SEPARATION AND PURIFICATION COUPLED PROCESS WITH HIGH HELIUM YIELD AND DIVERSIFIED PRODUCTS

Abstract

A separation and purification coupled process with a high helium yield and diversified products is provided The process is as follows. Firstly, a low-concentration helium-containing gas after being pressurized and pre-treated enters a two-stage and two-section membrane separation unit to produce a helium product with a medium concentration by concentrating stage by stage through the membrane separation unit. A part of the helium with medium concentration enters an adsorption unit for further concentration to produce a helium product above grade A.

Claims

1. A separation and purification coupled process with a high helium yield and diversified products, which is implemented based on a helium purification, separation and recovery coupled system, wherein the coupled system comprises: a compressor unit, a pretreatment unit, a membrane separation unit, and an adsorption unit; the compressor unit comprises a first compressor and a second compressor; the pretreatment unit comprises a first pretreatment unit and a second pretreatment unit; and the membrane separation unit comprises a first membrane separation unit, a second membrane separation unit, and a third membrane separation unit; the process comprising: mixing a helium-containing feed gas and a recycle gas, passing a first mixture of gases of the helium-containing feed gas and the recycle gas through the first compressor to be pressurized, entering a pressurized gas into the first pretreatment unit to remove liquid mist and dust through the first pretreatment unit and allow a temperature of the pressurized gas to be adjusted to 40 to 100° C., and entering a helium-containing gas into the first membrane separation unit; passing the helium-containing gas through the first membrane separation unit to be divided into two material flows, namely, a preliminarily concentrated helium-rich permeated gas which is the gas that permeates through the first membrane separation unit preferentially and a retentate gas on a basis that different gases have different permeation rates upon passing through a same membrane; passing the preliminarily concentrated helium-rich permeated gas through the second compressor to be pressurized, entering a pressurized helium-rich permeated gas into the second pretreatment unit to remove liquid mist and dust through the second pretreatment unit and allow a temperature of the pressurized helium-rich permeated gas to be adjusted to 40 to 100° C., entering a flow from the second pretreatment unit into the second membrane separation unit; and entering the retentate gas into the third membrane separation unit through an inlet of the third membrane separation unit; passing the flow through the second membrane separation unit to be divided into two material flows, namely, a retentate gas and a secondarily concentrated helium-rich permeated gas; discharging a first part of the secondarily concentrated helium-rich permeated gas to an outside as a product gas with medium helium concentration; entering a second part of the secondarily concentrated helium-rich permeated gas into the adsorption unit for further being concentrated to produce a helium above grade A; mixing the retentate gas of the second membrane separation unit and the retentate gas of the first membrane separation unit; and entering a mixed flow of the retentate gas and the retentate gas into the third membrane separation unit to be divided into two material flows, namely, a permeated gas and a retentate gas, through the third membrane separation unit, returning the permeated gas to an inlet of the first compressor for recycling, mixing the retentate gas and desorption gas from the adsorption unit, and discharging a mixture of gases of the retentate gas and a desorption gas out of a battery limit.

2. The separation and purification coupled process with the high helium yield and diversified products according to claim 1, wherein the membrane separation unit is a hollow fiber membrane component, a flat membrane component, a tubular membrane component, or a coiled membrane component.

3. The separation and purification coupled process with the high helium yield and diversified products according to claim 2, wherein the hollow fiber membrane component, the flat membrane component, the tubular membrane component, or the coiled membrane component is an organic membrane, an inorganic membrane, or an organic-inorganic hybrid membrane.

4. The separation and purification coupled process with the high helium yield and diversified products according to claim 1, wherein the pretreatment unit is a dispenser, a heat exchanger, a precise filter, and a demister.

5. The separation and purification coupled process with the high helium yield and diversified products according to claim 2, wherein the pretreatment unit is a dispenser, a heat exchanger, a precise filter, and a demister.

6. The separation and purification coupled process with the high helium yield and diversified products according to claim 3, wherein the pretreatment unit is a dispenser, a heat exchanger, a precise filter, and a demister.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0016] FIG. 1 is a principle process flow diagram of a separation and purification coupled process with a high helium yield and diversified products.

[0017] List of the reference characters: K1 first compressor; K2 second compressor; PR1 first pretreatment unit; PR2 second pretreatment unit; M1 first membrane separation unit; M2 second membrane separation unit; M3 third membrane separation unit; and PSA adsorption unit.

