# Mitigate elemental sulfur condensation in a compressor knockout drum

Produced natural gas must be compressed for export and further processing on the main processing platform. When sour gas (i.e., gas containing H_{2}S) is compressed, the compressor discharge gas is used as a seal gas that is routed to the inlet of the first stage of the compressor.

The bleed of sour gas being used as seal gas from higher pressure to lower pressure causes the formation of elemental monoclinic sulfur (S_{8}) (as a gas) by the condensation of H_{2}S gas. Monoclinic sulfur (melting point = 119°C and density = 1,980 kg/m^{3}) is stable between 96°C and 119°C. It is insoluble in water but soluble in carbon disulfide (CS_{2}). Monoclinic sulfur, also called prismatic sulfur, has S_{8} ring molecules in the crystalline structure. Monoclinic sulfur transforms to rhombic octahedral crystal sulfur (melting point = 112°C and density = 2,060 kg/m^{3}) below 96°C.

The S_{8} is routed to the suction knockout drum (KOD) of the first stage of the compressor, which can cause choking of the suction KOD and, consequently, disruption of the normal compressor operation. This article provides the concept and calculations for S_{8} formation and quantification, as well as methods for the mitigation of S_{8}.

**Introduction.** In sour gas compression, the purpose is to keep the sour gas in a gaseous state (**FIG. 1**). The operating pressure and temperature throughout the compression process should be such that it should fall below the monoclinic sulfur sublimation curve and right of the rhombic sulfur sublimation curve. The blue region in **FIG. 1** is the expected operating envelope. S_{8} does not form, and the sour gas remains in a gaseous state.

FIG. 1. Sulfur phase diagram. |

Based on the reaction kinematics and the stoichiometric equation of H_{2}S formation from its basic elements, H_{2} and S_{8}, the change in free energy of forward formation (Eqs. 1–3) can be calculated:

(1)

(2)

(3)

From the change in the free energy Arrhenius equation, the equilibrium constant (K_{eq}) for the forward reaction can be calculated. Once the K_{eq} value is known, the partial pressure of S_{8} at the compressor discharge pressure can be determined.

Knowing the equation for determining the compressor discharge temperature by adiabatic compression, the sulfur phase diagram can be used to determine the operating location and state of sulfur. Similarly, for the reverse reaction, K_{eq} can be calculated, along with the partial pressure of S_{8} at the compressor suction pressure and the bleed outlet temperature. (**Note:** The change in free energy will be constant; therefore, the free energy change calculated in the forward reaction can be used with the opposite sign in the reverse reaction K_{eq} calculation.) The outlet temperature may be lower than the compressor suction temperature, and it can be determined by the adiabatic expansion process. Based on the S_{8} partial pressure and temperature, the state of the S_{8} on the sulfur phase diagram can be checked.

Once the state of the sulfur is known, it can be determined if the sulfur is condensed to liquid and consequently a solid state, and if the temperature is below the melting point. Then, using the partial pressure equation, the mass rate of sulfur condensed into liquid/solid can be calculated.

**Calculation basis and assumptions.** The calculation basis and assumptions are as follows:

- Gas expansion though the bleed is an adiabatic process
- Hydrocarbon fuel gas molecular weight is 35
- Two-stage compression process is present
- The change in free energy for the forward reaction is equal to the change in free energy for the reverse reaction with the opposite sign
- First-stage compressor suction pressure is 100 bar, and temperature is 50°C
- First-stage discharge pressure is 250 bar, and temperature can be calculated with the adiabatic process gas equation (for this calculation, 65°C is assumed)
- Second-stage required discharge pressure is 500 bar, and temperature can be calculated with the adiabatic process gas equation (for this calculation, 100°C is assumed)
- Bleed gas is considered from the second-stage discharge, and flowrate is 1,000 kg/hr
- Bleed gas outlet pressure is equal to the first-stage suction pressure, which is 100 bar
- Bleed gas temperature can be calculated with the adiabatic expansion gas equation (for this calculation, 50°C is assumed)
- Heat capacity ratio of the hydrocarbon gas mixture is 1.4 and is assumed to be constant
- The compressibility factor of the gas is considered to be 1, for the sake of simplicity
- H
_{2}S in the compressor suction inlet gas is 50 ppm; therefore, 50 ÷ 10,000 = 0.005 mol% = 0.00005 mole fraction.

