U.S. patent application number 12/385444 was filed with the patent office on 2009-08-20 for crystalline amoxicillin trihydrate powder.
This patent application is currently assigned to DSM IP ASSETS B.V.. Invention is credited to Thomas Van Der Does, Jan Willem Groenendaal, Everardus Johannus Antoinious Maria Leenderts.
Application Number | 20090208999 12/385444 |
Document ID | / |
Family ID | 36697666 |
Filed Date | 2009-08-20 |
United States Patent
Application |
20090208999 |
Kind Code |
A1 |
Groenendaal; Jan Willem ; et
al. |
August 20, 2009 |
Crystalline amoxicillin trihydrate powder
Abstract
The invention relates to crystalline amoxicillin trihydrate
powder having a bulk density higher than 0.45 g/ml. The invention
also relates to a process for preparing crystalline amoxicillin
trihydrate powder, said process comprising: crystallizing
amoxicillin trihydrate from a solution containing dissolved
amoxicillin; separating the crystals from said solution; and drying
the separated crystals, resulting in crystalline powder having a
bulk density higher than 0.45 g/ml.
Inventors: |
Groenendaal; Jan Willem;
(Delft, NL) ; Leenderts; Everardus Johannus Antoinious
Maria; (Rhoon, NL) ; Does; Thomas Van Der;
(Wilnis, NL) |
Correspondence
Address: |
NIXON & VANDERHYE, PC
901 NORTH GLEBE ROAD, 11TH FLOOR
ARLINGTON
VA
22203
US
|
Assignee: |
DSM IP ASSETS B.V.
Heerlen
NL
|
Family ID: |
36697666 |
Appl. No.: |
12/385444 |
Filed: |
April 8, 2009 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
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10548266 |
Sep 7, 2005 |
7534781 |
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PCT/EP04/02989 |
Mar 19, 2004 |
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12385444 |
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60456188 |
Mar 21, 2003 |
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60456187 |
Mar 21, 2003 |
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Current U.S.
Class: |
435/43 ;
540/315 |
Current CPC
Class: |
A61K 9/2072 20130101;
A61K 9/2054 20130101; A61K 31/43 20130101; A61K 9/14 20130101 |
Class at
Publication: |
435/43 ;
540/315 |
International
Class: |
C12P 37/00 20060101
C12P037/00; C07D 499/04 20060101 C07D499/04 |
Foreign Application Data
Date |
Code |
Application Number |
Mar 21, 2003 |
EP |
03100731.3 |
Mar 21, 2003 |
EP |
03100732.1 |
Claims
1-20. (canceled)
21. Process for preparing crystalline amoxicillin trihydrate powder
having a bulk density higher than 0.45 g/ml and a d.sub.50 lower
than 100 .mu.m, said process comprising: resulting in crystalline
powder having a bulk density higher than 0.45 g/ml, and a d.sub.50
lower than 100 .mu.m.
22. Process according to claim 21, resulting in crystalline powder
having a tapped density higher than 0.6 g/ml, wherein said tapped
density is determined according to USP 24, method II.
23. Process according to claim 21, resulting in crystalline powder
having a d.sub.50 higher than 10 .mu.m.
24. Process according to claim 21, resulting in crystalline powder
having a d.sub.10 higher than 3 .mu.m.
25. Process according to claim 21, wherein the process comprises
mechanically impacting the crystals during said drying.
26. Process according to claim 21, wherein the process comprises:
preparing amoxicillin by reacting 6-amino-penicillanic acid or a
salt thereof, with para-hydroxyphenyl glycine in activated form in
the presence of an enzyme immobilized on a carrier; forming an
aqueous solution containing the amoxicillin, said aqueous solution
containing hydrochloric acid; and crystallizing amoxicillin
trihydrate from said aqueous solution.
27. Process according to claim 21, wherein the aqueous solution
from which the amoxicillin is crystallized has an amoxicillin
concentration of less than 0.6 mol/l.
28. Process according to claim 21, wherein the solution from which
the amoxicillin is crystallized contains less than 200 weight parts
of protein per 1.000.000 weight parts of the amoxicillin antibiotic
in said solution.
Description
[0001] The present invention relates to crystalline amoxicillin
trihydrate powder. The invention also relates to a process for
preparing crystalline amoxicillin trihydrate powder.
[0002] Crystalline powder of a .beta.-lactam antibiotic can be
obtained by crystallizing the .beta.-lactam antibiotic from a
solution containing the .beta.-lactam antibiotic in dissolved form,
separating the crystals obtained, and drying the crystals. In the
art, crystals of a .alpha.-lactam antibiotic are also referred to
as powder.
[0003] The known powders have poor flow properties. The particle
size is small, and the bulk density is low. This is for instance
described in WO-A-9733564 disclosing for instance powder of
amoxicillin trihydrate having an average volume-based grain size of
10 .mu.m to 30 .mu.m and a bulk density of 0.15 g/ml to 0.45 g/ml.
Due to the poor flow properties of the known powder, the known
powder as such is not suitable in applications requiring sufficient
flow characteristics, such as for instance filling of capsules.
[0004] In order to improve the flow properties, the known powder
can be subjected to processes referred to in the art as
granulation, compacting, agglomeration, or aggregation to form
larger particles having improved flow properties, said larger
particles typically having a average volume-based grain size of
greater than 100 .mu.m, see for instance WO-A-9733564 and
WO-A-9911261. The resulting larger particles having improved flow
properties may for instance be used as a filling material for
capsules or may be used for the preparation of tablets.
[0005] These processes require additional process steps, which is
disadvantageous. Moreover, if not properly applied these processes
may impair the properties of the antibiotic such as colour,
stability. Moreover, we found that the dissolution rate of the
resulting product is low.
[0006] Surprisingly we found crystalline amoxicillin trihydrate
powder having a bulk density higher than 0.45 g/ml; and a process
for the preparation thereof.
[0007] The crystalline powder according to the invention has
improved flow properties, without having to be subjected to
processes such as granulation, compacting, agglomeration or
aggregation. If it would still be desired to subject the
crystalline powder to processes such as granulation, compacting,
agglomeration or aggregation, and the like, applying these
processes is facilitated due to the improved flow properties of the
crystalline powder according to the invention. Moreover, an
increased quantity of crystalline powder can be fed into a capsule
of a given size.
[0008] As used herein crystalline amoxicillin trihydrate powder,
refers preferably to a product consisting mainly of crystals of
amoxicillin trihydrate. It will be understood that crystals do not
refer to aggregates formed by the build-up of crystals, for
instance with the aid of a binding agent like water or starch
paste, or mechanical force like roller compacting or extrusion.
Some unintended formation of aggregates may occur during usual
handling, for instance during drying. Aggregates can be seen using
optical microscopy applied at a magnification of 140.times.. As
used herein a product consisting mainly of crystals of the
.beta.-lactam antibiotic refers preferably to a product comprising
at least 70 wt. % crystals of amoxicillin trihydrate, preferably at
least 80 wt. %, more preferably at least 90 wt. %, more preferably
at least 95 wt. %, more preferably at least 98 wt. %. These
percentages can be determined using a combination of air jet
sieving and optical microscopy. Air Jet sieving is advantageously
carried out using an Alpine Air Jet 200LS-N air jet sieve during 1
minutes at 1200 Pa for a sample weight of 10 g). Optical microscopy
is advantageously carried out by taking a sample of 5 mg,
suspending the sample in 4 drops of paraffin oil on a surface on a
surface area of 22.times.40 mm, and using a magnification of
140.times..
