optimising your energy system

7/29/2019 Optimising your energy system

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WASTE HEAT RECOVERY

Waste heat recovery Optimizing your energy system


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Volcanoes are extraordinary sources of energy. For

example, the Laki eruption of 1783 in southern Icelandproduced 15 km3 of lava. The heat released from the

lava measured 80 exajoules; enough energy to keep all

the worlds industries running for six months


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Contents1. Proft on waste heat ................................................................................. 4

1.1 The challenge .....................................................................................................................6

1.2 Waste heat recovery ................................................................................................................8

1.3 Heat exchangers .....................................................................................................................91.4 Heat integration analysis ........................................................................................................ 10

2. Eight ways to proft rom waste heat ................................................... 12

2.1 Saving uel ............................................................................................................................. 14

2.2 Generating electricity and mechanical work .......................................................................... 16

2.3 Selling heat and electricity ..................................................................................................... 18

2.4 Reducing cooling needs ........................................................................................................20

2.5 Reducing utility investments ..................................................................................................22

2.6 Increasing production ............................................................................................................ 24

2.7 Reducing greenhouse gas emissions .................................................................................... 25

2.8 Transorming energy .............................................................................................................26

3. Recovering heat fve generic cases ................................................... 30

3.1 Preheating in interchangers ....................................................................................................32

3.2 Direct process heat integration ..............................................................................................35

3.3 Indirect process heat integration ............................................................................................38

3.4 Increased number o eects in evaporation systems ..............................................................42

3.5 Reduced ouling and maintenance .........................................................................................44

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1. Proft on waste heat

Rising energy prices are a major challenge or many industrial

plants. The days o cheap energy are over, and energy efciencyis becoming a crucial success actor.

Great potential ...

The good news is that most sites have a considerable

unexploited potential or energy savings. A report rom the

International Energy Agency states the industrial plants

throughout the world are using about 50% more energy thannecessary. By switching to the most energy-efcient technology

available, companies can make huge savings and signifcantly

reduce environmental impact.

... or higher proftability

Recovering waste heat using compact heat exchangers is a

straightorward and easy way to boost the energy efciency o aplant. The investments are oten very proftable and payback

periods oten less than one year.

Many process industries are already recovering heat, but use

shell-and-tube technology. Switching to compact heat

exchangers boosts the energy efciency and is a very good

investment in most cases.

Payback periods or waste heat recoveryinvestments are oten shorter than one

year thanks to the high thermal efciencyo Ala Lavals compact heat exchangers.


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1.1 The challenge

Increased demand

In the World Energy Outlook 2008 report*, the International

Energy Agency (IEA) predicts world energy demand to

increase by 45% over the next 20 years. They also predict the

supply o ossil uels will not be able to meet this demand,

even when taking new, undiscovered felds into account.

More and more governments around the world will probably

start charging industries or emitting CO2, with emission

credits becoming more and more expensive.

Higher energy prices

The result o all this will undoubtedly be increasing energyprices; just how much is hard to predict. In 2007, the IEA

predicted oil prices to stay at 50-55 dollars per barrel until 2030.

A year later, in June 2008, it peaked at 147 dollars per barrel

and at the time o writing (2011) it is above 100 dollars per barrel.

Figure 1.1

Oil price predictions have increased every year.

Source: International Energy Agency, World Energy

Outlook 2008

* International Energy Agency, World Energy Outlook 2008,www.worldenergyoutlook.org/2008.asp

Real price

Estimates WEO 2004

Estimates WEO 2005

Estimates WEO 2006

Estimates WEO 2007

Estimates WEO 2008

Oil price

USD/barrel

0

20

40

60

80

100

120

2003 2007 2011 2015 2019 2023 2027 2031

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and its common-sense solution

There are many alternative ways to battle the energy challenge.

Internationally renowned consulting frm McKinsey made a

thorough investigation into uture energy needs and supply,

comparing the benefts o dierent alternatives. They came to

the ollowing conclusion:

The natural starting point

As common sense predicts, the frst step towards lower

energy costs is to start using less energy. Increasing energy

efciency is the least costly and most easily implementedsolution to energy challenges or the average process plant.

Energy-saving investments oten have short payback periods,

even at much lower energy price levels than todays. In the

uture, energy efciency will most likely be a prerequisite or

staying in business.

The total energy-saving potential rom theworlds industries is estimated to be aboutthree times the worlds total nuclear powergeneration.

x3

McKinsey has looked long and hard to obtain an aordable,

secure energy supply while controlling climate change. Energy

efciency stands out as the single most attractive and aordable

component o the necessary shit in energy consumptionMcKinsey Quarterly January 2010

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1.2 Waste heat recovery

An eective way to increase energy efciency is to recover

waste heat.

