Condensers inlet, outlet temperature

The following parameters were then fixedi Glycol contactor inlet temperature Condensate cooler outlet temperature Water content of the gas from the glycol contoctor Maximum free woter content of treated condensate... 

These include undersized surface condenser area, water-side fouling, lack of water flow, condensate backup, leaking seal strips around the air baffle, and excessive cooling-water inlet temperature. To determine whether a poor vacuum in a surface condenser is due to such heat-transfer problems, plot the surface condenser vapor outlet temperature versus pressure on the chart shown in Fig. 25.4. If this point is on or slightly below the curve, it is poor heat transfer in the surface condenser itself that is hurting the vacuum. 

The condensing water temperature has an important effect on steam rate per refrigeration effecd, rapidly decreasing with colder condenser cooling water. Figure 11-108 presents data on steam rate versus condenser water inlet for given chiUed-water outlet temperatures and steam pressure. 

Thermocycle capacity is a function of the temperature difference between the chilled-water outlet temperature leaving the cooler and the inlet condenser water. The cycle finally stops when these two temperatures approach each other and there is not sufficient vapor pressure difference to permit flow between the heat exchangers. 

Environment Internal A mixture of steam, condensate, hydrogen, nitrogen, and carbon dioxide outlet temperature 165°F (75°C), inlet temperature 265°F (130°C), condensate pH 10... 

Condensing range - hydrocarbon inlet temperature to condensing zone minus hydrocarbon outlet temperature from condensing zone. 

In order to adequately describe the size of a heater, the heat duty, the size of the fire tubes, the coil diameters and wall thicknesses, and the cor lengths must be specified. To determine the heat duty required, the maximum amounts of gas, water, and oil or condensate expected in the heater and the pressures and temperatures of the heater inlet and outlet must be known. Since the purpose of the heater is to prevent hydrates from forming downstream of the heater, the outlet temperature will depend on the hydrate formation temperature of the gas. The coil size of a heater depeiuLs on the volume of fluid flowing through the coil and the required heat duty. 

The secondary air from the compressor must be cooled before mixing with the process gas stream at the absorber inlet to keep the absorber inlet temperature as low as possible. Take the outlet temperature as the same as exit gases from the cooler condenser, 40°C. 

The temperature difference between inlet and outlet temperature at the coil(s) of the refrigerant should be smaller than 1 °C (AT < 1 °C), to ensure a uniform condensation on the total coil. On warmer areas no ice will condense until the temperature at the ice surface has increased to the warmer temperature on the coil. For large surfaces it is necessary to use several coils or plates in parallel, each of which must be separately temperature controlled. If the condenser is operated in an overflow mode, the weight of the liquid column should not change the boiling temperature of the liquid at the bottom of the column measurably. 

Cooling water inlet and outlet temperatures are 80 and lOS F, respectively. The condenser heat transfer area is 1000 ft. The cooling water pressure drop through the condenser at design rate is 5 psi. A linear-trim control valve is installed in the cooling water line. The pressure drop over the valve is 30 psi at design with the valve half open. 

I now observed that the surface condenser cooling-water outlet temperature had increased from 100 to 135°F. This is a sign of loss of cooling-water flow. As none of the other water coolers in the plant had been affected, I concluded that the cooling-water inlet to my surface condenser was partly plugged. 

A 1-L, 3-necked, round-bottomed flask was equipped with magnetic stirrer, pressure-equalizing addition funnel with N2 inlet, low temperature thermometer, and a Friedrich condenser with N, outlet. The outlet was attached to two traps in series. The first was cooled in a Dewar of salt/ice water (- 15 C) and the second in a Dewar of dry ice/i-PrOH (— 78 C). 2-Bromo-3,3,3-trifluoropropene (50 g, 0.286 mol) and hexane (250 mL) were added to the flask. 1.6 M BuLi in hexane (190 mL, 0.304 mol, commercial) was added to the addition funnel. The flask was cooled with a hexane slush bath by addition of liquid N2 until the temperature of the solution inside the flask was - 85 °C. Then the BuLi soln was added over a period of 25 min at such a rate that the temperature remained below - 80 C. The slightly cloudy, yellowish solution was allowed to stir for an additional 10 min. Then, the hexane slush was removed, Upon reaching - 30 C, a gelatinous precipitate formed and the temperature rapidly rose to 28 "C. The volatile product was removed from solution by heating the mixture at reflux for 30 min with a slow flow of N2 through the system. The product was obtained from the dry ice trap yield 21 g (97%). 

Water is heated by passing it through a steam-heated kettle (Fig. 7.78) at a mass flowrate w. The inlet and outlet temperatures of the water are 9, and 9 respectively. Steam condenses in the jacket of the kettle at a temperature 0, and a pressure f. It is intended to control the temperature of the water by placing a temperature sensor in the water in the kettle and using this measurement to manipulate the flow of steam to the kettle jacket. In order to tune the controller it is necessary to derive the transfer functions relating 0o to 0j, 0, and w. 

Let us also mention that the temperature drop depends only on pressure differential inlet - outlet and does not depend on the inlet pressure value. So, in principle the unit can work with reasonably low initial pressure to achieve low temperatures. Here we do not bother ourselves with the dependence of condensation process intensity on pressure value. 

Determine the tube-side inlet and outlet temperatures on a scale with increasing heat transfer as the liquid condenses and the temperature decreases. This... 

A simple but common heat exchanger application in a chemical process plant is cooling a hot liquid or gas product from the process (called the process fluid ) to a temperature low enough that it can be safely stored. The coolant is likely to be air or water, which would be heated in the heat exchanger. If none of the fluids involved reach their boiling or condensing temperatures, no phase change occurs, and the process fluid is sensibly cooled and the coolant sensibly heated. A heat balance relates the inlet and outlet temperatures, the specific heats, and the mass... 

Where Q = Heat-Transfer Rate Fs = Steam Mass Flow AHs = Latent Heat of Vaporization F = Feed Rate Cp = Heat Capacity of Feed T0 = Steam Supply Temperature Pt = Steam Supply Pressure P2 = Steam Valve Outlet Pressure Ps = Condensing Pressure Tj = Inlet Temperature T2 = Outlet Temperature A Tm = Log Mean Temperature Difference Ts = Condensing Steam Temperature... 

A condenser consists of 30 rows of parallel pipes of outer diameter 230 mm and thickness 1.3 mm with 40 pipes, each 2 m long in each row. Water, at an inlet temperature of 283 K, flows through the pipes at 1 m/s and steam at 372 K condenses on the outside of the pipes. There is a layer of scale 0.25 mm thick of thermal conductivity 2.1 W/m K on the inside of the pipes. Taking the coefficients of heat transfer on the water side as 4.0 and on the steam side as 8.5 kW/m2 K, calculate the water outlet temperature and the total mass flow of steam condensed. The latent heat of steam at 372 K is 2250 kJ/kg. The density of water is 1000 kg/m3. 

Reverse-flow operation for Sulfur Production over Bauxite Catalysts by the Claus Reaction has been considered in Refs 9 and 31. The rate of H2S oxidation by SO2 on bauxite catalysts is very high even at ambient gas inlet temperature, but sulfur condensing at low temperatures blocks the active catalyst surface, and the reaction stops because of catalyst deactivation. In a reverse-flow reactor the periodic evaporation of condensed sulfur from the outlet parts of the catalyst bed occurs. Although it is difficult to remove all the sulfur condensed within the catalyst pellets at the bed edges, after a certain time a balance between the amount of sulfur condensed and evaporated is attained. Using a reverse-flow reactor instead of the two-bed stationary Claus process provides an equal or better degree of... 

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