Modeling and Optimization of Product Profiles in Biomass Pyrolysis

Abstract

Biomass feed comes in many varieties, but have common chief constituents of hemicellulose, cellulose, and lignin. As the relative proportions of these constituents may vary, customization of the pyrolysis process conditions is required to produce a desired product profile. By recognizing the sources of variation, the reactor settings may be intelligently controlled, to achieve optimal operation. These considerations include biomass classification, feed rate, moisture content, particle size, and inter-particle thermal gradients (which arise during pyrolysis based on heating rate and temperature distribution). This chapter addresses the optimization of product profiles during biomass pyrolysis from a modeling perspective. Fundamental models for packed bed and fluidized bed pyrolyzers are developed, using kinetics from existing literature. The proposed optimization approach (inclusive of the kinetic and process models) can guide practical achievement of desired product profiles of the biomass pyrolysis process.

1. Introduction

The chief constituents of any biomass are hemicellulose, cellulose, lignin and inerts [1]. The amounts of the chief constituents of various biomasses along with the elemental compositions are presented in Table 1. Generally, pyrolysis is a process where biomass or other carbonaceous material is heated in the absence of air supply or in the presence of inert gas supply such as nitrogen. During the biomass pyrolysis, the bonds between high molecular compounds are broken and low molecular weight compounds are formed. The range of pyrolysis products are gases, liquids, char, and ash. The ash is the inert material present in biomass. The fractions of these products depend on composition of biomass and process conditions such as heating rate, biomass feed rate, particle size, moisture content, and the rate of heat transfer. The rate of heat transfer depends greatly on mixing conditions in the pyrolyzers.

Type of biomass	Biomass constituents			Elemental composition					Ref.#
	HEMI* (%)	CEL* (%)	LIG* (%)	C (%)	H (%)	N (%)	S (%)	O (%)
Rice husk	19.1	44.6	36.3	39.8	5.7	0.5	0.2	39.8	[2]
Cotton stalk	23.5	48.2	28.4	46.8	6.4	0.3	0.2	46.8	[2]
Rice straw	28.5	54.5	17.0	38.8	6.7	0.2	0.2	38.8	[2]
Wheat straw	25.5	49.3	25.2	41.7	5	0.4	0.3	41.7	[2]
Corn stalk	52.9	28.0	19.1	43.8	5.7	0.9	0.1	48.9	[3]
Corn cob	35.4	47.0	17.7	43.6	5.8	0.7	1.3	48.6	[3]
Elephant grass	34.3	31.5	34.2	44.5	5.4	1.4	—	31.8	[3]
Hazelnut shell	17.4	25.4	57.2	52.3	6.5	5.2	9.2	26.8	[3]
Sugarcane bagasse	33.1	42.7	24.2	45.1	6.05	0.3	—	42.7	[3]
Switch grass	51.6	32.3	16.1	44.7	5.7	0.3	—	49.1	[4]
Hazelnut husk	22.8	38.2	38.9	42.6	5.5	1.1	0.1	50.6	[5]
Walnut shell	25.4	23.5	51.1	47.5	6.3	0.4	—	45.6	[6]
Pinewood waste	28.4	43.0	28.5	49.3	6	0.04	—	44.5	[7]
Apple pomace	27.8	47.5	24.7	47.9	6.6	0.7	—	37.4	[8]
Chestnut shells	23.3	32.6	44.0	48.1	5.4	0.6	—	45.7	[9]
Cherry stones	28.0	28.1	43.9	51.1	7.2	3	—	38.6	[9]
Grape seeds	22.9	16.9	60.2	51.5	6.3	1.7	—	40.3	[9]
P. juliflora	18.8	51.6	29.6	43.3	6.32	1.3	0.07	48.9	[10]
Cashew nut shells	18.6	41.3	40.1	58.3	7	0.7	0.06	32	[3, 11]
Coconut shell	27.9	40.3	31.9	53.9	5.7	0.1	0.02	39.4	[3, 11]
Cagon grass	28.8	50.9	20.4	44.3	5.6	0.8	0.09	49.0	[12]
Karanja fruit Hull	48.4	12.0	39.6	45.1	6.1	—	0.36	48.4	[13]
Cotton stalk	23.5	48.2	28.4	46.8	6.4	0.3	0.2	46.8	[2]
Hibiscus rosa sinensis	19.1	44.6	36.3	40–43	4.7–6.0	0.8–4.9	0.04–0.7	34–38	[14, 15]
Nerium oleander	23.5	48.2	28.4	44	6.7	0.5–1.2	0.04–0.2	30–35	[14, 16]

Table 1.

Different biomasses, their constituents and elemental analysis.

^*

HEMI, hemicellulose; CEL, cellulose; LIG, lignin.

Table 1 provides the chief constituents of biomass in wt% on dry and ash free basis along with the elemental composition for various biomasses. These chief constituents will vary depending on the type, location, and age of the plant. The error in values reported in Table 1 is 2–5%. The wt% of hemicellulose varies from 17.4 to 52.9, the wt% of cellulose varies from 12 to 54.5% and the wt% of lignin varies from 16.1 to 60.2.

As shown in Table 1, there is significant variation across different biomasses. Thus, products resulting from biomass pyrolysis will also vary widely, and hence, it will be difficult to control the product profiles if enough attention is not paid to these chief constituents along with the biomass processing conditions.

This book chapter considers packed bed and fluidized bed pyrolyzers, which vary significantly in their heat transfer capabilities because of the mixing conditions. Section 2 of the chapter describes different pyrolysis processes and their associated product profiles. In view of their importance in pyrolysis, the reaction kinetics are provided in Section 3. These kinetic parameters are obtained from a combination of prior published work and the authors’ experimental data, based on thermogravimetric analysis (TGA) and lumped parameter models. Section 4 deals with the modeling of continuous packed bed and fluidized bed pyrolyzers, accounting for the variation in product profiles due to variation in feed and operating parameters. Section 5 introduces the optimization of product profiles for these two types of pyrolyzers under continuous operation.

