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Li Q.,Luoyang Petrochemical Engineering Corporation
Petroleum Refinery Engineering | Year: 2012

As the size of spherical tanks becomes increasingly larger, the steel material requirement and the dimensions of tank pedal plates have become increasingly bigger, which results in a number of difficulties in petal plate forming, transportation, side lifting installation and welding, etc. It is necessary to design the spherical tanks based upon analysis design methods under the conditions of higher requirements in intrinsic safety of spherical tanks' construction and load. The integral stress calculations have been made for 4 loads of different load combination tanks and 2 structures. The force exerting on the spherical tanks at different loads are studied and stresses at the connections between supports and tanks are analyzed. It is concluded that, all stresses should be calculated based upon all possible loads combination, the central model and bestraddle model should be established for load calculation, the maximum stress should be at the connection between support and tank smooth transition should adopted and hexahedral element analysis should be applied for finite element analysis. Source


Li W.,Luoyang Petrochemical Engineering Corporation
Petroleum Refinery Engineering | Year: 2013

The sources and forms of sulfur in MTBE are introduced. The sulfur concentration in LPG fractionation unit and MTBE unit are analyzed and concentration cycle concept is presented. When FCC gasoline, reformate and MTBE are the blending components of gasoline, the blending ratio of reformate to MTBE shall be 2. 1/1 ∼5. 3/1 to meet the 10 μg/g mass percentage of sulfur in blending gasoline. Based upon the gasoline quantity and quality of a refinery in China, the blending of Guo V 95 gasoline is simulated using PIMS computer program. The addition of MTBE and addition of reformate of different sulfur mass percentages are calculated. When the sulfur mass percentage of MTBE is the same as that of objective sulfur mass percentage of FCC gasoline and Guo V gasoline, the MTBE addition is maximum, the blending is the most flexible and economic benefits is the highest. The addition of reformate increases with increase of sulfur mass percentage of MTBE, and addition of MTBE is gradually minimized (1.5%). The controlled objective sulfur mass percentage of MTBE is affected by the sulfur mass percentage of FCC gasoline. When the minimum MTBE addition is 8%, the sulfur mass percentage of gasoline is lowered to 8 μg/g from 10 μg/g, and the controlled objective sulfur mass percentage of MTBE increased to 30 μg/g from 12 μg/g. Whereas, reducing the sulfur mass percentage of FCC gasoline may reduce the octane number of gasoline. The optimization of MTBE feedstocks and optimization of operation of desulfurization unit can reduce the sulfur mass percentage in MTBE to 15 ∼60 μg/g-The application of distillation of MTBE product and distillation of C4s feedstock can lower the sulfur in MTBE to 10 μg/g. The comparison has found that the distillation of MTBE product is superior over distillation of C4s feedstock. Source


Wang H.,Luoyang Petrochemical Engineering Corporation
Petroleum Refinery Engineering | Year: 2015

This paper introduces the status quo of low-temperature waste heat utilization of refineries and the development, technical features and developing trend of low-temperature multi-effect evaporation seawater desalination (LT-MED) process. In a case study of a refinery, the scheme and economy of LT-MED technology for the utilization of waste heat are analyzed and studied. It is concluded that the recovery water temperature in the low-temperature waste heat recovery system of petrochemical company is generally 95 ∼ 100 °C and the heat temperature is generally 65 ∼ 70 °C, which meet the operation requirements of MED; The cost of primary desalted water produced by MED technology is generally 4 ∼ 6 Yuan/m3, and the price of the refinery primary desalted water is generally higher than the 7 Yuan/m3. The construction of MED system based on the desalted water demand will have a good benefit.. Source


Liu N.,Luoyang Petrochemical Engineering Corporation
Petroleum Refinery Engineering | Year: 2015

It is known from analysis of simulation results of a 2. 0 MM TPY hydrocracking unit that the flash points of kerosene and diesel only fluctuate 0 ∼ 2 ∼C when fractionator is flushed by different flowrates (0.5 ∼7 t/h) of steam, hydrogen or nitrogen at the same conditions. These three gases can be used as the fractionator flush medium if only their impact on products flash point is considered. As compared with hydrogen, the use of steam as flush gas for the fractionator bottom can raise fractionator bottom temperature by 18 ∼ 41 °C and reduce the fractionator diameter by 200 ∼ 1 200 mm, which are favorable for heat exchange and the reduction of investment and operation cost of fractionators. As compared with nitrogen, steam has the advantages of minimized impact on product oil storage and transportation and easy recovery and reutilization. Therefore, steam is the most suitable flush medium for fractionators in the three gaseous mediums. In addition, the low-pressure and high superheated temperature (no higher than 425 °C) conditions should be selected for the steam, and its flowrate should be selected in the areas where the initial boiling point of bottom product rises rapidly. In this case, the fractionation precision requirement is achieved, and the unit energy consumption is decreased. Whereas, with the upgrading of product oils and off-specification of water in product oils, effective dehydration equipment, flush medium and process technologies should be developed. Source


Shicheng Z.,Luoyang Petrochemical Engineering Corporation
Petroleum Refinery Engineering | Year: 2015

The reactor in DMTO unit and the regenerator in FCCU have a lot of unused space in dilute phase. If 3rd-stage cyclone is installed in it and the gas outlet of the 2nd-stage cyclone is welded with the cylinder of the 3rd-stage cyclone, the dust-laden gas can directly flow into the 3rd-stage cyclone; The dust in the pipe can be discharged at the top of the 3rd-stage cyclone and instead of at bottom in conventional practice. The installation of internal 3rd-stage cyclone is low in investment, small in plot area requirement, high in separation efficiency and reduced in air pollution. The installation of 3rd-stage cyclone has also reduced the requirements of pipe elbows, lowered the pressure drop and minimized the energy consumption. Its risk of safe operation is no greater than that of independent external cyclone. Source

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