Sinochem Quanzhou Petrochemical Co.

Quanzhou, China

Sinochem Quanzhou Petrochemical Co.

Quanzhou, China
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Li C.,Northeast Petroleum University | Yu H.,Northeast Petroleum University | Lin Z.,Sinochem Quanzhou Petrochemical Co. | Wang F.,Northeast Petroleum University | And 2 more authors.
Journal of Coordination Chemistry | Year: 2017

Three bidentate salicylaldimine nickel complexes containing different long-chain alkyl groups in their ligand backbone were synthesized in good yield. All the bidentate salicylaldimine ligands and their nickel complexes were fully characterized by FT-IR, 1H NMR, UV spectroscopies, and mass spectrometry. Three bidentate nickel complexes were evaluated as catalyst precursors in ethylene oligomerization. Upon activation with methylaluminoxane (MAO), the catalytic activity was 5.75 × 105 g/(mol Ni·h) and the oligomers were mainly butenes (52.10%) and octenes (32.63%) for bidentate nickel complex with 1-tetradecyl as core in the ligand backbone (R14-complex) using toluene as solvent. However, bidentate nickel complex with 1-octadecyl as core in the ligand backbone (R18-complex) produced mainly octenes (59.38%) and C10 + olefins (29.01%) and the catalytic activity was 2.23 × 105 g/(mol Ni·h). After activation with ethylaluminum sesquichloride (EASC) in toluene, three nickel complexes yielded mainly C10 + products which contained Friedel-Craft alkylated-toluene, and their catalytic activities were above 1.5 × 106 g/(mol Ni·h). For the bidentate salicylaldimine nickel catalysts with hyperbranched molecules as ligand backbones, the solvent and the reaction conditions had a large effect on catalytic activity as well as oligomerization distribution except the structure of the catalyst and the co-catalyst. © 2017 Informa UK Limited, trading as Taylor & Francis Group.

Xue X.,Beijing University of Chemical Technology | Liu J.,Sinochem Quanzhou Petrochemical Co. | Rao D.,Beijing University of Chemical Technology | Xu S.,Beijing University of Chemical Technology | And 4 more authors.
Catalysis Science and Technology | Year: 2017

The selective hydrogenation of benzene is one promising route to obtain cyclohexene, a key intermediate for the production of various value-added fine chemicals. Herein, we report the preparation of a novel Ru/TiO2 catalyst encapsulated by a porous TiO2 coating (denoted as (Ru/TiO2)@p-TiO2) for this reaction, in which the supported Ru particles serve as active sites for hydrogen dissociation while the porous TiO2 surface acts as the active center for benzene hydrogenation. By virtue of the shielding effect of the porous TiO2 layer with a suitable pore size, only hydrogen molecules can diffuse into the interior Ru surface for dissociation adsorption, followed by hydrogen spillover from Ru to the porous TiO2 surface and subsequent hydrogenation of adsorbed benzene there. Cyclohexene temperature programmed desorption (CHE-TPD) and DFT calculations demonstrate that cyclohexene shows a more beneficial desorption and a much higher activation energy for its further hydrogenation over the TiO2 surface in comparison with the Ru surface, accounting for the largely enhanced catalytic performance (benzene conversion: 98.1%, cyclohexene selectivity: 76.6%). This double-active-site synergistic catalysis, to the best of our knowledge, gives the highest cyclohexene yield ever reported. © The Royal Society of Chemistry 2017.

Li C.,Northeast Petroleum University | Wang F.,Northeast Petroleum University | Lin Z.,Sinochem Quanzhou Petrochemical Co. | Zhang N.,Northeast Petroleum University | Wang J.,Northeast Petroleum University
Applied Organometallic Chemistry | Year: 2017

Three hyperbranched salicylaldimine ligands with tetradecyl as core, with hexadecyl as core and with octadecyl as core were synthesized in good yields. These ligands were reacted with cobalt chloride hexahydrate to form three complexes (C1-C3). The compounds were characterized using Fourier transform infrared, 1H NMR, mass and UV spectroscopies and thermogravimetric and differential thermal analyses. The catalytic properties of the hyperbranched cobalt complexes were evaluated for ethylene oligomerization. The effects of solvent and reaction parameters (Al/Co molar ratio, temperature and reaction pressure) on ethylene oligomerization were studied using the cobalt complex C3 as pre-catalyst and methylaluminoxane (MAO) as co-catalyst. Under these conditions ([Co] = 5 μmol, Al/Co = 500, 25 °C, 0.5 MPa ethylene, 30 min), the catalytic activity of complex C3 in toluene was 1.85 × 105 g (mol Co)-1 h-1 and the selectivity for C8+ oligomers was 55.72%. The complex structure also had a significant influence on both the catalytic activity and selectivity. All three cobalt complexes, activated with MAO, showed moderate activities towards ethylene oligomerization and the activity of cobalt complex C1 was up to 1.99 × 105 g (mol Co)-1 h-1. The kinds of metal center of complexes (cobalt complex C1 and nickel complex with tetradecyl as core) and their catalytic properties were investigated in detail under the same conditions. © 2017 John Wiley & Sons, Ltd.

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.

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.

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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