2. Different pyrolysis processes

The primary products of the pyrolysis are gas, oil, char and water. The ratios of these products depend on parameters such as particle size, heating rate, degradation temperature, and feed rate of the material [14, 17, 18, 19, 20, 21, 22]. The different pyrolysis processes are flash/fast pyrolysis, intermediate pyrolysis, and slow pyrolysis [1, 17, 20, 23, 24, 25]. The pyrolysis process is classified based on the heating rate as well as the degradation temperature of biomass. The operating parameters of different pyrolysis processes are given in Figure 1.

Figure 1.

Different types of pyrolysis and their operating conditions.

2.1 Flash/fast pyrolysis

Flash/fast pyrolysis is performed with very high heating rates (∼1000 K/s) for less than a second. Since, the entire biomass particles are required to be heated for a very short time, only particles of very small size (<1 mm) can be pyrolyzed using this method. Because of small particle size and very short residence times, the thermal gradients within the particles are small, and hence, there is low product variation. This method is preferable if the number of components in the product stream is required to be low. With most of the biomasses during fast pyrolysis, the products are usually non-condensable gases.

2.2 Medium/intermediate pyrolysis

Intermediate pyrolysis is performed at medium heating rates. This kind of pyrolysis is preferred for biomass in the particle size range of 1–5 mm. During the intermediate pyrolysis, there are huge thermal gradients within the particle itself. Hence, intermediate pyrolysis is preferred when different products are required from the same biomass. Further, this type of reactor does not require a separate unit for product separation, especially, oil and water.

2.3 Slow pyrolysis

Slow pyrolysis is performed at very low heating rates ∼0.1 K/s. The particle size during slow pyrolysis is between 2 and 10 mm. Slow pyrolysis is preferred if the charring characteristic of biomass is very high [4]. This is also the preferred type of pyrolysis when the residence time required during the pyrolysis is high.

Because of variations in the feed and the pyrolysis process, the thermal gradients are very high. Due to these thermal gradients within the particle and in the reactor, the reactions that the particles are undergoing are different, resulting in different product profiles. To design pyrolysis reactors with controlled product selectivity, it is important to understand which reactions are taking place in the reactor/biomass particle. This means that it is required to understand the kinetic parameters such as reaction order, activation energy, and pre-exponential factor for the reaction [14, 17, 23, 26, 27, 28, 29]. Since, biomass particles are undergoing complicated reaction networks, the estimation of kinetic parameters were limited to the overall process in the early stages. Later, the kinetic parameters were estimated using the staged decomposition of biomass due to its chief constituents of biomass, namely, hemicellulose, cellulose, and lignin, and their relative proportions in a biomass [11, 14, 20, 30]. In the next section of this chapter, the kinetics of different biomasses are presented along with their corresponding parameters.

3. Pyrolysis kinetics and product profiles

Kinetics play an important role in the design of pyrolysis reactors. These kinetic parameters depend on the type of the biomass feed, mixing conditions in the reactor, and inter-particle & intra-particle thermal and mass transfer limitations. As mentioned earlier, the biomass pyrolysis consists of complicated reaction networks, making it difficult to analyze the pyrolysis kinetic parameters for individual reactions.

3.1 Pyrolysis kinetics

Different kinetic models were proposed by several authors working on the kinetics of the pyrolysis of biomass. Currently, there is no single model for the evaluation of kinetic parameters primarily based on the thermogravimetric (TGA) studies. The different types of kinetic models tested for the biomass pyrolysis are: (1) isoconversion (ISO) models such as Kissinger-Akahira-Sunose (KAS) model and Ozawa-Flynn-Wall (OFW) model, (2) generalized n^th order reaction model, (3) Coats-Redfern (CR) model, (4) three component mechanism with CR model, (5) Gaussian Distributed Activation Energy model (Gaussian DAEM), (6) Friedmann model, and (7) Starink model. The differences lie in their approach to relate them to rate of biomass degradation with kinetic parameters-mainly the activation energy and the pre-exponential factor.

The different models to analyze the pyrolysis thermal degradation data, were classified mainly into three categories namely, accelerating, decelerating, and sigmoidal model based on the shape of rate of degradation vs. time [17, 29]. The accelerating models are the ones whose rate of decomposition increases with the increase in time. For those biomasses which fall under this category a simple power law model with respect to rate of decomposition is more suitable [29]. The decelerating models are used whose rate of reaction decreases with increase in time, such as CR model and integral models (such as KAS and OFW models). This means, there are mass transfer limitations (diffusion limited) during the reaction due to the formation of products or inert layers that slows down the reaction. The sigmoidal models represent the autocatalytic type reactions during biomass pyrolysis, such as OFW and KAS models. The choice of the kinetic model purely depends on the rate of decomposition vs. time curve.

The isoconversion model and Gaussian DAEM will give only the activation of energy for the overall thermal degradation process, which is further used in Arrhenius type model for finding the pre-exponential factor.

Table 2 provides the kinetic parameters reported by researchers for different biomasses that are widely used in pyrolysis.

