance 97.7 98.0 97.2 98.8 98.9 (mass
collected/mass introduced) Quantified product balance 69.2 65.0
49.9 57.7 59.8 (products assayed/glycerol introduced)
The addition of molecular oxygen makes it possible to maintain the
glycerol conversion and the acrolein yield by inhibiting the
deactivation of the catalyst and the formation of certain
by-products.
Example 2
According to the Invention
[0046] In this Example 2, two types of catalyst (10 ml) are tested:
a sulfate zirconia (90% ZrO.sub.2-10% SO.sub.4) from Daiichi
Kigenso (supplier reference H1416) and a tungsten zirconia (90.7%
ZrO.sub.2-9.3% WO.sub.3) from Daiichi Kigenso (supplier reference
H1417). The first catalyst has a loss on ignition at 1000.degree.
C. of 8.81% and a specific surface area of 54.3 m.sup.2/g (BET, 1
point). The second catalyst is characterized by a loss on ignition
at 1000.degree. C. of 1.75% and a specific surface area of 47.4
m.sup.2/g (BET, 1 point). The results are given in Table 2
below:
TABLE-US-00002 TABLE 2 Cumulative glycerol introduced (g) 9 18 27
21 33 Catalyst Sulfate zirconia Tungsten 16.5 g zirconia 17 g
Glycerol conversion 100 100 100 100 100 Acrolein yield 42.3 53.8
52.5 54.9 53.0 Acrolein selectivity 42 54 52 55 53 Hydroxypropanone
yield 0.0 0.0 0.0 0.0 0.0 Acetaldehyde yield 10.3 9.1 8.2 9.8 8.7
Propanaldehyde yield 4.9 3.7 4.0 2.1 1.4 Acetone yield 0.0 0.4 0.0
0.1 0.1 Phenol yield 0.0 0.0 0.3 0.0 0.0 Material balance 96.5 98.0
98.0 97.2 97.9 (mass collected/mass introduced) Quantified product
57.5 66.9 65.0 66.9 63.2 balance(products aassayed/glycerol
introduced)
The formation of hydroxypropanone and of phenol is completely
inhibited in the presence of molecular oxygen.
Example 3
Comparative and According to the Invention
[0047] 10 ml of zeolite H-beta from Valfor (CP811BL-25)
representing a mass of 4.23 g were loaded into the reactor. For
this example, the flow rate of molecular oxygen used is 0.34 l/h.
The results are given in Table 3 below:
TABLE-US-00003 TABLE 3 Cumulative glycerol introduced (g) 8 16 25
35 9 16 24 32 Addition of no No no no yes yes yes yes oxygen
Glycerol 100 99 97 89 100 100 100 100 conversion Acrolein yield
45.6 56.9 52.3 47.9 42.9 57.3 56.4 56.3 Acrolein 46 57 54 54 43 57
56 56 selectivity Hydroxy- 6.9 9.6 9.5 9.7 0.4 0.9 0.2 0.4
propanone yield Acetaldehyde 5.1 5.2 5.1 4.8 6.6 7.2 6.8 6.1 yield
Propanal- 7.2 5.4 4.6 3.4 4.9 3.9 3.2 2.6 dehyde yield Acetone
yield 0 0 0 0.2 0 0 0 0 Phenol yield 1.3 0.7 0.5 0.4 1.2 0.5 0.4
0.1 Material 95.6 -- 98.6 98.9 97 99 98.9 99 balance (mass
collected/ mass introduced) Quantified 66.2 78.7 74.8 77.2 56 69.8
67 65.5 product balance (products assayed/ glycerol introduced)
The addition of molecular oxygen makes it possible to maintain the
glycerol conversion and the acrolein yield, while at the same time
reducing the formation of by-products.
Example 4
Comparative and According to the Invention
[0048] A phosphate zirconia (91.5% ZrO.sub.2-8.5% PO.sub.4) from
Daiichi Kigenso (Ref H1418) is used. This catalyst has a loss on
ignition at 1000.degree. C. of 4.23% and a specific surface area of
128.7 m.sup.2/g. 10 ml of this catalyst, representing a mass of
12.7 g, are loaded into the reactor. The results are given in Table
4 below.
