5 Must-Have Features in a Desulphurization Pump export

From the model application, Figure 9 illustrates that a short time contact time, τ, is needed in a CFB, and an average τ in a BFB. The required residence times in a pneumatic conveying line (>>100 s) make this solution in practice impossible since extremely long piping would be needed at a velocity of e.g., 2 m/s.

If you are looking for more details, kindly visit SGB.

4.2. The CFB Contact Mode

Using the parameters of 3.2, the model equations can be used to predict SO2 capture efficiencies and parameter influences.

1. Prior to performing detailed predictions, the effect of both

kg

and

De

were assessed. All other parameters remaining within the predicted range of 4.2, the effects of both

kg

and

De

are negligible. Increasing

kg

from 200 to m/s has a negligible effect on the predicted time for a given conversion: this was indeed expected due to the high Reynolds number in the riser, where flue gas film diffusion is of negligible influence.

Similarly, the variation of

De

by 2 orders of magnitude, at

kg

~300 m/s for an average particle size of 40 μm, has an effect well below 10% on the expected conversion. Pore diffusion is not a rate-limiting resistance when using small particles, as is common in CFB combustors.

kg

~ 300 m/s,

De

= 10'9 m2/s and

kc

= 5 × 10'2 m/s, the model equations predict the required time (t) for a given conversion. This is illustrated in

MR

being the remaining variable.

2. Using~ 300 m/s,= 10/s and= 5 × 10m/s, the model equations predict the required time (t) for a given conversion. This is illustrated in Figure 10 below,being the remaining variable.

Since the average gas-solid contact time in the CFB-riser is between 2.5 and 3 s and

MR

-values exceed 500, very high SO2-removal efficiencies are predicted.

3. The effect of CaO-particle size is important. For e.g.,

MR

= 400,

kg

= 300 m/s,

De

= 10'7 m2/s, the required contact time is between 2 sec (for 90% SO2 removal) and 3 sec (for 98% SO2 removal) when using 25 µm sorbent particles. Since for a continuous reaction system, required times are proportional with the particle size, these required contact times need to be multiplied by 2, respectively 4, when using sorbent particles of 50 or 100 µm.

Clearly, operating with coarser CaO-particles, increases the required reaction time for a required conversion. Commercial Ca(OH)2 normally has a particle size <<74μm, with an average around 40 μm: efficiencies well in excess of 95% can then be expected in the CFB.

Since particles in a CFB are subjected to attrition, their particle size will progressively decrease. They will be carried out of the system when their particle size is lower than the cut-size of the CFB cyclone [ 42 ]. The attrition will not affect the gas-solid contact mode, since the bulk CFB bed material will either be an inert powder (e.g., sand), and fresh reactant is continuously added. However, the reaction rate for small particles is inversely proportional to the particle size. Finer particles will therefore be more rapidly converted, thus providing a safely margin towards the required reaction time predicted by the model on the basis of the average particle size.

Are you interested in learning more about Desulphurization Pump export? Contact us today to secure an expert consultation!

2 removal rate over the range of operating conditions of the UPM-Kymmene (UK) Ltd (Caledonian paper mill, Irvine, Ayrshire, Scotland, UK) application the correspondence of predicted and measured removal yields is illustrated in

kc

at a conservative 0.03 m/s).

4. When using the model equations to predict the SOremoval rate over the range of operating conditions of the UPM-Kymmene (UK) Ltd (Caledonian paper mill, Irvine, Ayrshire, Scotland, UK) application the correspondence of predicted and measured removal yields is illustrated in Figure 11 (withat a conservative 0.03 m/s).

A very fair agreement is obtained. The limited over/or underestimation might be due to the

kc

-value taken at 0.03 m/s (at

kc

= 0.025 m/s, the predicted removal efficiencies decrease on average by about 0.2%); a slight overestimation of the reaction time, and/or the use of an average particle size of 40 μm: since the lime used has a wide size distribution and decreases due to attrition, the average particle size can be below 40 μm.

The experimental and model comparison however stresses the reliability of the model approach.

3-filler, with commonly quoted efficiencies of >99.9% [2 removal plants. In these applications, a CaCO3 circulating bed is used. At an average conversion of 50%, the CaCO3-content of the bed can be assumed as 50%.

