## Abstract

A new generation of concentrating solar power (CSP) technologies is under development to provide dispatchable renewable power generation and reduce the levelized cost of electricity (LCOE) to 6 cents/kWh by leveraging heat transfer fluids (HTFs) capable of operation at higher temperatures and coupling with higher efficiency power conversion cycles. The U.S. Department of Energy (DOE) has funded three pathways for Generation 3 CSP (Gen3CSP) technology development to leverage solid, liquid, and gaseous HTFs to transfer heat to a supercritical carbon dioxide (sCO2) Brayton cycle. This paper presents the design and off-design capabilities of a 1 MWth sCO2 test system that can provide sCO2 coolant to the primary heat exchangers (PHX) coupling the high-temperature HTFs to the sCO2 working fluid of the power cycle. This system will demonstrate design, performance, lifetime, and operability at a scale relevant to commercial CSP. A dense-phase high-pressure canned motor pump is used to supply up to 5.3 kg/s of sCO2 flow to the primary heat exchanger at pressures up to 250 bar and temperatures up to 715 °C with ambient air as the ultimate heat sink. Key component requirements for this system are presented in this paper.

## 1 Introduction

Efforts to identify and develop novel heat transfer fluids (HTFs) to harvest and store solar energy through concentrating solar power (CSP) technologies are underway. The U.S. Department of Energy (DOE) is currently funding research on Generation 3 CSP (Gen3CSP) technologies to develop technology to transfer heat from solid, liquid, or gaseous media to a supercritical carbon dioxide (sCO2) Brayton cycle [1]. The sCO2 Brayton cycle is of great interest as it reduces the footprint (due to smaller component size), cost, and has the potential to increase the thermal efficiency of the power cycle (close to 50%), making it competitive when compared with typical Rankine steam power plants [2,3].

The solid/liquid/gaseous Gen3CSP HTF paths (including primary heat exchangers (PHX) design and thermal energy storage) need to prove the capability and scalability of the different systems and require a cooling system for this task. To reach the goals set by the DOE and prove scalability, a cooling system capable of rejecting more than 1 MWth, and handling temperatures and pressures higher than 700 °C and 250 bar, respectively, is necessary.

This paper describes the design of a 1 MWth-scale sCO2 support loop to provide cooling to the PHX of any of the three Gen3CSP pathway projects following on previous scoping studies [46] and builds on experience gained from the design and operation of many previous systems.

## 2 1-MWth Heat Removal System

The combination of CSP with sCO2 Brayton power cycles is a topic of great interest due to the potential for increased efficiencies within the power cycle, reduced capital costs given the compact size of the necessary equipment compared with other commercial power cycles (e.g., steam power cycles), and the compatibility with dry cooling that would decrease the need for cooling water.

The Gen3CSP solid, liquid, and gas pathways, currently in development, require a test setup to evaluate their performance during operation. A system capable of working with any of the three media while supporting a minimum 1 MWth thermal rejection was to be designed.

### 2.1 Requirements.

A set of system requirements were established for the overall Gen3CSP system and are summarized in Table 1. The PHX requirements listed in Table 1 are deemed essential to meet the goals set by the DOE. At the same time, these requirements must be fulfilled when coupled to the sCO2 test system.

Table 1

Supercritical CO2 test system requirements

RequirementValue
Operating fluidCarbon dioxide
PHX outlet pressure250 bar
PHX outlet temperature715 °C
Thermal duty≥1 MWth
Operational time16 h/day
RequirementValue
Operating fluidCarbon dioxide
PHX outlet pressure250 bar
PHX outlet temperature715 °C
Thermal duty≥1 MWth
Operational time16 h/day

Additional requirements were derived after discussion with the PHX design teams. These requirements are primarily driven by the temperature and pressure needed at the PHX inlet and the thermal duty of the system. The derived requirements are summarized in Table 2, including the ability to accommodate a PHX pressure drop up to at least 5 bar.

Table 2

Supercritical CO2 test system derived requirements

RequirementValue
Allowable PHX pressure drop≥5 bar (2% drop)
PHX inlet temperature≤565 °C (150 °C ΔT min)
RequirementValue
Allowable PHX pressure drop≥5 bar (2% drop)
PHX inlet temperature≤565 °C (150 °C ΔT min)

Size, location, and operation of the sCO2 loop were also considered, and an initial set of size and power requirements were established. These requirements are shown in Table 3. The final location of the sCO2 test system is not yet defined. For this reason, the system has been designed as a set of modules including the inventory management system, flow management system, recuperation, and PHX flow conditioning modules. These modules can be disassembled, transported, and reassembled to a new location without requiring any onsite cutting or welding.

