Modelling and Simulation of Claus Furnace by Optimizing Basic Two Claus Reactions for Analysis of Percentage of Sulphur Recovery

DOI : 10.17577/IJERTV11IS060245

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Modelling and Simulation of Claus Furnace by Optimizing Basic Two Claus Reactions for Analysis of Percentage of Sulphur Recovery

Jigyasa Kumar1 , Dr. Manoj Srivastava2, Dipika3

University Of Allahabad, Prayagraj, India

Abstract:- Sulphur-bearing compounds are extremely detrimental to the environment and to the industrial process equipments. Sulphur containing compounds are usually found in oil and natural gas deposits and, in some mineral rocks. Sulphur containing hydrogen sulphide, occur in crude petroleum, but 90% of it is found in natural gas. Hydrogen sulphide (H2S) and sulphur dioxide (SO2) are the two sulphur containing compounds that needs special attention. Hydrogen sulphide is a highly corrosive gas, and sulphur dioxide is also toxic both for environment and industrial equipments.

Recovery of elemental sulphur from acid gas, during sour natural gas processing and refinery upgrading, is carried out using different processes. The Claus process is the most efficient and popular process employed worldwide for converting toxic hydrogen sulphide to sulphur in the hydrocarbon processing industries. The Claus process can be operated for higher hydrogen sulphide concentration and feed capacities, and has higher H2S conversion with respect to other processes. Maximum conversion of hydrogen sulphide to elemental sulphur takes place in Claus furnace and remaining H2S is converted by using catalytic converters.

The objective of this work is to design Claus Furnace and to achieve maximum recovery of sulphur by using only the basic two Claus reactions. The other several side reactions have been neglected in this work. The aim is to model a furnace which can recover maximum sulphur percentage by using only the main Claus reactions. Modelling of equations were done using Runge Kutta fourth order method for simultaneous differential equations. Simulation part is done using MATLAB.

Result obtained shows a feasible model which results in 47% conversion of hydrogen sulphide to sulphur by utilizing only the two Claus reactions, which is comparable with other models that are designed using several hundreds of side reactions taking place in the furnace.

Keywords : Hydrogen sulphide, Sulphur, H2S, SO2, Claus, furnace, reactor.

INTRODUCTION

Sulphur is used in various industries, major consumer being the fertilizer industry. Sulphur bearing compounds especially hydrogen sulphide and sulphur dioxide are highly corrosive in nature and thus needs special attention. Small amounts of hydrogen sulphide occur in crude petroleum, but 90% of it is found in natural gas. The refinery feedstock contains wide range off. Hydrogen sulphide is both an irritant and a chemical asphyxiant. H2S gas level at or above 100ppm is extremely dangerous to life and health. It is flammable and extremely hazardous gas. It is dangerous to equipments too in the presence of moisture. The damage can lead to pitting and step-wise cracking. Burning of H2S gives off sulphur dioxide which is toxic in nature. Thus sulphur needs to be recovered from refineries for the safety aspects of human being as well as instruments

There are various methods of reducing pollutants containing sulphur, but the most prevalent method is Claus process. The Claus process has been well known and used in industry for over 100 years. The Claus process is applicable for feeds with H2S composition greater than 30 mole % (in dry basis) and especially in large scale units with sulphur production greater than 2 tons/day [4]. For the sulphur recovery process, the main focus is on the Claus catalytic conversion reactor, but some studies have identified the Claus furnace as one of the most important part of this process. In the furnace the combustion reaction and initial sulphur conversion (through endothermic reaction) takes place.

  • ACID GAS BYPASS : Bypassing a portion of the feed around the furnace results in insufficient combustibles in a lean acid gas feed.. The bypassed gas is mixed with the burner effluent prior to the waste heat boiler. At temperature below 1200°F, SO2 and H2S will not react to form elemental sulphur without a suitable catalyst [1].

  • AMINE EXTRACTION: Gas containing H2S is passed through an absorber containing an amine solution (Monoethanolamine(MEA)), where the hydrogen sulphide is absorbed along with carbon dioxide. A typical amine gas treating process includes an absorber unit and a regenerator unit as well as accessory equipment.

    The traditional Claus process has been a reliable and relatively efficient way of removing H2S from the fuel gas and converting it into elemental sulphur. The first step is the thermal stage, where one-third of the H2S is oxidized, producing H2S and SO2 in a 2:1 ratio. This process is carried out in a reaction furnace at high temperature. Some sulphur is formed but the remaining unreacted H2S proceeds to the next step i.e. catalytic step. In catalytic stage the remaining H2S is reacted with the SO2 formed in the thermal stage at lower temperatures over a catalyst bed to make over sulphur. Two to four catalytic stages are needed to obtain 94 to 98% conversion [21]. The reactions are:

    3

    The thermal reaction furnace is the most important element. Oxidation of one-third of hydrogen sulphide to sulphur dioxide using air is done in the thermal furnace. Temperatures are usually in order of 1000 – 1400°C [15]. The oxidizing reaction is exothermic in nature and without any thermodynamic restriction.

