Abstract: Provided are an apparatus and a method for separation and recovery of propane and heavier hydrocarbons from LNG. The apparatus has, from the upstream side toward the downstream side of LNG supply, first column (3) equipped with first column overhead condenser (2), first column bottom reboiler (4) and side reboiler (5), and second column (14) equipped with second column overhead condenser (11) and second column bottom reboiler (15). The first column (3) separates methane and a part of ethane as an overhead vapor and separates remaining ethane and C3 or higher hydrocarbons as a bottom liquid. The second column (14) separates ethane as an overhead vapor and separates C3 or higher hydrocarbons as a bottom liquid.

Abstract: Cell frame 20 includes: frame body 21 having an opening 22, frame body 21 including through-hole 31 for passage of a fluid containing an active material, through-hole 31 penetrating from one surface of frame body 21 to the other surface thereof around opening 22, and groove-like slit 35 formed in one surface or the other surface and connecting through-hole 31 and opening 22; and rotor 40 made of an insulating material, rotor 40 received in slit 35 and forced to rotate by the flow of the fluid through slit 35 between through-hole 31 and opening 22.

Abstract: Redox flow battery 1 includes cell stack 2, first positive-electrode tank 11, second positive-electrode tank 12, first negative-electrode tank 21, and second negative-electrode tank 22. Cell stack 2 is divided into a plurality of cell groups 3, each of which consists of a plurality of cells 4. The plurality of cell groups 3 are connected to first and second positive-electrode tanks 11, 12 such that a positive-electrode fluid containing positive-electrode active material flows in parallel through the plurality of cell groups 3, and are connected to first and second negative-electrode tanks 21, 22 such that a negative-electrode fluid containing negative-electrode active material flows in parallel through the plurality of cell groups 3. The plurality of cells 4 in each cell group 3 are connected to each other such that the positive-electrode fluid flows in series through a plurality of positive cells 5 and such that the negative-electrode fluid flows in series through a plurality of negative cells 6.

Abstract: A closed loop refrigeration system using a gas hydrate having a temperature below 0° C. has: a first circulation loop extending through a gas hydrate formation device 1, an object 2 to be cooled and a separator 3 and back to the formation device 1 and including a gas hydrate line 10 for transporting a gas hydrate having a temperature below 0° C.; and a second circulation loop for gas extending through the formation device 1, a compressor 4, a cooler 5 and a decompressor 6 and back to the formation device 1, wherein an object to be transported in the first circulation loop is transported together with a liquid carrier.

Abstract: There is provided a process and an apparatus for urea production in which preheating of raw material ammonia or heating in a medium-pressure decomposition step can be performed at a relatively low pressure while preventing decrease in an overall heat transfer coefficient. A process for urea production includes: a synthesis step of generating a urea synthesis solution; a high-pressure decomposition step of heating the urea synthesis solution to separate a gaseous mixture containing ammonia and carbon dioxide from the urea synthesis solution; a condensation step of condensing the gaseous mixture; a medium-low-pressure steam generation step of reducing a pressure of medium-pressure steam condensate obtained in the high-pressure decomposition step to a medium-low pressure to generate medium-low-pressure steam and medium-low-pressure steam condensate; and one or both of a medium-pressure decomposition step and an ammonia preheating step.

Abstract: To provide a process for separating hydrocarbons capable of recovering ethane or propane, including improved cold heat recovery enabling a reduction in compressor power.

Abstract: A process for obtaining a product gas and product LNG having pressure P1 close to the atmospheric pressure from lean LNG, includes: a) branching the lean LNG to obtain a first flow and a second flow; b) cooling the second flow by using a refrigerant; c) branching a liquid flow derived from the cooled second flow to obtain refrigerant LNG and remaining LNG; d) subjecting the remaining LNG to pressure reduction and gas-liquid separation to obtain a gas phase flow and a liquid phase flow (product LNG) having pressure P1; e) subjecting the refrigerant LNG to pressure reduction; f) using a flow from the step e as the refrigerant; g) joining, before or after the step f, the gas phase flow having pressure P1 to a flow from the step e; h) liquefying a flow resulting from the steps f and g by pressure increase and cooling (through heat exchange with the first flow); i) increasing the first flow in pressure before the step h; j) obtaining the product gas by regasifying the first flow after the steps h and i; and k) joi

Abstract: Precipitation of an ammonium salt is prevented while suppressing an increase in water content of the aqueous urea solution which is to be supplied to a urea granulation step, when recovering and using urea and NH3 in a gas which contains urea dust and NH3 and which arises from a urea granulation step.