Table 3

Supercritical CO2 test system size and power requirements

RequirementValue
Weight≤89,000 N (≤20,000 lbs)
Supply power voltage480 3-Phase Y
Total footprint≤2.7 m × 3.4 m (≤9 ft × 11 ft)
Height≤2.3 m (≤7.5 ft)
RequirementValue
Weight≤89,000 N (≤20,000 lbs)
Supply power voltage480 3-Phase Y
Total footprint≤2.7 m × 3.4 m (≤9 ft × 11 ft)
Height≤2.3 m (≤7.5 ft)

### 2.2 Design.

Several options for the sCO2 loop configuration were considered and are summarized in Table 4.

Table 4

Metrics for different system configurations

ConfigurationCompression power (kW (hp))Total UA (W/K)Heating (MW)Required CO2 (kg)Primary challenge
Liquid blowdown164 (220)38,0004.3300,000CO2 supply
Gas blowdown1342 (1800)01.9300,000CO2 supply
Liquid Brayton5.9 (7.9)160,0003.9ClosedHeat exchange
Gas Brayton43 (58)20000ClosedHigh-temperature compression
Recuperated Brayton10 (14)54,0000ClosedHigh-temperature recuperation
Recuperated and mixed Brayton14 (19)71,0000.2ClosedMixing assembly
ConfigurationCompression power (kW (hp))Total UA (W/K)Heating (MW)Required CO2 (kg)Primary challenge
Liquid blowdown164 (220)38,0004.3300,000CO2 supply
Gas blowdown1342 (1800)01.9300,000CO2 supply
Liquid Brayton5.9 (7.9)160,0003.9ClosedHeat exchange
Gas Brayton43 (58)20000ClosedHigh-temperature compression
Recuperated Brayton10 (14)54,0000ClosedHigh-temperature recuperation
Recuperated and mixed Brayton14 (19)71,0000.2ClosedMixing assembly

Both liquid and gas blowdown open systems are not desirable for implementation because they require a constant supply of CO2, increasing the gas inventory cost and the complexity of the logistics to maintain enough CO2 available. Also, the liquid blowdown system requires an evaporator for cooling; the use of water for cooling is to be avoided to ensure that the test system can be deployed in areas with limited supply of water and ensure that similar systems can be installed in areas where CSP is typically utilized (i.e., water-scarce areas). Another consideration is that the gas-phase Brayton cycle requires further advancement of turbo-compressor technology; this topic is addressed in Sec. 3. A liquid system would allow for the use of pumps. For a liquid sCO2 system, high-pressure, commercially available water pumps can be used by requiring a minimum pump inlet density. Given the technology readiness of water pumps, the decision to use liquid cycles was taken.

The non-recuperated cycles both require significant investment in compression and heat exchanger equipment in addition to the advancement of low technology readiness level (TRL) components. Recuperated cycle layouts leveraging liquid pumping equipment like that shown in Fig. 1 were preferred because they required smaller equipment and the low TRL equipment has already been demonstrated for a 100 kWth-scale system. The recuperated Brayton cycle was chosen as the path to follow for this test system. Note that this is not an actual recuperated Brayton power conversion cycle, but shares the same flow path as this cycle with a pump instead of a compressor and no turbine. The nickel alloy recuperator is coupled with a stainless steel recuperator to reduce the quantity of nickel alloy needed. The Gen3CSP sCO2 loop includes throttle, recirculation, recuperator bypass, and pump speed control. The system was designed using the most conservative conditions expected (i.e., minimum PHX temperature rise, maximum PHX outlet temperature, and maximum PHX outlet pressure) in order to maximize margin for any given operating condition.

Fig. 1
Fig. 1
Close modal

A summary of the fluid states obtained during the analysis of the recuperated cycle is given in Table 5 and Fig. 2. The model (implemented in Engineering Equation Solver (ees)) includes actual pump performance curves, flowmeter pressure drop behavior, throttle valve Cv, and heat exchanger pressure drops assuming quadratic behavior with mass flowrate. The model assumes 2% pressure drop on PHX, 70% isentropic efficiency, and 27 °C ambient temperature.

