HYDROGEN PEROXIDE PLANT - FLUIDIZED BED TECHNOLOGY
SUMMARY
Hydrogen peroxide is produced by
cyclic reduction and oxidation of a mixture of 2-ethylanthraquinone (EAQ) and
2-ethyltetrahydroanthraquinone (H4EAQ). These anthraquinones are
dissolved in organic solvents (The mixture is called as Working Solution (WS)).
The anthraquinones are catalytically hydrogenated to form
2-ethyltetrahydroanthrahydroquinone (H4EAQH2). Catalyst
is separated from the working solution and returned back to the hydrogenator. Hydrogenated
working solution combines with air (oxygen) in the oxidizer to form hydrogen
peroxide. Hydrogen peroxide dissolved in working solution is extracted by
demineralised water in the extractor. The working solution is dried by
evaporation in the WS drier before it is returned to the hydrogenator feed
tank. The aqueous phase from the extractor can contain up to 40 wt-% hydrogen
peroxide but for efficiency reasons, normally max. 35 wt-% is produced. The
final product concentrations (50 and 70 wt-%) are reached by vaporization and
distillation of the crude hydrogen peroxide solution in the concentration unit
(see doc 2.5.3-02). In the product day tanks stabilizer is added to the
hydrogen peroxide solution to prevent decomposition.
PROCESS
DESCRIPTION
The design of this hydrogen peroxide
plant is based on the anthraquinone process (AO-process). It is based on cyclic
reduction and oxidation of a mixture of 2-ethylanthraquinone (EAQ) and 2-ethyltetrahydroanthraquinone
(H4EAQ), the so-called “All-tetra system”. This system got its name
since the only hydrogenated quinone is 2-ethyltetrahydroanthrahydroquinone
(H4EAQH2).
The anthraquinones are dissolved in
a mixture of organic solvents, the so-called working solution (WS). The main
components apart from anthraquinones are an aromatic solvent (non-polar solvent
for dissolving H4EAQ), tetrabutyl urea (polar solvent for dissolving
hydrogenated anthraquinone H4EAQH2) and trioctyl
phosphate (polar solvent and corrosion inhibitor). The main equipments in the
working solution loop are the hydrogenator (R1031), oxidizer (R2061), extractor
(C3011) and WS dryer (S3202).
1
Hydrogenation
Working solution from the
hydrogenator feed tank (T1021) is pumped by the
hydrogenator feed pump (P1022)
to the bottom of the hydrogenator (R1031)
via the WS cooler (E1025) and the
eductor (P1026). Recycled catalyst and
working solution from the primary
filters (F1101-F1105) are injected into the
working solution through the
eductor (P1026). The main working solution
stream works as motive flow for the
eductor and provides the driving force for
the recycle stream. Hydrogen enters
the hydrogenator (R1031) at the bottom
through spray nozzles. Working solution,
catalyst and hydrogen are intimately
mixed so that the main hydrogenation
reaction, conversion of anthraquinone
(H4EAQ) to anthrahydroquinone
(H4EAQH2), takes place in the hydrogenator
(R1031). The
conversion ratio is primarily controlled by the amount and activity
of the
catalyst present, temperature, agitation intensity, and hydrogen pressure.
The
temperature is controlled by a cylindrical cooling element inside the
hydrogenator (R1031), which also provides the necessary agitation.
cat
(H4EAQ) +3H2 -----------› (H4EAQH2)
Main hydrogenation reaction
In the top of hydrogenator (R1301)
working solution and catalyst are separated from excess hydrogen. Working
solution and catalyst flow through the primary filters (F1101-F1105) which have
sintered stainless steel filter elements. The filtrate flows through the filter
elements into the oxidiser feed tank (T2001). Catalyst particles are retained
on the elements and recycled to the eductor (P1026).
Much of the catalyst falls off the
filter elements due to the turbulent flow in the filter. However, the filter
elements can become coated with excessive quantities of catalyst, and for this
reason a periodic back-flush, where the flow direction through the filters is
reversed, is required. The back-flush is generated with working solution from
the oxidiser feed tank (T2001) pumped by the primary filter backwash pump
(P2005), if required it may be passed through the backwash cooler (E2007).
Hydrogen gas, separated from working
solution and catalyst, is discharged from the top of the hydrogenator (R1301).