[0009] It will be understood that the amoxicillin trihydrate may
contain some impurities. The crystalline amoxicillin trihydrate
powder according to the invention may for instance contain at least
90 wt. %, preferably at least 95 wt. %, more preferably at least 98
wt. % of amoxicillin trihydrate. These weight percentages are given
relative to the weight of the crystalline powder. Preferably, the
amoxicillin trihydrate powder is free of auxiliaries.
[0010] Preferably, the crystalline powder according to the
invention has a bulk density higher than 0.46 g/ml, preferably
higher than 0.5 g/ml, more preferably higher than 0.55 g/ml. This
further improves the flow properties. Moreover, an increased bulk
density is advantageous as crystalline powder may be fed into a
certain volume, for instance a capsule. There is no specific upper
limit for the bulk density. The bulk density may be less than 0.8
g/ml, for instance less than 0.7 g/ml. The bulk density is
preferably determined according to USP 24, method I, (page
1913).
[0011] Preferably, the crystalline powder according to the
invention has a tapped density higher than 0.6 g/ml, preferably
higher than 0.7, more preferably higher than 0.8 g/ml. An increased
tapped density improves the flow properties. Moreover, an increased
tapped density is advantageous as more products may be fed into a
certain volume, for instance a capsule. There is no specific upper,
limit for the tapped density. The tapped density may be less than
1.2 g/ml, for instance less than 1.1 g/ml, for instance less than
1.0 g/ml. The tapped density is preferably determined according to
USP 24, method II, (page 1914).
[0012] The invention also relates to crystalline amoxicillin
trihydrate powder, having a tapped density higher than 0.6 g/ml,
preferably higher than 0.7, more preferably higher than 0.8 g/ml.
This crystalline powder has improved flow properties compared to
the known powder. The tapped density may be less than 1.2 g/ml, for
instance less than 1.1 g/ml, for instance less than 1.0 g/ml.
[0013] Preferably, the crystalline powder according to the
invention has a bulk density and tapped density such that the ratio
d.sub.t/d.sub.b is less than 1.7, preferably less than 1.6,
preferably less than 1.5, preferably less than 1.45, wherein
d.sub.t=tapped density and d.sub.b=bulk density. This results in
improved flow ability. There is no specific lower limit for the
ratio d.sub.t/d.sub.b. The ratio d.sub.t/d.sub.b may be higher than
1.05, for instance higher than 1.1.
[0014] The invention also relates to crystalline amoxicillin
trihydrate powder, having a bulk density and tapped density such
that the ratio d.sub.t/d.sub.b is less than 1.7, preferably less
than 1.6, preferably less than 1.5, preferably less than 1.45. This
crystalline powder has improved flow properties compared to the
known powder. There is no specific upper limit for the ratio
d.sub.t/d.sub.b. The ratio d.sub.t/d.sub.b may be higher than 1.05,
for instance higher than 1.1.
[0015] Preferably, the crystalline powder according to the
invention has a bulk density and tapped density such that the
compressibility index as defined by ((d.sub.t-d.sub.b)/d.sub.t*100%
is less than 40%, preferably less than 35%, more preferably less
than 30%. This results in improved flow ability. There is no
specific lower limit for the compressibility index. The
compressibility index may for instance be higher than 10%.
[0016] The invention also relates to crystalline amoxicillin
trihydrate powder having a bulk density and tapped density such
that the compressibility index as defined by
((d.sub.t-d.sub.b)/d.sub.t)*100% is less than 40%, preferably less
than 35%, more preferably less than 30%. This crystalline powder
has improved flow properties compared to the known powder. There is
no specific lower limit for the compressibility index. The
compressibility index may for instance be higher than 10%.
[0017] The d.sub.10 and d.sub.50 are known ways for indicating a
particle size distribution, d.sub.50 referring to the value for the
particle size such that 50 vol. % of the particles has a particle
size smaller than said value. The d.sub.50 is also referred to as
average volume-based grain size. Likewise, d.sub.10 refers to the
value for the particle size such that 10 vol. % of the particles
has a particle size smaller than said value. A preferred way for
determining d.sub.10 and d.sub.50 is laser diffraction, preferably
using Malvern equipment. A suitable apparatus for determining
d.sub.10 and d.sub.50 is a Malvern particle sizer 2600 C obtainable
from Malvern Instruments Ltd., Malvern UK, for instance using an
objective of f=300 mm and a beam length of 14.30 mm. A polydisperse
analysis model may advantageously be used.
[0018] We found that crystalline powder having improved
flowability, bulk density and/or tapped density preferably have an
increased d.sub.50. The invention also provides crystalline
amoxicillin trihydrate powder having a d.sub.50 of higher than 10
.mu.m, preferably higher than 20 .mu.m, more preferably higher than
30 .mu.m, more preferably higher than 35 .mu.M, more preferably
higher than 40 .mu.m. There is no specific upper limit for the
d.sub.50. The d.sub.50 of the crystalline powder according to the
invention may be less than 150 .mu.m, for instance less than 100
.mu.m. The crystalline powder according to the invention preferably
has increased d.sub.10, preferably higher than 3 .mu.m, preferably
higher than 5 .mu.m, more preferably higher than 8 .mu.m, more
preferably higher than 10 .mu.m. There is no specific upper limit
for the d.sub.10 of the crystalline powder according to the
invention. The d.sub.10 of the crystalline powder according to the
invention may be less than 50 .mu.m.
[0019] The invention also provides a process comprising sieving the
crystalline powder according to the invention. This allows the
physical properties of the crystalline powder to be improved even
further. Preferably, air jet sieving is applied.
[0020] The crystalline powder according to the invention can
advantageously be used for the preparation of a pharmaceutical
composition.
[0021] The crystalline powder according to the invention can
advantageously be mixed with pharmaceutically acceptable
auxiliaries and/or with a second pharmaceutically active agent. The
crystalline powder according to the invention can for instance be
mixed with between 0 and 50 wt. %, preferably between 0 and 40 wt.
%, preferably between 0 and 30 wt. %, more preferably between 0 and
20 wt. %, preferably more than 1 wt. % of auxiliaries, relative to
the sum weight of the crystalline powder and the auxiliaries. The
crystalline powder according to the invention can for instance be
mixed with clavulanic acid in salt form, preferably as a potassium
salt, the weight ratio amoxicillin:clavulanic acid preferably being
between 1:1 and 15:1, preferably between 2:1 and 10:1, preferably
between 4:1 and 8:1. These weight ratios are calculated for the
anhydrous amoxicillin and clavulanate in acid form. Therefore, the
invention also relates to a mixture obtainable by a process
comprising mixing the crystalline powder according to the invention
with auxiliaries and/or a second pharmaceutically active agent. The
invention also provides a mixture comprising (i) the crystalline
powder according to the invention and (ii) auxiliaries and/or a
second pharmaceutically active agent.
[0022] As a second pharmaceutically active agent, clavulanic acid
in the form of a salt, preferably clavulanic acid in the form of a
potassium salt is preferably used.
[0023] As auxiliaries may for instance be used fillers, dry
binders, disintegrants, wetting agents, wet binders, lubricants,
flow agents and the like. Examples of auxiliaries are lactose,
starches, bentonite, calcium carbonate, mannitol, microcrystalline
cellulose, polysorbate, sodium lauryl sulphate,
carboymethylcelluslose Na, Sodium alginate, magnesium stearate,
silicon dioxide, talc.