The process industry mainly consumes two types o energy:

Fossil uel to generate process heat

Electric energy to drive motors and or use in specifcprocess steps, e.g. electrolysis

The energy and cost saving potential is closely linked to the

ow o heat in the plant in most cases. The basic idea behind

waste heat recovery is to try to recover maximum amounts o

heat in the plant and to reuse it as much as possible, instead

o just releasing it into the air or a nearby river.

Figure 1.2

Energy fow without

waste heat recovery

Figure 1.3

Energy fow with

waste heat recovery

Fuel

Heat generation

(boilers, heaters)

Process

Cooling

Surroundings

(rivers, air, etc.)

Fuel

Heat generation

(boilers, heaters)

Process

Cooling

Surroundings

(rivers, air, etc.)

Recove

red

heat

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A key component in waste heat recovery is the heat exchanger.

The proftability o an investment in waste heat recovery

depends heavily on the efciency o heat exchangers and

their associated lie cycle costs (purchase, maintenance, etc).

Dierent designs

All these actors vary considerably between dierent heat

exchanger technologies. Although compact heat exchangers

are very common in the process industry today,

shell-and-tube heat exchangers are still dominating.

Compact heat exchangers have many benefts over

shell-and-tubes: Up to fve times higher heat transer efciency

Lower costs or both initial investment and maintenance

Much smaller in size

These arguments are especially true or heat recovery

services where the dierences are maximal.

An important choice

The choice o heat exchanger is very important and has a

direct impact on the bottom-line result. In act, replacing old

shell-and-tubes with new compact heat exchangers in

existing heat recovery systems is oten a very good

investment, thanks to the strong benefts.

1.3 Heat exchangers

Compact heat exchangers are up to fve timesmore efcient than shell-and-tubes, making heatrecovery proftable even where the energy sourcestraditionally have been deemed worthless.

Figure 1.4

The diagram shows the heat recovery level as a function

of initial cost. The yield from compact heat exchangers

is up to 25% higher than or shell-and-tubes at a

comparable cost. To reach the same levels o heat

recovery, shell-and-tube solutions oten become

several times more expensive. The basis o compar-ison is a BEM shell-and-tube system with stainless

steel tubes and usion bonded AlaNova compact

heat exchangers. For more details, please visit

www.alalaval.com/waste-heat-recovery.

x5

Cost units

Heat recovery

Compact heat

exchanger

Shell-and-tube

heat exchanger

70%

75%

80%

85%

90%

95%

+25%

100%

0 1 2 3 4 5 6

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Boliden Harjavalta, Finland

Boliden Harjavalta recovers 20 MW (68.2 MMBtu/h)

o heat in its sulphuric acid plant. Hal o this energy

is used in Bolidens copper and nickel plants in the

area, and the other hal is sold to the local district

heating network.

1.4 Heat integration analysis

Recovering heat is only valuable i the heat can be reused.

The recovered heat must add to the bottom-line result in

some way or an investment to be justifable.

Finding the best opportunities

To fnd all the potential ways to create value rom recovered

heat, the whole energy system o the plant must be analyzed,

as well as the processes, the cooling system and surrounding

actors.

Oten the best way to proft on recovered heat is less obvious

than just saving uel. There are many parameters to take into

account, some being: How is process heat generated?

What is the optimum load on the boilers/burners?

How is electricity generated? Is there any spare capacity

in the co-generation systems?

Are there constraints in the cooling systems?

Are there bottlenecks related to heating or cooling?

Are there neighbouring plants or residential areas?

The owchart on the next page shows the basic

energy-related units ound in most plants, and will be the

starting point or the discussion in the next chapter on how to

make money rom waste heat.

Photo: Liisa Valonen

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Electricity generation

(steam turbines)

Purchased uels

(oil, gas, biomass, etc.)

Cooling system

(cooling towers, closed loop cooling, etc.)

ChillersMechanical work

Purchased electricity

Neighbouring plants

and residential areas

Heat transormation

systems (ORC, etc.)

ProcessUnit operations requiring

heating and cooling

Surroundings

(rivers, air, etc.)

Recovered

energy

Figure 1.5

The fow chart below shows the basic systems

found in most plants and is a good starting

point when discussing how to get maximum

results from reusing recovered energy.

Heat generation

(boilers, red heaters/urnaces)

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2. Eight ways to proft

rom waste heatBeore investing in waste heat recovery it is important to analyse

all potential gains, and assess the proftability o the investment.

