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SIT 2013 Paper no. 1045

Parallel Front-end Refining

A New Approach to Beet Factory Raw Sugar Refining

PAPER No 1045 FOR

SUGAR INDUSTRY TECHNOLOGISTS CONFERENCE

GHUANGZHOU, CHINA

12th

to 15th

MAY 2013

By

Malcolm Topfer, Philip Antier and Piers Bostock

E D & F MAN Sugar Ltd


Paper: Parallel Front-End Refining - A New Approach to Beet Factory Raw Sugar Refining

Authors: Mr Malcolm Topfer, Mr Philip Antier, Mr Piers Bostock

Abstract:

The need to extent the asset use of beet sugar factories through the ability to refine raw sugar in the beet off-

season has been modelled in a number of different ways across the industry with varying levels of success and

flexibility of operation.

One plant has now commissioned a parallel refinery operation to the beet sugar operation, which permits both

rapid change-over from beet operations to refining and allows the possibility of processing raw sugar in parallel

to the beet sugar operation to maintain the maximum sugar production in times when the sugar beet supply is

insufficient.

This paper describes the strategic thinking and application of that strategy in to an operational plant.

Keywords: beet sugar, refinery, flexibility, sugar production, strategy


Parallel Front-end Refining - A New Approach to Beet Factory Raw Sugar Refining

1. Introduction

The Russian beet sugar industry developed the ability to process raw sugar in the off season when the country

exported oil to Cuba and in return received raw sugar. The scheme developed was very simple involving no

affination, carbonatation with heavy liming, filtration and a conventional three product beet boiling scheme with

flow splitting centrifugals. Raw sugar input colours were typically around 3,000 ICUMSA and the output colour was around 100 ICUMSA. The task became a little easier with the demise of the Russia/Cuba

relationship and the advent of raws from Brazil although the price of the lower input colour was higher starch

levels and this persists with Brazil raw sugar to this day.

The scheme was subsequently modified with an additional decolourising step to produce Coke standard whites

(sub 35 ICUMSA) and has been used successfully in other refineries (Thomson et al. 2005).

The Russian method had (and still has) the disadvantage of having the factory configured either totally for beet

or totally for raws. This means that there is not an opportunity for the flexibility of parallel processing when the

beet input is reduced because of rain and that a significant change-over time is required between the seasons.

With this background in mind the authors were asked to develop a raws refinery to be added to an existing beet

factory in Chile.

2. Process Concept

2.1. Lengthy discussions were held with local staff regarding the possible options and equipment choice,

taking into account issues such as distance from major equipment manufacturers, current technology

in use and local experience and expertise. At all times the discussions focussed on the need to have a

process that had the following characteristics:

2.1.1. 1,000 tpd refined sugar output.

2.1.2. Input colours as high as 3,500 and down to 1,000 ICUMSA. 2.1.3. Output colour and other parameters to Coke standard – less than 35 ICUMSA.

2.1.4. Ability to co-process raws if beet capacity was reduced.

2.1.5. Minimal switchover time - have the ability to move into off crop refining quickly without

complicated and time consuming changeover of piping or resins in vessels.

2.1.6. Have sufficient raws storage at a location that did not impact on logistics costs.

2.1.7. Efficient energy usage – 1:1 on steam or better.

2.1.8. Maximum use of existing equipment.

2.1.9. Low capex.

2.1.10. Low in other operating costs – labour and consumables

2.1.11. Meet existing and projected environmental constraints,

2.1.12. Use technology that was familiar to existing staff (if possible).

2.2. Raw sugar refineries use a number of options to remove colour and impurities in the front end of the

process:

2.2.1. Affination. To be used if needed, depending on the source of sugar. It is not needed generally for

Brazils or VHP sugar but is essential for sugar from other origins. If it is included in the design,

it provides greater processing flexibility for raw sugar, but should have the option to be bypassed

when not required. For easier operation, the raw sugar should be transported into the factory as

dry material either to the mingler or to the main melter, but magma from the mingler can be

pumped to the melter as an option.

2.2.2. Syrup clarification. Both Carbonatation and Phosphatation have merits and demerits and their

selection may depend upon geographical influences or the preferences and experiences of the

technologists involved... Both systems should be considered and assessed. 2.2.3. Decolorisation systems. Ion exchange resins (IER), granular activated carbon columns (GAC)

and powdered activated carbon and filtration (PAC) are all technologies in use in the industry.