Fig. 2
Fig. 2
Close modal
Table 5

Supercritical CO2 fluid states

StateT (°C)P (bar)ρ (kg/m3)
156.7243800
257.6259807
3423256190
4565254153
5715250127
6575248147
7147245416
StateT (°C)P (bar)ρ (kg/m3)
156.7243800
257.6259807
3423256190
4565254153
5715250127
6575248147
7147245416

An off-design study of the Gen3CSP loop was also performed in ees to understand the range of test conditions attainable through the combination of recuperator bypass and mass flow control. Intermediate combinations of temperature rise and PHX inlet temperature can be achieved by modulating the flowrate and recuperator bypass flow. A summary of this work is shown in Fig. 3. PHX inlet temperatures as low as 440 °C can be provided while still operating with 1 MWth heat transfer duty and a PHX outlet temperature (or turbine inlet temperature, TIT) of 715 °C.

Fig. 3
Fig. 3
Close modal

### 2.3 Key Component Details.

The definition of four key components was initiated for the recuperated Brayton cycle as it was expected that lead times for manufacturing would be longer. In addition, final specifications for these key components are needed to complete the design of the rest of the system. The four key components are as follows:

1. supercritical carbon dioxide circulator,

2. nickel alloy recuperator,

3. stainless steel recuperator, and

and are described in this section.

#### 2.3.1 Supercritical Carbon Dioxide Circulator.

The sCO2 circulator is the most critical piece of equipment in the Gen3CSP sCO2 coolant loop because of its high cost, long lead-time, and moderate implementation risk. sCO2 compressors with significant commercial experience are typically rated for subcritical pressures in refrigeration applications or designed to operate on low-density fluid for gas pipeline compression applications. Several activities are underway to design compressors specifically for sCO2 applications [710], but no reliable and compact commercial option yet exists.

Instead, high-pressure liquid pumps used for boiler feedwater injection and other high-pressure applications are the most reliable option to use for the sCO2 circulator. Both canned motor and magnetically coupled configurations operate without any rotating shaft seals eliminating the need for a dry gas seal support system and significantly reducing the complexity of operation and amount of leakage from the system. In addition, these configurations rely on bushings lubricated by the process fluid (sCO2) within the rotor cavity or ball bearings for the coupled motor eliminating the need for a lubricating oil support skid.

The maximum pump head rise required can be estimated from various combinations of primary heat exchanger and individual component pressure drop allowances as shown in Fig. 4. For the baseline assumptions of 1.5% PHX and 1% component pressure drops, a pump head rise of approximately 168 m H2O (550 ft H2O) minimum is required. Varying from the baseline assumption for pressure drop allowances requires balancing decreases in component pressure drop with increases in PHX pressure drop depending on achievable pump performance.

Fig. 4
Fig. 4
Close modal

The maximum required pump flowrate can be determined for a range of mass flowrates based on the pump inlet density as shown in Fig. 5. For a baseline requirement of 5.3 kg/s, a pump flowrate of 341 lpm (90 gpm) is required for 950 kg/m3 conditions. This high-density condition is difficult to maintain on hot days using only dry cooling, so it is desirable to reduce the pump inlet density to the lowest value possible. In addition, higher flowrates would potentially provide more capability for the pump, leading to a desire to increase the pump flowrate up to as much as 454 lpm (120 gpm) at low-density conditions.

Fig. 5
Fig. 5
Close modal

For a nominal operating pressure of 250 bar at the primary heat exchanger outlet, the pump outlet pressure could range from 258 bar for the baseline assumption of 1% component pressure drop and 1.5% PHX pressure drop up to 270 bar as shown in Fig. 6. The most likely peak pressure expected is 265 bar (3896 psig) for a PHX allowable pressure drop of 4% (6% pressure drop from the pump outlet to the PHX outlet).

Fig. 6
Fig. 6
Close modal

A seal-less centrifugal pump suitable for the circulation of supercritical carbon dioxide was selected to serve as the fluid circulator. A high-pressure water pump was determined to be a feasible option to use as a commercially available circulator. The pump must be capable of working with sCO2 at a specific gravity of 0.9 or lower and a viscosity of 71 µPa·s (0.071 cP) at a design point of 278 lpm (100 gpm) and a head rise of 259 m (850 ft) at 0.9 specific gravity. Requirements are based on thermodynamics analysis performed on ees.