There are eight ways to proft rom waste heat:

Saving uel Generating electricity and mechanical work

Selling heat and electricity

Reducing cooling needs

Reducing capital investment costs

Increasing production

Reducing greenhouse gas emissions

Transorming the heat to useul orms o energy

Most plants have the opportunity to make use o recovered energy

in several ways. The optimum mix depends on the specifc

characteristics o the plant, its location, and energy prices.

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Increaseproduction

Reduce coolingneeds

Generateelectricity

Reduce capitalinvestment

costs

Save uel

Sell heat andelectricity

Reducegreenhouse

gas emissions

Figure 2.1

There are eight general ways to make

a prot on recovering waste heat.

Transormthe energy


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Process heat is usually generated in steam boilers and/or in

fred heaters/urnaces. In both cases, waste heat recovery

can lead to substantial uel savings.

Process heat rom steam boilers

Recovering waste heat oten reduces the need or steam in a plant.

Consequently the boilers uel consumption is reduced, as are

greenhouse gas emissions and the load on the cooling system.

Recovered heat can also be used or preheating the boiler

eed, lowering uel consumption.

Process heat rom fred heaters/urnacesThe uel consumption o a fred heater/urnace can be

reduced by using waste heat rom the plant or preheating the

heater eed. Again, this reduces uel bills, cooling system load,

and greenhouse gas emissions.

2.1 Saving fuel

Avdeevka Coke, Ukraine

Replacing two shell-and-tube heat exchangers in

the light oil recovery section o the plant with a

single Ala Laval Compabloc saved more than

100 m3 o coke oven gas per hour in a burner.

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2.2 Generating electricity and

mechanical work

Electricity

Many plants generate their own electricity by directing part o

the steam rom a process-heat boiler to a turbine.

Recovering waste heat reduces steam consumption in the

plant, making it possible to use a greater portion o the steam

or generating electricity (provided there is more capacity in

the turbines).

This can provide a very attractive way o reducing energy

costs or plants with a high consumption o electricity.

Mechanical work

Some plants use turbines to drive compressors or pumps

directly. Waste heat recovery will make it possible to generate

more mechanical work as described above.

Santelisa Vale, Brazil

Steam consumption was reduced by 40% to 50% inthis sugar and ethanol plant by replacing existing

shell-and-tubes with Ala Laval WideGap heat

exchangers. The excess steam is used or generating

electricity, which is sold to the national grid.

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(steam turbines)

Purchased uels


Cooling system




Neighbouring plants


Heat transormation

systems (ORC, etc.)


heating and cooling

Surroundings

(rivers, air, etc.)

Recovered

energy

Heat generation


Figure 2.3

Reducing the need or steam in the

process means more steam can be

used or electricity generation.

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2.3 Selling heat and electricity

The most proftable options are sometimes ound outside the

site. I the plant is situated in the vicinity o other plants or a

city, selling heat and electricity externally may be an excellent

business opportunity.

HeatI the plant is located in an industrial cluster, it may be possible

to sell heat to neighbouring sites.

Recovered heat can also be sold or use in district heating,

fsh breeding, greenhouse heating, etc.

Electricity

For plants where heat recovery oers the opportunity to increase

electricity generation, the new possible power output may be

greater than needed in the plant. In this is the case, it may be

possible to sell the surplus to neighbouring plants or to the grid.

Kemira, Sweden

Every year the Kemira sulphuric acid plant delivers

a total o 240 GWh (819 GBtu) o recovered heat to

the district heating network o the city o Helsingborg.

The payback period was less than one year.

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Figure 2.4

The recovered energy can be sold externally as

district heating or to a neighbouring plant. I heat

recovery leads to increased co-generation,

electricity may be sold to the grid.


(steam turbines)

Purchased uels


Cooling system




Neighbouring plants


Heat transormation

systems (ORC, etc.)


heating and cooling

Surroundings

(rivers, air, etc.)

Heat generation


Recovered energy

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2.4 Reducing cooling needs

Recovering heat oten has positive eects on the cooling

system. The more heat is recovered and reused, the less it

needs to be cooled o ater the process steps. This can be

valuable in a number o cases.

Bottlenecks

I cooling is a limitation in the plant, recovering heat can ree

up capacity and resolve cooling-related bottlenecks in other

parts o the plant.

Environmental constraints

Many plants have environmental constraints in terms o how

much cooling water can be taken rom a river and/or

temperature limitations on the returned water.

Waste heat recovery can be the solution to either one or both

o these problems, allowing the plant to run at ull capacity.

Operating costs

Solving cooling limitations through heat recovery has the addedbeneft o reducing operating costs. The load on circulation

pumps and cooling tower an systems is lowered, and in turn,

the consumption o electricity. Reduced need or cooling

water means reduced need or water treatment chemicals.