Excess hydrogen gas is recycled back to the hydrogenator (R1301) via the H2
recycle compressor unit (B1011). Make-up hydrogen combines with recycled hydrogen
and is fed to the hydrogenator (R1301).
Make-up hydrogen flow is the
determining factor in controlling the pressure in the hydrogenator (R1301).
When the pressure is below the set-point the make-up hydrogen control valve
(PV1039A) opens and make-up hydrogen is added to maintain the desired system
pressure.
A small amount of hydrogen is bled
off from the system to control the concentration of inerts. This purge is taken
from the discharge of the H2 recycle compressor unit (B1011). The
organic content of the purge is condensed in the H2 vent cooler
(E1015). The condensed solvent is returned to the seal liquid tank (S1012). The
purge gas is further purified in the hydrogen vent adsorbers (C1050A/B) before
being discharged to the atmosphere.
PROCESS
PARAMETERS
Hydrogenator (R1301)
Inlet temperature (WS) 44 °C
Outlet
temperature 52-59 °C
Operating
pressure 0.8-1.2 kg/cm2g
SAFETY
OF THE HYDROGENATION
As hydrogen has an extremely wide
explosive range with oxygen, it is important to keep control of the oxygen
content. The start-up phase is more critical than the normal operation, which
will be explained below.
To ensure the safety of the plant
two redundant oxygen meters (instrument AI 1002 and AI 1041) are installed in
the hydrogen loop. When hydrogen is fed at least one of the analysers must be
in operation (by pass is only allowed for calibration of one analyzer at the
time). During the venting before hydrogen cut in, both analysers are bypassed
(to avoid emergency shut down due to high oxygen content). When the oxygen
content is below a safe limit the analyzer alarms and interlocks are activated.
Hydrogen feed can not start until at least one analyzer is active.
As soon as the hydrogenation has
started the H4EAQH2 concentration starts to build up. Any
oxygen entering the system will be consumed by oxidation of the H4EAQH2,
forming hydrogen peroxide and H4EAQ. The H2O2 will
decompose due to the presence of catalyst, forming ½ hydrogen and water. Note
that the oxygen amount has been halved. These two reactions continue, and
ultimately the oxygen ends up as water. Hence, the system has an inherent
safety against oxygen during operation, although the reactions represent as
loss of overall yield.
2
OXIDATION
Working solution from the oxidizer
feed tank (T2001) is pumped by the oxidizer feed pump (P2002) through secondary
filters (F2011-F2013) and safety filters (F2021-F2022). The safety filters
(F2021-F2022) provides appositive safeguard against trace quantities of
catalyst entering the oxidizer (R2061) in event of failure of the secondary
filter system. After the safety filters (F2021-F2022) the working solution is
passed through the oxidizer cooler (E2042). It is necessary to cool the
solution prior to oxidation, since oxidation is an exothermic reaction.
Oil-free compressed air is supplied
to the oxidizer (R2061). The air intake shall be isolated as much as possible
from sources of atmospheric contamination such as power plant stack gases, etc.
Process air from process air compressor (B2051/B2052) is passed through the
process air buffer vessel, the oxidizer air filter (F2055A/B) and fed to the
oxidizer (R2061). The feed line is supplied with a loop that diminishes the
possibility of working solution flowing back into the air supply system in case
of compressor failure.
Air is supplied in the bottom of the
oxidizer (R2061) through spray pipes. The organic flow enters the oxidizer
(R2061) at the top of the vessel and flow counter-currently down through the
reactor. The oxidizer (R2061) is supplied with eight sieve trays (to ensure
good dispersion of air bubbles, required for mass transfer).
In the oxidation step hydrogen
peroxide is produced. Anthrahydroquinone (H4EAQH2) is
oxidised to anthraquinone (H4EAQ) and the oxygen is reduced to
hydrogen peroxide. At this point hydrogen peroxide is dispersed in the working
solution.
(H4EAQH2) +O2 -----------› (H4EAQ) + H2O2
Oxidiser reaction
The oxidiser off gas exits at the
top of oxidizer (R2061) and is passed through the oxidiser off gas chiller
(E2071) and the oxidizer off gas demister (S2072) into the solvent recovery
unit (X2501). In the solvent recovery unit the remaining organic solvent in the
off gas is recovered before the off gas is released to the atmosphere. The
working solution is discharged from the bottom of the oxidizer (R2061) through
the oxidiser outlet cooler (E2062) into the oxidiser degasser (S2063). The
purpose of the oxidiser degasser (S2063) is to maintain the amount of dissolved
air entering with working solution into the extractor (C3011). Release of air
in the extractor (C3011) will disturb the extractor.