Type of biomass	Model	Activation energy–Ea (kJ/mol)	Pre-exponential factor-A (min^−1)	Reference
Rice husk	Gaussian DAEM	85–110	10^5–10^7	[31]
Cotton stalk	Direct method; Integral method	Hemicellulose: 102.0; Cellulose: 98.5; Hemicellulose: 127.8; Cellulose: 72.5	1.22; 0.45; 2.6; 0.35	[32]
Rice straw	Kissinger model; OFW model; KAS model	172.6; 192.7; 193.6	10^11; 10^22; 10^15	[32]
Wheat straw	nth-order reaction model	Cellulose and hemicellulose: 78 (n-0.65); Lignin: 80 (n-2.7)	10^7; 10^6	[33]
Corn stalk	KAS model	62.7	10^7–10^8	[34]
Corn cob	CR model	64–80	10^3	[35]
Switch grass	KAS model	77.4	10^8–10^9	[34]
Elephant grass	Three component mechanism	Hemicellulose: 46.5–65.5; Cellulose: 108–127.2; Lignin: 45.6–53.5	10^4–10^6; 10^8–10^11; 10^2–10^3	[36]
Hazelnut husk	KAS model; OFW model; CR model	127.8; 131.1; —	—; —; 10^5–10^6	[37]
Hazelnut shell	Friedman model; KAS model; DE Algorithm; CR model	222.3; 216.3; First zone: 35–153; Second zone: 20–135; 35.9	—; —; 10^−3–10^8; 10^−4–10^6; 10^2	[38]
Walnut shell	Arrhenius model; CR model	69.3; 101.6	10^5; 10^5	[6]
Pine wood	Arrhenius model	150	10^11	[39]
Apple pomace	Friedman model; OFW model; KAS model; CR model	197.7; 213.0; 201.7; —	—; —; —; 10^−1–10^−3	[8]
Chestnut shells	Friedman model; KAS model; OFW model; Starink model; DAEM	127.2–194.8; 152.7–196.7; 154.1–196.1; 153.2–196.9; 175.2	—; —; —; —; 10^11–10^15	[40]
Cherry stones	Arrhenius equation	Hemicellulose: 197.7; Cellulose: 213.0; Lignin: 201.7	10^10; 10^7; 10^2	[41]
Grape seeds	Gaussian DAEM; Logistic DAEM	188 ± 3; 190 ± 2	10^−2; 10^−2	[42]
P. juliflora	KAS model; OFW model; Friedman model	204.0; 203.2; 219.3	10^11; 10^5; 10^21	[10]
Sugarcane bagasse	Direct method; Integral method	Hemicellulose: 53.5, cellulose: 43; Hemicellulose: 87.7, cellulose: 77	10^−1; 10^−1; 10^−1; 10^−1	[32]
Cashew nut shells	CR model	Hemicellulose: 130.2; Cellulose: 174.3	10^−1–10^−4; 10^−2–10^−3	[11]
Coconut shell	CR model	Hemicellulose: 179.6; Cellulose: 216.0	10^−1–10^−5; 10^−1–10^−3	[11]
Imperata cylindrical (Cagon grass)	DAEM; Global kinetic model	213.9; 60–64	10^13; 10^1–10^2	[12]
Karanja fruit Hull	KAS model; OFW model	61.0; 68.5	10^6; 10^6	[13]
Hibiscus rosa sinensis	CR model	Hemicellulose: 55–91; Cellulose: 9–62; Lignin: 65–142	10^6–10^8; 10^−1–10^3; 10^4–10^7	[14]
Nerium oleander	CR model	Hemicellulose: 29–51; Cellulose: 11–43; Lignin: 71–109	10^2–10^4; 10^−1–10^3; 10^2–10^5	[14]

Table 2.

Kinetic parameters of pyrolysis of different biomasses.

Comparing Tables 1 and 2, for the biomasses with high hemicellulose content, the activation energy is between 50 and 65 kJ/kmol, and the pre-exponential factor is between 10³ and 10⁸ min⁻¹. The activation energy for high cellulose content is between 170 and 220 kJ/kmol and the pre-exponential factor is between 10⁷ and 10²¹ min⁻¹. For the biomasses with high lignin content, the activation energy ranges from 65 to 140 kJ/kmol and the pre-exponential factor ranges from 10⁻¹ to 10⁷ min⁻¹. These wide variations in the kinetic parameters indicate that different reactions are occurring within the biomass particle.

3.2 Pyrolysis product profiles: lumped product distribution

It has been mentioned earlier that the products of biomass pyrolysis vary widely. There are not many studies aimed at intrinsic kinetic parameter estimation for each individual products of pyrolysis. The pyrolysis products are lumped based on their standard phase. The lumped reaction model for the biomass pyrolysis is given in Eqs. (1) and (2) [43, 44].

$$\text{Reaction}1:\mathit{\text{Biomass}}\begin{array}{l}\to \mathit{Gas}\\ \to \mathit{Tar}/\mathit{\text{Liquids}}\\ \to \mathit{\text{Char}}\end{array}$$ E1

The tar formed during the primary biomass decomposition shall further decompose into gas and char.

$$\text{Reaction}2:\mathit{Tar}\begin{array}{l}\to \mathit{Gas}\\ \to \mathit{\text{Char}}\end{array}$$ E2

For practical purposes, the products are classified into gases, liquids, and char. The lumped product distribution from pyrolysis of different biomasses, different pyrolysis methods, pyrolysis conditions and two different pyrolyzers (fixed bed and fluidized) are provided (Table 3).