[0024] Preferably, the mixture contains between 0 and 50 wt. %,
preferably between 0 and 40 wt. %, preferably between 0 and 30 wt.
%, more preferably between 0 and 20 wt. %, preferably more than 1
wt. % of auxiliaries. These weight percentages are given relative
to the sum weight of the amoxicillin trihydrate and the
auxiliaries.
[0025] Preferably the weight ratio amoxicillin:clavulanic acid is
between 1:1 and 15:1, preferably between 2:1 and 10:1, preferably
between 4:1 and 8:1. These weight ratios are calculated for the
anhydrous amoxicillin and clavulanate in acid form.
[0026] The crystalline powder according to the invention can
advantageously be used for filling a capsule for pharmaceutical
use, for instance a gelatine capsule. Therefore, the invention also
relates to a capsule containing the crystalline powder according to
the invention or a capsule containing the mixture according to the
invention. The crystalline powder according to the invention or the
mixture according to the invention may be fed into a capsule in any
suitable way. It will be understood by the skilled person that
feeding material into a capsule may comprise forming a plug of the
material, said plug being loosely comprised of the material. The
skilled man will understand that a capsule containing crystalline
powder or the mixture according to the invention also encompasses a
capsule containing a plug of crystalline powder or a mixture
according to the invention. The invention also relates to the use
of the crystalline powder according to the invention or the mixture
according to the invention for filling a capsule or for the
preparation of a tablet.
[0027] The invention also relates to a process for filling a
capsule, comprising feeding the crystalline powder according to the
invention, optionally in combination with auxiliaries and/or a
second pharmaceutically active agent, into the capsule. The
invention also relates to a process comprising mixing the
crystalline powder according to the invention with pharmaceutically
acceptable auxiliaries, optionally together with a second
pharmaceutically active agent, and feeding the resulting mixture
into a capsule.
[0028] We found that the improved flow properties of the
crystalline amoxicillin trihydrate powder according to the
invention facilitate processes such as dry and wet granulation,
agglomeration, tablet formation and the like. Therefore, the
invention also provides a process comprising compressing the
crystalline powder according to the invention or compressing the
mixture according to the invention to produce compressed products.
The compressed products may for instance be granules or tablets.
The invention also relates to granules or tablets comprising the
crystalline powder in compressed form or comprising the mixture
according to the invention in compressed form.
[0029] The invention also relates to a process for preparing
granules, comprising feeding the crystalline powder according to
the invention or the mixture according to the invention, optionally
in combination with auxiliaries and/or a second pharmaceutically
active agent, to a roller compactor to produce compacts; and
milling the compacts to produce granules. The granules produced may
advantageously be sieved to obtain a desired particle size
distribution. The invention also relates to granules obtainable by
this process.
[0030] The invention also relates to a process for preparing
granules, comprising mixing the crystalline powder according to the
invention or the mixture according to the invention with a binding
agent, the binding agent for instance being dissolved in a
moistening liquid; compacting the crystals whilst moist or dry;
granulating the compacts obtained through a sieve. The invention
also relates to granules obtainable by this process.
[0031] The invention also relates to a process comprising forming a
paste from the crystalline powder according to the invention or
from the mixture according the invention; kneading the paste at a
temperature of 10.degree. C. to 80.degree. C.; extruding the paste
in a double-screwed extruder, and, if desired, drying the granules
obtained. The invention also relates to granules obtainable this
process.
[0032] The invention also relates to a process comprising
compressing the granules according to the invention, optionally in
mixture with auxiliaries and/or a pharmaceutically active agent to
prepare tablets. The invention also relates to tablets obtainable
by this process.
[0033] The invention also provides a process comprising mixing the
crystalline amoxicillin trihydrate powder according to the
invention, with amoxicillin in another physical form, preferably
granules comprising amoxicillin trihydrate. The invention also
provides a mixture comprising (i) amoxicillin trihydrate powder
according to the invention and (ii) amoxicillin trihydrate in
another physical form, preferably granules comprising amoxicillin
trihydrate. In an embodiment, this mixture is auxiliary free. In an
embodiment, this mixture comprises auxiliaries and/or a second
pharmaceutically active agent. The granules comprising amoxicillin
trihydrate in the mixture (to be mixed) may be any suitable
granules, for instance having a d.sub.60 of between 100 and 1000
.mu.m. The d.sub.50 of granules is preferably determined by making
a sieve analysis. The granules may for instance comprise at least
90 wt. % of amoxicillin trihydrate, preferably at least 95 wt. %,
more preferably at least 98 wt. % of amoxicillin trihydrate.
Preferably, the granules are free of auxiliaries. The granules may
be obtained by any suitable process wherein powder is combined to
form granules, for instance by roller compacting, agglomeration,
extrusion, aggregation, wet or dry granulation.
[0034] In one aspect of the invention, the crystalline powder
according to the invention has a high dissolution rate. Preferably,
the crystalline powder according to the invention has a T.sub.85%
of less than 55 minutes, preferably less than 50 minutes,
preferably less than 40 minutes, preferably less than 30 minutes,
preferably less than 25 minutes, preferably less than 20 minutes.
T.sub.85% may for instance be above 5 minutes. As used herein
T.sub.85% refers to period required to effect dissolution of 85 wt.
% of a predetermined quantity (500 mg on an anhydrous basis) of the
amoxicillin trihydrate in 900 ml water of 37.degree. C. The
determination of T.sub.85% is preferably carried out under
conditions as defined in USP 27, chapter "amoxicillin capsules",
involving the use of apparatus 1 and applying a stirring rate of
100 rpm (USP 27, paragraph 711). Preferably, samples are taken at
regular intervals, e.g. each 5 minutes, to determine the quantity
of dissolved amoxicillin by UV absorption. Known products of
amoxicillin trihydrate having a bulk density higher than 0.45 g/ml,
for instance granules of amoxicillin trihydrate having a bulk
density higher than 0.45 g/ml, are not found to have such high
dissolution rates.
[0035] Therefore, the invention also relates to a product of
amoxicillin trihydrate, said product having:
(i) a T.sub.85% of less than 55 minutes, preferably less than 50
minutes, preferably less than 40 minutes, preferably less than 30
minutes, preferably less than 25 minutes; and (ii) a bulk density
higher than 0.45 g/ml, preferably higher than 0.5 g/ml, more
preferably higher than 0.55 g/ml. There is no specific upper limit
for the bulk density. The bulk density may be less than 0.8 g/ml,
for instance less than 0.7 g/ml. T.sub.85% may for instance be
above 5 minutes.
[0036] The invention also relates to a product amoxicillin
trihydrate, said product having
(i) a T.sub.85% of less than 55 minutes, preferably less than 50
minutes, preferably less than 40 minutes, preferably less than 30
minutes, preferably less than 25 minutes; and (ii) a tapped density
higher than 0.6 g/ml, preferably higher than 0.7, more preferably
higher than 0.8 g/ml. There is no specific upper limit for the
tapped density. The tapped density may be less than 1.2 g/ml, for
instance less than 1.1 g/ml, for instance less than 1.0 g/ml.
[0037] The invention also relates to a product of amoxicillin
trihydrate, said product having:
(i) a T.sub.85% of less than 55 minutes, preferably less than 50
minutes, preferably less than 40 minutes, preferably less than 30
minutes, preferably less than 25 minutes; and (ii) a bulk density
and tapped density such that the ratio d.sub.t/d.sub.b is less than
1.7, preferably less than 1.6, preferably less than 1.5, preferably
less than 1.45, wherein d.sub.t=tapped density and d.sub.b=bulk
density. This results in improved flow ability. There is no
specific lower limit for the ratio d.sub.t/d.sub.b. The ratio
d.sub.t/d.sub.b may be higher than 1.05, for instance higher than
1.1.
