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Background overview: The raw oil shale is crushed to a particle size of less than 25 millimeters and then sent to a dryer for moisture removal; the temperature of the dried oil shale is between 110–140°C. The dried raw material is mixed with a gray carrier at a temperature of 740–800°C in a certain ratio and fed into a reactor. This reactor is a horizontally rotating kiln, where the oil shale and the gray carrier come into full contact and mix evenly. The equilibrium reaction temperature is 470–490°C, with a residence time of approximately 14–16 minutes. The gases produced as a result of the reaction are immediately removed, and negative pressure is maintained inside the reactor； The shale oil in oil shale is extracted to the maximum extent. The oil and gas obtained through dry distillation are pumped to shale oil separation and classification equipment for processing and refinement ； After entering the rapid lifting device, the ash carrier and oil shale semi-coke mix with the compressed air at the bottom; as they are lifted rapidly, part of the semi-coke burns in an environment with insufficient air (a=0.89-0.95), raising the temperature of the material to 760–810°C before it enters the ash carrier container. The excess material goes into the ash storage tank, where some of it is used by the boiler to generate hot flue gas that supplies sufficient drying gas for the dryer. The remaining ash is processed in the ash slurry tank and then utilized as a raw material in cement production. The principle of this process was developed by the Energy Research Institute in Moscow, Russia; the UTT3000 unit was designed by the Atomic Energy Design Bureau in St. Petersburg. In 1979, two units for the dry distillation of particulate shale with a processing capacity of 3,000 tons per day were installed at the Narva oil shale power plant in Estonia. The operation of these units went through two phases: an experimental phase from 1980 to 1986, and a phase for process improvement from 1987 to 2002. Due to the complex process of this device, the large number of equipment and rotating machinery involved, the difficulty in operating it, and the significant effort and resources required from the operators, improvements were made ； The current operating conditions have returned to normal, with 6,200 hours of operation recorded in 2004. Information: If the laboratory oil recovery rate for shale is 14%, then using the Galoter device yields 12%, which is approximately 86%. The volumetric calorific value of the dry distillation gas is 11,000 Kcal/m3; it contains 30% olefins and can be used as a raw material for the chemical industry or as household gas. According to the St. Petersburg Design Institute, the steel and building materials required for constructing the UTT3000 unit are: 1,365 tons of carbon steel and pig iron, 50 tons of cast iron and heat-resistant steel, and 1,030 tons of shaped bricks and insulating bricks. Processing 1 ton of shale requires 30 kWh of electricity, 6 tons of water, and 10 kilograms of steam (at 6 atmospheres pressure). I would like to ask if there are any design companies that are familiar with this area. We are now looking to introduce a technology package, and by combining it with domestic fluidized bed technology, we want to develop a system suitable for our own use to process fine-grained oil shale. The oil content in the fine-grained oil shale here is around 12%, and we process 1 million tons per year. We are looking for a design institute that has the necessary qualifications and has expertise in this area. I heard that Sinopec Luoyang Petrochemical Engineering Company is a good choice; could anyone recommend a suitable design institute?