Unipar, Brazil

UNIPAR reduced steam consumption by 4.7 MW

(16 MMBtu/h) when installing an Ala Laval

Compabloc heat exchanger in its cumene

production plant. This also eliminated the need orcooling water in the cumene condenser. The

payback period was less than one year.

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Figure 2.5

Waste heat recovery oten leads to a

reduced load on the cooling system,

and may also resolve cooling-related

bottlenecks in the production.


(steam turbines)

Purchased uels


Cooling system




Neighbouring plants


Heat transormation

systems (ORC, etc.)


heating and cooling

Surroundings

(rivers, air, etc.)

Recovered

energy

Heat generation


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2.5 Reducing utility investments

Considering heat recovery can lead to substantial savings in

both new and existing plants when planning new utility

investments. It can cut both uture operating costs, utility

systems and capital investment costs.

Recovering process heat reduces investment costs in systems

or heat generation and cooling, as well as costs or space.

Boilers and burners

Recovering heat leads to a lower need or new heat, reducing

the capacity need o boilers, direct fred heaters and urnaces.

CoolingThe frst thing to consider when planning new cooling capacity is

how to reduce the input o heat into the system. Recovering

heat reduces the cooling need and a cooling tower o less

capacity will sufce.

Shell Sarnia, Canada

Installing Ala Laval Compabloc heat exchangers

led to a 13.5 MW (46 MMBtu/h) increase in heat

recovery. Recovering this heat means the steam

plant still has additional capacity to meet any

urther increase in demand.

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Figure 2.6

Waste heat recovery oten reduces

the load on the utility systems.


(steam turbines)

Purchased uels


Cooling system




Neighbouring plants


Heat transormation

systems (ORC, etc.)


heating and cooling

Surroundings

(rivers, air, etc.)

Recovered

energy

Heat generation

(boilers, fred heaters/urnaces)

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2.6 Increasing production

Debottlenecking

It is not uncommon to fnd limitations in boiler or cooling

capacity that hamper production rates. Waste heat recovery can

be an easy way to resolve these bottlenecks. Recovering heat

means the load on the cooling and heating systems is reduced

and the ree capacity can be used or increased production.

Space constraints

Ala Lavals compact heat exchangers are a perect match when

space is the limiting actor or increased production. The high

efciency and small ootprint means they oer much higher

capacity per square meter than shell-and-tube heat exchangers.

Higher by-product production rates

In some processes, such as sugar production rom sugar cane,

coke oven gas refning, and sugar-based ethanol production,

combustible by-products are burned to generate process

steam and heat.

With the introduction o a heat recovery system, the need to burnby-products as uel may be reduced and they can be sold instead.

Some Ala Laval customers have started proftable biomass

pellet operations, or gasifcation-based chemicals production.

Mulgrave Central Mill, Australia

When Mulgrave Central Mill installed Ala Laval M30

plate heat exchangers in its raw sugar plant, the

capacity o the evaporation system increased by2.5% to 5%.

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2.7 Reducing greenhouse gas emissions

Since waste heat recovery oten leads to signifcant uel savings,

CO2

emissions are oten reduced. The primary beneft o lower

emissions is o course the positive eects on our environment,

but they can have monetary value as well.

Many parts o the world have, or are about to introduce,

emissions trading systems (cap and trade), the European

Union Emission Trading Scheme being the largest in use.

Ater implementing waste heat recovery systems, companies may

fnd they have unused emission permits. These can then be

sold i the company is operating under a cap and trade system.

In countries without cap and trade systems there may still be

possibilities to sell emission permits to other parts o the worldthrough the UNs exible mechanisms.

Dow Wol Cellulosics, Belgium

Installing an Ala Laval Compabloc or energy recovery

in a solvent recovery column has resulted in substantial

energy savings and reduced CO2

emissions.

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2.8 Transforming energy

Recovered heat can also be used in combination with

waste-heat transormation technologies or producing:

Chilled water

Hot water

Distilled water

Electricity

Chilled water absorption chilling

Absorption chilling is a technology that converts low-temperature

waste heat to chiller capacity. Absorption chillers can be attractive

investments in plants with chilling need and large amounts o

available low-grade heat. Especially so i electricity prices are

high, since the power consumption o an absorption chiller is

practically negligible compared to that o a conventional chiller.

Figure 2.7

Recovering 20 MW at 95C or use in an absorption chiller can give 7 MW o chilling at 7C.

Input:

1.75 MW

electricity

Beore

Absorption

chiller

Input:

20 MW (68.2 MMBtu/h)

waste heat at

95C (203F)

Output:

7 MW (23.9 MMBtu/h)

chilling at 7C (44F)

Ater

1.75 MW electricity saved

Conventional

chiller

Output:

7 MW (23.9 MMBtu/h)

chilling

26

Figure 2 8


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(steam turbines)

Purchased uels


Cooling system




Neighbouring plants


Heat transormation

systems (ORC, etc.)


heating and cooling

Surroundings

(rivers, air, etc.)