    Fig1 : Schematic representation of Claus Process[23]

    Two-third of the unreacted hydrogen sulphide reacts with sulphur dioxide to produce elemental sulphur through the so-called Claus reaction:

    The off-gas leaving the furnace enters the waste heat boiler, where it is quenched to about 300°C, so as to prevent recombination reactions. The first separation of liquid elemental sulphur is carried out in the first condenser [17]. The hydrogen sulphide conversion goes on in the catalytic region, where further separation is carried out resulting in 99% recovery of sulphur. It is the main part of the sulphur recovery unit. Reaction furnace has two primal targets. First: Burning 1/3 of existent H2S in feed and product SO2 for Claus equilibrium process, catalytic process and preparation H2S / SO2 = 2/1 relation for doing Claus equilibrium process with predicting conversion. Second: Destruction and burning any type of component that may damage the downstream equipments operation.

    Claus furnace plays an important role in the unit. Many other factors are dependent on the performance of the furnace, from process efficiency to other equipment operations [22].

    MODELLING & SIMULATION

    A mathematical model is developed for the furnace used in Claus process for sulphur recovery. Claus furnace can be modelled using a non-ideal reactor, so the furnace can be represented by a plug flow reactor. There are multiple reactions taking place simultaneously in the furnace. In this work maximum amount of available kinetics has been used, but to avoid complexity, free radicals and complex reactions have been ignored.

    ASSUMPTIONS

    Following assumptions have been taken to model the Claus furnace:

  • Reynolds number is greater than 2100, so plug flow pattern is considered.

  • Prandtl number is much greater than1, radial diffusion of mass and energy is negligible.

  • Axial dispersion is negligible compared to mass transfer by convection in axial direction.

  • Due to low pressure and high temperature condition, the gas mixture is an ideal gas.

MODELLING

The funace is considered to be an adiabatic plug flow reactor. Reactor length is broken into small elements, and mass and energy balances are written for each element.

F(mol/sec) yi,out

yi Ac(m2)

z

T(K)

Figure 2: Differential element of plug flow reactor

Consider a small element of the plug flow reactor, of length 0.5 m. Mass balance for each component and energy balance are formed.

Here, F is the molar flow rate of feed yi – is the mole fraction of feed

yi,out – is the mole fraction of outlet stream z – is the length of the elemental section

Ac – is the cross- sectional area of the element and T is temperature in Kelvin scale.

The equations are solved using Runge Kutta fourth order method for simultaneous differential equations.

MASS BALANCE

(-F/A) * (dyi / dz) + i N (ri )= 0

=1

Mass balance along the axial direction in a differential element of the reactor for i component: here N= 5

ENERGY BALANCE

Energy balance along the axial direction in the differential element of the reactor:

(-F/A) * Cp*(dT/dz) + i =1N (ri )*(-Hf,i) = 0

CHEMICAL REACTIONS

There are many reactions taking place in the furnace. But, it is difficult to consider all the reactions. Nearly 1500 reactions, take place in the Claus furnace with about 150 molecules and radicals. To avoid complexity only the main reactions have been considered in this work neglecting free radicals and complex reactions. The reactions with their respective rate kinetics have been extracted from the references [18, 19, 22].

Claus reactions in the thermal section:

H2S + 1.5 O2 SO2 + H2O …. (1)

H2S+ 0.5SO2 3/2 S2 + H2O …..(2)

RATE KINETICS FOR THE TWO REACTIONS

O2

(-rH2S, 1) = 14*106*e-(11/RT)*H2S* 1.5

(-rH2S, 2) = 107* e-(10.6/RT)* H2S*SO20.5 0.5*106* e-(5.1/RT)* H2S* S2

Initially the feed containing acid gas stream and air is supplied from an external source. The feed consists mainly of hydrogen sulphide gas, water vapour. On entering the furnace, reactions take place and sulphur dioxide is formed, further from which elemental sulphur is extracted out in form of S2 liquid. The initial conditions of the input stream are as follows:

Table 1: Initial feed conditions

Feed stream

Stream Composition

Air Composition

Temperature(K)

640

210

F(mol/s)

200

200

Pressure (atm) 0.1747

Feed

Mole Fraction

H2S

0.45

—-

H2O

0.08

0.037

O2

—-

0.21

SO2

0

—–

S2

0

—-

N2

—-

0.753

CO2

0.4699

NH3

0.0001

Table 2: Initial feed conditions on N2, CO2, NH3 free basis

Feed stream

Stream Composition

T(K)

850

Feed

Mole Fraction

H2S

0.5828

H2O

0.1451

O2

0.2719

SO2

0

S2

0

N2

0.379

CO2

0.2249

NH3

0.00005

The above table shows the feed contents taking N2, CO2 and NH3 on free basis. These components are present in the input feed.

