Description:a) Prior art and problem to be solved: -

Helium is present in two phases i.e., gas phase and liquid phase. Liquid phase Helium has higher demand in market than the gaseous Helium as it is majorly used in the medical industry and also fetches a higher market rate i.e., about 20% more selling price compared to gaseous Helium per M3 volume. However, Liquid Helium can only be extracted partially up to 40% of total volume from the Helium received in ISO container, as there is a flash rate of 50% while decanting the Liquid Helium in the Dewars and also balance 20% is left in the ISO Container which is in the gaseous form.
The flash which is generated needs to be recollected & compressed by using very high pressure specialized Helium compressor up to 200 bar in cylinders which requires electricity up to 196 units / hrs. for gas production.
Earlier to this invention, the problem we were facing was that we were able to extract less volume of Liquid Helium from ISO Container i.e., up to 40% and there was a problem of formation of more flash i.e., more gaseous Helium, thereby requiring more electricity for recollection, compressing and production of Helium gas. Less Liquid Helium extraction resulted in less revenue generation for the Company. Thus, the problem was formation of more gaseous Helium and extraction of lesser volume of Liquid Helium i.e., only up to 40%.

b) Objects of the invention: -

Objects of our invention were as under:
(i) to minimize the flash generation rate of Helium and to maximize the extraction of Liquid Helium from ISO Containers Liquid Helium can be sold in the market with approximately minimum 20% higher price than the gaseous Helium and thus to increase revenue from more volume of Liquid Helium extracted.
(ii) to bring flexibility in our operations as per the Company’s Sales Dept.’s demand as we wanted to shift more of our Helium business from gaseous Helium to Liquid Helium as Liquid Helium business is more profitable than the gaseous Helium business but we were unable to do so because of practical limitations faced in the Liquid Helium extraction process.
(iii) Normally ISO Container containing Liquid Helium is received from its country of origin with 70 to 80 psi pressure & Liquid extraction of Helium is possible only below 8 psi. To reduce this pressure to 8 psi, approximately 550 cylinders of 200 bar pressure are required with compressor running for 45 hrs. with power consumption of Approx. Rs. 2,000 /hr. i.e. approximately Rs 90,000 is power consumption cost per ISO container. Hence the objective was to reduce this power consumption by extracting more Liquid Helium thereby formation of lesser volume of gaseous Helium.
, C , Claims:1. Preamble
A device used to increase Liq. Helium extraction in helium trans filling process.

2. Transitional Phase
As per traditional helium transfilling method we can only extract maximum 40% from ISO helium container which has been increased up to 60%.

3. Main body
In the process of liq. Helium extraction vacuum insulated hose commonly called siphon is connected to bottom of ISO Helium container and trans fill liquid helium to approximate 250 Ltr. water capacity cylinder commonly called Dewar, during this process very high flash generation occurs because if very low temperature ie. -269 Deg C. to minimize this flash generation we fixed said device toward end of siphon for filling Dewar. This control the flow and pressure of Helium trans filling and also re liquidize the flash around and thus increase liquid extraction.