Biomass type	Pyrolysis type	Pyrolysis conditions	Reactor type	Products (wt%)	Ref #
Rice husk	Intermediate	Temp.: >500°C; HR: >3.33 K/s; Size: <0.5 mm	Fluidized bed	Gas: 15%; Liquids: 37–40%; Char: 47%	[45]
	Slow	Temp.: >500°C; HR: >0.33 K/s; Size: <0.21 mm	Fixed bed	Gas: 32.7%; Liquids.: 30.1%; Char: 31.8%	[46]
Cotton stalk	Intermediate	Temp.: 490°C; HR: 9 K/s; Size: 1 mm	Fluidized bed	Gas: 23%; Liquids: 36%; Char: 16%	[47]
	Slow	Temp.: 600°C; HR: 0.3 K/s; Size: 3 mm	Fixed bed	Gas: 44.8%; Liquids: 17.1%; Char: 38%	[24, 48]
Rice straw	Intermediate	Temp.:500°C; HR: 3.3 K/s; Size: <0.5 mm	Fixed bed	Gas: 54%; Liquids: 6%; Char: 40%	[20]
	Slow	Temp.:600°C; HR: 0.16 K/s; Size: 0.3 mm	Fixed bed	Gas: 30%; Liquids: 45%; Char: 28%	[49, 50]
Wheat straw	Fast/flash	Temp.: 525°C; HR: 250–1000 K/s; Size: 0.25–1 mm	Fluidized bed	Gas: 26.9%; Liquids: 34.9%; Char: 28.0%	[28]
	Slow	Temp.: 450°C; HR: 0.03 K/s; Size: 1.33 mm	Fixed bed	Gas: 24%; Liquids: 34%; Char: 43%	[51]
Corn stalks	Intermediate	Temp.: 500°C; HR: 8.3 K/s; Size: <0.5 mm	Fluidized bed	Gas: 35%; Liquids: 38%; Char: 28%	[52]
	Slow	Temp.: 400°C; HR: 0.83 K/s; Size: <1 mm	Fixed bed	Gas: 12%; Liquids: 50%; Char: 38%	[53]
Corn cob	Fast/flash	Temp.: 550°C; HR: 1000 K/s; Size: 1–2 mm	Fluidized bed	Gas: 46%; Liquids: 36%; Char: 18%	[54]
	Intermediate	Temp.: 577°C; HR: 10 K/s; Size: 0.5–2 mm	Fixed bed	Gas: 49%; Liquids: 28%; Char: 23	[55]
Elephant grass	Fast/flash	Temp.: 480–520°C; HR: 4000 K/s; Size: 0.8–1.2 mm	Fluidized bed	Gas: 36.3%; Liquids: 37.6%; Char: 27.8%	[56, 57]
	Slow	Temp.: 500°C; HR: 0.16 K/s; Size: 0.21 mm	Fixed bed	Gas: 26%; Liquids: 44.7%; Char: 29.3%	[58]
Hazelnut shell	Slow	Temp.:550°C; HR: 0.1 K/s; Size: 0.85–1.8 mm	Fixed bed	Gas: 21.5; Liquids: 22.5%; Water: 25%; Char: 31%	[59]
	Intermediate	Temp.: 550°C; HR: 5 K/s; Size: 0.85–1.8 mm	Fixed bed	Gas: 27; Liquids: 34%; Water: 11%; Char: 28%	[59]
Sugarcane bagasse	Intermediate	Temp.: 500°C; HR: 3.3 K/s; Size: <0.5 mm	Fixed bed	Gas: 55%; Liquids: 10%; Char: 35%	[20]
	Slow	Temp.: 420°C; HR: 0.35 K/s; Size: <0.5 mm	Fixed bed	Gas: 24.4%; Liquids: 43%; Char: 32.6%	[60]
Switch grass	Fast/flash	Temp.: 510°C; HR: 1000 K/s; Size: 0.25–1 mm	Fluidized bed	Gas: 16.5%; Liquids: 57.9%; Char: 20.0%	[28]
	Slow	Temp.: 500°C; HR: 0.17 K/s; Size: 0 < 1 mm	Fixed bed	Gas: 43.2%; Liquids: 27.5%; Char: 29.3%	[61]
Walnut shell	Intermediate	Temp.: 500°C; HR: 5 K/s; Size: 0.6–1.8 mm	Fixed bed	Gas: 15.6%; Liquids: 31%; Char: 27.5%	[62]
	Slow	Temp.: 550°C; HR: 0.16–1 K/s; Size: 0.075 mm	TGA	Gas: 10%; Liquids: 25%; Char: 40%	[63]
Pine wood	Fast/flash	Temp.: 400–500°C; HR: >1000 K/s; Size: 0.25–0.425 mm	Fluidized bed	Gas: 22%; Liquids: 67%; Char: 11%	[64]
	Intermediate	Temp.: 500°C; HR: 5 K/s; Size: 06–0.85 mm	Fixed bed	Gas: 26%; Liquids: 43%; Char: 23%; Water: 14%	[65]
	Slow	Temp.: 700°C; HR: 0.16 K/s; Size: <1 mm	Fixed bed	Gas: 25%; Liquids: 58%; Char: 18%	[66]
Apple pomace	Slow	Temp.: 400°C; HR: 0.08–0.3 K/s; Size: 420–840 μm	Fixed bed	Gas: 71.5%; Liquids: 25.4%; Char: 3%	[23]
Coconut shell	Intermediate	Temp.: 500°C; HR: 3.3 K/s; Size: <0.5 mm	Fixed bed	Gas: 51%; Liquids: 10%; Char: 39%	[20]
	Slow	Temp.: 550°C; HR: 1 K/s; Size: 1.18–1.8 mm	Fixed bed	Gas: 30–33%; Liquids: 38–44%; Char: 22–31%	[67]
Cashew nut shells	Slow	Temp.: 400–450°C; HR: 0.166 K/s; Size: 0.25 mm	Fixed bed	Gas: 57.4%; Liquids: 23.5%; Char: 19.1%	[68]
Cherry stones	Slow	Temp.: 400–500°C; HR: 0.083–0.33 K/s; Size: 0.32–2 mm	TGA	Gas: 8.8–47.6%; Liquids: 32–58%; Char: 20–56.8%	[41]
P. juliflora	Fast/flash	Temp.: 450°C; HR: >4000 K/s; Size: 0.25–0.5 mm	Fluidized bed	Gas: 12.5%; Liquid: 62.5%; Char: 25%	[57, 69]
	Slow	Temp.: 600°C; HR: 0.33 K/s; Size: 0.2–0.5 mm	Fixed bed	Gas: 44; Liquid: 38.3%; Char: 36.8%	[70]
Cogon grass	Slow	Temp.: 500°C; HR: 0.36 K/s; Size: 0.25–1 mm	Fixed bed	Gas: 49.1–74.1%; Oil: 3.2–20.8%; Char: 22.6–30.5%	[12]

Table 3.

Product profiles from pyrolysis of different biomass in fixed and fluidized bed pyrolyzers.

Temp., temperature; HR, heating rate; size, biomass particle size.

From the data presented in Table 3, it can be generalized that the liquid products will be more in fluidized bed reactors, whereas more char is seen in fixed bed reactors. Further, slow pyrolysis results in more gas and char when compared to fast pyrolysis. This might be due to the liquid products formed in reaction 1, shown in Eq. (1), being further consumed by reaction 2, shown in Eq. (2) resulting in more gas and char. The relative proportions of these products depend on various parameters mentioned earlier.

4. Process modeling of pyrolysis reactors

The biomass pyrolysis has been mainly carried out in two types of reactors: fixed bed (or packed bed) reactors and fluidized bed reactors, by many authors, as presented in Table 3. The process models for these two reactors are developed from fundamental laws of conservation of mass and energy along with empirical relations for properties such as specific heat, density, diffusivity, mass and heat transfer coefficients, etc. The packed bed pyrolyzers are further classified as down-draft and updraft pyrolysis reactors. The detailed comparison of the general packed bed and fluidized bed reactors is given in Table 4.

