Size the heat pump from measured, time-resolved steam demand and the required pressure and temperature at each process—not from boiler nameplate capacity or a daily average. Map recoverable heat sources, separate lower-temperature hot-water duties from true steam loads, model batch schedules over a full year, and select capacity, storage and backup together. Without those site measurements, a responsible numerical nameplate recommendation is not possible.
What the sizing decision must deliver
A brewery heat-pump project can have several different objectives: replace all boiler steam, displace only a continuous base load, supply one kettle or process branch, preheat boiler feedwater, or provide hot water while an existing boiler handles peaks and backup. Those objectives produce different capacities even at the same brewery.
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The design output is not simply a kilowatt figure. It is a matched specification covering useful heat capacity, steam pressure and saturation temperature, source-temperature range, mass-flow turndown, startup response, annual operating hours, controls, thermal storage, backup equipment, electrical connection and economic assumptions. A heat pump that meets a short design peak but runs at low utilization may use more annual electricity and cost more than a smaller unit paired with storage or a boiler.
Brewery evidence illustrates why. In one modeled simultaneous-heating-and-cooling case, electricity use was 9.8% lower than the reference at design conditions but only 2.1% lower over the year because heating and cooling loads fluctuated. A single peak, a daily average or a design-point COP therefore cannot establish the best configuration.
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1. Define the service before calculating capacity
Specify the point of use
Record the pressure and temperature where steam enters each process, not merely the boiler outlet rating. Include wort kettles, hot-liquor tanks, cleaning systems, pasteurization, packaging, space or process heating and any steam used for sterilization. For saturated steam, pressure determines saturation temperature; superheat, pressure drop and steam quality may impose additional requirements.
For every branch, document required steam mass flow, minimum and maximum flow, acceptable response time, operating hours, condensate-return temperature and fraction, and whether the process can accept hot water instead of steam. Steam temperature alone is insufficient for equipment selection because the same temperature target can occur with very different flow rates and schedules.
Choose the project boundary
- Full boiler replacement: the heat pump must cover the required steam condition, peak flow, startup and abnormal operating cases, or another dependable source must cover those cases.
- Base-load displacement: the heat pump runs for long periods at high utilization while a boiler, electric boiler or stored steam covers peaks.
- Process-specific supply: one kettle, hot-water loop or production line is isolated so its demand can be measured and controlled independently.
- Heat recovery and feedwater preheating: a lower-temperature heat pump or direct recovery reduces the boiler duty without producing all final steam.
State the intended role in the design brief. A supplier cannot compare capacities or savings consistently when “replace steam” could mean any of these four boundaries.
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2. Build an interval steam-demand profile
Install temporary or permanent instrumentation and collect data over representative brew days, non-brew days, weekends, cleaning cycles and seasonal conditions. A brewery metering case measured steam generated by each boiler and used the results to identify consumption and circuit losses; the important practice is the measured, branch-level profile, not a particular meter brand.
- Measure steam mass flow. Use a meter rated for the pipe size, pressure, temperature, wetness and installation conditions. Log totalized mass and instantaneous flow.
- Log pressure and temperature at the relevant headers and branches. These values establish enthalpy, reveal pressure drops and show whether a “steam” load is actually a hot-water duty.
- Synchronize process signals. Capture brew starts, mash-in, wort boiling, cleaning-in-place cycles, pasteurization, packaging and idle periods with the same time base as the steam data.
- Separate coincident loads. Sum only loads that occur at the same interval. Adding every connected load produces an installed-load total, not a design peak.
- Record boiler and distribution losses. Track blowdown, warm-up, venting, trap losses and unreturned condensate so fuel input is not mistaken for useful process heat.
- Overlay the production plan. Include planned shifts, product mix, seasonal demand and expansion. A profile that represents one atypical brew week can mis-size the system.
Select an interval short enough to show batch peaks and switching—often minutes rather than hours—then retain the raw data. Aggregate later for annual energy analysis, but do not start with a daily average that hides short, high-flow events.
Distinguish demand categories
Tag each interval as production, cleaning, hot-water generation, space heating, standby or another category. Note simultaneous heating and refrigeration. If a refrigeration system rejects heat while a hot-water tank is charging, that coincidence can be more valuable than the maximum of either load considered alone.