[0038] The invention also relates to amoxicillin trihydrate, said
product having
(i) a T.sub.85% of less than 55 minutes, preferably less than 50
minutes, preferably less than 40 minutes, preferably less than 30
minutes, preferably less than 25 minutes; and (ii) a bulk density
and tapped density such that the compressibility index as defined
by ((d.sub.t-d.sub.b)/d.sub.t)*100% is less than 40%, preferably
less than 35%, more preferably less than 30%. This results in
improved flow ability. There is no specific lower limit for the
compressibility index. The compressibility index may for instance
be higher than 10%.
[0039] In a preferred embodiment, the product of amoxicillin
trihydrate according to the invention has abovementioned preferred
values for bulk density, tapped density, ratio d.sub.t/d.sub.b and
compressibility index mentioned above in combination.
[0040] The product of amoxicillin trihydrate according to the
invention may be amoxicillin trihydrate in any suitable form. It
will be understood that the product of amoxicillin trihydrate may
still contain some impurities. Preferably, the product of
amoxicillin trihydrate contains at least 90 wt. %, preferably at
least 95 wt. %, more preferably at least 98 wt. % of amoxicillin
trihydrate. These weight percentages are given relative to the
weight of the product. Preferably, the product of amoxicillin
trihydrate according to the invention is free of auxiliaries.
[0041] In one embodiment the product according to the invention is
crystalline amoxicillin trihydrate powder according to the
invention. In another embodiment embodiment the product according
to the invention is a mixture comprising (i) amoxicillin trihydrate
powder, preferably crystalline amoxicillin trihydrate powder
according to the invention and (ii) amoxicillin trihydrate in
another physical form, preferably granules comprising amoxicillin
trihydrate.
[0042] The invention also provides a process comprising mixing
amoxicillin trihydrate powder, preferably the crystalline
amoxicillin trihydrate powder according to the invention, with
amoxicillin in another physical form, preferably granules
comprising amoxicillin trihydrate to obtain the product according
to the invention. The quantities of amoxicillin trihydrate and
granules to be mixed can be chosen such that preferred combinations
of T.sub.85% and the bulk density, tapped density, ratio
d.sub.t/d.sub.b and/or compressibility index are achieved. The
amoxicillin trihydrate powder in the mixture (to be mixed) may be a
powder having for instance a d.sub.50 of between 1 and 100 .mu.m.
The crystalline amoxicillin trihydrate powder according to the
invention is preferred.
[0043] The granules comprising amoxicillin trihydrate in the
mixture (to be mixed) may be any suitable granules, for instance
having a d.sub.50 of between 100 and 1000 .mu.m. The d.sub.50 of
the granules is preferably determined by making a sieve analysis.
The granules may for instance comprise at least 90 wt. % of
amoxicillin trihydrate, preferably at least 95 wt. %, more
preferably at least 98 wt. % of amoxicillin trihydrate. Preferably,
the granules are free of auxiliaries. The granules may be obtained
by any suitable process wherein powder is combined to form
granules, for instance by roller compacting, agglomeration,
extrusion, aggregation, wet or dry granulation.
[0044] The product according to the invention can advantageously be
used for the preparation of a pharmaceutical composition.
[0045] The product according to the invention can advantageously be
mixed with pharmaceutically acceptable auxiliaries and/or with a
second pharmaceutically active agent. The product according to the
invention can for instance be mixed with between 0 and 50 wt. %,
preferably between 0 and 40 wt. %, preferably between 0 and 30 wt.
%, more preferably between 0 and 20 wt. %, preferably more than 1
wt. % of auxiliaries, relative to the sum weight of the product and
the auxiliaries. The product according to the invention can for
instance be mixed with clavulanic acid in salt form, preferably as
a potassium salt, the weight ratio amoxicillin:clavulanic acid
preferably being between 1:1 and 15:1, preferably between 2:1 and
10:1, preferably between 4:1 and 8:1. These weight ratios are
calculated for the anhydrous amoxicillin, and clavulanate in acid
form. Therefore, the invention also relates to a mixture obtainable
by a process comprising mixing the product according to the
invention with auxiliaries and/or a second pharmaceutically active
agent. The invention also provides a mixture comprising (i) the
product according to the invention and (ii) auxiliaries and/or a
second pharmaceutically active agent.
[0046] As a second pharmaceutically active agent, clavulanic acid
in the form of a salt, preferably clavulanic acid in the form of a
potassium salt is preferably used.
[0047] As auxiliaries may for instance be used fillers, dry
binders, disintegrants, wetting agents, wet binders, lubricants,
flow agents and the like. Examples of auxiliaries are lactose,
starches, bentonite, calcium carbonate, mannitol, microcrystalline
cellulose, polysorbate, sodium lauryl sulphate,
carboymethylcelluslose Na, Sodium alginate, magnesium stearate,
silicon dioxide, talc.
[0048] Preferably, the mixture contains between 0 and 50 wt. %,
preferably between 0 and 40 wt. %, preferably between 0 and 30 wt.
%, more preferably between 0 and 20 wt. %, preferably more than 1
wt. % of auxiliaries. These weight percentages are given relative
to the sum weight of the amoxicillin trihydrate and the
auxiliaries.
[0049] Preferably the weight ratio amoxicillin:clavulanic acid is
between 1:1 and 15:1, preferably between 2:1 and 10:1, preferably
between 4:1 and 8:1. These weight ratios are calculated for the
anhydrous amoxicillin and clavulanate in acid form.
[0050] The product according to the invention can advantageously be
used for filling a capsule for pharmaceutical use, for instance a
gelatine capsule. Therefore, the invention also relates to a
capsule containing the product according to the invention or a
capsule containing the mixture according to the invention. The
product according to the invention or the mixture according to the
invention may be fed into a capsule in any suitable way. It will be
understood by the skilled person that feeding material into a
capsule may comprise forming a plug of the material, said plug
being loosely comprised of the material. The skilled man will
understand that a capsule containing product or the mixture
according to the invention also encompasses a capsule containing a
plug of product or a mixture according to the invention. The
invention also relates to the use of the product according to the
invention or the mixture according to the invention for filling a
capsule or for the preparation of a tablet.
[0051] The invention also relates to a process for filling a
capsule, comprising feeding the product according to the invention,
optionally in combination with auxiliaries and/or a second
pharmaceutically active agent, into the capsule. The invention also
relates to a process comprising mixing the product according to the
invention with pharmaceutically acceptable auxiliaries, optionally
together with a second pharmaceutically active agent, and feeding
the resulting mixture into a capsule.
[0052] We found that the improved flow properties of the product
according to the invention facilitate processes such as dry and wet
granulation, agglomeration, tablet formation and the like.
Therefore, the invention also provides a process comprising
compressing the product according to the invention or compressing
the mixture according to the invention to produce compressed
products. The compressed products may for instance be granules or
tablets. The invention also relates to granules or tablets
comprising the product according to the invention in compressed
form or the mixture according to the invention in compressed
form.
[0053] The invention also relates to a process for preparing
granules, comprising feeding the product according to the invention
or the mixture according to the invention, optionally in
combination with auxiliaries and/or a second pharmaceutically
active agent, to a roller compactor to produce compacts; and
milling the compacts to produce granules. The granules produced may
advantageously be sieved to obtain a desired particle size
distribution. The invention also relates to granules obtainable by
this process.
