The C3 splitter in an olefins
plant is one of the most important and critical pieces of equipment: it
separates polymer-grade propylene from propane. The relative volatility between
propylene and propane is so low that it requires a significantly large number
of trays to achieve the desired specification and product recovery. Saudi Kayan
had been operating a C3 splitter with two physical columns, C-16040A
and C-16040B (FIGS. 1
and 2), each
equipped with 100 four-pass trays. The column overhead is coupled with a heat
pump system to generate the necessary reflux and vapor load from the reboiler.
The trays operated satisfactorily as long as the tower was not pushed near its
original design capacity. When Saudi Kayan tried to increase the feed to the C3
splitter tower’s capacity, propylene losses from the bottom of the tower were
so high that the loss of production went well beyond acceptable limits.
Subsequently, this was followed by tower flooding that affected stable column
operation. Saudi Kayan wanted to address the problem of the poor tray
efficiency as well as increase the capacity of the column to handle higher
throughput, considering future expansion.
Operating
condition before revamp. The authors’ companies worked together
to evaluate the performance of the column. Sulzer performed several analyses
based on various sets of operating data collected during 2018–2019. The operating data
collected in June 2019 will be presented in this paper. This data was used as a
basis for the revamp of this column. The feed flowrate to this column was not
measured. The top and bottom product flowrates were used to back-calculate the
feed flowrate and feed composition. The overall mass balance before the revamp
is presented in TABLE 1.
Note: All flowrates in TABLES
1–5 have been normalized to match 1,000 kg/hr as the feed flow to
the plant before revamp. This normalization was enacted to protect confidential
operating data.
The column was
simulated based on Sulzer’s proprietary vapor-liquid equilibrium (VLE) and
enthalpy model to generate the internal vapor and liquid loads. Sulzer then
performed the tray’s hydraulics rating based on the existing geometry of the
trays. It was noticed that the four-pass trays were never balanced to regulate
the flow of liquid from the off-center downcomer (OCDC). A typical arrangement
of a four-pass tray is presented in FIG. 3. The OCDC downcomer provides the liquid
to both the side downcomer (SDC) and center downcomer (CDC) on the tray below.
Based on the geometry using an equal flow path length type design, the active
area of Panel B is larger than Panel A. However, the weir length of the CDC is proportionally
much larger when compared to the SDC. Therefore, Panel B was getting more
liquid than Panel A. Subsequently, the froth height and pressure drop of Panel
B is larger than Panel A. In this situation, more vapor will tend to go to Panel
A, where there is the least resistance and pressure drop. Ultimately the vapor/liquid
ratio on these two tray panels will become unequal.1
Based on Sulzer’s calculations, it was
found that the vapor/liquid (V/L) ratio in the tray panels were 1.35 and 0.8,
respectively. The V/L ratio is a measure of the relative amount of vapor and
liquid on each tray panel. This means that Panel B of the four-pass tray panels
was getting very high liquid compared to Panel A. Generally, the vapor should
distribute proportionately to each tray panel as per the active area; however, the
liquid presents several variables (weir length, weir height, downcomer
clearance area) that must be satisfied to allow it to match the vapor
distribution to each tray panel (and enable a V/L ratio of 1.0 on each tray
panel).
The unbalanced design of these trays
contributed to a very high degree of mal-distribution inside this column.
Subsequently, this contributed to lower tray efficiency and a higher than
anticipated reflux ratio to achieve the desired product purities. Ultimately,
this efficiency reduction negatively affected the tower’s overall capacity. Overall
tower tray efficiencies were estimated to be at about 60% of design operating
conditions. The polymer-grade propylene purity cannot be compromised. The only
option is to lose propylene in the bottom product and keep the column in
operation.
To reduce the propylene losses in the
bottom product, Saudi Kayan tried to further increase the reflux to the column.
The column overhead vapor was compressed in the heat pump system to heat the
reboiler. The maximum reflux was limited by the capacity of the compressor. The
reflux flow to column was increased until the compressor was operating at its
maximum limit. This can be seen in the compressor curve (FIG. 4), where the
operating point before revamp is indicated.
Based on this curve, it is clearly
understood that the operating point before the revamp was outside the standard
operating curve. Therefore, no further reflux was available in the system
without revamping or getting a new compressor, which is a major capital
expense. At this point, Saudi Kayan decided to focus on the column internals
rather than increasing the compressor capacity.
Several revamp ideas were considered,
including performing a partial revamp and fixing the most critical section of
the tower to improve tray efficiency. A partial revamp, however, would leave
unbalanced trays in some sections of the tower, which would continue to suffer
poor tray efficiency. Considering future expansion requirements, it was decided
to conduct a complete revamp of the full C3 splitter tower.
Revamp
proposal.
In
2019, Saudi Kayan was interested in not only achieving the original design
capacity, but also wanted to de-bottleneck the entire tower to obtain
additional capacity over the original design.