Recovered energy

Heat generation


Figure 2.8

Valuable assets can be produced

using recovered waste heat thanks

to heat transormation technologies.

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Example

In 2008 Ala Laval supervised a thesis rom Lund University

where waste-heat powered absorption chilling was studied.

Assuming there is a high need or chiller capacity and good

supply o low-temperature waste heat, absorption chillers

proved to be a proftable investment, both when replacing

existing chillers and in new plants.

Heat pumps and mechanical vapour recompression (MVR)

Heat pumps and MVRs are used when the temperature o the

waste heat stream is too low to be used or heat recovery.

Both heat pumps and MVRs raise the temperature o the

waste heat, but require an input o electricity or mechanical

work (or driving a compressor). However, electrical energy is

usually only a raction, typically 25%, o the amount o heat

energy that can be upgraded to higher temperatures.

Waste heat to pure water

In areas where pure water is a scarce resource, recovered waste

heat can be used or producing demineralised water. This

application is especially interesting i planning a new installation,

since an evaporative desalination system will have minimal

operating costs. It is oten possible to cut lie-cycle costs o

water by 50% to 75% compared to a reverse osmosis system.

0

2

4

6

8

10

12

0 20 40 60 80 100 120 140

Pay back period (years)

Pay back period(revamp) years

Pay back period newplant (reduced capex

conventional chiller)

Electricity price (EUR/MWh)

Figure 2.9

Absorption chilling

The payback period or a system with heat integration and

absorption chilling as a unction o electricity price. For

assumptions, see www.alfalaval.com/waste-heat-recovery.

Coastal Aruba Refning Company, Aruba

The Coastal Aruba renery uses an Ala Laval desali-

nation system to generate resh water rom seawater.

, ,

,

.

,

.

,

,

,

,

.

.

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Electricity organic Rankine cycle (ORC) systems

An ORC system works according to the same principles as a

normal steam turbine. The main dierence is that an organic

uid is used instead o water, and that waste heat is used to

vapourize the uid instead o a boiler. Commercially available

systems can generate electricity rom temperatures as low as

55C (131F).

Example

The graph shows a proftability analysis based on inormation

rom a supplier o organic Rankine cycle systems. The cycle

converts waste heat to electricity with an efciency o

approximately 10%. In this case the ORC system converts

approximately 7 MW (23.9 MMBtu/h) o waste heat into

0.7 MW o electricity, i.e. an annual production o 5,880 MWh.

0

1

2

3

4

5

6

7

8

9

0 20 40 60 80 100 120



Figure 2.10

ORC system

Payback period or an ORC system. The annual saving

amounts to 5,880 MWh. For assumptions, see www.

alalaval.com/waste-heat-recovery.

Opcon, Sweden

Opcon develops and markets cutting-edge products or waste

heat recovery. Opcon Sweden uses A la Laval heat exchangers

in its organic Rankine cycle systems. The systems are used

or generating electricity rom waste heat with temperatures

as low as 55C (131F).

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3. Recovering heat fve generic casesBuilding blocks

Unit operations are the basic building blocks o process industries. The

conditions and media vary, but the operating principles and several typical

heat transer services within these process systems are the same.

This section presents the results o fve in-depth proftability analyses rom

fve dierent industries. One or more o the heat transer services in the fve

cases are ound in most process plants and the results can be applied to

many industries.

The cases are:

Preheating in interchangers

Direct process-heat integration

Indirect process-heat integration

Increased number o eects in evaporation systems

Reduced ouling

When calculating a cost-optimized heat recovery level, people oten use

data or inefcient shell-and-tube heat exchangers. Since cost is higher

and output is lower or shell-and-tubes than or compact heat

exchangers, the calculations are oten misleading, resulting in

unnecessary losses o energy and proftability. The ollowing studies all

examine the proftability when using compact heat exchangers the

most efcient technology.

30

Figure 3.1


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Overview o a typical process

plant energy system.

Purchased uels


Cooling system


Surroundings

(rivers, air, etc.)

Recovered

energy

Heat generation


ProcessHeating and cooling consumers

Evaporation systems Leaching tanks

Distillation columns Electrolytic cells

Reactors Absorption stripping systems

Condensate and waste

treatment plants

Process water and eedstock

treatment and heating

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3.1 Preheating in interchangers

Feed/euent heat exchangers, lean/rich interchangers,

in-and-out heat exchangers, and eed/bottoms heat

exchangers are all dierent names or the same concept:

preheating o an ingoing stream o a unit operation using heat

rom the outgoing stream.