3. Convert steam flow into useful heat
Use measured mass flow and thermodynamic properties at the actual pressure and feedwater condition:
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Useful heat rate = steam mass flow × (steam specific enthalpy at the required condition − feedwater or condensate enthalpy)
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Obtain enthalpy from steam tables for the site pressure and temperature. Keep units consistent—for example, kilograms per second and kilojoules per kilogram produce kilowatts. Calculate each process branch before summing the coincident intervals.
Condensate return matters. Hot condensate reduces the heat required per kilogram of new steam; a cold or intermittent return increases it. Feedwater temperature, deaerator operation, blowdown and flash steam also change the useful duty. Boiler fuel consumption alone is not a valid substitute because it includes combustion efficiency, stack loss, jacket loss, blowdown and distribution losses.
Check the load-duration curve
From the interval series, calculate:
- the highest coincident useful-heat rate and its duration;
- the sustained base load during production;
- the hours in each load band;
- the annual useful heat delivered;
- the number and duration of starts, shutdowns and idle periods.
This curve lets you test a full-peak heat pump against a base-load unit with storage or backup. It also supplies the operating hours needed for annual electricity and maintenance estimates.
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4. Map heat sources and lower-temperature sinks
List every potential source by temperature, available heat rate, fouling risk, cleanliness, distance, schedule and seasonal availability. Candidates can include refrigeration or chiller rejection, wort-cooling heat, warm wastewater, exhaust or vapour and ambient air. Measure the source temperature during the same intervals as the steam load; a source that is hot only after a batch may not support a continuous rating.
Then list sinks separately. Hot-liquor water, cleaning water, mash processes, pasteurization and feedwater generally require lower temperatures than direct steam. Direct heat recovery should serve the lowest-temperature duty that can accept it before a heat pump raises temperature further. Reducing hot-water and feedwater demand can shrink the final steam requirement.
A 2026 Technical University of Denmark pinch-analysis study used 21.4 kWh per hectolitre as the total heat demand for a generalized brewery model and compared electrification arrangements. That is a study input, not a universal brewery benchmark. The same work reported 5 to 3.6 kWh per hectolitre of electricity for its studied alternatives; those values are architecture-specific results, not a promise for another site.
5. Select an architecture that fits the temperature lift
Temperature lift is the difference between the useful source temperature entering the heat pump and the required sink temperature at the process. Measure both under operating conditions. A larger lift generally lowers COP and may reduce capacity, increase compressor stages or require a different refrigerant and cascade.
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|---|---|---|---|
| Centralized high-temperature heat pump | One system supplies a steam or high-temperature header for several processes. | Simpler central control and potentially direct boiler displacement. | Must meet the highest pressure and temperature; poor matching can leave the unit oversized for most hours. |
| Two heat pumps | A CO2 heat pump charges a warm-water or heat-recovery tank; a high-temperature booster serves wort boiling or another high-lift duty. | Separates efficient lower-lift recovery from the hardest process duty and can use storage between batches. | Requires two sets of controls, heat exchangers and operating limits; booster capacity must follow the batch profile. |
| Integrated CO2, high-temperature booster and mechanical vapour recompression (MVR) | Combines recovery, temperature boosting and MVR for a high-temperature process such as wort boiling. | Can exploit several temperature levels and recycle vapour within the process. | Highest integration and controls complexity; fouling, vapour quality and transient behavior need site engineering. |
| Simultaneous heating and cooling | Recovers refrigeration-side heat while supplying a heat sink such as hot water or steam. | Can reduce purchased cooling and heating energy when schedules coincide. | Benefits depend on coincidence. One modeled case achieved 9.8% electricity reduction at design conditions but 2.1% annually. |
The three brewery arrangements above were compared in a modeled study, not certified as universally optimal. Ask each integrator to model the same interval profile, source limits, steam specification, storage and backup so the comparison is on equal boundaries.
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6. Translate the profile into a nameplate and operating strategy
Full-peak sizing
A full-peak heat pump is appropriate when the process requires firm heat-pump supply at the maximum coincident load, the source is available at that time and the electrical connection can support compressor startup and operation. Verify that the published capacity is available at the worst source temperature and highest sink pressure, not only at a favorable rating point.
