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Zheng Q.,Sinochem Quanzhou Petrochemical Co. | Mu Y.,Sinochem Quanzhou Petrochemical Co. | Chen X.,Sinochem Quanzhou Petrochemical Co.
Petroleum Processing and Petrochemicals | Year: 2015

The analysis indicates that the abnormal phenomena of quench tower, SO2 concentration in flue gas and hydrogenation system during the commissioning of No. 2 tail gas treatment system for sulfur recovery is due to the activity decline of the hydrogenation catalyst. It is found that the reason for hydrogenation activity losing is due to the bias current in catalyst bed. Effective measures are then adopted, including sealing part of the reactor entrance opening, adding porcelain ball screen mesh at the top of the catalyst bed and adjusting the operation of the reactor system. The bias current in the catalyst bed is thus controlled effectively and the hydrogenation activity improves significantly by these measures, resulting in smooth operation of the tail gas system of the sulfur recovery unit. © 2015, Research Institute of Petroleum Processing, SINOPEC. All rights reserved.

Lu M.,Sinochem Quanzhou Petrochemical Co. | Song S.,Sinochem Quanzhou Petrochemical Co. | Yang T.,Sinochem Quanzhou Petrochemical Co. | Cui X.,Sinochem Quanzhou Petrochemical Co.
Petroleum Processing and Petrochemicals | Year: 2015

LS-951T catalyst developed by Research Institute of Qilu Petrochemical Company is a new hydrogenation catalyst for treating sulfur recovery tail gas. LS-951T catalyst, with the advantages of uniform distribution of active components, light bulk density and high hydrogenation activity, has a good applicability. The properties of the catalyst and the commercial processes of catalyst loading, presulfurization in a 380 kt/a sulfur recovery tail gas unit in SINOCHEM Quanzhou Petrochemical Co., Ltd. were described. The performance of the catalyst was examined and compared in low and high load operation case. The loading pattern of LS-951T catalyst was modified because it's easy to flow in the later case. The application results after modification of loading show that the catalyst presents good hydrogenation activity ever if in high load case. The SO2 content is less than 300 mg/m3 in the treated gas, lower than the country's emission standard of 960 mg/m3.

Zhang Q.,Sinochem Quanzhou Petrochemical Co. | Meng X.,Sinochem Quanzhou Petrochemical Co. | Sun S.,Sinochem Quanzhou Petrochemical Co. | Zhou H.,Sinochem Quanzhou Petrochemical Co.
Petroleum Processing and Petrochemicals | Year: 2015

The industrial applications of the positive ion resin catalyst Amberlyst 35 in FCC light gasoline etherification unit of A and B companies were introduced. The results indicate that the catalyst has outstanding characteristics of high activity and simple starting-up. Both A and B company can produce low olefin and premium etherified gasoline over the catalyst. By a three-stage etherification, the total conversion rates of isoamylene are 97. 59%, 95. 54% and the selectivities of tertiary amyl methyl ether (TAME) are 93. 48%, 97. 15% under the working conditions of case I and case II, respectively in company A. The total conversion rate of isoamylene is 97. 21% and the TAME selectivity is 87. 15 % in company B.

Jian C.,Sinochem Quanzhou Petrochemical Co.
Petroleum Refinery Engineering | Year: 2013

Salt will deposit on the blades of recycle hydrogen compressor of residue hydrogenation unit in the refinery after operation for a period of time, which will produce eccentric force and vibration on compressor rotor or even lead to shutdown of the compressor in serious case. An unscheduled shutdown of a centrifugal compressor in a 1. 5 MM TPY residue hydrogenation unit is introduced, and the causes of salt deposit on compressor are analyzed. Measures for preventing salt deposition in unit operation are presented, such as stabilizing reactor operation, application of stainless steel for equipment upstream of recycle hydrogen compressor, control and reduction of oxygen in desalted water, strict control of amount and temperature of amine liquid, timely cleaning of fouling in the equipment and pipelines upstream of recycle hydrogen compressor and good control of liquid level and interface of cold HP separator.