This is commonly done in:

Reactors

Electrolytic cells

Absorption stripping systems

Leaching tanks

Stripper- or distillation columns

Evaporation systems

Changing to compact heat exchangers is a straightorward

way to improve heat recovery levels. This reduces the heat/

steam consumption, resulting in either uel savings and reduced

emissions, or increased electricity generation. Cooling needs

are also oten reduced, which is valuable in many situations.

Figure 3.2

Preheating in interchangers.

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Example: Feed/euent heat exchanger

condensate stripper

The ollowing example is based on a heat exchanger

specifcation rom a condensate treatment stripper. An

existing shell-and-tube heat exchanger is replaced with a

Compabloc welded plate heat exchanger, which increases

heat recovery by 3.8 MW (13 MMBtu/h). It is assumed that 85%

o the recovered heat translates into saved steam and, in turn,

uel savings or increased electricity generation. The two diagrams

on the next page show the payback period or the investment.

Assumptions

8,400 operating hours per year

Overall pressure drop increases by approximately 1 bar, but no new pump isneeded (only operating costs increase)

Physical properties on both sides are similar to water

Installation factor = 3, i.e. the heat exchanger represents 33% of the total project cost

Cold side fow rate 75 m3/h and hot side 90 m3/h

Boiler eciency 90% (boile r case)

Turbine isentrop ic eciency 80% (electricit y case)

Results

SI American

Increased heat recovery 3.8 MW 13 MMBtu/h

Reduced cooling water temperature,

fxed ow o 1,000 m3/h (4,400 gpm)

3C 5.4F

Reduced cooling water ow,

fxed T = 10C (18F)

300 m3/h 1319 gpm

Reduced CO2

emissions 5,600 metric tons/year

Figure 3.3

Condensate treatment stripper beore and aterrevamp.

Feed solution

170C (338F)

Efuent solution

225C (437F)

Steam

25 bar(a)(363 psia)

Feed solution

40C (104F)

Efuent solution

100C (212F)

Beore

Feed solution

210C (410F)

Efuent solution

225C (437F)

Feed solution

40C (104F)

Efuent solution

55C (131F)

Ater

3.8 MW (13 MMBtu/h ) recovered heat

Steam

25 bar(a)

(363 psia)

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Figure 3.4

Fuel savings in boiler

Payback period as a unction o energy price when using the recovered

energy or saving uel.

0

0,5

1

1,5

2

2,5

3

0 10 20 30 40

Steam price (EUR/ton)


New plant (reduced utility

investments also taken

into account)

Revamp (replacing

an existing shell-

and-tube)

Figure 3.5

Increased electricity generation


energy or electricity generation.


Revamp (replacing an existing shell-and-tube)

00,5

1

1,5

2

2,5

3

3,5

4

4,5

5

0 50 100 150


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3.2 Direct process heat integration

Process heat integration means heat that was previously cooled

o is recovered and reused in another unit operation. With direct

process heat integration, heat is transerred directly rom one

process stream to the other in a single heat exchanger.

The two streams need to be airly close to each other, and

there should not be any dangers involved i the streams mix in

case o a leak.

The result is a reduced load on both the heating and cooling

utility systems, which transorm into value in many ways, as

described in chapter 2.

There are numerous examples in chemical plants where direct

process heat integration can be utilized, or example:

In refneries, the heat rom several waste streams can be

used to preheat crude oil upstream o a fred heater.

Preheating o naphtha or eed gas in steam reormers.

Preheating o the eed in fred heaters.

Preheating o mill water and chlorine dioxide in chemical

pulp mills.

Column integration in multistage distillation.

Figure 3.6

Direct process heat integration.

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Example: Feed preheating in direct fred heater/urnace

In this example heat rom a process gas stream is recovered and

used or preheating the eed gas o a direct fred heater. A shell-

and-tube is replaced by a compact heat exchanger, increasing

heat recovery and reducing gas consumption. The result is an

increase in heat recovery by 1.7 MW (5.814 MMBtu/h).

Hot process gas

250C (482F)

Hot process gas

165C (329F)

Cold eed gas

50C (122F)

Preheated eed gas

180C (356F)

Direct red

heater/

urnace

Feed gas ater

heater

300C (572F)

Hot process gas

250C (482F)

Hot process gas

130C (266F)Cold eed gas

50C (122F)

Preheated eed gas

225C (437F)

Direct red

heater/

urnace

Feed gas ater

heater

300C (572F)

1.7 MW (5.8 MMBtu/h ) increased heat recovery

Beore Ater

Figure 3.7

Direct process heat integration beore and ater revamp.