Gasifier type	Specifications/conditions
Updraft fixed pyrolyzer	The biomass is fed from the top of the pyrolyzer, and the inert gas (if any) fed from bottom. Char resulting from pyrolysis falls down and may accelerate the pyrolysis. The pyrolysis gases and along with the liquid tar (in the form of gas) leaves from the top of the pyrolyzer. The ash (inert component of the biomass) is collected at the bottom of the gasifier. Operating temperature ranges from 300 to 750°C.
Downdraft fixed bed pyrolyzer	The biomass is fed from top of the pyrolyzer along with inert gas allowing the feed and gases move in the same direction. The feed is broken down, falling down the gasifier under gravity. A bed of hot char through which the gases are allowed to pass through (a secondary reaction zone) ensures the pyrolysis products travelling from top are further broken down. This increases the residence time through the pyrolysis stage. An exit for the pyrolysis products is provided just above the bottom of the pyrolyzer. The ash collected under the grate at the bottom the pyrolyzer. Operating temperature ranges from 300 to 750°C.
Fluidized bed reactor	A bed of fine inert solid material is present at the bottom of the pyrolyzer. The inert gas is fed from the bottom of the pyrolyzer fast enough (1–3 m/s) to agitate the material. The biomass feed is fed in from the side, mixes with the inert gas and the products of the pyrolysis leave from the top. The operating temperature is below 900°C to avoid ash melting and sticking to the wall.

Table 4.

Comparison of fixed bed and fluidized bed pyrolyzers.

The biomass usually contains moisture. The moisture needs to be removed before the pyrolysis stage. If this is carried to the pyrolysis stage, the gasification reactions such as steam reformation may kick off resulting in undesirable products. The modeling of the packed bed and the fluidized bed pyrolyzers is discussed in detail below.

The major difference between the updraft pyrolyzer and the downdraft pyrolyzer is only the inlet and outlet locations, which changes the residence time and mixing conditions. For the purpose of the modeling of biomass pyrolysis and optimization of product profiles, the updraft and downdraft pyrolyzers are treated as fixed bed pyrolyzers.

4.1 Modeling of packed bed pyrolysis reactor

The modeling of the packed bed pyrolysis reactors is divided into drying stage and the pyrolysis stage. The modeling of these two stages has been is presented in detail below.

4.1.1 Modeling of drying stage in packed bed pyrolyzers

The drying of biomass particles will happen in two stages: (a) constant rate period and (b) falling rate period. The rate of drying in these two stages is given separately by the following equations.

The rate of drying during the constant rate period is given by [71]

$$\frac{\mathit{dX}}{\mathit{dt}}=-k_c=1.3\times {10}^{-9}{T}_g^{4.112}{v}_g^{0.219}$$ E3

The rate of drying during the falling rate period is given by [71]

$$\begin{array}{l}\frac{\mathit{dX}}{\mathit{dt}}=-K\left(X-X_{\mathit{eq}}\right)\\ K=0.011exp\left(-201.8/T_g\right)\end{array}$$ E4

Eqs. (3) and (4), provide an estimation of rate of drying in both constant and falling rate periods, with rate of drying depending on the particle temperature. During the pyrolysis process, the biomass particle temperature depends on the rate of heat transfer between the gas and the particle. This rate of heat transfer depends on the flow characteristics involving Reynolds and Prandtl number. For 20 < Re < 1000, the heat transfer coefficient is given by [71, 72]

$$\begin{array}{l}h=3.26C_{\mathit{pg}}{G}_g{Re}^{-0.65}{Pr}^{\raisebox{1ex}{$2$}\!\left/ \!\raisebox{-1ex}{$3$}\right.}\\ {Re}_p=\frac{{\rho }_{\mathit{gas}}{U}_o{d}_p}{\mu }\end{array}$$ E5

where k_c is the mass transfer coefficient at constant drying period in s⁻¹; K is the mass transfer coefficient at falling drying period in s⁻¹; Re is the Reynolds number of gas; Pr is the Prandtl number of gas; T_g is the gas temperature in °C; $v_g$ is the gas velocity in m/s; $C_{\mathit{pg}}$ is the heat capacity of gas in J/(kg K); ${\epsilon }_{\mathit{mf}}$ is the porosity at minimum fluidization; $X$ is the moisture content in the biomass; X_eq is the moisture content at the end of constant rate period; $G_g$ is the gas mass flux in kg/(m² s).

4.1.2 Modeling of pyrolysis in packed bed reactors

Eqs. (1) and (2) represents the reactions reported during pyrolysis of biomass with lumped product approach. Since the reaction presented in Eq. (1) involves only the solid biomass as reactant, most of the reactions are treated as first order reactions using Arrhenius type model [73]. The Arrhenius model parameters for the lumped reaction model that produces gaseous, liquid, and char for different constituent of biomass are given in Table 5.

Pyrolysis product→	Gas		Tar/liquids		Char
Biomass component↓	A (s^−1)	Ea (J/mol)	A (s^−1)	Ea (J/mol)	A (s^−1)	Ea (J/mol)
HEMI*	2.1 × 10^16	1.8 × 10^5	8.7 × 10^14	2.0 × 10^5	2.6 × 10^11	1.5 × 10^5
CEL*	2.8 × 10^19	2.4 × 10^5	3.3 × 10^14	1.9 × 10^5	1.3 × 10^10	1.5 × 10^5
LIG*	9.6 × 10^8	1.1 × 10^5	1.5 × 10^9	1.4 × 10^5	7.7 × 10^6	1.1 × 10^5

Table 5.

Kinetic parameters for lumped models for biomass pyrolysis.

*HEMI, hemicellulose; CEL, cellulose; LIG, lignin.