For material compatibility, only austenitic stainless steels or nickel alloys can be used for wetted surfaces and polymer and elastomer materials should be limited to Nylon, Buna-N, urethane, and polyethylene (high-density polyethylene). Since no water will be present during operation, the bearings must be able to function with sCO2 as lubricant.

The specifications for a canned motor pump that closely meets all requirements pump are listed in Table 6. This pump has a vertical configuration (radial load expected to be minimal) and includes a radial bearing wear monitoring coil with remote indictor to track bearing wear. The pump includes a variable frequency drive (VFD) for motor control.

Table 6

Centrifugal pump technical specifications

RequirementValue
Inlet temperature/°C (°F)37.7 (100)
BEP head/m H2O (ft H2O)259 (850)
BEP flow/lpm (gpm)378 (100)
Max head/m H2O (ft H2O)287 (942)
Max flow/lpm (gpm)689 (182)
MAWP/barg (psig)282.7 (4100)
MDMT/°C (°F)93.3 (200)
Bearing materialGraphite
Weight/N (lbf)20,000 (4500)
Motor size/kW (hp)64.1 (85.9)
Current/A312
Impellor OD/mm260
Number of stages1
Min flow/lpm (gpm)170 (45)
RequirementValue
Inlet temperature/°C (°F)37.7 (100)
BEP head/m H2O (ft H2O)259 (850)
BEP flow/lpm (gpm)378 (100)
Max head/m H2O (ft H2O)287 (942)
Max flow/lpm (gpm)689 (182)
MAWP/barg (psig)282.7 (4100)
MDMT/°C (°F)93.3 (200)
Bearing materialGraphite
Weight/N (lbf)20,000 (4500)
Motor size/kW (hp)64.1 (85.9)
Current/A312
Impellor OD/mm260
Number of stages1
Min flow/lpm (gpm)170 (45)

The system curves for different pressure drops overlaid with the pump curves (vendor provided) for the selected option, and other pumps evaluated are shown in Fig. 7. The canned motor pump can provide the needed flowrate of 354 lpm (93.5 gpm) of CO2 for the 1 MW power system.

Fig. 7
Fig. 7
Close modal

#### 2.3.2 Nickel Alloy Recuperator.

The nickel alloy recuperator is a printed circuit heat exchanger (PCHE) with both hot and cold sides designed for supercritical carbon dioxide. Key requirements and related fluid properties are listed in Table 7. Note that the hot side inlet and outlet temperature corresponds to a PHX outlet temperature of 715 °C and a PHX temperature drop of 150 °C. Given the location within the system, the nickel recuperator is exposed to the highest temperature and pressure within the system as it is the component in the test system closest to the PHX and therefore must be constructed from nickel alloys to avoid excessive corrosion even in a short time as discussed later. During operation, the recuperator will be insulated to maintain a thermal efficiency of 95% or above (i.e., maximum allowed loss of 50 kWth). The overall heat transfer coefficient-area product (UA) has been approximated to be 6630 W/K.

Table 7

Key parameters of the nickel recuperator

Value
RequirementCold sideHot side
Fluid flowrate (kg/s)5.255.25
Temperature (in/out) (°C)413565715565
Pressure (in) (MPa)25.725.0
Density (in/out) (kg/m3)194153127149
Viscosity (µPa · s)34.738.642.638.5
Value
RequirementCold sideHot side
Fluid flowrate (kg/s)5.255.25
Temperature (in/out) (°C)413565715565
Pressure (in) (MPa)25.725.0
Density (in/out) (kg/m3)194153127149
Viscosity (µPa · s)34.738.642.638.5

The nickel alloys considered for construction were unified numbering system (UNS) N08810, UNS N06625, UNS N06617, UNS N06230, and UNS N07740. The material selected was UNS N06625 as a suitable diffusion bonding procedure had been developed in a previous project. Diffusion bonding procedures for the other alloys are also underway but are not expected to be completed in time for this system.

#### 2.3.3 Stainless Steel Recuperator.

The stainless steel recuperator is a PCHE with both hot and cold sides designed for supercritical carbon dioxide. Key requirements and related fluid properties are listed in Table 8. The temperature drop across the stainless steel recuperator is more dramatic since it interfaces with the nickel recuperator and the pump. Since the pump can only handle sCO2 close to density conditions near to those of water, the stainless steel recuperator must have a much higher heat transfer coefficient (approximated as UA = 26,900 W/K) to handle such different densities.