RESULT AND DISCUSSION

The main objective of this work is to attain sulphur recovery from sulphur containing compounds. The focus is on the variation in sulphur compounds i.e. mole fraction of S2 and SO2 at the outlet stream.

Initially the temperature taken is 850K. By burning combustible substances in the beginning, temperature rises to 1500K. Then, the temperature starts decreasing and after reaching 750K it nearly becomes constant. The exothermic reaction and the increasing temperature provide suitable condition for other reactions to occur. The ratio H2S/SO2 starts decreasing as sulphur dioxide is formed and finally 2.29 ratio is reached.

The thermal section gives nearly 40% to 60% sulphur at outlet. For 90% recovery catalytic reactors should be added. Since, only two main reactions are considered in this work, all the side reactions have been neglected so the 40% recovery is optimum, that suggests that on considering all the side reactions recovery will reach to 90~95% as the other reactions are supporting reactions that will enhance sulphur recovery.

The table shown below gives a comparative chart of both input feed and the output stream values for each component.

Table 3: Output feed stream

Feed Composition

Input Feed stream

Output Feed stream

T(K)

850

879.5191

H2S(mole fraction)

0.5828

0.1133

H2O

0.1451

0.2266

O2

0.2719

0.1752

SO2

0

0.0493

S2

0

0.4695

Table 3 gives a comparative chart of the input and output feed stream. H2S concentration decreased from 0.528 to 0.1133 which shows its consumption and thus formation of SO2. Temperature initially increased to 1400K, as SO2 starts forming, and finally temperature of the outlet stream was 879.5K.

Figure 2 represents the variation of temperature with the mole fraction of S2. It is the desired product and its final recovery is 47% that is comparable with that of plant.

Figure 2: Temperature profile against mole fraction of S2

Figure 3 represents the temperature profile with respect to SO2. Initially as the input feed enters the furnace temperature starts increasing and SO2 starts forming, so its value keeps on increasing at the desired ratio SO2 becomes 0.0493.

Figure 3: Temperature profile against SO2

The temperature v/s H2S plot represents the variation of temperature with the H2S concentration. Initially the temperature taken at 850 K, increases to 1200 K and then to 1509 K, since the reactions are exothermic in nature. On increasing the length of the reactor temperature starts decreasing and concentration of H2S also starts dropping to lower concentration as it is getting consumed.

Figure 4: H2S profile against temperature

CONCLUSION & RECOMMENDATION

In this work modelling and simulation of Claus Furnace was performed using a kinetic model. There is a slight deviation in values, since this work consists of only two main reactions and not the other reactions. The aim was to first study the nature of temperature and, the nature of ratio decrement with respect to temperature and sulphur recovery which can result in maximum recovery of sulphur. Secondly, to avoid complexity, while the works [18, 19 , 22,21] includes 12 to 15 reactions.

Effect of furnace outlet temperature to inlet temperature, fuel concentrations at outlet, H2S/SO2 ratio, sulphur recovery, H2S consumption were investigated in this work. Maximizing sulphur recovery was the main aim of this work, and H2S/SO2 ratio parameter should be as close to 2 for better performance. The equations were solved using Runge Kutta method for simultaneous differential equations. Sulphur was recovered to 0.4695 mole

fraction frm zero, that is 47% that suggests that on considering all the other side reactions recovery will reach to 90~95% as the other reactions are supporting reactions.

Thus, the Claus furnace is a good candidate for increasing sulphur recovery and to eliminate contaminant emission.

Recommendations that can be given after this work are: Firstly, if only few more reactions are taken into account it would decrease the furnace length, since furnace length should also be as small as possible taking cost into account, and if few other reactions are taken into consideration, then ratio of H2S/SO2 could be reached earlier, with higher percentage of sulphur recovery in thermal stage.

The model thus obtained gives 47% sulphur recovery. Hence it is proved, that only Claus reactions are sufficient to eliminate sulphur, but since refineries have thousand tons of feed stream containing H2S.Origin of these streams are from different process reactors, so they usually contain many different species and radicals, which while reacting in the Claus furnace results in different complex reactions. These radicals finally have to be taken into account for elimination process and maximum sulphur recovery.

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