All three options should be considered and have differing advantages, disadvantages, capital and

operating cost implications. PAC has the lowest capital outlay and the highest operating cost;


GAC has a high capital cost with low operating costs; IER has a medium capital cost, the

production of a difficult-to-treat effluent in regeneration and high resin replacement costs.

2.3. The following major points were identified as a design basis:

2.3.1. The option of installing affination should be actively considered – there will be a point where the

capital cost becomes uneconomical but the working group needed to take it into consideration.

2.3.2. Carbonatation should be the preferred option over phosphatation. Carbonatation is robust, the

local staff were familiar with its principles and there was sufficient equipment available at other

sites.

2.3.3. The decision regarding the use of IER vs GAC vs PAC was less clear. GAC is not favoured

because of high capital cost and because the plant will not operate for 2/3 of the year. The PAC

option was considered but rejected because the local staff were not familiar with the concept or

operation. The factory had already been using an earlier form of IER for decalcification of beet

thin juice.

2.3.4. As the existing factory had extensive effluent ponds, the problem of handling the heavily discoloured effluent from an ion exchange system was discounted, because the effluent could be

held in the ponds over the summer, diluted and discharged during the winter beet processing

season.. This eventually led to the decision to install an IER system, with a nanofiltration station

to regenerate 75% of the regeneration brine.

2.4. Thus the refinery concept became:

2.4.1. Switchable affination.

2.4.2. Melting.

2.4.3. Carbonatation.

2.4.4. Filtration.

2.4.5. Ion exchange system 2.4.6. Evaporation

2.5. These first six steps were designed to be operated in a parallel manner to the day to day operation of

the beet factory thus meeting the requirements for fast changeover and to be able to introduce raws

into the system while processing beet.

2.6. A side problem was the need to design the carbonatation step to handle flows that varied from 25 to

100% of capacity. As a result, a series of issues related to residence times and maintaining proper gas

mixing and liquor turbulence had to be addressed by sizing two carbonatation tanks precisely to match

flows of 25%, 50% and 100% in combinations of vessels.

2.7. From a new separate evaporation station, the syrup was delivered to the beet factory crystallisation house, which had some modifications to its equipment to enable it to handle the raw sugar syrups.

2.8. Common utilities included the boilers and turbines, lime kiln and sugar handling areas, as well as

utilising the central control room with a new process software package for the refinery operation.

2.9. In addition, it was necessary to install a closed circuit cooling tower system for the crystallisation

station, because it would not be possible to discharge water to the Nuble river in the summer season,

as it was in the beet processing winter season. The intention was to install a year-round closed circuit

system to improve the factory’s environmental footprint.

2.10. The boiling scheme used was originally an R1, R2 scheme but this was subsequently modified to become a single product or R1 scheme requiring further design work on process yields and overall

recoveries.

3. Process Design

3.1. The first step in the process design was to develop an appropriate concept for sugar refining at a beet

sugar factory. The previous experience of the design team in Russia, Israel, Ukraine, Italy and

Portugal enabled the team to examine all the options in the process stages with the aim of minimising

any Capex required at the back end, minimising energy consumption and maximising yield. Not


surprisingly, in view of the success that the authors had enjoyed with the simplified boiling scheme,

this model was chosen to drive the crystallisation process.

3.2. The required refinery base parameters were:

3.2.1. Throughput of 1,000 tpd RSO.

3.2.2. Energy consumption 1:1 on steam if not better – dependent on incoming raw sugar quality. 3.2.3. Sugar output colour less than 30

3.2.4. Refinery yield better than 97% - again dependent on incoming quality.

3.2.5. Other quality parameters to Coke standard.

3.3. The next stage was to develop a Sugars™ model to submit to and agree with the factory management

team. Developing an effective and reliable model based around a mix of existing equipment, new and

second hand imported equipment was not a simple task, involving a number of iterations of the model

in order to achieve optimal results, both in production quality and energy. As in any use of the

Sugars™ model, key assumptions had to be made with respect to crystal yield and colour reduction.

3.4. There followed a series of discussions with the company and factory management to work through the

model, make any modifications and to establish a basic equipment list required for the project based

on the flows, temperatures and brixes generated by Sugars™.

3.5. With the addition of limited raw sugar storage facilities, the steps in the refining process were as

defined above with raw sugar initially being elevated to gravity feed through either affination or direct

to a melter. Unfortunately, after the initial design was developed, a large earthquake intervened (8.9

on the Richter scale) at the end of February 2009, centred offshore but close to Chillan factory,

damaging the plant.

