A high-magnesium concentrated liquid is disclosed. In a first embodiment, the high-magnesium concentrated liquid comprises magnesium ranged from 60000-70000 ppm, sodium ranged from 1000-3200 ppm, potassium ranged from 300-3000 ppm, calcium ranged from 100-300 ppm, and the balance of water. In a second embodiment, the high-magnesium concentrated liquid comprises magnesium ranged from 40000-50000 ppm, sodium ranged from 8000-18000 ppm, potassium ranged from 8000-17000 ppm, calcium ranged from 15-250 ppm, and the balance of water.

Systems and methods for producing acid deficient uranyl nitrate from a dilute uranyl nitrate solution are disclosed. In one form, the present disclosure provides a system comprising a feed evaporation system and a diffusion dialysis system. The feed evaporation system is configured to receive a feed stream and to boil off water, under vacuum, from the feed stream to produce a concentrated uranyl nitrate solution and a distilled water product. The diffusion dialysis system is configured to counter flow the concentrated uranyl nitrate solution and the distilled water product across a plurality of membrane vessels to promote nitrate migration from the concentrated uranyl nitrate solution to the distilled water, and to produce a dialysate stream and a recycle acid stream. The feed stream may include a product of a solvent extraction process used to recycle spent nuclear fuel and/or a recovery stream from other fuel fabrication activities.

Separation processes using osmotically driven membrane systems are disclosed generally involving the extraction of solvent from a first solution to concentrate a solute by using a second concentrated solution to draw the solvent from the first solution across a semi-permeable membrane. Pre-treatment and post-treatment may also enhance the osmotically driven membrane processes.

Separation processes using osmotically driven membrane systems are disclosed generally involving the extraction of solvent from a first solution to concentrate a solute by using a second concentrated solution to draw the solvent from the first solution across a semi-permeable membrane. Pre-treatment and post-treatment may also enhance the osmotically driven membrane processes.

Apparatuses for treating radioactive material using a multi-membrane are disclosed. The apparatus for treating radioactive material uses a multi-membrane capable of increasing the usage capacity and life of the storage tank with a multi-membrane process by discharging liquid (e.g., water in waste water) in which radioactive material is removed from waste water to the outside and by storing solidified waste containing radioactive material in the storage tank.

The combination multi-effect distillation and multi-stage flash evaporation system integrates a multi-stage flash (MSF) evaporation system with a multi-effect distillation (MED) system such that the flashing temperature range of the MSF process is shifted upward on the temperature scale, while the MED distillation process operates in the lower temperature range. The multi-stage flash evaporation system includes a plurality of flash evaporation/condensation stages, such that the multi-stage flash evaporation system receives a volume of seawater or brine from an external source and produces distilled water. The multi-effect distillation system includes a plurality of condensation/evaporation effects, such that the multi-effect distillation system receives concentrated brine from the multi-stage flash desalination system and produces distilled water.

A recycling treatment system for tannery wastewater is fixed between a sequencing batch reactor (SBR) and filter press equipment, and the recycling treatment system contains: a first ultrafiltration unit, a second ultrafiltration unit, a cation exchange unit, an osmosis processing unit, a recycling tank, a RO concentration tank, and an evaporation unit. The first ultrafiltration unit includes a filtering tank, a plurality of ultrafiltration sets with plural first ultrafiltration bags and a fluid tube. The second ultrafiltration unit includes a concentration tank, at least one rotary ultrafiltration assembly, a backwash pipe, and a discharge pipe. The cation exchange unit includes a reaction sink and cationic resin. The osmosis processing unit includes plural first reverse osmosis sets and plural second reverse osmosis sets. The RO concentration tank is mounted beside the osmosis processing unit, and the evaporation unit is configured between the RO concentration tank and the recycling tank.

A recycling treatment system for tannery wastewater is fixed between a sequencing batch reactor (SBR) and filter press equipment, and the recycling treatment system contains: a first ultrafiltration unit, a second ultrafiltration unit, a cation exchange unit, an osmosis processing unit, a recycling tank, a RO concentration tank, and an evaporation unit. The first ultrafiltration unit includes a filtering tank, a plurality of ultrafiltration sets with plural first ultrafiltration bags and a fluid tube. The second ultrafiltration unit includes a concentration tank, at least one rotary ultrafiltration assembly, a backwash pipe, and a discharge pipe. The cation exchange unit includes a reaction sink and cationic resin. The osmosis processing unit includes plural first reverse osmosis sets and plural second reverse osmosis sets. The RO concentration tank is mounted beside the osmosis processing unit, and the evaporation unit is configured between the RO concentration tank and the recycling tank.

The invention relates to processes for preparing aldehydes by hydroformylation of alkenes, in which an alkene-containing feed mixture is subjected to a primary hydroformylation with synthesis gas in the presence of a homogeneous catalyst system, the primary hydroformylation being effected in a primary reaction zone from which a cycle gas containing at least some of the products and unconverted reactants of the primary hydroformylation are drawn off continuously and partly condensed, with recycling of uncondensed components of the cycle gas into the primary reaction zone, and with distillative separation of condensed components of the cycle gas in an aldehyde removal stage to give an aldehyde-rich mixture and a low-aldehyde mixture. The problem that it addresses is that of developing the process such that it achieves high conversions and affords aldehyde in good product quality even in the case of a deteriorating raw material position. More particularly, a solution is to be found for making legacy oxo process plants capable of utilizing lower-value raw material sources. This problem is solved by separating the low-aldehyde mixture into a retentate and a permeate by means of a membrane separation unit in such a way that alkenes present in the low-aldehyde mixture become enriched in the permeate, while alkanes present in the low-aldehyde mixture become enriched in the retentate. The alkene-rich permeate is then transferred into a secondary reaction zone and subjected to a secondary hydroformylation therein with synthesis gas in the presence of an SILP catalyst system. The reaction product obtained from the secondary hydroformylation is recycled into the aldehyde removal stage.

Integrated, sequential stages of nanofiltration, forward osmosis, and reverse osmosis and related membranes provide an Integrated Osmosis structure, systems and methods. By optimally placing and using the desired characteristics of each membrane, performance and cost effectiveness not attainable individually is obtained. Integrated Osmosis systems provide high diffusive and osmotic permeability, high rejection, low power consumption, high mass transfer, and favorable Peclet number, by manipulating convection, advection and diffusion, low concentration polarization gradients, low reverse salt flux and effective restoration of performance after cleaning fouled membranes. Benefits include increased permeate recovery and decreased waste concentrate volume from reverse osmosis processes or other elevated osmotic pressure solutions. Integrated Osmosis first employs nanofiltration for selective harvesting of solutes, proffering a reduced osmotic pressure permeate. Forward osmosis dewaters the lowered osmotic pressure permeate generating a dilute draw solution which serves as feed to a reverse osmosis process. Reverse osmosis permeate provides freshwater and concentrate provides draw solution for the forward osmosis process.