Base-load sizing with peak backup
A smaller unit can operate for more hours at a favorable lift while a boiler or electric boiler supplies short peaks, startup and maintenance. Compare the annual electricity, fuel, demand charges, emissions, maintenance and capital cost. The correct fraction is site-specific; the reviewed evidence does not establish a universal brewery percentage or peak factor.
Storage-assisted sizing
Thermal storage can decouple a heat pump’s steadier output from batch demand. Size storage from the measured energy deficit during a batch, the available charging window, allowable temperature swing, tank losses and maximum charge/discharge rate. Do not apply a generic buffer-volume rule: the available sources do not establish one for breweries.
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Multiple compressors or modules can improve turndown and provide partial redundancy. Compare their part-load COP, minimum stable output, sequencing logic and maintenance isolation. A single large machine may have lower installed complexity but can be unavailable during service; several units may cost more while matching variable demand better.
7. Evaluate COP and temperature lift at real conditions
The International Energy Agency reported that industrial heat pumps can exceed COP 3 at a 30–50°C temperature lift. That is a broad observation, not a guaranteed brewery result. COP normally falls as lift rises, so a supplier’s rating at a low lift cannot be used for a high-pressure steam duty.
Request a capacity and COP map covering the measured source-temperature range, required steam pressure, part-load points, ambient conditions, startup, defrost or source-side limits and maximum sink temperature. Ask whether the value is electrical COP at the compressor terminals or includes pumps, fans, controls, auxiliary heaters and storage losses. Use the same system boundary for every option.
One 2026 brewery demonstration report described 300 kW of heat supply, approximately 100°C source vapour and steam varying from 123°C to 130°C. It reported COP above 5 and above 6.5 at lower lifts over 700 trial hours. The report states that the performance information came from the vendor and was not third-party validated; treat it as a demonstration result, not typical or independently verified performance.
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8. Use current technology limits without overpromising
Technology capability is moving quickly. The IEA’s 2026 Heat Pump Monitor says industrial heat pumps below 120°C have entered commercial operation and systems below 160°C are beginning to enter commercial operation. Its 2025 industrial analysis describes large-scale heat pumps as well established up to 150°C, while electric boilers can produce steam to about 350°C and around 70 bar.
These are broad technology-status statements. They do not prove that a particular supplier can deliver the brewery’s flow, pressure, source temperature, refrigerant, water quality, turndown or duty cycle. Obtain a written performance guarantee at the exact operating envelope, and identify any temperature or pressure limits that require a secondary boiler.
9. Model annual operation and economics
Run the measured interval profile through an hourly or sub-hourly model for a representative year. Include production changes, cleaning, maintenance shutdowns, source curtailment, storage state of charge, boiler dispatch, startup energy and control dead bands. Compare at least:
- annual useful heat delivered by the heat pump;
- electricity consumption, including auxiliaries;
- remaining fuel or electric-boiler energy;
- peak electrical demand and demand charges;
- hours at each COP and temperature lift;
- curtailment or unmet load;
- maintenance and expected replacement intervals;
- capital cost, grid upgrades and installation work;
- energy tariffs, gas-to-electricity price ratio and applicable policy incentives.
Grid connection costs, electricity-to-gas price ratios and policy can materially change deployment economics, according to the IEA. A payback calculated from a nameplate COP and annual steam total will miss those constraints. Report sensitivity cases for electricity price, source availability, production growth, condensate return and backup-fuel price.
10. Give suppliers a complete design package
A comparable quotation should include the following information and test conditions:
- interval steam-flow files and branch-level pressure and temperature;
- required saturation temperature, pressure, steam quality and allowable response time;
- feedwater temperature, condensate-return fraction and blowdown practice;
- source temperatures, flow rates, fouling characteristics and availability by season;
- minimum, average and maximum load, plus the load-duration curve;
- planned production expansion and annual operating hours;
- available electrical capacity, voltage, transformer limits and demand tariff;
- space, noise, water treatment, drainage and maintenance access;
- required redundancy, boiler backup, storage volume and control hierarchy.