3.6. This necessitated a change in plan and the design had to be modified to reduce any high level building

loading to a minimum and items, such as the raw sugar mingler were relocated from a high level to a

location within the raw sugar warehouse and thus requiring a pumped magma system. The final new

steps that were required were as follows:

3.6.1. Raw sugar delivery to site and storage

3.6.2. Raw sugar magma production and pumping either to:

3.6.3. Affination station, if required by raw sugar colour, or to:

3.6.4. Raw sugar melting station,

3.6.5. Carbonatation station

3.6.6. Filtration station


3.6.7. Decolorisation station using Ion Exchange

3.6.8. Evaporation

3.6.9. Transfer to existing factory crystallisation and sugar handling (with modifications).

3.7. In addition, as some beet factories in Chile were being closed, there were opportunities to obtain and

move some equipment from the closed factories and install them at Chillan as part of the refinery project. This involved detailed calculations for the size and quantity of plant items required and

matching those parameters to the equipment available.

3.8. As an additional complicating factor, the initial design of the steelwork had to be revisited following

revised earthquake factors. This resulted in some additional costs and a time delay to the overall

project.

3.9. The Sugars™ scheme for the R1 and R2 boiling scheme will be displayed in the presentation and

provided the foundation for the development of the P&IDs, from which was generated an equipment

list complete with tag numbers.

3.10. This in turn was fed into a cost estimating matrix to provide an overall project budget forecast.

3.11. As in all projects, there was a delay in waiting for capital expenditure approval and this delay was

used to develop and issue detailed specifications for the major new equipment. The detailed quotations

that were received gave comfort that the budget was looking achievable.

3.12. Effluent management arose again as a major issue during the procurement phase of the project and had

the potential to bring it to a halt. After the initial choice of an IER Decolorisation plant had been

made, the factory requested a non-effluent producing IER system, in order to eliminate the need to

manage effluent during the summer when discharge to the river is prohibited. It was eventually

conceded that the proposal was impossible, but, by then, the project has advanced to a point where the

IER system was fully integrated and could not be changed for an alternative. Given a similar position with the same options for decolorisation, it is not a foregone conclusion that IER would be selected.

4. Planning and Construction

4.1. Capital approval was finally received in September 2009, which enabled project planning to restart

and major equipment procurement to commence.

4.2. Construction work on site commenced in July 2010 in areas of the factory unaffected by the beet

processing operation, taking place from April to September each year. This included the raw sugar

warehouse and raw sugar delivery system, the foundations for the new cooling towers and for the new

refinery building addition to the main factory.

4.3. The second-hand equipment from the closed factories was also removed, transported to Chillan, where

modification and maintenance was undertaken.

4.4. As soon as the beet campaign had been concluded, the filtration station in the main factory was

modified, with additional pipework and valves installed to change the duties of the existing filters and

a further three second-hand filters added to the station. This work was completed in time for the next

beet processing season in 2012, providing a fully switchable filtration station.

4.5. In June 2010, negotiations took place in London with the potential suppliers of the major European-

purchased items of equipment, including heat exchangers, ion exchange plant for decolourisation and

evaporators. The successful tenderers were approved during that week and contracts placed shortly afterwards. Delivery of the equipment was required by April 2011. These orders accounted for nearly

30% of the project value.

4.6. While in theory, the parallel front end refinery construction could proceed while the factory was

processing beet, the reality of the situation was that resources were necessarily limited with the result

that the initial deadline of commissioning the refinery in September of 2011 was not met. The usual

suspects of piping, electrical and I&C were the main culprits but pleasingly, there was little cost

impact. Eventually, the new project was ready for a first short commissioning stage in late February

of 2012.


5. 1st Commissioning February 15

th – March 13

th 2012

5.1. The authors have had considerable experience in commissioning stand alone and refinery conversions

in the last number of years. It never fails to surprise when the comment is made that “sugar is sugar”

and that there is little difference between beet and raw sugar processing. The reality is that the there is

a very real difference in the product’s characteristics, particularly in the viscosity, temperature effect

and chemistry control and has a number of implications on the chemical engineering (pumping), the operation of carbonatation and crystallization and the control of set points.

5.2. Not all of this was understood by the factory management and operators, in spite of many discussions,

visits to other operating refineries and significant training input.

