The history of and latest progress in the research on direct oxidation of methane to methanol are reviewed,including gas-phase reaction,gas-solid phase catalytic reaction and gas-liquid phase catalytic reaction.The main trends in this field are also outlined.

Recent research works on gas phase direct epoxidation of propylene on silver catalyst were reviewed,including causes of low selectivity to propylene oxide and the way to the development of high efficiency silver catalyst.

The reaction kinetics and catalyst deactivation kinetics of furaldehyde liquid phase hydrogenation on a Raney cobolt catalyst were studied in a high-pressure batch reactor.Kinetic model of the reaction and catalyst deactiviation was proposed and order,activation energy and rate constant of the reaction as well as rate constant of deactivation were obtained.Service life the cobolt catalyst was also evaluated.

A new method for evaluation of macro-activity of spherical(Co-Mo) and cylindrical (Fe-Cr) CO shift catalyst is proposed on the basis of a concept called Catalystic Reaction Unit.In this method,catalyst particles are arranged regularly in layers,with the space between the particles and layers filled with samll inert particles.Result from catalyst evaluationtests with spherical and cylindrical CO HTS catalysts carried out according to this method show high degree of confudence.Rate constant k_T of the second order reaction obtained from the tests can be used as criterion for macro-activity evaluation of the catalysts.The rate constant value has nothing to do with namber of the catalyst layers.

The B113-2 type CO high temperature shift catalyst was developed for low steam/gas ratio operations in large energy-saving type ammonia plant.As a variation of B113 type HTS catalyst,it not oly has the advantages of B113,such as low bulk density,high strengh,high activity and selectivity,low inherent sulfur content and good water-tolerant property,but can also inhibit F-T reaction.

The Fushun Research Institute of Petroleum and Petrochemical (FRIPP) of SINOPEC has developed 13 type of hydrotreating catalysts which are being used in 64 commercial plants in domestic refineries.The capacity of these plants totals 16.19Mt/a. The article reviews the commercial performance of these catalysts.

Test and industrial industrial application of T907 type carbonyl sulide hydrolysis catalyst used in the purification of high-CO₂ coal gas,carbon monoxide,carbon dioxide and liquid propylene are reported.Tests and industrial use show that the catalyst is suitable for various feedstrocks with high COS conversion and good oxygen-tolerant property.Theoptimal operating temperating temperature ranges are 100-120℃ with gas feedstocks and 15-40℃ with liquid feedstrocks.

The performance of T907 type carbonyl sulfide hydrolysis catalyst and Tc-22 type ambient temperature desulfrizer for ambient temperature liquid phase fine desulfrization of propylene was studied and their industrial application outlined.Bench-scale tests and industrial check run show that these two desulfurizers can effectively remove the sulfides in liquid propylene.When sulfur content in propylene(H₂S+COS) is less than 15ppm,the two desulfrizer arranged in series can cut the sulfur level in propylene down to less than 0.1ppm at 10~40℃,which means theri performance has reached the advanced level of similar products in the world.With excellent performance,simplicity in manufancture,high strength and low cost,then will fing wide use desulfurization of liquid propylene.

This article described the performance of a fine desulfurization technology developed by Kunshan Res Inst Fine Chemicals,which consists of COS hydrolysis catalyst and KT301 type ZnO sulfur absorbent.Its use in ammonia-methanol coproduction has resulted in prolonged service life of methanol synthesis catalyst and thus better economic benefit.

On the basis of study on causes of activity declining and mechanism of resulfiding of Co-Mo wide temperature-range CO shift catalyst,method and scheme for resulfiding treatment of the catalyst were proposed.Performance of the catalyst after resulfiding has proved that this resulfiding technology is feasible and can result in remarkable economic benefit.

Worldwide status of the developments and application of dechlorination agents is reviewed and some suggestions on the development of new dechlorination agents are also made.

Researches on the catalysts,carriers and reaction conditions for the synthesis of HFC-134a from trichoroethylene by gasous phase catalytic fluorination,via HCFC-133a intermediate,were reviewed. The mechanisms of halogen exchange reaction were also outline.It is suggested that AlF₃ supported metal catalysts with higher fluorinating performance and less Gr³⁺ or other metal be developed.

The catalyst for methacrolein oxidation to methacrylic acid was studied.Effect of its K,Cs,Rb,Tl,B and Mo content on the catalytic activity was investigated,respectively.Activity evaluation showed that with respect to catalytic composition Mo_aPb_bV_cCu_dAs_cZ_fO_x,better catalytic activity could be obtioned when a=8~15、b=0.5~2、c=0.08~0.4、d=0.05~0.3、e=0.1~1、f=0.1 and z=K.At reaction temperature of 200℃, when the contents of Mo,B and K are 10,0.1 and 0.08,respectively,the conversion of methacrolein is over 92%,and the yied of methacrylic acid is 74%.