Before the revamp, the column was
operating with full compressor capacity in the integrated heat pump system. However,
the heat pump system was unable to provide any additional reflux. As a result
of this, the plant was unable to achieve design propylene purity specification.
Considering overall economics, it was decided that revamping the compressor was
an infeasible option to enhance capacity. Therefore, revamping the tower with
high-capacity and high-efficiency trays was pursued with Sulzer, which decided
to focus on all aspects of the new tray’s design to achieve both the column
capacity and higher efficiency. The proposed new trays should be able to work
at much higher tray efficiency to reduce propylene slippage, and should have
additional spare capacity to cater to future requirements. Sulzer observed that
it would be difficult to use any conventional tray technology to achieve higher
efficiency with higher capacity. Based on detailed assessment of Saudi Kayan’s
requirements and current tower operations, it was decided to use high-capacity
the company’s proprietary downcomer traysa trays with its proprietary
valvesb and enhanced downcomers technology to achieve higher
efficiency and capacity (FIGS.
5 and 6).
The proprietary valveb
releases the vapor laterally onto the tray deck, which allows the liquid to
flow without obstruction. This helps to reduce the liquid gradient along the
flow path length, reduces the vertical jetting and minimizes the entrainment to
increase the deck capacity, which is critical to meet future capacity
requirements. The company’s valves are punched out of the tray deck and have no
moving parts, providing longer life without any wear or tear. The downcomers
for the proposed new tray design need to handle the increased liquid load. The
downcomer velocity was very high at 0.102 m/sec, as shown in TABLE 3.2
In a four-pass tray, the side downcomer
is typically limited by high weir loading. This is a geometrical limitation
when compared to the weir length of center and off-center downcomers. It was
proposed to use proprietary type side downcomersc, which increases
outlet weir length and reduces the weir loading. To improve the tray
efficiency, push valves were employed to minimize the liquid gradient on the
relatively long flow path lengths. These devices also improve liquid plug flow,
enhance liquid aeration, eliminate any vapor cross flow channeling, and improve
the mass transfer efficiency.3,4 Sulzer put together an aggressive
design that maximized both capacity and tray efficiency with a fully balanced four-pass
tray design.
Turnaround
installation and operating data after revamp. Sulzer
executed all installation activities on a turnkey basis, including labor,
consumables, crane, scaffolding, power generators, ventilation, air
compressors, forklift, trailers, etc. The company also complied with all
necessary labor safety training and certification to meet SABIC Safety, Security,
Health and Environmental Management Standards (SHEMS) procedures. The
installation was carried out during the peak of the COVID-19 pandemic. There
was a resource crunch for both labor and material due to travel restrictions. Additionally,
when installation work was in progress, onsite personnel were faced with very
high winds for several days. This high wind reduced the installer’s ability of
crane movement and work at elevated locations inside the tower.
The project team was also impacted
significantly due to the COVID-19 pandemic. Constant video surveillance monitored
all activities inside the column and resources were expedited whenever
necessary. Shutdown was scheduled for 25 d and the Sulzer installation crew
managed to complete the installation safely and successfully within the schedule.
The plant restarted after the revamp in
April 2021. Following plant stabilization, Sulzer analyzed the operating data
over a duration of 2 mos and examined the detailed process trends such as flowrate,
pressure and temperature. A 24-hr operating window was chosen in May 2021. This
set of data showed stable operating conditions and was suitable for the plant’s
performance evaluation. The laboratory analysis for the top and bottom product
purity was also available during this period. As mentioned earlier, the feed flowrate
was not measured, but was calculated based on the top and bottom product flow
streams. The composition of the feed was also calculated based on the mass
balance of the product streams.
The operating data presented in TABLE 4 was used as a
basis for the simulation to analyze the operating performance of the column.
The reflux ratio is the reflux flowrate to the column before flash over the distillate
flowrate. The number of theoretical stages in the simulation was adjusted to
match the measured reflux flowrate. The C3 splitter is designed with
two physical columns and the plant instrumentation can measure the reflux fed
into both the upper and lower columns. To validate the calculated tray
efficiency, the simulated results were verified based on reflux flow
measurements from both towers. Based on a rigorous plant simulation model and
validation of the operating data, it was confirmed that a tray efficiency of >
95% was achieved for the new traysa in this C3 splitter
using the authors’ company’s proprietary VLE and enthalpy model. The vapor and
liquid internal loads from the simulation were used to perform hydraulic
ratings for the trays. The results of the evaluation are presented in TABLE 5. FIGS. 7, 8 and
9 represent the
impact of the tray revamp on key process trends like steam consumption in the
heat pump turbines, and propylene losses in the bottom of the C3 splitter.
As shown in these figures, due to the improved efficiency of the revamped
trays, the overall steam consumption, propylene losses and reflux flow have
decreased significantly, reiterating the increased tray efficiency.