PROCESS
PARAMETERS
Oxidiser (R2061)
Inlet temperature (WS) 42 °C, min. 37 °C
Inlet
temperature (air) 40 °C
Outlet
temperature 52 °C, max. 60°C
Operating
pressure (top) ~1.5 kg/cm2g
Oxidiser degasser (S2063) Operating
Pressure Atmospheric
SAFETY
IN THE OXIDATION
The most critical parameters to
control in the oxidation system are the temperature and off gas oxygen content.
During start up, the temperature shall be kept as low as possible to reduce the
risk of explosions in the top of the oxidizer. During operation high
temperature results in loss of product due to increased decomposition rate. Off
gas oxygen content shall be kept below 10 vol-%, which ensures safe operation
of the reactor and solvent recovery.
It is very important that no
catalyst enters the oxidiser. To ensure this the WS is passed through secondary
and safety filters. A catalyst detector is installed to indicate catalyst
slipping through the secondary filters.
In the oxidiser feed tank (T2001)
working solution is held as a buffer for the oxidiser. In case of hydrogen
release the oxidiser feed tank (T2001) atmosphere is kept inert by nitrogen.
3
EXTRACTION
Working solution from the oxidiser
degasser (S2063) is fed by the extractor feed pump (P3001) into the bottom of
the extractor (C3011). Demineralised water is fed to the top of the extractor
(C3011). Stabiliser, in the form of phosphoric acid, is added to the the
extractor (C3011). In the column, water is the continuous phase and working
solution is the discontinuous phase. Due to the difference in of the two phases
(working solution being the lighter) the working solution rises and discharges
from the top of the extractor (C3011) after being stripped of its hydrogen
peroxide. The aqueous phase discharging from the bottom of the extractor
(C3011) is controlled about 35 wt-% of hydrogen peroxide.
The extractor (C3011) consists of 32
sieve trays. The trays are specially designed in order to maintain the required
residence time, good separation of hydrogen peroxide from the working solution
and good re-dispersion of WS above the trays. Working solution passes through a
coalescing polyethylene mesh before it is collected below the trays until it is
forced through the holes, forming bubble droplets that rise through the water
phase to the next tray.
In top of the column a coalescer pad
is installed to improve the performance by reducing the overhead aqueous
content. Working solution from the extractor (C3011) top passes the WS
coalescer (S3015). The WS coalescer (S3015) is designed to coalesce and remove
(by settling) the major part of the entrained water.
PROCESS
PARAMETERS
Extractor (C3011)
Operating temperature 37-45 °C
Operating pressure Atmospheric
SAFETY
IN EXTRACTION
It is important to ensure that the
hydrogen peroxide content in the product does not exceed 41 wt-%, as the risk
for reaction with working solution components increases with increased
concentration. 40-41 wt-% is a well established safe concentration in the
operating temperature range.
The temperature in the extraction
must be carefully monitored for the same reason. In case of shutdowns that last
more than one hour is very important to ensure that the working solution is well
extracted, and that the hydrogen peroxide concentration in the bottom of the
column is below 20 wt-% before working solution circulation is restarted. Failure
to do this may result in so called reverse extraction, when hydrogen peroxide
is transferred from the aqueous solution to the working solution. Then there is
a risk that hydrogen peroxide is carried over to the hydrogenation, resulting
in violent decomposition.
4
CRUDE PRODUCT PURIFICATION AND
INTERMEDIATE STORAGE
Crude hydrogen peroxide from the
extractor (C3011) is passed through the
crude cooler (E3017) into the crude
coalescer 1 (S3120) either by the crude
product pump (P3016) or by gravity
(depending on product flow). The crude
coalescer 1 (S3120) and crude coalescer
2 (S3121) are connected in series and
are designed to coalesce and remove the
majority of entrained solvent. The
removed liquid is decanted in the bleed
decanter (S3122) and the removed
solvent is returned back to the oxidiser
degasser (S2063). Hydrogen peroxide
from the crude coalescer 2 (S3121) and
recovered hydrogen peroxide from the
bleed decanter (S3122), flows by gravity
to the first product holding tank
(T3501).