The intrinsic and macroscopic kinetic model of COS hydrolysis over γ-906 catalyst were investigated in a gradientless reactor with internal-recycle under following conditions:30~70℃ ,atmospheric pressure and reducing atmosphere.Multiple regression method was to estimate the parameters of the kinetic model of this system.The established intrinsic kinetic model is as follow:r_cos=4.593×10⁶exp（-35370/RT）y^0.66_COSy^0.06_H2O and the macroscopic kinetic midel is:r_cos=1.025×10⁵exp(-31266/RT)y^0.66_COSy^0.06_H2O 0.66-order and 0.06-order behavior were obersived for COS and H₂O,respectively.

CIP-1 catalyst, a multiple zeolites containing catalyst,is appliced to type Ⅱ(DCC-Ⅱ)deep catalytic cracking process.The catalyst is characterized by producing light isoolefins as well as high octane gasoline.The industrial application of CIP-1 catalyst showed that at reaction temperture of 505℃，gasoline,propylene,isobutylene and isoamylene are 40.98,12.52,4.57 and 5.78wt%,respectively;at reaction temperature of 530℃,gasoline,propylene,isobutylene and isoamylene are 38.45,14.43,4.75 and 5.93wt%,respectively.

The mechanism of ethanol oxo-reaction on Ni-Pb.C catalyst was studied through characterization of the catalyst before and after oxo-reaction with XPS and XRD.The study showed that Ni0 is the ative entre of Ni catalyst;addition of Pb makes more Ni2+ to be reduce Ni0 and thus incress the number of ative centres;H2 has double function of both reduceing Ni2+ and enriching Ni0;CO scatters the enriched metal during reaction while C2H5I stabilizes the dispersed active sites.Addition of Pb narrows the energy gap between oxided and reduced nickel though lelctric charge transfer between support and nickel,promotes circulation of nickel during reaction and enhances the catalytic activitu.

Type Ⅱ deep catalytic cracking process is a new catalytic conversion method for producing propylene and isoolefins and oproducing high octane gasoline from heavy oil.The newly developed shape selective catalyst can be used to convert vaccum gas oil,vacuum gas oil blended with residual oil or pretreated vacuum residual oil,and atmospheric residual oil in this process.Using Linsheng vacuum gas oil mixed with about 25wt% deasphalted oil as feedstock,12.5wt%~14.43wt% propylene,11.23wt%~11.41wt% butylene and about 40wt% premium gasoline with high octane number were obtained in commerrical production.Type Ⅱ deep catalytic cracking technology has opened a novel route for production of light olefins and high octane gasoline from heavy feedstocks.

A-6 type catalyst for amination of methanol to methylamine was test for 500h at LHSV 11.7h^-1,which showed methanol conversion of 97.52mol%,stable catalytic activity and nearly unchanged product distribution with tim.The catalyst has been in industrial operation for 150 days,with methanol conversion of 98%~99mol%.The percentages(wt) of methylamine,dimethylamine and trimethylamine in raw product are 29.24%,40.76% and 30.00%,respectively.

The structure characterization of silica-supported copper catalysts prepared by deposition-precipitation from homogeneous solution was studied by XRD,DSC,TGA,Thermal Analysis and pore structure analysis.The results indicated tha the catalyst was reduce between 120℃ and 350℃ in a hydrogenflow.The catalytic active components for water-gas shift reaction is extremely small copper particles dispersed in silica and binding with it.

The coke formed on LA-2 catalysts during the conversion of propylene oxide and alcohols to propylene glycol ethers is studied by ¹³C CP/MAS NMR spectrostroscpy and ¹H、¹³C NMR spectrostroscopy for the soluble components in coke.The mechanism of coke formation and the reason of catalyst deactivation are also discussed.

The progress in propylene oligomerization catalysts was reviewed in this article, including the reaction mechanism and industrial application. The trends of research in this field was also suggested.

The cause of over temperature phenomenon during the heating procedure of high-temperature shift(HTS) catalysts, as well as the effect of remaining lower-valent iron and higher valent chromium, during catalyst preparation, on the performance of HTS catalyst were discussed. The route for enhancing the crashing strength of reduced Fe-Cr based HTS catalyst were also proposed.

