Energy utilization

When steam is generated, energy should be utilized effectively. But there are several issues here: 1. What is the heat transfer coefficient of cracked tail oil? 2 The viscosity-temperature properties of the catalytic cracking residue oil; 3 The heat capacity of the catalytic cracking residue oil. If these issues are overcome, then steam generation should be possible. As for the issue of unstable traffic, I don’t think that’s the reason. One of the key reasons why the overall energy consumption of refineries abroad is much lower than that in China is the careful optimization of energy use in the production processes. Personal thoughts!

1 Heat transfer coefficient of catalytic cracking tail oil 2 Viscosity-temperature behavior of catalytic cracking tail oil 3 Heat capacity of catalytic cracking tail oil? Before entering the air cooler, the tail oil still passes through the reboiler at the bottom of the jet fuel tower as well as undergoes heat exchange with the feed oil. The three conditions mentioned above, namely 1 and 3, should be satisfied. I think the viscosity-temperature properties will allow it to pass through the air cooler smoothly; so will it be very difficult for it to pass through the heat exchanger?

The hydrogenated tail oil from our unit first enters a heat exchanger to heat the light fractions, and then serves as a heat source for the reboiler. I believe this approach is feasible and can be used as a technical improvement during maintenance; it generates steam at 1.0 pressure which is then fed into the pipeline network. This way, fluctuations will not be significant, as the amount of steam produced is not substantial compared to the overall needs of the plant’s pipeline network. Moreover, when steam at 1.0 pressure is unavailable, the steam produced internally can be used, and the advantages outweigh the disadvantages

I have some questions regarding those on the upper floor: can it reach a maximum temperature of around 230 degrees, and can it generate steam at 1.0 MPa? I asked the technician today, and he said it’s possible to achieve 0.4 MPa, but additional equipment is needed. He said he doesn’t know yet how to utilize this energy – quite unexpected!

The relationship between the saturated vapor pressure of steam and temperature: Saturated vapor pressure (absolute pressure), Saturated vapor temperature. MPa, Kg/cm2, °C; MPa, Kg/cm2, °C. 0.0098, 0.1, 45.45; 2.744, 28, 228.98; 0.046, 0.5, 80.86; 2.94, 30, 232.76; 0.098, 1, 99.09; 3.43, 35, 241.41; 0.147, 1.5, 110.79; 3.92, 40, 249.18; 0.196, 2, 119.62; 4.41, 45, 256.21; 0.245, 2.5, 126.75; 4.9, 50, 262.7; 0.294, 3, 132.88; 5.39, 55, 268.69; 0.343, 3.5, 138.19; 5.88, 60, 274.3; 0.392, 4, 142.92; 6.37, 65, 279.53; 0.441, 4.5, 147.2; 6.86, 70, 284.47; 0.49, 5, 151.11; 7.35, 75, 289.16; 0.588, 6, 158.08; 7.84, 80, 293.16; 0.686, 7, 164.17; 8.33, 85, 297.85; 0.784, 8, 169.61; 8.82, 90, 301.91; 0.882, 9, 174.53; 9.31, 95, 305.8; 0.98, 10, 179.04; 9.8, 100, 309.53; 1.176, 12, 187.09; 10.78, 110, 316.58; 1.372, 14, 194.13; 11.27, 115, 319.86; 1.568, 16, 200.43; 11.76, 120, 323.31; 1.764, 18, 206.15; 12.74, 130, 329.31; 1.96, 20, 211.39; 13.72, 140, 335.1; 2.15, 22, 216.24; 14.7, 150, 340.57; 2.352, 24, 220.76; 15.19, 155, 343.16; 2.548, 26, 224.99; 15.68, 160, 345.75. As can be seen from the table above, the saturated vapor temperature at 1.0 MPa is approximately 185 degrees Celsius; therefore, the temperature required for heat exchange should be around 190 degrees Celsius, resulting in incomplete utilization of the energy in the residual oil. There is another issue here regarding the injection of water into the reaction effluent: the pressure is around 14.7 MPa and the temperature is around 140 degrees, while the temperature of saturated steam is 340 degrees. How can it be that a portion of the water vaporizes? It seems to be 20%; is the vapor pressure of water only around 0.4 MPa? This post was last edited by zndong666 on 2009-3-27 19:30.]