Abstract: Diabatic distillation column 1 includes first and second cooling devices 11, 12 configured to indirectly cool fluid in rectifying section 2 with a circulating working fluid, first and second heating devices 21, 22 configured to indirectly heat fluid in stripping section 3 with the circulating working fluid, first compressor 31 configured to compress the working fluid from first cooling device 11 on first circulation path P11-P14 between first cooling device 11 and first heating device 21, second compressor 32 configured to compress the working fluid from second cooling device 12 on second circulation path P21-P24 between second cooling device 12 and second heating device 22, first expansion device 41 configured to expand the working fluid from first heating device 21 on first circulation path P11-P14, and second expansion device 42 configured to expand the working fluid from second heating device 22 on second circulation path P21-P24.

Abstract: The present invention provides a solar heat collecting device having good heat collection efficiency. A uniaxial solar-tracking reflective mirror group is arranged such that each longitudinal axis thereof faces the same direction. A first biaxial solar-tracking reflective mirror group and a second biaxial solar-tracking reflective mirror group are arranged lined up in a direction orthogonal to the longitudinal axis direction of uniaxial solar-tracking reflective mirrors. The uniaxial solar-tracking reflective mirror group is arranged so as to be sandwiched on both sides by the first biaxial solar-tracking reflective mirror group and the second biaxial solar-tracking reflective mirror group. Each mirror group sends solar heat received during uniaxial or biaxial tracking in accordance with the position of the sun, to a heat collecting device.

Abstract: Disclosed are: a treatment method comprising (1) a step in which an aqueous solution containing urea, ammonia and carbon dioxide is introduced into a first stripper (PCS1) and subjected to stripping, and the aqueous solution after stripping is introduced into a urea hydrolyzer (UHY), (2) a step in which urea in the aqueous solution is hydrolyzed in the urea hydrolyzer (UHY), and the aqueous solution after hydrolysis is introduced into a second stripper (PCS2), (3) a step in which the aqueous solution is subjected to stripping in the second stripper (PCS2), and (4) a step in which a part of the aqueous solution before being stripped in the first stripper (PCS1), and/or, a part of the aqueous solution after being stripped in the first stripper (PCS1) but before being hydrolyzed in the urea hydrolyzer (UHY) is introduced into an exhaust gas treatment equipment equipped with an ammonia scrubbing equipment (ASCR); and a treatment equipment therefor.

Abstract: Provided are urea manufacturing method and apparatus, which can increase the conversion ratio into urea and to reduce the consumption of steam. The temperature of the reactor is increased by introducing the entire amount of raw material ammonia and introducing a portion of the decomposed gas from the stripper into the reactor. The raw material ammonia is preferably heated using the steam condensate generated in the purification step, and/or the steam generated by the heat of condensation of the decomposed gas and the unreacted substances in the condensation step. The heating temperature is preferably between 70 and 140° C.

Abstract: Provided are urea manufacturing method and apparatus, which can increase the conversion ratio into urea and to reduce the consumption of steam. The temperature of the reactor is increased by introducing the entire amount of raw material ammonia and introducing a portion of the decomposed gas from the stripper into the reactor. The raw material ammonia is preferably heated using the steam condensate generated in the purification step, and/or the steam generated by the heat of condensation of the decomposed gas and the unreacted substances in the condensation step. The heating temperature is preferably between 70 and 140° C.