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Results

SI American

Increased heat recovery 1.7 MW 5.814 MMBtu/h


fxed ow o 1,000 m3/h (4,400 gpm)

1.5C 2.7F


fxed T = 10C (18F)

150 m3/h 660 gpm

Reduced CO2

emissions 3,300 metric tons/year

Assumptions

Operating hours: 8,400 hours/year

Installation actor: 3

Heat recovered beore/ate r: 4.3/6 MW

Fired heater eciency: 80%

Gas pressures 20-30 barg only centriugal compressors used

Physical properties similar to syngas on process side and natural gas on eed side P: same beore and ater technology change

Figure 3.8

Fuel savings in direct fred heater/

urnace

Payback period or heat recovery system as a unction

o uel price.

0

1

2

3

4

5

6

7

8

9

0 2 4 6 8 10 12 14 16

Gas price (USD/MMBtu)


Revamp (replacing

an existing S&T)New plant (reduced utility

investments also taken

into account)

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3.3 Indirect process heat integration

Indirect process heat integration diers rom direct process heat

integration in that an intermediate circuit is used or transerring

heat between the two process streams. The transer medium

(water or thermal oil) absorbs heat in one part o the plant and

releases it in another. This approach is used when:

Direct contact between heat source and heat sink is notallowed. The intermediate circuit works as a saety

barrier and leakages can be detected in the loop, beore

the process uids mix.

Long distances need to be covered.

Flexibility and reduced interdependence is required.

Equipping the intermediate circuit with standby coolers and

heaters makes it easier to disconnect a unit operation or

maintenance, avoiding interdependence between plants.

One heat sink requires multiple heat sources.

Indirect process heat integration opens up a vast range o

possibilities. Common application examples are:

Sulphuric acid and mineral processing industries.

Boiler eed-water heating where it is important to avoidinterleakage and/or where there is a long distance

between boiler and heat source.

Ammonia still condenser systems with integrated

mother liquor heating in the soda ash industry.

Caustic soda pre-evaporation by recovery o

electrolysis heat.

Figure 3.9

Indirect process heat integration.

Intermediate circuit

Unit operation 2

Unit operation 1

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Example: Sulphuric acid plant

The ollowing is a typical example rom a metallurgical sulphuric

acid plant. Here there are oten opportunities to recover waste heat

rom the acid plant absorption towers and reuse it or heating in

mineral processing steps. Examples where the heat can be reused

are copper electrolyte heating, spent acid and zinc sulphate

solution heating in zinc plants, boiler eed water heating, etc.

Beore the technology change, the hot sulphuric acid rom the

absorption towers was cooled o in a shell-and-tube heat

exchanger. Aterwards, the heat is transerred to a heat integration loop

via a compact heat exchanger and released to an electrolyte heating

bath. The result is 10 MW (34 MMBtu/h) o recovered energy.

Results

SI American

Increased heat recovery 10 MW 34 MMBtu/h


fxed ow o 1,000 m3/h (4,400 gpm)

8.5C 15.3F


fxed T = 10C (18F)

860 m3/h 3784 gpm

Reduced CO2 emissions 18,000 metric tons/year

Assumptions

60 W/m heat loss in pipeline

Boiler eciency 90% (uel savings case)

Turbine isentropic eciency 80% (electricity generation case)

Total system operating and capital cost estimation based on real quotations

Demineralized water used in intermediate loop

Installation actors 1.5-2 or heat exchangers

Installation actor 3 or pipeline construction (insulated pipes)

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Figure 3 .11

Fuel savings, revamp o existing plant

Payback period as a unction o energy price when using

the recovered energy or saving uel.


0

0,5

1

1,5

2

2,5

3

3,5

0 5 10 15 20 25 30 35

200 m (656 ft)

between plants1,000 m (3,280 ft)

between plants

Steam price (EUR/ton)

Figure 3.10

Beore and ater indirect process heat integration.

10 MW (34 MMBtu/h ) process heat recovery

Cooling water Condensate

Cold sulphuric acid

Cold

process

fuidHot

sulphuric

acid

Hot process fuid

Beore

Intermediate

loop

Cold sulphur ic ac id Cold process fu id

Hot sulphuric aci d Hot process fuid

Ater

115C

(239F)

80C(176F)

30C (86F) 20C (68F)

90C

(194F)

60C

(140F)

Steam,

pressure

10 bara

(145 psia)

80C(176F)

115C

(239F)

60C(140F)

90C

(194F)

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Figure 3.12

Electricity generation, revamp o existing plant


energy or electricity generation.

Figure 3.13

Fuel savings, new plant

Payback period or new plant (reduced utility investments).

1,000 m between unit operations.