5.3. An external technical assistance team, comprising technical experts, supervisors and operators,

together with suppliers’ engineers, was put into place before commissioning commenced to provide

support to the factory operations team. The team comprised members from Spain, Portugal, UK,

France and Germany.

.

5.4. Full commissioning (cold and hot testing into the first melting of raw sugar) was not possible until early February, by which time there was significant marketing and time limitation pressure to start

production. The beet processing campaign was due to start in April and the factory needed one month

of no-production to complete the maintenance.

5.5. Raw sugar melting commenced on 10th February 2012, after 3 days of hot testing of the plant, but

rapidly ran into mechanical problems with the raw sugar mingler and then the main dissolver stirrers,

each requiring a 16 hour stop to repair. Both of these repairs were temporary and some re-design

would be required after the first season.

5.6. Settling the carbonatation station to achieve stable, consistent liquor for filtration proved very difficult

as Milk of Lime (MOL) concentration and flow and CO2 concentration were not controlled tightly

enough and resulted in filtration problems. The factory had decided to use the beet limekiln system for MOL and gas production, rather than buying in CaOH and using boiler flue gas for CO2 supply. This

meant that the MOL system, designed for beet, did not have the fine baumé control needed for the

lower flow in refining and the baumé fluctuated more than desired. The CO2 from the lime kiln had to

be diluted to reduce the concentration from 28% to 10% and this also proved difficult to control.

5.7. The Putsch HKF filters, some of which existed at the factory (4) and the others (3) had been brought

from the closed factories, also gave the commissioning team problems in operation. Various

modifications were made to these units “on the run” over the first month of operation in order to

improve their performance, including changing the syrup distribution, improving the venting and

altering the steam addition for cloth cleaning.


5.8. As a result of the problems detailed above, the commissioning and operation of the Decolorisation Ion

Exchange plant proved difficult and the supplier’s engineers struggled with unstable conditions. The

decolorisation itself was very effective and the regeneration systems and brine recovery eventually

settled in operation. The failure of the carbonatation and filtration system resulted in some sediment

passing through the filters and this material ended up on top of the resin beds.

5.9. As a result of the key issues in 4.5, 4.6 and 4.7 above, getting the factory settled into steady refining

proved to be very challenging and the opportunity for optimisation before the factory stopped

operations on 13th March was very limited.

5.10. It was clearly seen during this first commissioning stage that main failures during operations (except

the mingler) were due to poor maintenance of the existing boiling house and boiler performance

issues.

5.11. Main process performance data achieved during this 1st stage of commissioning were:

12,788 tonnes of raw melted and 10,680 tonnes of commercial refined sugar produced

Steam consumption of 1.68 tonnes per tonne raw sugar

Total downtime (loss of production time): 27% Best day of production: 746 tonnes melted and 815 tonnes of commercial sugar produced

Whilst this was not a stellar performance, it did prove that the process worked and indicated that the

design parameters could be achieved. The only concerning areas were the steam consumption and the

operational state of the steam boilers.

6. Re-thinking the Design

6.1. At the end of the first refining period, the factory was going to prepare for a beet processing campaign,

which would be followed by an extended raw sugar refining season in October 2012 until the next

beet campaign in April 2013.

6.2. This gave breathing space to the project team to analyse the issues raised during the first operating

season and identify what changes needed to be made before the next operation.

6.3. The clear issues were:

6.3.1. The re-design of the mingler drive and mixer to provide a stronger, more powerful unit

6.3.2. A new volumetric pump with VF in order to get better control on brix at the melter station.

6.3.3. The modification and testing of the main dissolver stirrers to ensure that they were fit for

purpose,

6.3.4. To work at higher alkalinity at the inlet of the first carbonated vessel

6.3.5. The installation of measurement and controls on MOL and CO2 concentration to improve the

carbonatation operation, 6.3.6. Further work on the HKF filters to ensure that their operation was improved (new VF drive on

prefiltration step).

6.3.7. New heaters installed on sweet water and slurry before the PKF station

6.3.8. The use and management of water and its disposal, particularly in respect of the closed circuit

cooling tower for crystallisation. The factory had not had a closed circuit system before and the

pan boilers did not really understand the implications and responsibilities they had to use it

correctly. Thus, the operators tended to their former approach of using as much water as they

wished on the condensers, so that the cooling towers were constantly overflowing.

