Abstract: A process for producing high-quality polycarbonate grade bisphenol A directly by removing phenol from the adduct crystal of bisphenol A with phenol via a gas-solid reaction at low temperature comprises directly feeding the adduct crystal into a vacuum or pneumatic dephenolizing device under vacuum a inert gas stream, controlling the temperature of the adduct crystal below its melting point, decomposing the adduct crystal into gas phase and solid phase, removing the gas phase phenol and condensing phenol for recovery, well leaving the rest being the desirable bisphenol A. The process possesses easy operation, short procedure, low energy consumption, and high purity and good color of bisphenol A obtained. Bisphenol A produced according to the process of the invention may be used as the raw material for producing polycarbonates for optical use.

Abstract: A cracking catalyst for the production of light olefins comprises 0-70% (based on the weight of the catalyst) of clay, 5-99% of inorganic oxides, and 1-50% of zeolite. The zeolite in the catalyst is a mixture of 0-25 wt % of REY or high silica Y zeolite and 75-100 wt % of phosphorus and rare earth containing high silica zeolite having a structure of pentasil. The catalyst exhibits higher hydrothermal activity-stability, conversion level, and C.sub.2 -C.sub.4 olefin yields in cracking reaction, comparing with the catalyst using HZSM-5 zeolite as active component.

Abstract: A hydrocarbon conversion catalyst for converting petroleum distillates of different boiling ranges, residue oils, and crude oils, especially the heavy hydrocarbons containing high nickel, into high quality gasoline and C.sub.3 and C.sub.4 olefins. The catalyst of the invention comprises three zeolitic active components consisting of a rare-earth-containing pentasil type high silica zeolite ZRP, a REY zeolite, and a high silica Y zeolite, in a total content of 10-40 wt % based on the total weight of the catalyst, and the remainder synthetic matrix or semi-synthetic matrix comprising 10-40 wt % silica and/or alumina binder. In the total amount of the active components, zeolite ZRP, REY, and the high silica Y are 3-50, 12-75, and 12-75 wt % respectively. The zeolite ZRP used in the catalyst is characterized in an anhydrous chemical composition of the formula 0.01-0.30 RE.sub.2 O.sub.3.0.4-1.0 Na.sub.2 O.Al.sub.2 O.sub.3.20-60 SiO.sub.

Abstract: A dehydrogenating catalyst for saturated hydrocarbons comprising platinum, tin, sodium and .tau.-alumina. The support of the catalyst is a large pore diameter .tau.-Al.sub.2 O.sub.3 with dual pore diameter distribution. At least 40% of the total pore volume is contributed by pores with pore diameter in the range of 1000-10000 .ANG.. Platinum, tin, and sodium are impregnated onto support by co-impregnation method, followed by drying, calcinating, and steam-treating, as well as reducing by hydrogen, to prepare a long life dehydrogenating catalyst.

Abstract: A process for producing LPG rich in propylene, butylenes and high octane number gasoline by catalytic conversion which comprises contacting the preheated hydrocarbon feedstock with a solid acidic catalyst which contains rare-earth-containing high silica zeolite having the structure of a pentasil (ZRP), rare-earth-Y zeolite (REY) and high silica Y zeolite in a riser or a fluidized bed reactor, at a temperature in the range of from about 480.degree. C. to about 550.degree. C., a pressure in the range of from about 130 KPa to about 350 KPa, a weight hourly space velocity in the range of 1 to 150 hr-1, a catalyst-to-oil ratio in the range of 4 to 15, and a steam-to-feedstock ratio in the range of 0.05 to 0.12:1 by weight.

Abstract: An equipment for treating sewage, comprises a horizontal plate with a water sinking hole dividing the equipment into two portions: an upper portion of biofilter and a lower portion of contact oxidation pond. Within such equipment, a two-stage sewage biochemical treatment is accomplished. The equipment of the present invention has the advantages of less land occupation, less energy consumption, higher pollutant removing rate, higher shock resistance, easy management, no excess sewage and waste gas being drained off and less secondary pollution.