0

1

2

3

4

5

6

7

0 20 40 60 80 100 120 140



200 m (656 ft)

between plants

1,000 m (3,280 ft)

between plants

0

0,5

1

1,5

2

2,5

3

0 5 10 15 20 25 30 35

Steam price EUR/ton


41


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Eect 1 Eect 2 Eect 3

Previous eects Added eect

Steam

Concentrated product Product eed

4.4 MW (15 MMBtu/h ) reduced heat consumption

Figure 3.15

Increasing the number o eects in an evaporation system dramatically reduces the steam consumption.

43

3 5 Reduced fouling and maintenance


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3.5 Reduced fouling and maintenance

Shell-and-tube heat exchangers gradually lose efciency in

applications with heavy ouling. The result is lower energy

transer and high maintenance costs.

Spiral heat exchangers on the other hand have a sel-cleaning

design, making them much less prone to these problems and

very suitable or handling highly ouling uids. Examples o wherespiral heat exchangers are used include oil refneries, pulp and

paper mills, mineral processing plants, and petrochemical

plants, typically in services most suering rom ouling.

Example oil refnery visbreaker cooler/interchanger

This example is based on input rom a European oil refnery,

where spiral heat exchangers replaced shell-and-tubes in a

visbreaker cooler service (interchanger) in an existing plant.

There are usually multiple heat exchangers operating in parallel in

this service, but this example shows a one-to-one comparison

between the two technologies.

The increased heat recovery in this case originates rom two

actors; reduced downtime and better perormance due to less

ouling build up. Reduced ouling also means reduced cleaning

requency and lower cleaning costs.

The two alternatives in this example represent two dierent

maintenance philosophies; making ew or many stops or cleaning.

Figure 3.16

The sel-cleaning design o spiral heat exchangers

make them the ideal choice or ouling duties.

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Improved perormance and reduced cost when using spiral heat exchanger

Compared to shell-and-tube

cleaned twice per year

Compared to shell-and-tube

cleaned 12 times per year

Increased perormance 41% 11%

Reduced annual

cleaning cost 6,000 66,000

Assumptions

Heat transer at startup = 1 MW (3.4 MMBtu/h)

Operating hours per year = 8,400

Working days per cleaning = 1.5

Cost per day or cleaning = 4,000

Installed cost o spiral heat exchanger = 200,000

Shell-and-tube cleaned twice per year Annual cleaning cost = 12,000

Average perormance loss = 30%

Annual heat recovery loss due to cleaning = 0.86%

Total perormance loss = 31% or 0.31 MW (1.1 MMBtu/h, 0.21 barrels o oil/hour)

Shell-and-tube cleaned 12 times per year

Annual cleaning cost = 72,000

Average perormance loss = 7.5%

Annual heat recovery loss due to cleaning = 5.14%

Total perormance loss = 12.5% or 0.125 MW (0.43 MMBtu/h, 0.1 barrels o oil/hour)

Spiral heat exchanger cleaned once per year

Annual cleaning cost = 6,000

Average perormance loss = 2.9%

Total perormance loss = 2.9% or 0.029 MW (0.10 MMBtu/h, 0.02 barrels o oil/hour)

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Figure 3.17

Shell-and-tubes versus spiral heat exchangers

Perormance in heavy ouling services

Heat transer eciency or spiral heat exchangers and shell-and-tubes in

oil renery visbreaker cooler.

Figure 3.18

Replacing existing shell-and-tube with spiral heat

exchanger

Payback period when changing rom shell-and-tubes to spiral heat

exchanger.

0%

20%

40%

60%

80%

100%

120%

0 2 4 6 8 10 12

Heat transfer coefficient

compared to design value

Months in operation

Shell-and-tube cleaned twice per year

Spiral heat exchanger

Shell-and-tube cleaned 12 times per year

0

1

2

3

4

5

6

7

8

0 20 40 60 80 100 120 140

Oil price (USD/barrell)


Spiral heat exchanger vs. shell-and-tubecleaned twice per year per year

Spiral heat exchanger vs. shell-and-tube

cleaned 12 times per year

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Ala Laval in brieAla Laval is a leading global provider o

specialized products and engineering solutions.

Our equipment, systems and services are

dedicated to helping customers to optimize

the perormance o their processes.

Time and time again.

We help our customers to heat, cool, separate

and transport products such as oil, water,

chemicals, beverages, oodstus, starch and

pharmaceuticals.

Our worldwide organization works closely with

customers in almost 100 countries to help

them stay ahead.

How to contact Ala LavalContact details or all countries are continually

updated on our web site. Please visit

www.alalaval.com to access the inormation.

www.alalaval.com/waste-heat-recovery

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