[0054] The invention also relates to a process for preparing
granules, comprising mixing the product according to the invention
or the mixture according to the invention with a binding agent, the
binding agent for instance being dissolved in a moistening liquid;
compacting the crystals whilst moist or dry; granulating the
compacts obtained through a sieve. The invention also relates to
granules obtainable by this process.
[0055] The invention also relates to a process comprising forming a
paste from the product according to the invention or from the
mixture according the invention; kneading the paste at a
temperature of 10.degree. C. to 80.degree. C.; extruding the paste
in a double-screwed extruder, and, if desired, drying the granules
obtained. The invention also relates to granules obtainable this
process.
[0056] The invention also relates to a process comprising
compressing the granules according to the invention, optionally in
mixture with auxiliaries and/or a pharmaceutically active agent to
prepare tablets. The invention also relates to tablets obtainable
by this process.
[0057] Crystalline amoxicillin trihydrate powder may be obtained by
preparing a solution comprising dissolved amoxicillin,
crystallizing the amoxicillin trihydrate from said solution to form
crystals, separating the crystals from said solution, and drying
the separated crystals. As used herein the term crystalline powder
includes, but is not limited to, the dried product obtained and/or
obtainable by this process.
[0058] It was surprisingly found that crystalline powder having
improved flow properties, in particular the high bulk density
and/or high tapped density can be obtained by selecting the
crystallizing, separation and/or drying conditions.
[0059] It was found that preparing crystalline powder having
improved flow properties, in particular high bulk density and/or
high tapped density, preferably includes carrying out the process,
in particular the crystallizing, separating and drying, under such
conditions that the dried crystals have an increased particle size,
in particular increased d.sub.50 and/or d.sub.10.
[0060] Preferred crystallization conditions may include a
relatively long residence time, relatively low concentrations of
amoxicillin in the aqueous solution, relatively low concentrations
of protein in the aqueous solution and/or using an aqueous solution
having high purity. Further preferred conditions are described
hereinafter.
[0061] It was further found that, in particular for crystals having
an increased size, the extent of mechanical impact, for instance
during crystallization, separation and/or drying influences the
bulk density and tapped density. If the crystals are subjected to
mechanical forces, for instance during drying and/or separating or
transport of the crystals, the bulk density and tapped density are
surprisingly found to increase compared to the situation where
there is no mechanical impact. However, if the mechanical forces
are too high, the bulk density and tapped density are found to
decrease. Mechanical impact during separating can for instance be
achieved during centrifuging. Mechanical impact during drying can
for instance be achieved by using a contact dryer, for instance a
Vrieco-Nauta contact dryer, or a flash dryer. Mechanical impact can
also be achieved by applying pneumatic transport, for instance
pneumatic transport of the amoxicillin trihydrate from the
separation step to the drying step. Without wishing to be bound by
any scientific theory, it is believed that a limited extent of
mechanical impact has the effect that relatively large crystals
having the shape of needles are broken, thereby resulting in an
increase of the bulk density and/or tapped density. However, a too
high extent of mechanical forces is believed to result in the
production of crystals that are too fine, thereby reducing the bulk
density and/or tapped density. Using this insight provided by the
invention and by varying the mechanical forces the skilled man is
able to find out the conditions where the optimal bulk density
and/or tapped density are achieved.
[0062] Accordingly, the invention provides a process for preparing
crystalline amoxicillin trihydrate powder, said process comprising:
crystallizing the amoxicillin trihydrate from a solution containing
dissolved amoxicillin; separating the crystals from said solution;
drying the separated crystals; wherein the process, preferably the
crystallizing, separating and/or drying, is carried out under such
conditions that the resulting crystalline powder has a bulk density
higher than 0.45 g/ml, preferably higher than 0.5 g/ml, more
preferably higher than 0.55 g/ml. There is no specific upper limit
for the bulk density. The process, preferably the crystallizing,
separating and/or drying, may for instance be carried out under
such conditions that the bulk density is less than 0.8 g/ml, for
instance less than 0.7 g/ml.
[0063] The invention also provides a process for preparing
crystalline amoxicillin trihydrate powder, said process comprising:
crystallizing amoxicillin trihydrate from a solution containing
dissolved amoxicillin; separating the crystals from said solution;
drying the separated crystals; wherein the process, preferably the
crystallizing, separating and/or drying, is carried out under such
conditions that the resulting crystalline powder has a tapped
density higher than 0.6 g/ml, preferably higher than 0.7 g/ml, more
preferably higher than 0.8 g/ml. There is no specific upper limit
for the tapped density. The process, preferably the crystallizing,
separating and/or drying, may for instance be carried out under
such conditions that the tapped density is less than 1.2 g/ml, for
instance less than 1.1 g/ml, for instance less than 1.0 g/ml.
[0064] The invention also provides a process for preparing
crystalline amoxicillin trihydrate powder, said process comprising:
crystallizing amoxicillin trihydrate from a solution containing
dissolved amoxicillin; separating the crystals from said solution;
drying the separated crystals; wherein the process, preferably the
crystallizing, separating and/or drying, is carried out under such
conditions that the resulting crystalline powder has ratio
d.sub.t/d.sub.b of less than 1.7, preferably less than 1.6,
preferably less than 1.5, preferably less than 1.45, wherein
d.sub.t=tapped density and d.sub.b=bulk density. There is no
specific lower limit for the ratio. The process, preferably the
crystallizing, separating and/or drying, may for instance be
carried out under such conditions that the ratio d.sub.t/d.sub.b is
higher than 1.05, for instance higher than 1.1.
[0065] The invention also provides a process for preparing
crystalline amoxicillin trihydrate powder, said process comprising:
crystallizing amoxicillin trihydrate from a solution containing
dissolved amoxicillin; separating the crystals from said solution;
drying the separated crystals; wherein the process, preferably the
crystallizing, separating and/or drying, is carried out under such
conditions that the compressibility index as defined by
((d.sub.t-d.sub.b)/d.sub.t*100% is less than 40%, preferably less
than 35%, more preferably less than 30%, wherein d.sub.t=tapped
density and d.sub.b=bulk density. There is no specific lower limit
for the compressibility index. The compressibility index may for
instance be higher than 10%.
[0066] The invention also provides a process for preparing
crystalline amoxicillin trihydrate powder, said process comprising:
crystallizing amoxicillin trihydrate from a solution containing
dissolved amoxicillin; separating the crystals from said solution;
drying the separated crystals; wherein the process, preferably the
crystallizing, separating and/or drying, is carried out under such
conditions that the resulting crystalline powder has a d.sub.50 of
higher than 10 .mu.m, preferably higher than 20 .mu.m, more
preferably higher than 30 .mu.m, in particular higher than 35
.mu.m, more preferably higher than 40 .mu.m. There is no specific
upper limit for the d.sub.50. The process, preferably the
crystallizing, separating and/or drying, may for instance be
carried out under such conditions the d.sub.50 of the resulting
crystalline powder is less than 150 .mu.m, for instance less than
100 .mu.m. Preferably, the process, preferably the crystallizing,
separating and/or drying, is carried out under such conditions that
the dried crystals have a d.sub.10 of higher than 3 .mu.m,
preferably higher than 5 .mu.m, more preferably higher than 8
.mu.m, more preferably higher than 10 .mu.m. There is no specific
upper limit for d.sub.10. The process, preferably the
crystallizing, separating and/or drying, may be carried out under
such conditions that d.sub.10 of the resulting crystalline powder
is less than 50 .mu.m.
