8results about "Multiple-effect/fractional condensation" patented technology

Methods and systems for converting waste plastics into various useful downstream recycle content products are provided. More particularly, the present systems and methods involve integrating a pyrolysis facility with a cracker facility by introducing at least one r-pyrolysis gas stream into the cracker facility. In the cracker facility, the r-pyrolysis gas can be separated to form one or more recycle content products, and operation of the facility can be improved.

A greenhouse gas treatment apparatus for stagewise condensation and collection of atmospheric gases including water vapor, nitrous oxide, and carbon dioxide. The apparatus includes a primary cooling chamber and an independent secondary cooling chamber, each supplied with low-temperature air via dedicated supply pipes, with the secondary chamber maintained at a lower temperature than the primary chamber. A condensation pipe passes sequentially through the primary and secondary cooling chambers. As suctioned air travels through the condensation pipe, water vapor is condensed and collected in the primary cooling chamber. Remaining greenhouse gases, including carbon dioxide, are subsequently condensed and collected in the secondary cooling chamber for storage in a separate tank.

This invention discloses an air separation system and method for co-producing hydrogen, belonging to the field of air separation and hydrogen production technology. It includes four oxygen-permeable membrane reactors and two condensers. The oxygen-producing outlet of the fourth oxygen-permeable membrane reactor (R4) is connected to the second condenser (C2), which has a condensate drain outlet and an oxygen outlet. The nitrogen-producing inlet of the third oxygen-permeable membrane reactor (R3) is connected to the air-producing outlet of the fourth oxygen-permeable membrane reactor (R4). The fuel-producing inlet of the second oxygen-permeable membrane reactor (R2) is connected to the fuel-producing outlet of the third oxygen-permeable membrane reactor (R3). The fuel-producing inlet of the first oxygen-permeable membrane reactor (R1) is connected to both the fuel-producing outlet and the hydrogen-producing outlet of the second oxygen-permeable membrane reactor (R2), and the hydrogen-producing outlet of the first oxygen-permeable membrane reactor (R1) is connected to the first condenser (C1), which has a condensate drain outlet and a hydrogen outlet. This invention simultaneously produces hydrogen, oxygen, and nitrogen through a reasonable process arrangement. The method is simple, efficient, and highly economical and practical.

A method for condensing a vapor uses a multi-stage bubble-column vapor mixture condenser that includes at least a first stage, a second stage, and a third stage, each with a carrier-gas inlet and outlet as well as a condensing bath and a volume of carrier gas above the condensing bath. The carrier-gas inlet of the second and third stages is in the form of a sieve plate. The first-stage condensing bath is at a temperature of 60° C. to 90° C. Carrier gas flows at a temperature above 60° C. and up to 93° C. into and through the carrier-gas inlet of the first stage, then into and through the condensing bath in the first stage, and then into and through the volume of carrier gas above the condensing bath in the first stage. The carrier gas then similarly flows through the second- and third-stage condensing baths, each of which is at least 5° C. cooler than the temperature of the condensing bath in the preceding stage. Additional carrier gas is injected through an intermediate-exchange inlet into the volume of carrier gas above the condensing bath in at least one of the first and second stages to control the heat and mass profile of the carrier gas flowing through the stages of the multi-stage bubble-column vapor mixture condenser and to thereby maintain the temperature differentials between the condensing baths in the first, second, and third stages.

Chemical precursor recovery systems and methods of recovering and reusing semiconductor manufacturing chemistry are disclosed. The recovery systems include a cold trap inlet line in fluid communication with a plurality of cold traps and a cold trap outlet line. The plurality of cold traps is configured to condense the chemical precursors and are arranged based on semiconductor manufacturing process conditions.

A system and method for improving the water quality of a dehydration tower in a purified terephthalic acid device includes a dehydration washing device, a tail gas condensation device communicating with the top of the dehydration washing device, and a water separation device communicating with the tail gas condensation device. The system reduces energy consumption. The tail gas condensation device uses low-pressure vapor of about 0.05 MPa generated by an Nm-th-stage condenser as a heating medium. Working media are water and the low-pressure vapor, and no organic phase is involved in a process, and a reaction is stable and intrinsically safe. The water in the water separation tower is purified water and concentrated water, the purified water is returned to the top of the dehydration tower, and the concentrated water is mixed with a mother liquor and then enters the dehydration tower.

The application discloses a coal chemical CO2 low-temperature capturing device and a capturing method. The capturing device comprises a dehumidification tower, three filling beds arranged in parallel, a gas-liquid separation unit, a liquid nitrogen pipe, a nitrogen pipe and a CO2 removal gas pipe. The application firstly carries out gas-liquid separation in a low-temperature mode to obtain part of liquid carbon dioxide. The mixed gas after liquefied separation continues to be cooled and condensed in the filling bed, and the carbon dioxide is separated out. The dry ice obtained by condensation separation is liquefied and collected by heat exchange with the CO2-containing gas, and the pressure and temperature are controlled, so that the obtained dry ice can be directly melted into liquid carbon dioxide and will not be gasified into gas. The system fully recovers the cold energy of the system. The dry ice is condensed and captured by the filling bed to capture the carbon dioxide, which can avoid the dry ice freezing and blocking phenomenon of the conventional equipment. The gas does not need to be re-compressed, the energy consumption is low, the capturing purity of the carbon dioxide is improved, and the carbon dioxide capturing rate is increased.

The present application belongs to the technical field of sulfur preparation, and particularly relates to a low-sulfur-emission acid gas sulfur recovery process. The low-sulfur-emission acid gas sulfur recovery process comprises a Claus unit and a tail gas treatment unit. The tail gas treatment unit first performs selective hydrogenation on tail gas flow from the Claus unit, and then performs subsequent treatment. The selective hydrogenation catalyst contains 2-3 wt% of cobalt in the form of CoO, 1.5-2 wt% of nickel in the form of NiO, 11-13 wt% of molybdenum in the form of MoO3, and 3-4 wt% of lanthanum in the form of La2O3, and the rest is a carrier component. The carrier component contains 80-85 wt% of TiO2, and the rest is CaSO4. In the present application, the outlet gas flow of the selective hydrogenation reactor can reach the low-sulfur-emission level after being treated by a conventional method, the technical requirements for the subsequent treatment process are relatively low, and the preceding Claus unit has a wide range of operation flexibility.