The product holding tanks
(T3501-T3504) are connected in series with a small
difference in height over
the ground level, thus allowing the filling of T3504 via
T3503 and T3502 from
T3501 by gravity flow. Over time, organic material (from
the crude hydrogen
peroxide feed), may appear as a light organic phase in top
of the product holding
tanks (T3501-T3504). These organics are batch-wise
recycled back to the
AO-process by the solvent return pump (P3510).
The crude hydrogen peroxide from
T3504 is pumped by the concentrator feed
pump (P3540A/B) to the hydrogen
peroxide concentration unit.
PROCESS
PARAMETERS
Crude coalescer 1 (S3120) & crude coalescer 2 (S3121)
Operating temperature 40 °C
Operating pressure Atmospheric
Crude hydrogen peroxide
concentration 35 wt-%
SAFETY
IN THE PRODUCT HOLDING TANKS
The temperature in the product
holding tanks is the most critical parameter to
watch, both as an indicator of
and to suppress decomposition. As a rule of
thumb the decomposition rate of
hydrogen peroxide is doubled for every 10 °C
increase in temperature. Under normal conditions hydrogen peroxide is stable,
<1.0 % decomposition per year at 30 °C. Increased
decomposition rate is
usually due to impurities. Organic substances or
oxidisable metal ions will
drastically increase decomposition rate.
Decomposition of hydrogen peroxide is
an exothermic reaction. Unexpected rise
in temperature in a storage tank is
therefore an indication of decomposition.
All product holding tanks for
hydrogen peroxide solution are equipped with
temperature indicators. In case of
accelerated decomposition, water can be
pumped by the DMW pump (P3532A/B) from
the DMW tank (T3531) to dilute
and cool the tank content. The DMW tank (T3531)
is connected to all the
hydrogen peroxide product holding tanks (T3501-T3504).
5
WORKING SOLUTION DRIER
The working solution from the WS
coalsescer (S3015) is heated in the WS
heater (E3201) before entering the WS
drier (S3202). The pressure in the WS
drier (S3202) is reduced by the vacuum
pump (B3221) to flash the water from
the working solution. The dried working
solution from the WS drier (S3202) is
returned by gravity to the hydrogenator
feed tank (T1021). The purpose of
drying the working solution is to optimize
the catalyst behavior. Free water is
adsorbed onto the catalyst, resulting in
loss of catalyst fluidization and activity.
The flashed water is condensed in
the drier condenser (E3211) and in the
vacuum pump unit (B3221). The condensate
is led to the solvent/water
separator (S3231) where entrained solvent is
recovered. The water from the
solvent/water separator (S3231) is recycled to
the DMW feed tank (T3535)
where it can be reused as extractor feed.
PROCESS
PARAMETERS
WS drier (S3202)
Operating temperature 50-55 °C
Operating
pressure 0.06 kg/cm2a
6
REGENRATION OF WORKING SOLUTION
Due to the circulating working
solution, undesirable compounds (principally
different quinones) can accumulate
in the system. In order to keep the
concentration of the undesirable compounds
in the working solution to a low
level, it is essential to convert them into
active quinones. This is carried out in
columns with activated alumina, the
process is known as regeneration.
A side stream of about 7 % of the
main working solution flow is regenerated in
an activated alumina bed
(regeneration column C2221 or C2222). The
regeneration stream is hydrogenated
working solution taken from oxidiser feed
tank (T2001). The working solution is
pumped through the regeneration system
by the regeneration system by the
regeneration feed pump 1 (P2211). It is
heated to the required temperature in
the regeneration economiser (E2213) and
the regeneration feed heater (E2215)
and fed to the bottom of the activated
alumina packed regeneration column
(C2221 or C2222). In this column the
undesirable quinones are converted to active
quinones and the irreversibly
degraded
quinones are removed by adsorption over the activated alumina bed.
Working
solution from the regeneration column (C2221 and C2222) is passed
through the
regeneration economiser (E2213) and through the regeneration
polishing filter 1
(F2225) on its way back to the oxidiser feed tank (T2001).
The optional regeneration stream is
oxidized working solution from the
hydrogenator feed tank (T1021). The working
solution is pumped through the
system by the regeneration feed pump 2 (P2228).