6.3.9. The operation of the steam boilers. In the event, further serious issues with the boilers during the

beet campaign resulted in a major overhaul of the units before the next refining season.


6.4. In addition and after much discussion, the project team decided that, for VHP quality raw sugar at

least, the use of a two product boiling system was counter-productive and was causing additional

complications for the factory team and operators. It was decide to revert to the single product boiling

scheme, as used in the beet campaign and in other refineries, with back-boiling to recover sugar.

6.5. During the beet campaign, a detailed modification plan was drawn up to achieve this and the plan was

implemented immediately after the campaign and before the raw sugar refining started at the end of

October 2013.

7. Re-commissioning and Second Operation

7.1. From October 30th 2012 to March 24th 2013, the refinery melted approximately 100,000 tonnes of raw

sugar (Pol = 99.05). Due to low input colour (< 1,500 UI), the affination station has not so far needed

to be used. Whilst the input colour was good, the starch level was high at > 300 ppm.

7.2. The external technical assistance team was brought in again to support the factory operations team

during both the retesting and commissioning and also the first weeks of operation. This team was

disbanded after the first month of production with the success of the restart.

7.3. The results of the modifications made and of this operation were:

7.3.1. Mingler station and melter stations worked perfectly well and have been proved able to feed

1,000 tonnes raw sugar /day to the refinery.

7.3.2. Carbonatation station. The plant easily achieved 40 to 50% of decolorisation at a lower capacity

and indicates that decolorisation will be achievable at full capacity, but the station will need care

and attention to detail to maintain a good performance.

7.3.3. HKF filter station. Closer attention to the control and management of the filters’ operation,

together with some “on the run” focus on maintenance, isometrics of the piping and software

changes had a significant effect on the performance. However, the main difficulty was the

optimisation of this station with high starch content raw sugar. Without the use of an industrial

enzyme, the factory would not have been able to maintain a target for sugar input rate > 35tphr.

7.3.4. Decolorization station. The station had no difficulty in maintaining a high decolorisation rate, but

control of the operation was not easy. Training and supplier support was essential because of the


complexity of operation, particularly in the use of a single column and around all the

interconnections in the regeneration phases.

7.3.5. Evaporation stage. The modifications improved its performance such that an average brix before

crystallization up to 71 Brix was achieved.

7.3.6. Crystallization / Centrifugal control. At each station, a back-boiling system was used to control

and reduce the molasses production and losses. It took some time to settle purity target at each

stage correctly.

7.3.7. The total downtime remained too high at 11%, against a target of 5%.

7.3.8. Operators have now understood that their input is needed to control a fully automated refinery on

an hourly basis, but have not yet learnt how to manage the plant in the event of system control or

instrumentation failure.

8. Results & Discussion

After 19 weeks of production, we can consider that we have achieved the commissioning stage and our

main results are detailed below on a monthly basis.

Table 1: 2nd

operation period at Nuble

Average Nov. 12 Dec.12 Jan.13 Feb.13 Mar.13 Up to date

Raw sugar melt / day

(tonnes) 586 662 668 733 800 722

Sugar Recovery

(t sugar / t Pol raw sugar) 96.4 96 96.9 94.5 97.8 * 96.4

Steam consumption

(t steam /t raw sugar melt) 1.32 1.28 1.27 1.16 1.15 1.22

Time loss % 6.6 10.9 14 15.7 5.8 11.4 * Includes liquidation of refinery


8.1. Maintenance organization and support to process must be largely reviewed to achieve greater stability

during production in order to reduce losses with better energy control.

8.2. A new maintenance management system must be developed for the factory as a whole and particularly

for the crystallisation station and power station that will now be working 10 months per year.

8.3. Beet technologists from the Ñuble factory today understand better the refinery challenges:

8.3.1. The concept of resident time and temperature control still needs to be fully understood.

8.3.2. Full management involvement is needed at all times to achieve high sugar recovery and

efficiency, together with positive support and pressure from managers to their operators to

achieve better results.

8.4. Table 2 below shows a first comparison between Nuble refinery and a similar stand-alone refinery in

the Middle East, both using our single product boiling system with back-boiling. Whilst Nuble

operates on Carbonatation and IER, the Middle East refinery operates on Carbonatation and PAC and

only receives VHP raw sugar. The table shows that there is still some work to do at Nuble in order to

match the operation at the other refinery.