The volume and the moles of the products of the pyrolysis zone was found with the help of the plug flow reactor (PFR) design equation.

$$\begin{array}{l}\frac{V}{F_{\mathit{\text{Biomass}}}}=\underset{0}{\overset{X_f}{\int }}\frac{{\mathit{dX}}_{\mathit{\text{Biomass}}}}{-r_{\mathit{\text{Biomass}}}}\\ \left(-r_{\mathit{\text{Biomass}}}=r_{\mathit{Gas}}+r_{\mathit{\text{Liquids}}}+r_{\mathit{\text{Char}}}\right)\end{array}$$ E6

where V is the volume of the pyrolyzer in l, $F_{\mathit{\text{Biomass}}}$ is the molar feed rate of biomass in mol/s; $X_f$ is the desired biomass conversion; $-r_{\mathit{\text{Biomass}}}$ is the rate of biomass consumption in mol/(lit. s); $r_{\mathit{Gas}}$ is the rate of formation of gaseous products in mol/(lit. s); $r_{\mathit{\text{Liquids}}}$ is the rate of formation of liquid products in mol/(lit. s); $r_{\mathit{\text{Char}}}$ is the rate of formation of char in mol/(lit. s).

Since, the pyrolysis stage is non-isothermal in nature, it is essential to model the temperature along the length of the pyrolyzer which involves external heating. The energy balance equation was obtained based on the shell energy balance to find the temperature profile along the length of the pyrolysis zone. The steady state energy balance equation results in the following differential equation:

$$k\frac{d^{2}T}{{\mathit{dr}}^2}-\rho C_p{v}_z\frac{\mathit{dT}}{\mathit{dz}}+\frac{{\epsilon }_R}{R}\sigma \left({T_W}^4-T^4\right)-\mathrm{\Delta }{H}_R{F}_{\mathit{AO}}{\mathit{dX}}_A=0$$ E7

where k is the thermal conductivity in W/(m. K); ρ is the density in kg/m³; C_p is the specific heat capacity in J/(kg. K); $v_z$ is the gas velocity in m/s; ε_R is the emissivity of the body during radiation; $\sigma$ is the Stephan-Boltzmann constant = 5.67E−08 W/(m² K⁴); R is the radius of oxidation zone in m; T_W is the source temperature in K; T is the reactor temperature in K; $r,z$ are the radial and axial directions.

Since, Eq. (7) is combined convection diffusion equation with heat source (heat of reaction) and external heat supply, two boundary conditions are required: one in radial direction and one in axial direction.

The boundary conditions for solving the energy balance equation are:

$$\begin{array}{l}@r=R,k\frac{\mathit{dT}}{\mathit{dr}}=\mathit{\text{Radiation\hspace{0.17em}flux}}\\ @r=0;k\frac{\mathit{dT}}{\mathit{dr}}=0\left(\mathit{\text{Tempearature\hspace{0.17em}minimum\hspace{0.17em}condition}}\right)\\ @z=0;T=T_o\end{array}$$

4.2 Modeling of fluidized bed pyrolysis reactor

As mentioned in the modeling of the packed bed pyrolysis, the pyrolysis process occurs after the drying of the biomass.

4.2.1 Modeling of drying stage in fluidized bed pyrolyzers

The equations for the drying stage in a fluidized bed pyrolyzers are similar to those in a packed bed pyrolyzer, as provided in Section 4.1.1. Because there is vigorous mixing in the fluidized bed pyrolysis, the extent of heat and mass transfer is very high. Kunii and Levenspiel confirmed that there is more than one phase during bubbling fluidization [74]. These two phases are named as bubble phase (primarily the fluid used as fluidizing the medium) and emulsion phase (mixture of biomass particles and fluid). The interface between these two phases is named as “cloud.” The concept of two-phase model along with the mass transfer between the two phases is depicted in Figure 2. It is to be noted that the primary reactions during biomass pyrolysis shall occur only in the solid phase (i.e., in the emulsion phase) and the secondary reactions occur in both phases.

Figure 2.

The two-phase model for fluidized bed pyrolyzer.

The most widely used Kunii and Levenspiel model (K-L model) expresses the overall heat and mass transfer coefficient in a bubbling fluidized bed considering the resistance for heat and mass transfer between the bubble-cloud interface and resistance for heat and mass transfer between emulsion and cloud [74]. The cloud-bubble interface heat and mass transfer are functions of gas velocity and conduction/diffusion from a thin cloud layer into the bubble. The emulsion and cloud transfer are only due to conduction/diffusion between the emulsion phase and the cloud boundary. They had also suggested additional mass transfer resulting from particles dispersed in the bubbles. However, recent advanced imaging technique, have shown bubble free particles in most cases.

Based on the two-phase model, the overall mass transfer coefficient is estimated using Eqs. (8)–(10) [75].

Cloud-bubble mass transfer coefficient

$$k_{\mathit{cb}}=1.5\frac{U_{\mathit{mbf}}}{d_b}+5.85\left(\frac{{D_{\mathit{AB}}}^{0.5}{g}^{0.25}}{d_b^{1.25}}\right)$$ E8

Dense-cloud mass transfer coefficient

$$k_{\mathit{dc}}=6.77\left(\frac{D_{\mathit{AB}}{\epsilon }_{\mathit{mf}}{U}_b}{d_b^3}\right)$$ E9

Overall mass transfer coefficient (in s⁻¹)

$$\frac{1}{k_{\mathit{\text{overall}}}}=\frac{1}{k_{\mathit{cb}}}+\frac{1}{k_{\mathit{dc}}}$$ E10

The heat transfer coefficient is estimated using the correlation given in Eq. (11) [76].