Table 8

Key parameters of the stainless steel recuperator

Value
RequirementCold sideHot side
Fluid flowrate (kg/s)5.255.25
Temperature (in/out) (°C)37413565123
Pressure (in) (MPa)26.024.8
Density (in/out) (kg/m3)900194149487
Viscosity (µPa · s)91.334.738.538.7
Value
RequirementCold sideHot side
Fluid flowrate (kg/s)5.255.25
Temperature (in/out) (°C)37413565123
Pressure (in) (MPa)26.024.8
Density (in/out) (kg/m3)900194149487
Viscosity (µPa · s)91.334.738.538.7

Also, the nickel recuperator size was to be minimized to decrease the amount of nickel alloy needed, hence reducing the cost of the recuperation subsystem. During operation, the recuperator will be insulated to maintain a thermal efficiency of 95% or above (i.e., maximum allowed loss of 150 kWth).

A 1 MWth cooler/radiator is used as the heat sink to support the full duty of the test system need. For this heat exchanger, the hot side is designed for carbon dioxide and the cold side for ambient air. Key requirements and parameters for the radiator are listed in Table 9. The temperature range needed for the radiator allows for use of stainless steel to minimize the cost of the exchanger. Finally, the calculated “UA” is approximately 27,600 W/K.

Table 9

Value
RequirementHot side (CO2)Cold side (air)
Fluid flowrate (kg/s)5.2535 (62,000 cfm)
Temperature (in/out) (°C)145533867
Pressure (in) (MPa)24.5Ambient
Density (in/out) (kg/m3)4208141.21.0
Viscosity (µPa · s)35742729
Value
RequirementHot side (CO2)Cold side (air)
Fluid flowrate (kg/s)5.2535 (62,000 cfm)
Temperature (in/out) (°C)145533867
Pressure (in) (MPa)24.5Ambient
Density (in/out) (kg/m3)4208141.21.0
Viscosity (µPa · s)35742729

### 2.4 Minor Component Details.

Other important considerations for the design of the Gen3CSP and that are described in this section.

#### 2.4.1 Inventory Management.

The Gen3CSP sCO2 loop will require an inventory control system to provide for filling, pressurization, venting, and inventory recovery. The baseline design for this system is shown in Fig. 8 to leverage commercially available two-phase CO2 dewars, ambient temperature vaporizers, CO2 compression equipment, and remote-actuated regulators and valves for automation. The dewar tanks require only intermittent filling with liquid CO2 and power for minor electrical loads and does not rely on facility compressed air or significant electrical power for vaporization or compression.

Fig. 8
Fig. 8
Close modal

#### 2.4.2 Piping.

Corrosion and high-temperature operation considerations are important to ensure the piping compatibility. Walker et al. [11] compared corrosion rates for several alloys operating in high temperature and pressure sCO2 environments across a range of studies. Based on these results from sample weight gain measurements, stainless steel alloys are expected to have low corrosion rates up to 550 °C and moderate rates up to 600 °C, but will likely have excessive corrosion rates above 600 °C. High nickel alloys, however, appear to have low corrosion rates up to at least 700 °C. Precise corrosion allowance guidance would require sample thickness reduction measurements which are not yet available for sCO2 environments, so these general expectations for corrosion were used with industrial guidance for corrosion allowances ranging from 0 to 2.54 mm (0–0.1 in.) with a value of 0 used for materials with low expected rates of corrosion, 1.27 mm for moderate rates, and 2.54 mm for high corrosion rates given the relatively short operating life of the Gen3CSP system.

The pipe strength was evaluated using Eq. (1) per ASME B31.1 requirements where P is the internal pressure, S is the maximum allowable stress, E is the weld joint efficiency factor, OD is the pipe outer diameter, t is the pipe wall thickness, y is a coefficient based on material and temperature read from tables in the B31.1 piping code, and A is the corrosion allowance. A value of 0.4 was used for the y parameter in Eq. (1) based on the expected temperatures observed for the alloys considered (nickel and austenitic steels):
$PS=2E(t−A)OD−2y(t−A)=2(1)(t−A)OD−2(0.4)(t−A)$
(1)

The pressure containment ratio more intuitively captures the sharp transition for each material from allowable stress ratings based on yield stress at lower temperatures to those based on creep limits and can be directly compared with the geometric strength ratio. Figure 9 shows P/S ratios at different temperatures based on maximum allowed stress for different materials. Most stainless steels and N06625 quickly lose strength or are not allowed above 537 or 593 °C (1000 or 1100 °F) with pressure containment ratios ranging from 0.15 to 0.4 across several materials. N07740 and N06617 are the only viable code-approved options for significantly higher temperatures with pressure containment ratios around 0.28 for N07740 and 0.48 for N06617 at 735 °C (1355 °F).

