| The problems that the C5 contents some useful C6, C9~ contents some useful C8 and that the loss of C6梸C8 is too much, etc., are resolved in this paper. These problems usually exist in the petroleum cracking hydrogenating equipment of Qilu petroleum ethylene plant . The mathematical and thermal models for depentanizer tower (H-DA-1O1) and BTX tower (H-DA-102) are built up to make simulating calculation and analysis. The interfaces of the software of the equipment抯 simulating calculation are developed by 慥isual Basic language. Meanwhile, the analysis of operation flexibility is also carried on, connecting with the calculation of tray liquid dynamics. The conclusions of this thesis are as follows: (1)The mathematical , thermal models and the representative components that are chosen for the pre-distillation condition are fundamentally correct. (2) The calculation results of the mathematical mode] for the pre-distillation have been consistent well with the designed values, though they have certain deviation with the actual values for many reasons While generally speaking, the calculation results can still reflect the real production conditions. (3)The dominant reason for the loss of C6 in H-DA-101 tower is that the volume of the flow-out on top of the tower is too large. (4) The dominant reason for the loss of C8 in H-DA- 102 tower is that the back-flow rate is too small. (5)The interfaces of the simulating system are easy to understand , and have also made the operations simple. When the operators are making simulating calculations and do results analysis , they can easily complete the whole operation on the visual forms, without facing a lot of computer programs themselves (6)The methods for the tray liquid dynamics analysis and the corresponding operation flexibility analysis of the tower are not only simple but also have certain utility, which providing some fundamental values and theoretical methods for the operation adjustment and the innovation of the tower for promoting production. |
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