Abstract: A mild hydrocracking catalyst contains amorphous matrix, zeolite, at least one metal compound selected from Group VIB and at least one metal compound selected from Group VIII. The catalyst is characterized in that the incorporated REUHP zeolite has dual pore distribution at <20 .ANG. and around 200 .ANG. and 3-10 percent by weight lanthanum, cerium, or mixed rare earth oxide. The amorphous matrix is .gamma.-Al.sub.2 O.sub.3 in which 80% total pore volume is contributed by pores having a diameter larger than 50 .ANG. and 60% total pore volume is contributed by pores having a diameter in the range of 50-100 .ANG.. A phosphorus promoter may be incorporated into the catalyst of this invention. The atom ratio of VIII/(VIII+VIB) in the catalyst is in the range of 0.2-0.8. The catalyst of this invention is especially suitable for one-stage once-through mild hydrocracking of heavy oil boiling above 350.degree. C. The tail oil boiling above 350.degree. C. is a high-quality feedstock for steam cracking.

Abstract: A naphtha-reforming catalyst is prepared by using aluminum hydroxide as a feed stock, which is acidificated in steam at high temperature, then shaped and calcined to form .gamma.-Al.sub.2 O.sub.3 support which is supported with metals of Pt, Re and Ti and halogens. The Pt content is 0.075-0.8 Wt %, Re/Pt ratio is 0.1-3.0 (Wt.). Since the .gamma.-Al.sub.2 O.sub.3 support having high purity, high crystallinity and concentrated middle pores has been adopted, the activity, selectivity and stability of the catalyst are increased considerably while the Pt content decreased.

Abstract: This invention relates to a system for recuperation and utilization of exhaust heat from a reformer, in which a plurality of arc passageways are formed respectively on the opposite outside walls of the reformer body with a plurality of arc-shaped steel sheet or zinc-plated steel sheet, said arch passageways together with the bottom chamber under the reformer body serve as preheating duct, and at least one air inlet above each passageway is disposed above the top of the reformer. Under the effect of a blower, the air above the reformer top passes through the said preheating duct, and absorbs the heat dispersed from the reformer body. The preheated air makes indirect heat exchange with the flue gas through a heat pipe excharger. The temperature of the air after heat exchange rises from the environmental to about 220.degree. C. and the air is then introduced to the reformer and auxiliary boiler for combustion. The temperature of the flue gas drops from about 300.degree. C. to about 160.degree. C.

Abstract: The present invention relates to a fluidized-bed catalyst for propylene ammoxidation to produce acrylonitrile, which consists of silica support and a composite of the formulaA.sub.a B.sub.b C.sub.c Ni.sub.d Co.sub.e Na.sub.f Fe.sub.g Bi.sub.h M.sub.i Mo.sub.j O.sub.xwherein A is potassium, rubidium, cesium samarium, thallium, or mixture thereof; B is manganese, magnesium, strontium, calcium, barium, lanthanum, rare earth, or mixture thereof; C is phosphorus, arsenic, boron, antimony, chromium, or mixture thereof; M is tungsten, vanadium, or mixture thereof. The catalyst of the present invention is highly active and selective for preparing acrylonitrile, more specifically, is suitable for catalyzing the reaction between air and propylene at a rather low ratio hence to greatly enlarge the processing capacity of the reactor. By using the catalyst of the present invention, the processing capacity of the reactor increases by 10-15 percent compared with that using conventional catalysts.

Abstract: A supplementary catalyst for long term maintaining the activity of the fluidized bed catalysts for ammoxidation of propylene to produce acrylonitrile. Particularly, the present invention provides a supplementary catalyst for compensating for the loss of the fluidized bed catalyst caused by the volatilization of molybdenum and loss of fine particles during operation. By adopting the supplementary catalyst, the life-time of the fluidized bed catalysts for ammoxidation of propylene to produce acrylonitrile in fluidized bed reactors can be increased from 1-1.5 years to 4 or more than 4 years.