Compressor discharge temperature is based on adiabatic compression. If f suction (1) and discharge (2) are known, then Eq. 4 can be used to calculate compressor discharge temperature:

(4)

Then, S_{8} partial pressure in the forward reaction at compressor discharge pressure and temperature can be calculated, using Eqs. 5–15:

(5)

(6)

(7)

(8)

∆G^{0} = –267,200 J/mole (9)

∆G^{0} = –(R × T)ln(K_{eq}) (10)

–267,200 = –(8.314 × (273 + 100)ln(K_{eq}) (11)

86.162 = ln(K_{eq}) (12)

K_{eq} = (2.629) × 10^{37 } (13)

(14)

(15)

From the forward balance equation stoichiometry, partial pressure of H_{2} = partial pressure of S_{8}^{8}, as shown in Eqs. 16–17:

p_{H}_{2} = 8p_{s}_{8} (16)

(17)

Alternatively, see Eqs. 18–21:

(18)

(19)

(20)

(21)

From these results, it can be ascertained that the state from the sulfur phase diagram at p_{s}_{8} = (8.8521) × 10^{–5} bar and 100°C is below the S_{8} sublimation curve. S_{8} partial pressure in the reverse reaction at compressor suction pressure and bleed temperature can be calculated, using Eq. 22–27:

(22)

–267,200 = –[8.314 × (273 + 50) ln(K_{eq})] (23)

104.34 = ln(K_{eq}) (24)

K_{eq} = (2.0619) × 10^{45} (25)

(26)

(27)

From the forward balance equation stoichiometry, partial pressure of H_{2} = partial pressure of S_{8}^{8}, as shown in Eqs. 28–29:

p_{H}_{2} = 8p_{s}_{8} (28)

(29)

Alternatively, see Eqs. 30–33:

(30)

(31)

p_{H}_{2} = 0.00005 × 100 = 0.005 bar (32)

(33)

From these results, it can be ascertained that the state from the sulfur phase diagram at p_{s}_{8} = 0.04187 bar and 50°C is above the rhombic S_{8} sublimation curve. It means that H_{2}S will condense into the compressor suction KOD in the form of rhombic S_{8}, which will cause compressor damage.

S_{8} condensation into liquid/solid in the compressor suction KOD can be quantified, using Eqs. 34–36:

p_{s}_{8} (S_{8} partial pressure) = S_{8} mole fraction × Total pressure (34)

0.04187 bar = S_{8} mole fraction × 100 bar (35)

S_{8} mole fraction = 0.0004187 (36)

If the total number of moles = 1, then condensed rhombic S_{8} moles = 0.0004187. Total assumed bleed gas flowrate = 1,000 kg/hr = 1,000 ÷ 35 = 28.571 kg moles/hr. This means condensed rhombic S_{8} = 28.571 × 0.0004187 = 0.01196 kg/hr. In 24 hr, 0.01196 × 24 = 0.2871 kg rhombic S_{8} will form in the suction KOD.

**Mitigation options.** Any proposed mitigation should reduce the equilibrium constant K value. The K value can be reduced by increasing the temperature of the bleed stream and reducing the partial pressure of H_{2}S in the gas stream. In this experiment, the temperature was increased by electrical heating of the bleed gas pipe. However, the partial pressure of the H_{2}S could not be reduced below the suction pressure of the first stage.

In conclusion, the results show that bleed stream pressure cannot be reduced below the compressor's first-stage suction pressure. However, the compressor suction hydrocarbon gas stream can be diluted to reduce the mole fraction of H_{2}S. The second option increases the bleed gas temperature by electrical heating to the temperature of the suction hydrocarbon gas. With these optimizations, the sulfur problem can be solved. **GP**

**LOKESH KUMAR SINGH** is a Senior Process Engineer based in Abu Dhabi. He is also an independent researcher and a Chartered Member of the IChemE UK Council since 2014. He has extensive experience in process simulation and modeling for steady state and transient studies, and is conducting research and development work in the fields of mathematical modeling and computation simulation. Mr. Singh is working to develop mathematical models and equations to solve critical engineering problems. He is also working to develop a water network hydraulic study and surge pressure analysis simulation software, using his own mathematical modeling. He holds a BEng degree in chemical engineering.

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