[0067] The water activity that may be used to specify the extent to
which a product is dried, may have any suitable value. Drying may
be carried out such that the resulting crystalline amoxicillin
trihydrate powder has a water activity of for instance higher than
0.05, for instance higher than 0.1, for instance higher than 0.15,
for instance higher than 0.2, for instance higher than 0.25, for
instance higher than 0.3, for instance less than 0.7, for instance
less than 0.6, for instance less than 0.5. The water activity of
the crystalline amoxicillin trihydrate powder according to the
invention may for instance be higher than 0.05, for instance higher
than 0.1, for instance higher than 0.15, for instance higher than
0.2, for instance higher than 0.25, for instance higher than 0.3.
The water activity of the crystalline amoxicillin trihydrate powder
according to the invention may for instance be less than 0.7, for
instance less than 0.6, for instance less than 0.5. These values
refer to the water activity measured at 25.degree. C. The water
activity is known to be defined as the equilibrium relative
humidity divided by 100%. A preferred method for determining the
water activity of a sample is to bring a quantity of the sample in
a closed chamber having a relatively small volume, measuring the
relative humidity as a function of time until the relative humidity
has become constant (for instance after 30 minutes), the latter
being the equilibrium relative humidity for that sample.
Preferably, a Novasina TH200 Thermoconstanter is used, of which the
sample holder has a volume of 12 ml and which is filled with 3 g.
of sample.
[0068] Preferably, a process for preparing crystalline amoxicillin
trihydrate powder according to the invention comprises preparing
amoxicillin by reacting 6-amino-penicillanic acid or a salt
thereof, with para-hydroxyphenyl glycine in activated form in the
presence of an enzyme immobilized on a carrier; forming an aqueous
solution containing the amoxicillin, said aqueous solution
containing hydrochloric acid; and crystallizing the amoxicillin
trihydrate from said aqueous solution.
[0069] Preferably, the solution from which the amoxicillin
trihydrate is crystallized is an aqueous solution. Any suitable
aqueous solution may be used. Suitable aqueous solutions include
solutions wherein the weight ration water:organic solvent is
between 100:0 and 70:30, preferably between 100:0 and 80:20,
preferably between 100:0 and 90:10, preferably between 100:0 and
95:5, preferably between 100:0 and 99:1.
[0070] Preferably, the solution from which the amoxicillin
trihydrate is crystallized contains less than 200 weight parts of
protein per 1.000.000 weight parts of amoxicillin (total
concentration of amoxicillin, whether or not in dissolved form),
preferably less 100 weight parts of protein, more preferably less
than 50 weight parts of protein, more preferably less than 35
weight parts of protein.
[0071] Preferably, the solution from which the amoxicillin
trihydrate is crystallized is an aqueous solution having an
amoxicillin concentration (total concentration of amoxicillin,
whether or not in dissolved form) of less than 0.6 mol/l,
preferably less than 0.5 mol/l, more preferably less than 0.4
mol/l, more preferably less than 0.3 mol/l.
[0072] The aqueous solution from which the amoxicillin trihydrate
is crystallized, is preferably a solution containing hydrochloric
acid or chloride. The aqueous solution from which the amoxicillin
trihydrate is crystallized preferably contains between 0.9 and 5
mol of hydrodrochloric acid or chloride per mol amoxicillin (total
concentration of amoxicillin, whether or not in dissolved form),
preferably between 0.9 and 3 mol hydrochloric acid or chloride per
mol amoxicillin, more preferably between 0.9 and 1.5 mol
hydrochloric acid or chloride per mol amoxicillin. The aqueous
solution from which the amoxicillin is crystallized preferably
contains more than 1.0 mol of hydrochloric acid or chloride per mol
of amoxicillin.
[0073] Preferably, the amoxicillin trihydrate is crystallized from
an aqueous solution at a pH of between 2 and 7, preferably between
3 and 6. Preferably, the process comprises crystallizing
amoxicillin trihydrate from the aqueous solution in a first step
preferably at a pH of between 2 and 5, preferably between 3 and 4,
and in a second step at a pH higher than in the first step,
preferably between 4 and 7, preferably between 4.5 and 6.
[0074] Preferably, amoxicillin trihydrate is crystallized from the
aqueous solution at a temperature of between 5.degree. C. and
40.degree. C., preferably between 10 and 30.degree. C., more
preferably between 15 and 25.degree. C.
[0075] The solution from which the amoxicillin trihydrate is
crystallized may be prepared in any suitable way. The aqueous
solution containing dissolved amoxicillin may be prepared by
dissolving amoxicillin trihydrate. It is possible to add
amoxicillin trihydrate to a solution, and to effect dissolution of
the added amoxicillin trihydrate. It is also possible to prepare an
aqueous suspension by forming crystals of amoxicillin trihydrate in
situ in a solution, and effecting dissolution of the crystals of
amoxicillin trihydrate in said suspension. In a process for the
preparation of amoxicillin, the process preferably comprises
preparing an aqueous solution containing dissolved amoxicillin,
said aqueous solution having an amoxicillin concentration of less
than 0.6 mol/l, preferably less than 0.5 mol/l, more preferably
less than 0.4 mol/l, more preferably less than 0.3 mol/l. The
process preferably comprises preparing an aqueous solution
containing dissolved amoxicillin, said aqueous solution having a pH
of between 0 and 1.5, preferably between 0.5 and 1.2. Dissolving
amoxicillin, may be carried out in any suitable way, for instance
by adding an acid, preferably by adding hydrochloric acid to an
aqueous suspension containing crystals of amoxicillin trihydrate.
An acid, preferably hydrochloric acid, may be added in an amount of
between 0.9 and 5 mol of hydrodrochloric acid per mol amoxicillin,
preferably between 0.9 and 3 mol hydrochloric acid per mol
amoxicillin, more preferably between 0.9 and 1.5 mol hydrochloric
acid per mol amoxicillin. Preferably more than 1.0 mol of
hydrochloric acid is added per mol of amoxicillin. In a preferred
embodiment, the process comprises keeping the (aqueous) solution or
(aqueous) suspension at a pH of less than 1.5, preferably less than
1.2, during a period of less than 60 minutes, preferably less than
30 minutes, more preferably less than 15 minutes, more preferably
less than 10 minutes, more preferably less than 8 minutes, as this
may improve the purity of the amoxicillin. Preferably, the process
comprises mixing the aqueous solution or aqueous suspension with
the acid using a fast mixer, for instance a static mixer. This can
reduce the time during which the aqueous solution or suspension is
kept low pH. Mixing of the acid with the aqueous suspension may be
carried out at any suitable temperature, for instance higher than
-5.degree. C., for instance higher than 5.degree. C., for instance
higher than 10.degree. C., for instance higher than 15.degree. C.,
for instance less than 50.degree. C., for instance less than
40.degree. C. Preferably, the process comprises filtering the
solution prior to said crystallizing. Preferably, the process
comprises filtering the aqueous solution containing dissolved
amoxicillin, said aqueous solution preferably having a pH of
between 0 and 1.5, preferably between 0.5 and 1.2. The solution may
be passed through any suitable filter. Preferably, a filter is used
having a pore size of less than 40 .mu.m, preferably less than 20
.mu.m, preferably less than 10 .mu.m, and more preferably less than
5 .mu.m.