$$h_c=0.15\frac{k_g}{d_p}{{Re}_p}^{0.35}{\mathit{Ar}}^{0.25}\left(V_{\mathit{gas}}\le U_o\right)$$ E11

$${Re}_p=\frac{{\rho }_{\mathit{gas}}{U}_o{d}_p}{\mu }$$ E12

$$\mathit{Ar}=\frac{d_p^3{\rho }_{\mathit{gas}}\left({\rho }_{\mathit{\text{solid}}}-{\rho }_{\mathit{gas}}\right)g}{{\mu }^2}$$ E13

where $k_{\mathit{dc}}$ is the mass transfer coefficient between dense emulsion and cloud in m/s; $k_{\mathit{cb}}$ is the mass transfer coefficient between bubble and cloud in m/s; $k_{\mathit{\text{overall}}}$ is the overall mass transfer coefficient between bubble and cloud in m/s; $h_c$ is the overall heat transfer coefficient in W/(m² K); ${Re}_p$ is the Particle Reynolds number; $\mathit{Ar}$ is the Archimedes number; $U_{\mathit{mbf}}$ is the bubble velocity at minimum fluidization in m/s; $D_{\mathit{AB}}$ is the binary diffusivity in m²/s; $U_b$ is the bubble velocity in m/s; ${\epsilon }_{\mathit{mf}}$ is the bed voidage at minimum fluidization; ${\rho }_{\mathit{\text{solid}}}$ is the density of biomass particle in kg/m³; ${\rho }_{\mathit{gas}}$ is the density of fluidizing gas in kg/m³; $d_b$ is the bubble diameter in m.

4.2.2 Modeling of pyrolysis stage in fluidized bed pyrolyzers

Due to vigorous mixing in the fluidized beds, the following assumptions are made for modeling of the pyrolysis stage in the fluidized bed reactors:

1. Isothermal operation of the reactor,

2. No radial variations, and

3. Reactions occurring only in the solid phase (only in the emulsion phase).

Based on these assumptions, the following models (separately for emulsion phase and bubble phase) can be obtained from the fundamental component balance:

$$\mathit{\text{Bubble\hspace{0.17em}phase}}:\epsilon u_b\frac{{\mathit{dC}}_{A,b}}{\mathit{dz}}-k_L\left(C_{A,b}-C_{A,e}\right)=0$$ E14

$$\mathit{\text{Emulsion\hspace{0.17em}phase}}:\left(1-\epsilon \right)u_e\frac{{\mathit{dC}}_{A,e}}{\mathit{dz}}+k_L\left(C_{A,b}-C_{A,e}\right)-\left(1-\epsilon \right)D_{\mathit{eff}}\frac{d^2{C}_{A,e}}{{\mathit{dz}}^2}+\left(-r_A\right){\rho }_e\left(1-\epsilon \right)=0;$$ E15

where b is the bubble phase and e is the emulsion phase.

5. Optimization of product profiles in biomass pyrolysis

As discussed in Section 1, since the product profiles of biomass pyrolysis are known to greatly depend on various parameters, it is necessary to determine the parameters that have the largest effect on the ratios of important lumped products discussed in Section 2.

5.1 Response surface optimization methodology: the mixture design

The following quantifiable factors were chosen for the optimization.

The biomass-based factors are:

1. Hemicellulose fraction

2. Cellulose fraction

3. Lignin fraction

The process-based parameters have been divided into two categorical type parameters.

1. The type of pyrolysis-slow and fast/flash pyrolysis

2. The type of reactor-fixed bed and fluidized bed reactors

The variation of constituent composition of biomass is obtained from Table 1. The amounts of gaseous, liquid, and products for each biomass for different process parameters and different reactor types are obtained from Table 3.

Since hemicellulose, cellulose, and lignin are biomass constituents, the sum of their fractions must be equal to one. Accordingly, a mixture design was chosen for the statistical design of the experiments.

A total of 52 data sets were selected combining Tables 1 and 3 (based on the variations in mixture design), and the experiments conducted and data analyzed.

The depletion of fossil fuels has created interest in obtaining the fuels from alternate sources such as biomass, especially for transportation fuels. Therefore, the objective of the product profiles from biomass pyrolysis is aimed to maximize the liquid (tar) products and simultaneously minimize the production of gas and char. The reason for the minimization of gaseous products is that they may contain carbon monoxide and carbon dioxide which are of less calorific value when compared to the hydrocarbons.

Ternary diagrams are common in representing factor levels in a mixture design. In such a diagram, with three factors (x1, x2, and x3), the vertex represents a pure component (i.e., x1 = 100%) while its opposite edge holds a value of x1 = 0 (with x2 + x3 = 100%). The same holds for the other two vertices and edges.

However, it may be noted that in certain experiments the sum of proportions of the three components may be deliberately constrained to equal a specific value. This feature has been used in our experimental design. For example, referring to Figure 3, the three vertices represent hemicellulose, cellulose and lignin. The maximum fraction of these three constituents is 0.764, 0.742 and 0.7444 for hemicellulose, cellulose and lignin, respectively. The 0.119, 0.117, and 0.139 marked on the sides of the triangle represent the minimum values for the biomass constituents.

Figure 3.

Contour plot of gas yield in biomass pyrolysis for fast pyrolysis in fluidized bed reactor.

5.2 Optimization of gas yield

The analysis of minimization of gas yield is separated into two types: (a) fast pyrolysis in fluidized bed pyrolyzer and (b) slow pyrolysis in fixed bed pyrolyzer. These two were chosen to account for the extremities of the process conditions. The contour plot for fast pyrolysis in fluidized bed is shown in Figure 3. The three vertices of the triangle are the maximum points of hemicellulose, cellulose, and lignin. For the minimization of gaseous products during fast pyrolysis in fluidized bed, the hemicellulose content in biomass is required to be high, when compared to the cellulose and lignin. More than 40% hemicellulose and ∼20% of each of lignin and cellulose in the biomass feed will minimize the gas yield during fast pyrolysis in fluidized bed. This is easily achievable, because there are biomasses with hemicellulose content higher than 40% (please refer to Table 1). Considering fast pyrolysis of wheat straw in fluidized bed reactor, which contains 25.5% hemicellulose, 49.3% cellulose, and 25.2% of lignin, the gas yield is ∼30%, which is consistent with the experimentally obtained data presented in Table 3.

The gas yield during slow pyrolysis in fixed bed pyrolysis is higher than that of fast pyrolysis in fluidized bed reactors. This is due to the fact that the residence time in the fixed bed reactors is higher when compared to that of fluidized bed reactors. Due to longer residence times, there are secondary reactions, that is, the conversion of liquid into gas and char. The optimal minimum gas yield during slow biomass pyrolysis in fixed bed reactors is ∼16%, as shown in contour plot in Figure 4. The minimum gas yield can be obtained at various conditions. Specifically, it is obtained either at high hemicellulose content or at medium cellulose and lignin content in the biomass. Considering the wheat straw decomposition during slow pyrolysis in fixed bed, the gas yield is 16–26% as given by Figure 4.