TABLE-US-00004 TABLE 4 Cumulative glycerol introduced (g) 8 16 24
32 41 9.8 17.9 26.3 34.5 42 Addition of oxygen 0 0 0 0 0 0.34 0.34
0.34 0.34 0.82 Glycerol conversion 100 100 100 100 99 100 100 100
100 100 Acrolein yield 16.6 40.4 46.7 45.2 46.2 23.3 42.0 43.0 44.2
38.2 Acrolein selectivity 17 40 47 45 46 23 42 43 44 38
Hydroxypropanone yield 0.0 9.4 13.0 13.5 14.7 0.0 0.0 0.0 0.1 0.0
Acetaldehyde yield 6.9 6.3 5.0 4.7 4.3 12.2 11.7 9.9 7.7 10.6
Propanaldehyde yield 15.0 14.2 11.7 11.1 9.8 6.3 5.9 5.4 3.7 3.9
Acetone yield 0.0 0.0 0.0 0.0 0.0 2.0 0.6 0.0 0.2 0.2 Phenol yield
4.2 4.4 2.9 2.5 1.8 0.9 0.4 0.2 0.1 0.2 Material balance 95.0 98.2
95.2 97.7 97.6 -- 97.8 97.9 98.8 98.6 (mass collected/mass
introduced) Quantified product balance 42.7 74.6 79.3 77.0 77.4
44.8 60.7 58.5 56.0 53.1 (products assayed/glycerol introduced) The
hydroxypropanone, propanaldehyde and phenol by-products are in
markedly lower amount when the process is performed in the presence
of oxygen.
Example 5
Comparative of the Prior Art
[0049] 10 ml of H.sub.3PO.sub.4/alpha-alumina catalyst prepared as,
described in U.S. Pat. No. 5,387,720, representing a mass of 10 g,
were loaded into the reactor. The catalyst was prepared in the
following manner: 15.9 g of alpha-alumina from Ceramtec (Ref
EO-19--specific surface area 0.7 m.sup.2/g--mean pore diameter 2.5
.mu.m--apparent porosity 65%--supplied in the form of rings and
ground so as to retain only the particles of diameter 1-1.4 mm)
were impregnated with 4 g of a 20% by weight phosphoric acid
solution (prepared by addition of 16.25 ml of water and 5 g of 85%
by weight phosphoric acid). The solid is then dried on a rotavapor
at 80.degree. C. and used directly. The results are collated in
Table 5.
TABLE-US-00005 TABLE 5 Cumulative glycerol introduced (g) 8 16 25
32 Glycerol conversion 91 69 42 17 Acrolein yield 54.5 32.2 20.6
3.8 Acrolein selectivity 60 46 49 23 Hydroxypropanone yield 12.3
9.3 6.5 2.1 Acetaldehyde yield 0.1 0.0 0.0 0.0 Propanaldehyde yield
0.3 0.2 0.1 0.0 Acetone yield 0.0 0.0 0.0 0.0 Phenol yield 1.0 0.1
0.1 0.0 Material balance 98.6 98.7 nd 98.9 (mass collected/mass
introduced) Quantified product balance 77.6 72.6 84.9 89.4
(products assayed/glycerol introduced)
Example 6
Comparative of the Prior Art
[0050] 10 ml of an H.sub.3PO.sub.4/alpha alumina catalyst,
representing a mass of 8.55 g, were loaded into the reactor. The
catalyst was prepared in the same manner as for Example 5, but,
after drying at 80.degree. C., the solid was activated in air at
300.degree. C. for 3 hours in order to fix the phosphoric acid to
the support.
[0051] The results are given in Table 6 below.
TABLE-US-00006 TABLE 6 Cumulative glycerol introduced (g) 8 16 24
32 Glycerol conversion 70 37 9 8 Acrolein yield 42.1 18.2 4.6 3.1
Acrolein selectivity 60 50 50 41 Hydroxypropanone yield 10.3 4.8
0.0 0.0 Acetaldehyde yield 0.0 0.0 0.0 0.0 Propanaldehyde yield 0.0
0.0 0.0 0.0 Acetone yield 0.0 0.0 0.0 0.1 Phenol yield 0.8 0.0 0.0
0.0 Material balance 98.5 98.9 98.0 99.0 (mass collected/mass
introduced) Quantified product balance 83.2 86.2 95.5 95.6
(products assayed/glycerol introduced)
Rapid deactivation of the catalyst is noted in these two
comparative Examples 5 and 6.
* * * * *