[0076] Amoxicillin trihydrate may advantageously be crystallized
from said aqueous solution by increasing the pH, for instance by
adding a base, for instance NaOH.
[0077] The crystallization may be carried out batch wise or
continuously. When the process is carried out batch wise, addition
of seed crystals to the aqueous solution is preferred. Preferably,
the crystallization is carried out continuously.
[0078] Amoxicillin is preferably prepared by reacting
6-amino-penicillanic acid or derivatives thereof, for instance a
salt of 6-amino-penicillanic acid, with an acylating agent selected
from para-hydroxyphenyl glycine in activated form in the presence
of an enzyme in an aqueous reaction medium. The para-hydroxyphenyl
glycine in activated form is preferably an ester or amide of
para-hydroxyphenylglycine. Suitable esters include for instance 1
to 4 alkyl esters, for example methyl ester, ethyl ester, n-propyl
or isopropyl esters. Glycol esters, for instance an ethylene glycol
ester, may also be used. An amide that is unsubstituted in the
--CONH.sub.2 group may be used.
[0079] The enzyme may be any enzyme having hydrolytic activity
(hydrolase). The enzyme may for instance be an acylase, inter alia
Penicillin G acylase, amidase or esterase. Enzymes may be isolated
from various naturally occurring microorganisms, for example fungi
and bacteria. Organisms that have been found to produce penicillin
acylase are, for example, Acetobacter, Aeromonas, Alcaligenes,
Aphanocladium, Bacillus sp., Cephalosporium, Escherichia,
Flavobacterium, Kluyvera, Mycoplana, Protaminobacter, Pseudomonas
or Xanthomonas species.
[0080] Processes for the preparation of amoxicillin in the presence
of an enzyme have been described in WO-A-9201061, WO-A-9417800,
WO-A-9704086, WO-A-9820120, EP-A-771357, the contents of which are
incorporated by reference.
[0081] The reaction may be carried out at any suitable pH,
preferably at a pH of between 5 and 9, preferably between 5.5 and
8, more preferably between 6 and 7.5. The reaction may be carried
out at any suitable temperature, for instance carried out at a
temperature of between 0 and 40.degree. C., preferably between 0
and 30.degree. C., more preferably between 0 and 15.degree. C.
[0082] The amoxicillin formed may be crystallized under the
conditions at which the reaction is carried out. Crystallization of
amoxicillin may for instance be effected at a pH of between 5 and
8, preferably between 5.5 and 7.5.
[0083] Preferably, the enzyme is an enzyme immobilized on a
carrier. Any suitable carrier may be used. Preferably, the carrier
comprises a gelling agent and a polymer containing free amino
groups. Preferably, the polymer is selected from alginate amine,
chitosan, pectin, or polyethylene imine. Preferably, the gelling
agent is gelatin. This carrier and the preparation thereof are
described in EP-A-222 462 and WO-A-9704086. Prior to
immobilization, the isolated enzyme is preferably purified using
ion exchange chromatography.
[0084] Preferably, the enzyme is an enzyme immobilized on a
carrier, and the process preferably comprises separating a product
comprising the amoxicillin formed from the immobilized enzyme. Said
separating of the product from the immobilized enzyme may be
carried out using any suitable method, for instance by using
gravity or a screen that is not permeable to the major part of the
immobilized enzyme. Preferably, the product separated from the
immobilized enzyme contains less than 200 weight parts of protein
per 1.000.000 weight parts of the amoxicillin, preferably less 100
weight parts of protein, more preferably less than 50 weight parts
of protein, more preferably less than 35 weight parts of protein
per 1.000.000 weight parts of the amoxicillin. This is preferably
achieved by applying an enzyme sufficiently immobilized on a
carrier to avoid separation of small amounts of protein from
amoxicillin trihydrate. This has the advantage that the final
amoxicillin trihydrate obtained contains less than 200 weight parts
of protein per 1.000.000 weight parts of the amoxicillin,
preferably less 100 weight parts of protein, more preferably less
than 50 weight parts of protein, more preferably less than 35
weight parts of protein per 1.000.000 weight parts of amoxicillin.
The product separated from the immobilized enzyme may be an aqueous
solution containing amoxicillin in dissolved form. The product
separated from the immobilized enzyme may also be a wet cake. The
separated product is preferably an aqueous suspension comprising
amoxicillin trihydrate crystals. Preferably, the process comprises
dissolving said amoxicillin trihydrate crystals to form an aqueous
solution containing dissolved amoxicillin.
[0085] The invention also relates to crystalline amoxicillin
trihydrate powder obtainable by the process according to the
invention.
[0086] The invention will be further elucidated by means of the
following examples, without however being limited thereto.
EXAMPLES AND COMPARATIVE EXPERIMENT
Examples I-V
Preparation of Immobilized Enzyme
[0087] Escherichia coli penicillin acylase was isolated as
described in WO-A-9212782, purified using ion exchange
chromatography, and immobilized as described in EP-A-222462 and
WO-A-9704086.
[0088] As definition of penicillin G acylase activity the following
is used: one unit (U) corresponds to the amount of enzyme that
hydrolyses per minute 1 .mu.mole penicillin G under standard
conditions (100 g.l.sup.-1 Penicillin G potassium salt, 0.05 M
potassium phosphate buffer, pH value 8.0, 28.degree. C.).
Production of Amoxicillin
[0089] 162.2 g of 6-APA (6-amino-penicillanic acid) and 184.8 g of
HPGM (D(-)-p-hydroxyphenylglycine methyl ester) were suspended in
450 ml of water. The suspension was cooled to a temperature of
10.degree. C. To this reaction mixture 32850 Units of immobilized
penicillin acylase were added, and water was added to a final
volume of 1500 ml. The mixture was stirred for 6 hours. During the
reaction the pH increased to 6.9, and at the end of the reaction
the pH had decreased to 6.2. To this mixture 750 ml of water was
added, and the suspension was filtrated over a sieve (with a mesh
of 100 micrometer) in 2 hours to separate off the immobilized
enzyme. The suspension obtained containing the amoxicillin
trihydrate crystals was cooled to 0.degree. C. The suspension
contained less than 50 ppm of protein relative to amoxicillin
trihydrate (less than 50 weight parts of protein per 1.000.000
weight parts of amoxicillin trihydrate).
[0090] An aqueous suspension containing amoxicillin in water (100 g
amoxicillin trihydrate per liter of suspension) as obtained above
was mixed with a 32 wt. % HCl solution (at a temperature of
25.degree. C.) using a static mixer such as to obtain a solution
having a pH of 1. The residence time in the static mixer was 1.5
minutes. The acidic solution obtained is pumped through two
filters, the first filter having pores of 40 .mu.m, the second
filter having pores of 4.5 .mu.m. The residence time in the filters
was about 3 minutes. The acidic filtered solution and is fed to a
first stirred tank in which a pH of 3.7 is maintained by addition
of 8 M NaOH solution. The temperature in the first tank is between
17 and 23.degree. C. The residence time in the first tank is 45
minutes. The contents of the first tank are fed to a second stirred
tank in which a pH of 5.0 is maintained by addition of a 8 M NaOH
solution. The temperature in the second stirred tank is between 17
and 23.degree. C. The residence time in the second stirred tank is
15 minutes. The contents of tank 2 fed to a third stirred tank in
which the a temperature of 1 to 5.degree. C. is maintained, the
residence time in the third tank being more than 4 hours. The
contents of the third stirred tank are fed to an inverted filter
centrifuge such as to isolate the amoxicillin crystals, resulting
in a wet cake containing 86 wt. % solid material. The wet cake was
washed with water, pneumatically transported to a conical vacuum
contact drier (Vrieco-Nauta), in which it was dried at a
temperature of 30 to 40.degree. C. and a pressure of 30 mbar during
7 hours.