With respect to the lowest necessary sulfur content in the sulfiding of sulfur-tolerant CO shift catalyst, we deen it inadequate to determine the lowest necessary sulfur content through thernodynic balance calculation of the hydrolysis and sulfiding reaction of only bulk phase MoS₂. The problem of lowest necessary sulfur content was discussed fromthe angles of both chemical balance and kinetics and on the basis of experimental results and industrial operation. It was concluded that the influence of H₂S concentration in process gas on the catalytic activity are mainly on its kinetics. This influence is also dependable on the composition and structure of the catalyst. So it is advisable to determine the relationship between activity and H₂S concentration experimentally and then chose the suitable lower limit of H₂S concentration in the light of application conditions.

This article reported the results of R&D, trial manufacture and industrial test use of CB-5B reforming catalyst, which was developed by Fushun Research Institute of Petroleum & Petrochemistry(FRIPP), manufactured ty Changling Refinery and used for the first time in Shanghai Refinery of Gaoqiao Petrochemical Co.

The CR-3 type new medium-pressure hydrotreating catalyst exhibits high hydrogenation activity, adequate cracking activity, good regenerability and excellent stability, which has been successfully used in one-step single-catalyst hydrotreating process in a 260 kt/a, hydrocracking installation of Daqing Petrochemical Works with considerable economic benefit.

The development, performance test and commercial use of T406 type new dechlorination agent were reported in this article. The tests in comparison to similar well-known dechlorination agents, both at home and abroad, and industrial use showed that the dechlorination agent, developed and manufactured by the Northwest Research Institute of Chemical Industry, is featured by high crushing strength, purification efficiency and dechlorination capacity. It can be used in ambient-temperature dechlorination of bort gasous and liquid feedstocks. It exhibits dechlorination capacity as high as over 18 wt% even at lower temperature (4 ℃) with off-gas chloride concentration around 0.2ppm. It can also remove sulfursimultaneously. This agent has been commercially used in the dechlorination of mixed and hydrogen feedstocks with good results.

A technique for the re-dispersion of platinum particles on partially deactivated reforming catalyst was studied especially with respect to the influence of process conditions such as H₂O/Cl ratio on the redispersion. The results showed that the dispersion of platinum particles increased from 0.4～0.5 to 0.85 after treatment with Cl-containing stream in the presence of O₂ at 515 ℃and H₂O/Cl atom ratom ratio of 5~20. The mechanism of platinum re-dispersion was discussed on the basis of the study of oxide-state platinum during regeneration.

The installation, reduction and commercial operation of A201 type ammonia synthesis catalyst are reported. The operation data show that the catalyst exhibits excellent performance and results in considerable increase in output and savings.

The structure of a SO₄^2-/TiO₂-Al₂O₃ catalyst was studied by Hammett indicator,NH₃-TPD,FT-IR,TG-DTA,XRD and SEM. The results show that the catalyst is a solid superacid. There is good correspondence between surface acidity of the catalyst and roast temperature. There is SO₄^2- on the surface of the catalyst. The good thermal stability suggests that the chemical bond between SO₄^2- and metal oxide is very firm. After repeated use the strucfure of the catalyst remains unchanged. The catalyst exhibits long service life and good regenerability. It has a loose surface structure which makes it highly active.

The characteristic pore structural parameters of natural gas steam reforming catalysts and carbon fibre carriers were measured in a multi-purpose diffusion cell by means of fixed-pressure and at 30~500 ℃,the obtained tortuosity factor(τ) of the catalyst and carbon fibre are 1.8-3.5 and (5~9)×10^-3～(5~9)×10^-4,respectively. The availability factor (η) of the catalyst calculated from experimental data are as follows:0.119-02-0.165,Z107-0.207,Z110y-0.208,Chuan Ⅲ -0.215,C10-0.223.CN-18-0.299.The experimental results were briefly evaluated. The diffusion through carbon fibre is approximately bulk diffusion, which means that it is an ideal carrier for catalysts.

A new and highly-sensitive method for determination of trace Os(Ⅷ) was developed on the basis of Os(Ⅷ) catalysted reaction of Luminol and O2 which generates chemiluminescence. The detection limit of this method is as low as 1.8×10^-14 g/mL for Os(Ⅷ) and the relative standard deviation (RSD) for determination of 1.0×10^-13 g/mL Os(Ⅷ)(n=13) is 4.2%. These is a linear relationship between chemiluminescence and Os(Ⅷ) concentration in the range of 3.3×10^-13 g/mL to 1.3×10^-9 g/mL. The method proved to be simple and effective for determination of trace osmium, with good reproduceability and high sensitivity.