Zhong J.,Sinochem Quanzhou Petrochemical Co. | Chen L.,Sinochem Quanzhou Petrochemical Co. | Meng X.,Sinochem Quanzhou Petrochemical Co.
Petroleum Refinery Engineering | Year: 2013

The chemical compositions of process condensate water from hydrogen generation plant is analyzed, and the recovery process for the process condensate water is introduced. The condensate water recovered from bottom of stripper can not be directly utilized because of its higher total Fe ions which can easily contaminate the pipelines and make the steam produced off-specifications. When the total Fe ions in the bottom condensate does not exceed 100 ppm, it can be treated in deaerator and with chemicals and used as the boiler feed water. 8. 74 × 104 tons of steam is directly drained from tower overhead and the annual loss is 1 048. 3 × 10 4 RMB ¥. When the steam is recovered and supplied for steam reformer, the hydrogen yield can be improved and energy consumption can be reduced, which is the most practical scheme for the utilization of condensate water of the unit.

He L.-N.,Sinochem Quanzhou Petrochemical Co. | Ge X.,Sinochem Quanzhou Petrochemical Co.
Xiandai Huagong/Modern Chemical Industry | Year: 2013

For slide valve malfunction of the regenerated catalyst used in catalytic cracking unit, the slide valve malfunction phenomenon, analysis and the solution are given in this paper.

Ding W.,Liaoning University | Ding W.,China University of Petroleum - Beijing | Zhao Y.-P.,Liaoning University | Wan C.,Sinochem Quanzhou Petrochemical Co. | Zhao D.-Z.,Liaoning University
Xiandai Huagong/Modern Chemical Industry | Year: 2016

A novel combined process of hydrotreating and FCC for residue oil is introduced in this paper. The disadvantages of traditional hydrogenation for residue oil and the superiority of combined process of hydrotreating and FCC are simply explained. The metal impurities are removed from the residue in the fixed-bed reactors. Then the clean fuel with ultra-low sulfur are producd through a separately hydrotreating step to improve the content of hydrogen for the FCC heavy diesel. The optimum conditions in one-stage hydrogenation section are determined as: 6.5 MPa of the pressure, 400℃ of the temperature, 1.6 h-1 of the space velocity and 600:1 of the ratio of hydrogen to oil. Under the optimal conditions, the hydrogenation by combined process of hydrotreating and FCC is the best. The liquid yield of final products reaches 91.76%. The average removal rates of HDM, HDS, HDN and HDCCR are 94.00%, 89.01%, 62.22% and 90.35%, respectively. © 2016, China National Chemical Information Center. All right reserved.

Ren G.-Q.,Sinochem Quanzhou Petrochemical Co. | Feng W.-X.,Sinochem Quanzhou Petrochemical Co.
Xiandai Huagong/Modern Chemical Industry | Year: 2012

In order to shorten the start-up time of the residual oil hydrogenation plant during renewing the catalyst, the key influencing factors on start-up time are identified. The limitations elements in the elevating temperature and pressure process of the system are analyzed.The optimized method is given.After optimization, the start-up time can shorten 48 h.

Ren G.,Sinochem Quanzhou Petrochemical Co. | Yu C.,Sinochem Quanzhou Petrochemical Co. | Feng W.,Sinochem Quanzhou Petrochemical Co.
Petroleum Processing and Petrochemicals | Year: 2016

The wax oil as a sulfidation agent carrying oil was firstly used for residue hydrotreating catalysts at both high and low temperature presulfidation process in a commercial unit. The method avoids the switching between diesel and wax oil in conventional presulfidation process, thus shortening start-up time more than 20 hours. The fluid distribution in catalyst bed and the activity of the catalysts presulfided by wax oil were analyzed in terms of temperature changes during catalyst wetting, reactor pressure differential, radial temperature difference, and uneven temperature distribution index of bed and compared with the conventional process using diesel as a presulfidation agent carrying oil. It is concluded that the fluid distribution is even in the wax oil presulfidation process and the presulfiding effect meets the process requirements.

Jian C.,Sinochem Quanzhou Petrochemical Co.
Petroleum Refinery Engineering | Year: 2015

The causes of failure of magnetic level meter and differential pressure level meters for a hot high-pressure separator in a 3.3 MM TPY residue hydrotreating unit are analyzed through case study. The analysis indicates that the causes are high liquid level, demagnetization of magnetic float and failure of magnetic level meter, poor heat tracing of differential pressure level meter, and flushing hydrogen unused etc. Measures for the prevention of failure of liquid level meters of hot high-pressure separator are proposed such as application of unused flushing hydrogen, good insulation and heat tracing for level meters, scheduled inspection and testing of magnetic level meter, scheduled switching and testing of level control valve of hot high-pressure separator and stable operation.

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