Measurement of Particle Size Distribution, Bulk Density and Tapped
Density.
[0091] The particle size distribution (including d.sub.10 and
d.sub.50) of samples from the mixer was determined using a Malvern
particle sizer 2600 C with objective f=300 mm, malvern sample
measurement unit PS1 and a Malvern dry powder feeder PS 64. The
beam length was 14.30 mm. A polydisperse analysis model was
used.
[0092] The bulk density was determined according to USP 24, method
I, (page 1913).
[0093] The tapped density was determined according to USP 24,
method II, (page 1914).
[0094] Five different batches were prepared using the method
described above. Table I shows the tapped density, bulk density,
d.sub.50, d.sub.10 of the resulting crystals.
Example VI
[0095] The powder of example V was subjected to air jet sieving
(200 LS-N air jet sieve manufactured by Hosakawa Alpine). Sieving
was carried out using a 75 .mu.m screen during 10 minutes. A few
agglomerates formed during said sieving were removed from the
overheads fraction (not passed through the sieve) using a vibrating
sieve (425 .mu.m), after which tapped density, bulk density,
d.sub.50, d.sub.10 of the resulting crystals of the overheads
fraction was determined. The results are indicated in table 1. This
example shows that the compressibility and the Hausner ratio are
further decreased. The resulting powder flows through Klein cup 8
mm.
TABLE-US-00001 TABLE 1 Bulk dens. Tap. dens. (d.sub.b) (d.sub.t)
d.sub.b*(1/d.sub.b - 1/d.sub.t) d.sub.50 d.sub.10 (g/ml) (g/ml)
d.sub.t/d.sub.b *100% (.mu.m) (.mu.m) Ex. I 0.51 0.73 1.43 30% 43.1
11.4 Ex. II 0.56 0.78 1.39 28% 42.8 8.8 Ex. III 0.56 0.81 1.45 31%
47.8 9.9 Ex. IV 0.54 0.81 1.50 33% 37.0 7.0 Ex. V 0.58 0.79 1.36
26% 61 19 Ex. VI 0.59 0.74 1.25 20% 86 36 Comp. A 0.26 0.55 2.12
53% 17 4.0 Ref. B 0.26 0.47 1.8 45% 66.3 17.4
Comparative Experiment A
[0096] In a chemical process for the preparation of amoxicillin, a
solution containing amoxicillin in dilute HCl and isopropanol was
obtained. This solution was fed to a stirred tank. The pH was kept
at 3.7 at a temperature of 20.degree. C. Subsequently the pH was
raised to 5.0 by adding NaOH. The resulting mixture is maintained
in a vessel at 1 to 5.degree. C. during 3 to 12 hours. The
amoxicillin was separated using a centrifuge, and dried using a
fluid bed dryer. Table 1 shows the tapped density, bulk density,
d.sub.50, d.sub.10.
Reference Experiment B
[0097] Example I was repeated with the difference that a the drying
was not carried out using the a conical vacuum contact drier
(Vrieco Nauta), but using a drier wherein the material was not
mechanically impacted (Ventilation stove). Drying was carried out
at a temperature of 35.degree. C. during 16 hours. The results are
indicated in table 1. Comparison of examples I-IV with example B
shows that the use of mechanical impact during drying results in an
increased bulk density and tapped density.
Example VII
[0098] 6 Gelatine capsules (size 0) were filled by hand with of
crystalline amoxicillin trihydrate powder of example IV (500 mg on
an anhydrous basis per capsule). No auxiliaries were added.
Dissolution tests were applied using apparatus 1 under the
conditions as described in USP 27 under paragraph "amoxicillin
capsules", including a stirring rate of 100 rpm and a temperature
of 37.degree. C. Six beakers each containing 900 ml of water were
used. Samples were taken each 5 minutes, and the quantity of
dissolved amoxicillin were determined employing UV absorption at
the wavelength of maximum absorbance at 272 nm.
84 wt. % of the amoxicillin was dissolved in 15 minutes. 90 wt. %
of the amoxicillin was dissolved in 20 minutes.
Comparative Experiment C
[0099] Example VII was repeated using commercial granular
auxiliary-free amoxicillin trihydrate granules obtained by roller
compacting of amoxicillin trihydrate powder having the size
distribution as indicated in table 3. After 60 minutes 82.0 wt. %
of the amoxicillin was dissolved
Comparative Experiment D
[0100] Example VII was repeated using commercial granular
auxiliary-free amoxicillin trihydrate having a different particle
size distribution as indicated in table 3. The results are
indicated in FIG. 1. After 60 minutes 84.4 wt. % of the amoxicillin
was dissolved
TABLE-US-00002 TABLE 2 125- 250- 500- 850- <125 250 500 850 1000
>1000 Bulk Tapped .mu.m .mu.m .mu.m .mu.m .mu.m .mu.m density
density Ex. C 14.5 4.9 20.7 53.7 5.6 0 0.68 0.85 Ex. D 8.6 3.1 24.9
57.1 6.3 0.3 0.69 0.83
Example VIII
[0101] 20 g of amoxicillin trihydrate crystalline powder according
to the invention, 2 g of microcrystalline cellulose (Avicel.RTM.
PH102) were weighed in a 200 ml container and mixed in a Turbula
T2C blender for 5 minutes. 0.1 g of Magnesium stearate was added
mixed for an additional 2 minutes.
[0102] Part of the mixture was transferred to a die with a diameter
of 7 mm and a height of 2.3 cm, such that the die was completely
filled. A punch was placed on top of the die and a pressure of 5 kg
was applied during 5 seconds. The resulting empty space in the die
was completely filled and a pressure of 5 kg was applied again.
This procedure was repeated until no volume decrease was observed.
Finally, the formed plug was released from the die in fed into an
empty gelatine capsule body nr.0 Star-locks of Capsugel. The
composition of the formulation is as follows:
TABLE-US-00003 Amoxicillin trihydrate crystalline 570.1 mg (500 mg
amoxicillin) powder Microcrystalline cellulose 57.1 mg Magnesium
stearate 2.8 mg Sum 630.0 mg
This example shows that the crystalline powder according to the
invention can directly be used for filling capsules without
compactation or granulation step in a specified quantity of 500 mg
amoxicillin (calculated as amoxicillin anhydrate)
Example IX
[0103] 297.5 g of amoxicillin trihydrate crystalline powder
according to the invention, 88.5 g of microcrystalline cellulose
(Avicel.RTM. PH200), 10 g of croscarmellose sodium
(Ac-Di-Sol.RTM.), and 1 g of silicium dioxide colloidal
(Aerosil.RTM. 200), are weighed in a 1000 ml container and mixed in
a Turbula TC2 blender for 10 minutes, 3 g of magnesium stearate is
added and mixed for an additional 2 min.
[0104] The mixture is transferred to a hopper of a Korsch.RTM. EKO
excenter tablet press, and tablets are pressed with the following
properties:
[0105] The composition of the formulation is as follows:
TABLE-US-00004 Amoxicillin trihydrate crystalline 581.7 mg (500 mg
amoxicillin) powder Microcrystalline cellulose 190.3 mg
Croscarmellose sodium 20 Silicium dioxide colloidal 2 Magnesium
stearate 6 mg 800 mg
* * * * *