Table 2: 1st Comparison of two stand-alone refineries

Raw Sugar

tonnes

Raw

Sugar

Pol

Raw Sugar

Colour (IU)

Sugar

produced

tonnes

Recovery

%

% Invert

SIM (dry

basis)

Ñuble refinery

Last 5 weeks

(before liquidation)

28,540 99.00 1371 27,278 96.54 6.7

Middle East refinery -

Oct 2012/February 2013 109,749 99.43 819 106,462 97.56 13.8

8.5. Better control of C crystallisation station was developed during the last month in order to reduce the

losses and stabilise the sugar colour before the carbonatation station. The process managed to return C

and B sugar below 1,500 ICU to the carbonatation station.

8.6. pH control was optimised throughout the process after the decolorization station and using back –boiling on each station before the C-pan. The quality of run-off was controlled, as was the invert sugar

produced, such that molasses as % raw sugar was less than 3%.

8.7. The refinery will be able to achieve 97% on a continuous basis, even with raw sugar Pol being < 99.3,

as these results were achieved in between long stoppages which caused sugar losses (operational

errors, old beet piping system not adapted to the refinery usage, etc.).

8.8. The second problem on losses was due to poor vacuum control at the crystallization station, with pan

temperatures unacceptably high at over 80°C on many occasions. The probable reasons for this

situation were identified as:

8.8.1. Mechanical: Continuously steam/water leaks on different pans (old calandrias),

8.8.2. Capacity: Never able to get pan pressure below 0.3 bars absolute on all pans when the refinery is working above 800 tonnes / day,

8.8.3. Cooling water system: with best cooled water temperature seen > 47°C, cold water to the

barometric columns without any beneficial effect.

9. Conclusions 9.1. The next step for the refinery, at full capacity, is to carry out fine tuning in order to reduce losses

according to the raw sugar quality and to get better control of the energy cost.

9.2. With the results achieved, we have proved the following points:

9.2.1. Using A single boiling system, R1 as described in precedent papers (M.Inkson et al. 2010, P

Antier et al. 2012), is a reliable and efficient system for new refinery looking for high sugar

recovery, continuous control on sugar quality and energy. As proved, this system is suitable with different decolorization system (IER or PAC). In this particular case, beet operators feel

immediately comfortable with the boiling system as it is very similar to their existing boiling

arrangement scheme.


9.2.2. The refinery can anticipate increasing sugar recovery in the next refining season. The lower

reducing sugar production, due to the choice of an I.E.R. system, is a significant advantage.

Indeed, IER permits the maintenance of high pH all along the process and aids the control of our

back-boiling operations.

9.2.3. There are still some bottlenecks to deal with before the next refining season: the piping system around the sugar house needs some modification, some improvement to the vacuum control on

the vacuum pans and further assessment of the cooling water system.

10. Future Perspectives 10.1. The refinery has not yet been used in parallel with the beet factory operations, for times when the beet

supply is short or the capacity of the beet factory is reduced for other reasons.

10.2. After the two refining seasons, the plant and its operators are now sufficiently far up the learning

curve to be able to take on this new phase.

10.3. The design of the refinery is such that it could be operated at 15 tonnes/hr (25% of full capacity) or 30

tonnes/hr (50%), but it is most likely to be used at 25% capacity, when the beet factory is suffering

from beet supply shortage or poor beet quality.

10.4. The key parameters that need to be managed at each station are: 10.4.1. Mingler: Mingling temperature controlled at very low temperature (<40 oC) and a VF drive on

volumetric pump from the mingler.

10.4.2. Carbonatation: Using only one carbonatation tank (either 1st for 50% or 2nd for 25% capacity)

and a second specific in-line MOL mixer.

10.4.3. First Filtration: redistribution of HKF Filters: A maximum of 2- 3 HKF filters for the refinery

and 4 to 5 for carbonated thin juice.

10.4.4. I.E.R. System: will work on single pass, single column and, because to the column size, some

recirculation of the decolorized liquor will be required in order to maintain adequate pressure

on the resin beds.


The authors wish to thank IANSA, Chile, for their permission to use the information developed during this

project in the production of this paper.

Bibliography:

1 Thompson et al (2005), “Thoughts on Refinery Boiling Schemes”, SIT Paper #875

2 Inkson et al. (2010), A single strike boiling scheme”, SIT Paper #982 3 P. Antier et al. (2012) Refinery performances using a single product scheme, British Society of Sugar Technologists Meeting, April 2012

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