Fig. 9
Fig. 9
Close modal

Based on the information for the pressure containment ratio presented above, and the pressure containment ratio for different pipe sizes and thicknesses, Table 10 lists pipe schedule sizes that can perform at the high pressures and temperatures required for the Gen3CSP loop. N07740 and N06617 are the only viable B31.1 material options for temperatures above 593 °C (1100 °F), while numerous options are available for temperatures below 315 °C (600 °F) including most common austenitic stainless steels. For temperatures between 315 and 593 °C (600 °F and 1100 °F), N06625, N08800, and S34709 are the most viable options.

Table 10

Pipe size and schedule of different alloys for use in the Gen3CSP loop

Material/MAWP/MDMT/P/SSCHMaximum nominal pipe size
UNSbar°CA = 0 mm (A = 0 in.)A = 1.3 mm (A = 0.05 in.)A = 2.5 mm (A = 0.1 in.)
N077402807350.27Various3.5 SCH160≥6 SCHXXS4 SCHXXS
N066172807260.45XXS32.5NA
N066252805900.21Various≥6 SCH160≥6 SCH160≥6 SCHXXS
N088002805900.32XXS433
S347092805900.31XXS443
S347002803150.28XXS654
S316002803150.32XXS433
S304002803150.33XXS432.5
Material/MAWP/MDMT/P/SSCHMaximum nominal pipe size
UNSbar°CA = 0 mm (A = 0 in.)A = 1.3 mm (A = 0.05 in.)A = 2.5 mm (A = 0.1 in.)
N077402807350.27Various3.5 SCH160≥6 SCHXXS4 SCHXXS
N066172807260.45XXS32.5NA
N066252805900.21Various≥6 SCH160≥6 SCH160≥6 SCHXXS
N088002805900.32XXS433
S347092805900.31XXS443
S347002803150.28XXS654
S316002803150.32XXS433
S304002803150.33XXS432.5

Another important consideration for piping design is the minimum pipe size to limit pressure drop. Assuming a total pressure drop limitation of 0.1% and allowing the high-temperature piping greater pressure drop due to the limited selection of pipe sizes expected the pressure drop per foot of straight pipe must range from 0.005 bar/m (0.02 psi/ft) on the cold end to 0.02 bar/m (0.1 psi/ft) on the hot end of the system. This metric is trivial to meet for straight pipe even at the smallest expected pipe sizes of 2 nominal pipe size (NPS) SCHXXS, but the loss for even a small number of pipe fittings could quickly exceed the relatively low target of 0.31 bard (4.5 psid) pressure drop total in the piping for small pipe sizes.

An analysis was performed with the preliminary piping layout as shown in Fig. 10 and summarized in Table 11. This minimum sizing yields average cross-sectional flow velocities ranging from 1 to 17 m/s depending on the flow temperature which is roughly in line with conventional guidelines of 1–2 m/s for liquids and 10–30 m/s for gasses as the density of sCO2 transitions from liquid-like to gas-like over this temperature range.

Fig. 10
Fig. 10
Close modal
Table 11

Fittings and flow resistance for operation of the Gen3CSP loop

PipingAbove 593.3 °C (1100 °F)Between 593.3 °C and 315.5 °CBelow 315.5 °C (600 °F)
Elbows114
Run tees022
U-bends000
Allowable pressure drop/kPa (psi)5.5 (0.8)10 (1.5)14 (2.0)
Minimum pipe size3 NPS SCHXXS3 NPS SCHXXS3 NPS SCHXXS
Flow velocity (m/s)14–179–142–9
PipingAbove 593.3 °C (1100 °F)Between 593.3 °C and 315.5 °CBelow 315.5 °C (600 °F)
Elbows114
Run tees022
U-bends000
Allowable pressure drop/kPa (psi)5.5 (0.8)10 (1.5)14 (2.0)
Minimum pipe size3 NPS SCHXXS3 NPS SCHXXS3 NPS SCHXXS
Flow velocity (m/s)14–179–142–9