Require capacity, COP, auxiliary power, turndown and outlet conditions at several source and sink combinations. Ask for startup time, ramp rate, minimum stable load, trip recovery, source-side freeze or fouling protection and performance during simultaneous hot-water and steam production. Make clear which values are guaranteed, simulated, factory-tested, vendor-reported or independently verified.
Independent reader supportYour contribution helps us test, update, and keep practical guides available for everyone.11. Integrate controls, storage and backup
Define a control priority before commissioning. A typical hierarchy might serve direct heat recovery first, charge hot-water storage when surplus heat is available, run the heat pump within its efficient envelope, and call the boiler or electric boiler for peaks, startup, unavailable source heat or emergency operation. The actual sequence must reflect food-safety requirements and process interlocks.
Coordinate steam pressure control with heat-pump ramp limits. A sudden kettle demand can exceed compressor response even when the daily energy balance is favorable. Keep enough stored energy or boiler capacity for that transient. Include alarms for source temperature, high discharge pressure, low flow, condensate problems and storage stratification.
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Commission against the same measured intervals used for design. Verify steam flow, pressure, temperature, electrical power, source heat and condensate return with calibrated instruments. Recalculate field COP using a stated boundary, then compare delivered capacity and annualized operating behavior with the supplier’s guarantee.
12. Common sizing mistakes and corrections
Using boiler nameplate capacity as heat-pump capacity
Boiler nameplate capacity may include spare margin and does not reveal coincident process demand. Replace it with measured useful heat at the process boundary.
Using a daily or monthly average
Averages hide kettle batches, cleaning peaks and startup. Use short intervals for capacity and aggregate only for annual energy analysis.
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Changing return temperature changes enthalpy per kilogram of steam. Measure it rather than applying a generic allowance.
Assuming a high COP at the wrong lift
Request ratings at the actual source and steam conditions. A low-lift demonstration cannot validate a high-lift design.
Sizing for every connected load simultaneously
Connected loads are not necessarily coincident. Use synchronized process data and a documented production scenario.
Treating a case study as a guarantee
The 300 kW demonstration and its reported COP values are vendor-supplied and not third-party validated. Use them as a reference point only.
Leaving backup and grid work until the end
Confirm electrical capacity, tariffs, boiler duty, storage and emergency operation during concept design. A technically adequate heat pump can be uneconomic or unusable if the site cannot supply its peak electrical demand.
Published figures that need qualification
| Figure | What it represents | How to use it |
|---|---|---|
| 21.4 kWh/hl | Generalized brewery total heat demand used in a 2026 Technical University of Denmark pinch-analysis model. | Use only as a literature comparison; do not treat it as a site benchmark. |
| 5 to 3.6 kWh/hl electricity | Range reported for the modeled alternative electrification solutions in that study. | Architecture-specific result, not a guaranteed consumption range. |
| 9.8% at design; 2.1% annually | Electricity reduction for one modeled simultaneous-heating-and-cooling brewery case compared with its reference. | Shows why annual fluctuating operation matters more than design-point benefit. |
| 300 kW; approximately 100°C source vapour; 123–130°C steam | Conditions described in a 2026 report on a 2025 brewery demonstration with 700 trial hours. | Vendor-provided, not third-party validated and not typical performance. |
| COP greater than 5, and greater than 6.5 at lower lifts | Performance figures reported for that demonstration. | Apply only to the reported conditions until independently verified at the proposed site. |
| COP above 3 at a 30–50°C lift | General IEA observation for industrial heat pumps. | Directional context, not a brewery guarantee. |
| Up to 150°C for established large-scale heat pumps; electric boilers to about 350°C and 70 bar | Broad IEA technology-status statements from 2025. | Verify current equipment and exact operating limits with suppliers. |
What a defensible sizing result looks like
The final design should show the measured interval profile, the steam enthalpy calculation, source and sink maps, temperature-lift assumptions, architecture comparison, annual dispatch simulation, electrical and fuel boundaries, storage and backup duties, and supplier guarantees at actual conditions. It should identify which loads the heat pump serves, which remain with the boiler, and what happens during source loss, maintenance and production expansion.
If those inputs are unavailable, the correct conclusion is not a guessed capacity. Complete the metering campaign and process survey first, then have a qualified industrial heat-pump integrator validate thermodynamics, controls, electrical infrastructure, food-process requirements and economics for the specific brewery.
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