Takeaways. This paper
illustrates a successful revamp of a C3 splitter that was installed
safely within a plant’s narrow turnaround window during the global COVID-19
pandemic. The revamp of the Saudi Kayan C3 splitter, with proprietary
traysa, achieved > 95% efficiency, which was higher than the
target requirement for this revamp. Subsequently, it also helped to reduce
propylene losses in the bottom product. One of the main reasons for the initial
low tray efficiency of the original trays was the employment of an unbalanced four-pass
tray design that was expected to operate very near to its maximum capacity.
Following the
tower revamp, the reflux ratio required to minimize product losses and achieve
the desired product quality was reduced by ~25%. Because of this, the heat pump compressor’s
duty has been significantly reduced, which translated to lower steam consumption
in the turbines. The plant is presently showing stable operation at design
capacity without any challenges. Based on a tower hydraulics assessment using
the operating data after the revamp, it was confirmed that the C3 splitter
equipped with the authors’ company’s traysa has a margin to
accommodate more than 25% additional feed capacity. HP
ACKNOWLEDGEMENTS
The authors would like
to thank Saudi Kayan and Sulzer for supporting the publication of this article.
NOTES
a Sulzer Chemtech
Ltd.’s VGPlus™ trays
b Sulzer
Chemtech Ltd.’s MMVG™
valves
c Sulzer
Chemtech Ltd.’s ModArc™
downcomers
LITERATURE CITED
SENTHIL
KRISHNAMOORTHY is a Key Application Specialist for Sulzer Chemtech USA.
With more than 20 yr of experience, he is responsible for column design in
major olefins and styrene projects around the globe. He has published
several technical articles on distillation column design and troubleshooting
and holds one European patent for column internals. He has served as a member
of the FRI Design Practices Committee since 2020. Krishnamoorthy received an
MS degree in chemical engineering from the Regional Engineering College in
India.
SHASHANK
LATURKAR is an
Application Manager for Sulzer India.
VINIT KALE is Head of the Sales downstream
business at Sulzer Chemtech and has 18 yr of experience in refinery, petrochemical
and specialty chemical processing. He holds a BS degree in chemical engineering
from India and has published five technical papers.
Until
January 2021, DANIEL R. SUMMERS served as the Tray Technology Manager
for Sulzer Chemtech. He was a 1977 graduate in chemical engineering from the
State University of New York (SUNY) at Buffalo, New York, and also worked for Union
Carbide, UOP, Stone & Webster, and Nutter Engineering. His entire career
has been focused on distillation. Summers is the author of more than 70 papers
and is a listed inventor on three U.S. patents. He now works as a consultant
for Fractionation Research Inc.’s (FRI’s) Design Practices Committee and was
the Chair of that committee for 12 yr. Additionally, he serves as a Director of
AIChE’s Separations Division, is a Fellow of AIChE and is a registered Professional
Engineer in New York and Oklahoma. Summers is also the recipient of the 2016
AIChE Gerhold Award for outstanding work in chemical separations technology.
DIPAK
SHAHARE is a
highly experienced process engineer with more than 18 yr of experience in the
petrochemical industry. Employed by Saudi Kayan, a SABIC affiliate, for the
past 8 yr, Shahare also spent a decade working for Reliance Industries Ltd. in
India. He has significant expertise in managing olefins, benzene, utilities
processes and energy management. He holds a degree in chemical engineering from
Sardar Vallabhbhai National Institute of Technology, Surat, India, and is also
a certified Energy Auditor by the Bureau Of Energy Efficiency (BEE), India.
MOHAMMAD A.
KHAWDAH is the Process
Engineering Department Senior Manager at Saudi Kayan Petrochemical Complex, a SABIC
affiliate company. He earned a BS degree in chemical engineering from King Fahd
University of Petroleum and Minerals and has more than 13 yr of international
technical experience working with a world-leading technology licensor in the oil
and gas industry specializing in process technology licensing, catalysts and
adsorbents manufacturing. Khawdah has served in several technical positions as Technical
Advisor, engineering technology Superintendent, and process engineering and operation
Manager for pre-commissioning and commissioning activities of mega-project startup
and operational technical support for a number of refineries, petrochemicals
and gas processing plants worldwide.
MOHAMMAD
ALI AL-SEKHAN
is responsible for global cracker technology at SABIC.
MAHESH
KUMAR S is the
Chief Scientist with SABIC and has 19 yr of experience in the petrochemical
industry with a focus on identifying areas for improvement resulting in
feedstock maximization, asset utilization, yield Improvement and loss
minimization. Key aspects of his work include working with an interdisciplinary
team to address process issues in crackers and to identify new opportunities
and implement cost-effective solutions. He has published more than 15 papers in
peer reviewed journals and has filed and been granted five international
patents.
MISFER AL
GHAMDI is
responsible for process safety and process risk management at SABIC.
DR. ANDREI MERENOV is the Chief Scientist with SABIC.