Abstract: Chemical heat pump system 1 includes: endothermic unit 3 that contains a slurry containing a solid product and that absorbs heat supplied from an outside to perform an endothermic reaction at first pressure P1; exothermic unit 2 that contains a slurry containing a solid reactant and that performs an exothermic reaction at a second pressure P2 that is higher than the first pressure P1 to generate heat; gas recovery supply unit 4 that recovers a gas reactant that has been decomposed in endothermic unit 3 and that supplies the gas reactant to exothermic unit 2; and circulation unit 5 that supplies the slurry containing the solid reactant, that has been decomposed in endothermic unit 3, to exothermic unit 2 after pressurizing the slurry from first pressure P1 to second pressure P2, and that supplies the slurry containing the solid product, that has been produced in exothermic unit 2, to endothermic unit 3 after depressurizing the slurry from second pressure P2 to first pressure P1, so as to circulate the slurry b

Abstract: Precipitation of an ammonium salt is prevented while suppressing an increase in water content of the aqueous urea solution which is to be supplied to a urea granulation step, when recovering and using urea and NH3 in a gas which contains urea dust and NH3 and which arises from a urea granulation step.

Abstract: The present invention is a urea production method, including: a first concentration step of concentrating an aqueous urea solution; a granulation step of producing solid urea from the concentrated urea solution generated in the first concentration step; a urea recovery step of treating exhaust gas from the granulation step and recovering urea dust in the exhaust gas to generate a recovered aqueous urea solution, the granulation step being configured so as to treat a concentrated urea solution containing an additive; and a second concentration step of concentrating the recovered aqueous urea solution as an additional concentration step, wherein the concentrated recovered urea solution generated in the second concentration step is joined to the concentrated urea solution in the downstream of the first concentration step, and an additive is added downstream of the first concentration step.

Abstract: Method and apparatus that enable the more efficient manufacture of urea are provided. Before unreacted substances are removed from a urea synthesis solution obtained from a stripper, the urea synthesis solution is placed under pressure reduced from the synthesis pressure. Thus, a gas-liquid mixture is obtained. The gas-liquid mixture is heated with a decomposed gas from the stripper using a shell-and-tube heat exchanger, and then introduced into a purification system. In the heating, the gas-liquid mixture is introduced into the shell of the heat exchanger while the decomposed gas is introduced into the tube side of the heat exchanger.

Abstract: A solar heat collector with high heat collection effect is provided. The solar heat collector includes a first heat collection pipe and a second heat collection pipe. The first heat collection pipe receives reflected light from a single-axial tracking solar type reflective mirror group to collect heat. The second heat collection pipe receives reflected light from the single-axial tracking solar type reflective mirror group and dual-axial tracking solar type reflective mirror groups to collect heat. The second heat collection pipe has an amount of heat collection per unit area larger than the first heat collection pipe. Therefore, compared with the use of only the first heat collection pipe, this ensures obtaining larger energy.

Abstract: Chemical heat storage system 1 based on an exothermic reaction that produces a solid product from a solid reactant and a gas reactant and an endothermic reaction that decomposes the solid product into the solid reactant and the gas reactant, includes: endothermic unit 3 that contains a slurry containing the solid product and that absorbs heat supplied from the outside to perform the endothermic reaction; exothermic unit 2 that contains a slurry containing the solid reactant and that performs the exothermic reaction to generate heat; and gas recovery supply unit 4 that recovers the gas reactant that has been decomposed in endothermic unit 3 and that supplies the gas reactant to exothermic unit 2.

Abstract: Provided are an apparatus and a method for separation and recovery of propane and heavier hydrocarbons from LNG. The apparatus has, from the upstream side toward the downstream side of LNG supply, first column (3) equipped with first column overhead condenser (2), first column bottom reboiler (4) and side reboiler (5), and second column (14) equipped with second column overhead condenser (11) and second column bottom reboiler (15). The first column (3) separates methane and a part of ethane as an overhead vapor and separates remaining ethane and C3 or higher hydrocarbons as a bottom liquid. The second column (14) separates ethane as an overhead vapor and separates C3 or higher hydrocarbons as a bottom liquid.