This stream is not heated
before entering the regeneration column (C2221 and
C2222). The regenerated
working solution is returned to the hydrogenator feed
tank (T1021) via
regeneration polishing filter 2 (F2229). This path is used to
make use of the
remaining adsorption capacity before discharging the spent
alumina. If this path
is used with fresh alumina bed, the reversed
hydrogenation of anthraquinones
will take place. An option that is used to control the EAQ/H4EAQ relation
in the
working solution.
PROCESS
PARAMETERS
Regeneration column
Operating temperature
From
T2001 71 °C
From
T1021 52 °C
Operating
pressure 3.5 kg/cm2g
7
PRODUCT STORAGE
This hydrogen peroxide plant has the
following storage facility.
The
product tank farm area consisting of five product day tanks (T5001-T5005) and
five product storage tanks (T5006-T5010). The capacity of each the product day
tanks are for T5001-T5004 60 m3 and for T5005 40 m3. The
product storage tanks T5006 has a capacity of 20 m3, T5007-T5009 a
capacity of 120 m3 each and T5010 80 m3.
The concentrated product
from the hydrogen peroxide concentration unit is
taken to the product day tanks
(T5001-T5005). The last product day tank
(T5005) and the last product storage
tank (T5010) are separated from the other
tanks and are used for product with
low concentration (35 wt-%) or high
concentration (70 wt-%). In the product day
tanks (T5001-T5005) stabilizer
adjustments are made. The hydrogen peroxide
shall be kept in the product day
tanks (T5001-T5005) until the correct concentration,
purity and stability has
been verified by the laboratory. Then the final
product is transferred by the
product transfer pump (P5021A/B) or the product
storage pump 2 (P5027) to
the product storage tanks (T5006-T5009 or T5010).
From the product storage
tanks (T5006-T5010) the product can be pumped to
filling station for trucks or
(for T5006-T5009) pumped by the filling station feed
pump (P6003/P6004) to
the filling station buffer tank (T6005). From there the
product flows by gravity
to the different filling stations X6010, X6011 and
X6012 for 30/50 kg carboys
and X6110 for 50 kg carboys/250 kg drums.
If necessary, unstabilised
product in the product day tanks (T5001-T5005) can
be sent to the hydrogen
peroxide concentration unit for further concentration.
For
this purpose the concentration feed pump (P5035A/B) is used. It is very
important not to send stabilised product back to the concentration unit where
the stabiliser can cause severe corrosion damages.
PROCESS
PARAMETERS
Operating temperature Ambient
Operating pressure of storage tanks Atmospheric
Crude hydrogen peroxide
concentration 35 wt-%
Hydrogen peroxide concentration 50 and 70 wt-%
SAFETY
IN THE PRODUCT STORAGE
The temperature in the
storage tanks is the most critical parameter to watch,
both as an indicator of
and to suppress decomposition. As a rule of thumb the
decomposition rate of
hydrogen peroxide is doubled for every 10 °C
increase in
temperature. Under normal conditions hydrogen peroxide is stable,
<1.0 %
decomposition per year at 30 °C.
Increased decomposition rate is usually due to
impurities. Organic substances
or oxidisable metal ions will drastically increase
decomposition rate.
Decomposition of hydrogen peroxide is an exothermic
reaction. Unexpected rise
in temperature in a storage tank is therefore an
indication of decomposition.
All storage tanks for
hydrogen peroxide solution are equipped with temperature
indicators. In case of
accelerated decomposition, water can be pumped by the
DMW pump (P3532A/B) from
the DMW tank (T3531) to dilute and cool the tank
content. The DMW tank (T3531)
is connected to all the hydrogen peroxide
day/storage tanks (T5001-T5010).
8
STABILISER ADDITION
In order to improve the stability of
hydrogen peroxide solution, stabilisers are
added to the extractor (C3011) and
to the product day tanks (T5001-T5005).
For stabilisation in the extractor (C3011)
phosphoric acid is used. Concentrated
phosphoric acid from barrels is pumped by
the acid addition pump (P5191) to
the diluted acid (stabiliser) tank (T5171)
where it is diluted with demineralised
water. The solution from the diluted
acid (stabiliser) tank (T5171) is pumped by
the acid (stabiliser) dosing pump
(P5172A/B) to the extractor (C3011).
For stabilising the end product in
the product storage tanks (T5001-T5005)
many different stabilisers can be used.