#### 2.4.3 Non-Welded Connections.

Clamp connections are used for all piping at any temperature and pressure required. Conventional components are only rated to 537.7 °C (1000 °F), but higher temperature and pressure ratings are available on request. Several different seal ring sizes from 1 to 6, equivalent to 1 NPS to 6 NPS pipe, are available up to 537.7 °C in standard 316 and 304 grades of stainless steel at both 281.7 and 298.2 barg (4085 and 4325 psig). Vendors recommend the use of high carbon grades or “H-grades” of austenitic stainless steels or nickel alloys for hubs, blinds, and clamps for process temperatures above 537.7 °C where the hubs, blinds, and clamps are fully insulated together with the process piping. In addition, silver-coated UNS N07718 or another suitable seal ring material must be used in order to aid in sealing, prevent seizing of the hub material at high temperatures, and provide sufficient seal rigidity at high temperature.

For uninsulated connections, the clamp material is generally assumed to be at a temperature below 80% of the process temperature, allowing the use of standard 304 or 316 materials up to 676.6 °C (1250 °F). In addition, clamp connections are rated under the ASME code for long-term service such that the short term operation at higher temperatures will likely not cause acute or permanent damage to the joint. The expected failure mode of clamps at higher temperatures is eventual fatigue cracking, but this has not been seen in practical service according to vendor representatives. Threaded connections were not considered because no satisfactory thread sealant material has been found for long-term service in sCO2 at elevated temperatures and threaded connections larger than 1/2; NPS are not allowed under B31.1 piping code.

Inspection ports and instrumentation feedthroughs will be required throughout the system to assess fluid conditions, inspect for corrosion, wear, and contamination, and to provide flexibility to change out connections over time. Due to the small pipe diameters used for this system, standard thermowells are often not available or cannot meet the temperature requirements of a given location and custom thermowells must be designed. Clamp or ferrule connections are utilized for inspection ports depending on their size with ferrule connections limited to temperatures below 537.7 °C (1000 °F) after accounting for thermal standoff effects. Gland-based feedthroughs are used for instrumentation where welded thermowells are not practical. Several sizes provide sufficient pressure ratings with feedthrough ports ranging from 1/8 NPS to 3/8 NPS.

### 2.5 Implementation and Modularity.

The Gen3CSP sCO2 loop is currently being designed as a modular system to provide additional layout options to the teams currently developing the rest of the CSP system and to ease in transportation once final location for the system is selected. Given the size of the components (based on initial size estimates and experience with previous similar systems) and the function they serve, the loop is split into four modules as shown in Figs. 10 and 11.

Fig. 11
Fig. 11
Close modal

## 3 Conclusion

This work summarizes the design of a 1 MWth-scale sCO2 test system to provide up to 5.3 kg/s of sCO2 flow to the primary heat exchanger of any Gen3CSP thermal storage system operating at pressures up to 250 bar and temperatures up to 715 °C. This system is critical to validate design expectations for performance, lifetime, and operability of a CSP PHX with full or near-full scale modules to de-risk their application in commercial plants. A set of high-level requirements based on conservative numbers have been established to ensure delivery of a suitable system, while the potential to accommodate various PHX temperature rises, power levels, and alternative system components has been designed in from the beginning. Finally, the use of ASME codes and standards for design lifetime and reasonable allowances for corrosion provides confidence that this system can be leveraged for future testing after the Gen3CSP program to demonstrate a complete, integrating CSP pilot facility.

## Acknowledgment

Sandia National Laboratories is a multimission laboratory managed and operated by National Technology & Engineering Solutions of Sandia, LLC, a wholly owned subsidiary of Honeywell International Inc., for the U.S. Department of Energy's National Nuclear Security Administration under contract DE-NA0003525. This paper describes objective technical results and analysis. Any subjective views or opinions that might be expressed in the paper do not necessarily represent the views of the U.S. Department of Energy or the United States Government. SAND2020-13464 J.

## Conflict of Interest

There are no conflicts of interest.

## Funding Data

• U.S. Department of Energy Solar Energy Technologies Office under Award No. DE-EE0001697 34151.

## Nomenclature

• y =

coefficient accounting for temperature

•
• A =

corrosion allowance

•
• E =

weld joint efficiency factor

•
• P =

pressure

•
• S =

maximum allowable stress

•
• T =

pipe wall thickness

•
• OD =

outer diameter

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