In the initial stage of the pre-hydrogenation unit, the raw material contains more chlorine, which causes some equipment to be corroded. The reaction system of the unit adopts a step-down operation, and the pressure of the control separator does not exceed 3.0 MPa. In this expansion and reconstruction, In order to control harmful substances, especially chlorine and sulfur, within the required range under the condition that the device circulating hydrogen compressor is not replaced, a pre-hydrogenation reactor (specification Φ2100mm×4700mm) is added, which is the same as the original one. The reactors were used in series, and two reactors were charged with 12tLY29302 domestic hydrotreating catalyst. The platinum reforming unit platinum reforming unit originally used UOP R232 reforming catalyst to treat hydrorefined naphtha and hydrocracked naphtha. After the expansion, the platinum reforming unit adopts UOP R2132 reforming catalyst, which improves the liquid hourly space velocity of the reactor, reduces the hydrogen oil molar ratio, and improves the processing capacity without changing the reactor and the recycle gas compressor. 30%. In order to meet the requirements of capacity expansion, the platinum reforming unit has undergone the following major modifications: (1) Adding a heating furnace with a thermal load of 82.18 GJ/h as a new feed No. 1 heating furnace. The radiant chamber furnace tube adopts U-shaped tube, the material of the furnace tube is Cr9Mo, and the material of the collecting tube is Cr2Mo1. There are three sets of coils in the convection section: one set is steam generator coil, which is used to generate high pressure steam of 3.4MPa and 390°C, gas production It is 19.67t/h; one set is a superheated steam coil; one set is a boiler feed water preheating coil. (2) The original No. 1 and No. 2 reaction heating furnaces were used in series, and used as the No. 2 reaction heating furnace after reform (heat load was 72.27 GJ/h). The furnace tubes of the original No. 3 and No. 4 reaction heating furnaces were lengthened and the wall was modified to increase the heat load to 56.89 GJ/h and 53.25 GJ/h, respectively. After the catalyst continuous reforming unit reforming unit is expanded, the carbon content of the catalyst is increased from 5% to 6.5%. In order to improve the scorch ability of the regenerator, the inner and outer nets of the catalyst regenerator are lengthened by 300 mm to increase the charred area. Increasing the scorch ability by about 5%. Three thermocouples were added in the transition section to monitor the temperature in the area. The charred area was 6 and the chlorination zone was 4. Other transformation contents The dechlorination tower after the pre-hydrogenation reaction was originally made of 10MnR, which was not resistant to high temperature, and was placed between the last two reaction in and out of the heat exchanger. The modified dechlorination tower is made of 16Mo5 and placed at the outlet of the prehydrogenation reactor to increase the adsorption capacity of the dechlorination agent and increase the specification of the dechlorination tower (Φ2600mm×11000mm). In addition, a new refrigeration compressor system is added, which is used interchangeably with the original system. A dechlorination tower is added to treat the HCl in the top gas of the reforming depentanizer tower to reduce the blockage of the ammonium burner to the burner of the furnace. The load of the deheptane column rectification section reached 83% of the flood point load, and the operation flexibility was small. In the transformation, the rectification section trays were all replaced, and the number of openings was increased to 1524. After the reforming of the reforming device, the calibration is the main technical and economic indicators of the device after the reform. Under the guidance of UOP experts, the reforming device was calibrated, and the pre-hydrogenation and regeneration devices were also evaluated for high-load operation. The guaranteed value of UOP to the device is: hydrogen production of 4.933t/h (corresponding to hydrogen yield of 2.82%), total aromatics of 111.615t/h (corresponding to aromatics yield of 63.88%), and R2132 catalyst dust of 25kg/d ( This corresponds to 0.11% of the catalyst circulation rate). The processing capacity of the calibration condition reforming unit is 170488kg/h (227.99m3/h), which has reached 98% of the design load; the mass space velocity is 1.35h-1, the volumetric space velocity is 0.976h-1; the circulating gas flow rate (standard The state is 113497 m3/h; the separator temperature is 33 ° C, and the pressure is 0.72 MPa; the inlet and outlet pressures of the compressor are 0.712 and 1.10 MPa, respectively. See the operating conditions of each reactor. The composition and properties of the raw materials for calibration and design are listed. About 60% of the feedstock used during the calibration of the reformer is from the heavy naphtha of the hydrocracking unit, 40% from the composition and properties of the feedstock, the target value of the design value group /% of the deparaffin bottom of the alkane prehydrogenation unit. oil. The aromatic content of the raw materials in the raw materials is 12.33 percentage points higher than the designed value; the impurity content and the ASTM 2D86 distillation range meet the requirements. See the material balance of the material balance reformer. Its input and output are basically balanced, and the recovery rate is 99.45%. Conclusion After nearly two years of operation and calibration data, the expansion of the continuous reforming unit of the aromatics plant of Yangzi Petrochemical Co., Ltd. was successful. By the end of June 1999, the equipment had accumulated 2.2734 Mt of raw materials and 85.93 batches of regenerated catalyst. The performance of the catalyst after regeneration was able to reach the design index. The cumulative life of R2132 catalyst was 14.93 t/kg. Cas 61788-45-2,Tallow Amine Structure,Tallow Amine 61788-45-2,Hydrogenated Tallow Alkyl Amines Sichuan Yibin United Import & Export Ltd. , https://www.ybund.com