Stabiliser solution from barrels is
pumped by the stabilize addition pump
(P5182) to the stabiliser tank (T5181)
where it can be diluted with
demineralised water. From the stabiliser tank
(T5181) the stabiliser solution
is pumped by the stabiliser dosing pump (P5182)
to any of the product day tanks
(T5001-T5005). Controlled stabiliser addition is
done in stages after checking
the stabiliser concentration of the hydrogen
peroxide in each stage.
PROCESS
PARAMETERS
Operating temperature Ambient
Operating pressure of stabiliser
tanks Atmospheric
Acid concentration to extractor
(C3011) 10 wt-%
9
WORKING SOLUTION MAKE-UP
The working solution is primarily
composed of solvents and 2
ethylanthraquinone, which are continuously lost
during production and must be
periodically compensated to maintain steady
working solution composition and
inventory.
Working solution is prepared in
batches in the WS make-up tank (T2201). The
WS make-up tank (T2201) is equipped
with an agitator and steam half pipe
jacket. Required amount of the solvents
(aromatic solvent, TBU and TOP) and 2
ethylanthraquinone are fed to the WS
make-up tank (T2201) and heated to the
desired temperature during agitation
(for uniform mixing). Periodic checking of
the mixed solution is done to see if
there is undissolved anthraquinone. When
no undissolved anthraquinone is found,
the working solution is pumped by WS
transfer pump (P2202) through WS make-up
polishing filter (F2203) to the WS
coalesce (S3015).
Solvent evaporated during the
working solution preparation is condensed by WS
make-up condenser (E2205) and
returned to the WS make-up tank (T2201).
PROCESS
PARAMETERS
Operating temperature 50-85 °C
Operating pressure Atmospheric
SAFETY
IN THE WORKING SOLUTION MAKE-UP
To avoid explosive mixtures or
aromatic solvent and air in the WS make up tank
(T2201) the atmosphere is made
inert with nitrogen gas when heated over 60
°C.
10
PRIMARY FILTER CLEANING
Periodically the filter elements in
the primary filters (F1101-F1105) will have to
be cleaned from precipitated
anthraquinones, catalyst etc. to maintain a low
pressure drop over the filters.
While doing this the filter elements are taken out
of the production line and
put into the filter cleaning system, i.e. filter cleaning
vessel (T1501). The
filter elements are cleaned in the following sequence:
§
Pure
solvent from solvent tank (T1531), 60 °C.
§
Low
pressure steam.
§
Caustic
soda (10%) from caustic tank (T1521), 50-70 °C.
§
Demineralised
water.
§
Nitric
Acid (30%) from nitric acid tank (T1541) at ambient temperature.
§
Demineralised
water.
§
Low
pressure steam.
§
Drying
with N2.
Solvent, caustic and
nitric acid need to be partly exchanged after a certain
amount of filter
cleaning cycles. Solvent is returned to the WS make-up tank
(T2201) and used in
the WS system after approval of quality, e.g., pH.
Caustic solution is
depleted of solvent residues by absorption on activated
carbon in the NaOH
carbon filter (F1551). The caustic is taken to the caustic
tank (T2303) for
reuse in the and for neutralisation of the acidic effluent from
the rest of the
plant in the neutralisation unit (X9600).
Spent nitric acid is
taken to the NA tank (T2320).
11
DRAIN WATER TREATMENT
All drain water from the process
containing solvents is collected as much as
possible of the solvent fraction is
returned to the plant.
Condensates fractions containing
solvents are collected in the regeneration
decanter (S2261). The light solvent
phase will rise to the surface. It is returned
to the circulating working
solution by the solvent transfer pump (P2262). The
water phase flow by gravity
to the pump pit tank (T7001).
Other fluid overflow and waste
streams from the process, containing water and
working solution, are collected
in the pump pit tank (T7001) and the separator
tank (S7006). The content of the
pump pit tank (T7001) is transferred to the
separator tank (S7006) by the pump
pit pump (P7002). In the separator tank
(S7006) the water and solvent fraction
are separated. The solvent fraction flow
to the separated solvent tank (T7016)
from where it is returned to the
regeneration decanter (S2261) by the separated
solvent pump (P7017). The
water fraction is taken via the separated water tank
(T7011) to the
neutralisation system (X9600) for neutralisation or directly to
the effluent
treatment plant for neutralisation there.
PROCESS
PARAMETERS
Operating temperature Ambient
Operating pressure Atmospheric
pH treated waste water 6-8
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