MR

values in this case vary between and 14,000 for SO2 = 600 ppmv and U decreasing from 6 to 3 m/s respectively. For SO2 = 400 ppmv the

MR

-values increase to 11,000 and 21,000 respectively at 6 and 3 m/s.

This was a further assessed for the case of using CaCO-filler, with commonly quoted efficiencies of >99.9% [ 38 ], and widely applied in the Lurgi CFB-SOremoval plants. In these applications, a CaCOcirculating bed is used. At an average conversion of 50%, the CaCO-content of the bed can be assumed as 50%.values in this case vary between and 14,000 for SO= 600 ppmand U decreasing from 6 to 3 m/s respectively. For SO= 400 ppmthe-values increase to 11,000 and 21,000 respectively at 6 and 3 m/s.

It is hence clear that SO2 removal efficiencies in a CFB-riser are excellent and are achieved by a simple direct contact between the Ca2+ reactant and SO2.

Flue gas desulfurization towers are commonly used equipment in coal-fired power plants and industrial processes to remove sulfur dioxide from flue gas. Selecting the appropriate pumps for these towers is a critical factor in ensuring their stable and efficient operation. This article will discuss the types of pumps suitable for flue gas desulfurization towers, highlighting their characteristics and advantages.

The Need for Pumps in Flue Gas Desulfurization Towers: Flue gas desulfurization towers are widely employed in industrial applications, where they play a vital role in reducing environmental pollution by absorbing and converting sulfur dioxide gas into solid or liquid forms using oxidizing and absorbing agents. Pumps are essential for conveying absorbents, oxidizing agents, and waste liquids, ensuring the proper functioning of the desulfurization tower. Choosing the appropriate pumps for flue gas desulfurization towers is crucial for achieving efficient and clean operations.

Types of Suitable Pumps: The following are several commonly used pump types suitable for flue gas desulfurization towers:

1.Centrifugal Pumps: Centrifugal pumps are one of the most widely used pump types. They offer stable flow rates and pressure characteristics, making them adaptable to the varying operating conditions within flue gas desulfurization towers. Centrifugal pumps are typically made of corrosion-resistant materials to withstand the corrosive nature of the chemicals involved.

2.Submersible Pumps: Submersible pumps are directly installed in the liquid and can reduce the pumping head, minimizing suction requirements. In flue gas desulfurization towers, submersible pumps are commonly used for handling waste liquids containing suspended particles. These pumps provide excellent sealing performance, enabling them to handle high-concentration and corrosive liquids.

3.Screw Pumps: Screw pumps feature large capacities and low pulsation, making them suitable for conveying high-viscosity and concentrated absorbents. Screw pumps provide stable flow rates and pressure within flue gas desulfurization towers and have good carrying capacity for solid particles.

4.Characteristics and Advantages: When selecting pumps suitable for flue gas desulfurization towers, the following characteristics and advantages should be considered:

5.Corrosion Resistance: Given the corrosive nature of liquids and gases in flue gas desulfurization towers, pumps should be constructed from corrosion-resistant materials, such as stainless steel and high-alloy steel, to ensure long-term operational stability.

6.High Efficiency: Pumps should possess high conveying capacity and stable flow control to adapt to the varying operating conditions within flue gas desulfurization towers. Efficient pumps enhance operational efficiency, reduce energy consumption, and minimize maintenance costs.

7.Reliability and Safety: Pump reliability and safety are critical in flue gas desulfurization towers. Pumps should have excellent sealing performance, stable operation, and automatic protection functions to prevent leaks and failures, ensuring a safe working environment.

8.Maintenance and Operational Convenience: Pump design should consider ease of maintenance and operation, facilitating cleaning, repairs, and component replacements. This helps reduce downtime and enhances operational efficiency.

Selecting suitable  flue gas desulfurization towers pumps is essential for ensuring efficient and environmentally friendly operations. Centrifugal pumps, submersible pumps, and screw pumps are commonly used and offer advantages such as corrosion resistance, high efficiency, reliability, and operational convenience. When choosing pumps, specific operating conditions and requirements should be considered, taking into account these characteristics to ensure the stable operation of flue gas desulfurization towers and environmental protection. By selecting the appropriate pumps, we can effectively reduce sulfur dioxide emissions, protect the environment, and achieve sustainable development.

If you want to learn more, please visit our website Marine Dredging Pump wholesaler.