DETAILED DESCRIPTION OF THE EMBODIMENTS

[0018] Specific embodiments of the present disclosure will be described below in detail with reference to technical solutions and accompanying drawings.

[0019] A separation and purification coupled process with a high helium yield and diversified products is implemented based on a helium purification, separation and recovery coupled system. The helium purification, separation and recovery coupled system includes: a compressor unit, a pretreatment unit, a membrane separation unit, and an adsorption unit PSA. The compressor unit includes a first compressor unit K1 and a second compressor unit K2. The pretreatment unit includes a first pretreatment unit PR1 and a second pretreatment unit PR2. The membrane separation unit is a hollow fiber membrane component, a flat membrane component, a tubular membrane component, or a coiled membrane component, and includes a first membrane separation unit M1, a second membrane separation unit M2, and a third membrane separation unit M3. A specific embodiment is as follows.

[0020] A low-concentration helium-containing tail gas treated by using the separation and recovery process according to the present disclosure is used as a conventional tail gas exhausted from natural gas liquefaction, and the flow rate of the helium-containing tail gas is 500 Nm.sup.3/h. The helium-containing tail gas has a pressure of 100 KPaG, a temperature of 40° C., a helium content of 4.95 vol %, a nitrogen content of 12.74 vol %, and a methane content of 82.31 vol %.

[0021] A helium-containing feed gas f1 and a recycle gas f10 are mixed and then are pressurized through the first compressor K1; the mixed gas of the helium-containing feed gas f1 and the recycle gas f10 enters the first pretreatment unit PR1 to remove liquid mist and dust through the first pretreatment unit PR1; a helium-containing gas f2 with a temperature adjusted to 40 to 100° C. enters the first membrane separation unit M1. The helium-containing gas 12 entering the first membrane separation unit M1 is divided into two material flows, namely, a preliminarily concentrated helium-rich permeated gas f3 and a retentate gas f4, through the first membrane separation unit M1. The preliminarily concentrated helium-rich permeated gas f3 is pressurized through the second compressor K2, subsequently enters the second pretreatment unit PR2 to remove liquid mist and dust through the second pretreatment unit PR2 and allow its temperature to be adjusted to 40 to 100° C., and then a flow f5 enters the second membrane separation unit M2. The retentate gas f4 passes through an inlet of the third membrane separation unit M3. The flow f5 is divided into two material flows, namely, a retentate gas f6 and a secondarily concentrated helium-rich permeated gas f7, through the second membrane separation unit M2. A first part of the secondarily concentrated helium-rich permeated gas 17 serves as a product with a medium helium concentration, and a second part of the secondarily concentrated helium-rich permeated gas f7 enters the adsorption unit PSA for further concentration to produce a helium above grade A. The retentate gas f6 of the second membrane separation unit M2 and the retentate gas f4 of the first membrane separation unit M1 are mixed, and then enters the membrane separation unit M3. A mixed flow f9 is divided into two material flows, namely, a permeated gas f10 and a retentate gas f11, through the third membrane separation unit M3. The permeated gas f10 is returned to an inlet of the first compressor K1 for recycling. The retentate gas f11 and a desorption gas f8 from the adsorption unit PSA are mixed and discharged out of a battery limit to serve as gas-oil displacement and the like or are emptied.

[0022] Particles and the liquid mist which are pressurized by the compressor (K1), treated by the pretreatment unit (PR1), and then enter the membrane separation unit, all have diameters of less than 0.01 um, a temperature of 75° C., and a pressure of 2.3 MPaG.

[0023] The particles and the liquid mist which are pressurized by the compressor (K2), treated by the pretreatment unit (PR2), and then enter the membrane separation unit, all have diameters of less than 0.01 um, the temperature of 75° C., and the pressure of 2.4 MPaG.

[0024] The hollow fiber membrane components used by the first membrane separation unit M1, the second membrane separation unit M2, and the third membrane separation unit M3 are all glassy polyimide membranes.

[0025] The cycling flow inside the membrane separation unit: namely, the flow f10 has the helium content of 5.19 vol %.

[0026] In the present embodiment, a helium product gas 1 has the helium content of 94.72 vol %, a helium product gas 2 has the helium content of 99.99 vol %, and the recovery rate reaches 99%.

[0027] The above-mentioned embodiments only illustrate the implementations of the present disclosure, but cannot be construed as a limitation to the scope of the patent of the present disclosure. It should be noted that a number of variations and improvements may also be made by those skilled in the art without departing from the conception of the present disclosure, and all of these fall within the scope of protection of the present disclosure.