Figure 4.

Contour plot of gas yield in biomass pyrolysis for slow pyrolysis in fixed bed reactor.

The gas yield during biomass pyrolysis may be obtained from statistical modeling, presented in Eq. (16). This equation was obtained after removing the model terms that were not statistically significant, that is, terms with p-value < 0.05.

$$\mathit{\text{GasYield}}\left(\%\right)=-{20.4}^{\ast }H+{108.8}^{\ast }C+{111.3}^{\ast }L-{377.8}^{\ast }{C}^{\ast }L-{18.3}^{\ast }{H}^{\ast }P+{50.1}^{\ast }{H}^{\ast }{L}^{\ast }R$$ E16

where H is the hemicellulose fraction in biomass; C is the cellulose fraction in biomass; L is the lignin fraction in biomass; P is the pyrolysis type (fast or slow); R is the reactor type (fluidized bed or fixed bed).

The coefficients present in Eq. (16) represents whether the effect is positive or negative. The coefficient for hemicellulose is negative. This means, the higher the hemicellulose content, lesser will be the gas yield. From Eq. (16), there are interactions between cellulose-lignin, hemicellulose-pyrolysis type and hemicellulose-lignin-reactor type. These interactions could be either synergistic (positive coefficient) or antagonistic (negative coefficient). For the gas yield%, the cellulose-lignin and hemicellulose-pyrolysis are antagonistic, whereas hemicellulose-lignin-reactor type is synergistic.

Equations similar to gas yield%, presented in Eq. (16) were also obtained for liquid yield% and char yield%.

5.3 Optimization of liquid yield

As mentioned in Section 5.1, it is important find the level of biomass constituents and operating conditions for pyrolysis to maximize the liquid yield, while minimizing both gas and char yield.

Figure 5 presents the contour plot of liquid yield as function of biomass constituents during fast pyrolysis. The maximum liquid yield may be obtained at high hemicellulose, low lignin and low cellulose content. For biomasses whose cellulose content is high, the liquid yields are very low and for the biomasses whose lignin content is high, the liquid yield ranges from 40 to 60%. For example, one of the biomasses containing high hemi cellulose is switch grass, for which, if decomposed during fast pyrolysis in fluidized bed, the liquid yield is more than 51% (from Figure 5), which is consistent with the experimentally obtained data.

Figure 5.

Contour plot of liquid yield in biomass pyrolysis for fast pyrolysis in fluidized bed reactor.

Figure 6 shows the liquid yield during slow pyrolysis in fixed bed pyrolyzes. Comparing Figure 5 with Figure 6, it can be concluded that, the liquid yield is higher in fast pyrolysis in fluidized bed than slow pyrolysis in fixed bed. Further, the maximum liquid yield that can be obtained is ∼40%. This can be obtained only at high hemicellulose content, medium cellulose content and low lignin content. The liquid yield for the high hemicellulose content biomasses, such as switch grass, during slow pyrolysis in fixed bed reactor, the liquid yield will vary from 25 to 40%, which can be obtained from Figure 6.

Figure 6.

Contour plot of liquid yield in biomass pyrolysis for slow in fixed bed reactor.

5.4 Optimization of char yield

Minimization of char is also important during biomass pyrolysis. Figure 7 shows the contour plot of char yield during fast pyrolysis in fluidized bed and Figure 8 shows the char yield during slow pyrolysis in fixed bed. Lower char yields may be obtained during fast pyrolysis in fluidized bed from biomasses containing higher amount of lignin, medium amounts of hemicellulose and lower amounts of cellulose (lignocellulosic biomass in other words). For example, the high lignin biomasses such as hazelnut shell will yield less char during fast pyrolysis in fluidized bed reactor.

Figure 7.

Contour plot of char yield in biomass pyrolysis for fast pyrolysis in fluidized bed reactor.

Figure 8.

Contour plot of char yield in biomass pyrolysis for slow pyrolysis in fixed bed reactor.

Low char yields may be obtained for biomasses with high hemicellulose and high lignin during slow pyrolysis in fixed bed operation.

6. Conclusions

Biomasses vary widely in their chief constituents namely, hemicellulose, cellulose, and lignin. The order of the degradation temperature for the three chief constituents is hemicellulose < cellulose < lignin. For obtaining controlled and useful product profiles such as liquid fuels via pyrolysis, it is important to understand the pyrolysis process conditions, such as heating rate and temperature. For optimization, the pyrolysis operating parameters are classified as slow and fast pyrolysis and the reactors are classified as fluidized bed and fixed bed. The data required for optimization was obtained from many sources, including experimental data for various biomasses and process conditions. The response surface optimization was performed using mixture design with three levels for biomass constituents and two levels each for pyrolysis type and reactor type. The objective of this book chapter is to model the reaction using lumped (gas, liquids, and char) approach and find the feed and operating parameters to maximize the liquid yield. In general, the liquid yield was found to be higher during fast pyrolysis/fluidized bed reactors when compared to slow pyrolysis/fixed bed reactors. This is due to the large residence time in the slow pyrolysis/fixed bed reactors. The maximum yield may be obtained for the biomasses containing high hemicellulose such as switch grass and corn stock.

The authors recommend further optimization with respect to particle size, heating rate, and biomass feed rate.

Acknowledgments

The authors acknowledge the financial support from the Center of Excellence in Advanced Materials & Green Technologies, granted under the Frontier Areas of Science and Technology (FAST) scheme to establish the Centers of Excellence by Ministry of Human Resource Development (MHRD), Government of India.

Conflict of interest

There is no conflict of interest.

Notes/Thanks/Other declarations

The authors would like to thank the students who attended the course “Waste to Energy part of Masters in Materials Science and Engineering program, Amrita Vishwa Vidyapeetham,” who had helped in obtaining the data and supported the work through discussions.