KR101838141B1 - Apparatus and method for high permeable gas separation - Google Patents

Apparatus and method for high permeable gas separation Download PDF

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KR101838141B1
KR101838141B1 KR1020160001330A KR20160001330A KR101838141B1 KR 101838141 B1 KR101838141 B1 KR 101838141B1 KR 1020160001330 A KR1020160001330 A KR 1020160001330A KR 20160001330 A KR20160001330 A KR 20160001330A KR 101838141 B1 KR101838141 B1 KR 101838141B1
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gas
membrane module
separation membrane
target
value
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KR20170082210A (en
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이순재
이상협
최재우
이종석
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한국과학기술연구원
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B01D53/228—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion characterised by specific membranes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/30—Controlling by gas-analysis apparatus
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/54—Nitrogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/501—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion
    • C01B3/503—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion characterised by the membrane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/10—Single element gases other than halogens
    • B01D2257/108—Hydrogen
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01D—SEPARATION
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Abstract

In the present invention, in recovering a highly permeable target gas contained in a gas to be separated by using two gas separation membrane modules (a first gas separation membrane module and a second gas separation membrane module) Permeable gas collecting apparatus and method capable of selectively controlling the recovery rate of a target gas while maintaining a target gas concentration in the first permeable gas constant. The high permeable gas collecting apparatus according to the present invention is a high permeable gas collecting apparatus A separation target gas supply unit for supplying a separation target gas containing a highly permeable target gas; A gas mixing unit for mixing the object gas to be separated and the second transparent gas; A first gas separation membrane module for separating a mixed gas of a gas to be separated and a second transparent gas into a first transparent gas and a first residual gas in accordance with a first SC value (? 1 ) set; And a second gas separation membrane module for separating the first residual gas into a second permeable gas and a second residual gas in accordance with a second SC value < RTI ID = 0.0 > ( 2 ) < The first SC value (? 2 ) is supplied so that the target gas concentration of the second transparent gas coincides with the target gas concentration of the gas to be separated to maintain the target gas concentration of the first transparent gas constant .

Figure R1020160001330

Description

TECHNICAL FIELD The present invention relates to a high permeable gas recovery apparatus and a high permeable gas separation apparatus,

The present invention relates to a highly permeable gas recovery apparatus and method, and more particularly, to a high permeable gas recovery apparatus and method using two gas separation membrane modules (a first gas separation membrane module and a second gas separation membrane module) Permeable gas recovery device and method capable of selectively controlling the recovery rate of the target gas while keeping the target gas concentration in the first permeable gas separated by the first gas separation membrane module constant and recovering the gas will be.

Membrane - based gas separation technology for separating and recovering a specific gas using a gas separation membrane is rapidly developing. The gas separation process using a separation membrane is a process of separating a gas in such a manner that a high permeable gas having a small molecular size is permeated through the pores of the membrane and a low permeable gas having a large molecular size is retained in the membrane. Which is simple in principle and has a small energy consumption.

There are a variety of industries that require gas separation. For example, the separation of carbon dioxide (CO 2) from natural gas, concentration from the air-nitrogen (N 2), separation of SF 6 from the waste gas of a semiconductor plant, the carbon dioxide (CO 2) and the separation of the methane (CH 4), methane (CH 4 ) and hydrogen (H 2 ), and separation of propylene (C 3 H 6 ) and propane (C 3 H 8 ).

The present applicant has proposed a technique for maintaining a target gas concentration in a recovery gas at a certain level based on two gas separation membrane modules through Korean Patent Laid-Open No. 2015-122984. On the other hand, in the technique disclosed in Korean Patent Laid-Open No. 2015-122984, the target gas means a low permeable gas having a large molecular size such as SF 6 contained in the feed gas.

Korean Patent Publication No. 2015-122984

In the present invention, in recovering a highly permeable target gas contained in a gas to be separated by using two gas separation membrane modules (a first gas separation membrane module and a second gas separation membrane module) Permeable gas recovery apparatus and method capable of selectively controlling the recovery rate of a target gas while maintaining a target gas concentration in the first permeable gas at a constant level.

Further, the present invention controls the first SC value so that the target gas concentration in the second permeable gas separated by the second gas separation membrane module is in conformity with the target gas concentration in the target gas, so that the target gas concentration in the first permeable gas is constant Permeable gas recovery device and method capable of maintaining a high permeability of the gas.

In addition, the present invention is characterized in that, in a state in which it is assumed that the target gas concentration in the second permeable gas and the target gas concentration in the gas to be separated coincide, the high permeability And to provide a gas recovery apparatus and method.

According to an aspect of the present invention, there is provided a highly permeable gas recovery apparatus comprising: a separation target gas supply unit for supplying a separation target gas containing a highly permeable target gas to be recovered; A gas mixing unit for mixing the object gas to be separated and the second transparent gas; A first gas separation membrane module for separating a mixed gas of a gas to be separated and a second transparent gas into a first transparent gas and a first residual gas in accordance with a first SC value (? 1 ) set; And a second gas separation membrane module for separating the first residual gas into a second permeable gas and a second residual gas in accordance with a second SC value < RTI ID = 0.0 > ( 2 ) < The first SC value? 1 is supplied to the mixing portion so that the target gas concentration of the second permeable gas coincides with the target gas concentration of the separation target gas to maintain the target gas concentration of the first permeation gas constant .

The first SC value? 1 can be specified by the following equation.

(expression)

Figure 112016001074711-pat00001

( 1 is the first SC value, Z F is the target gas concentration of the separation target gas,? 1 is the selectivity of the first gas separation membrane module, and? 2 is the selectivity of the second gas separation membrane module)

If the selectivity of the first gas separation membrane module and the selectivity of the second gas separation membrane module are equal to each other, the first SC value (? 1 ) can be specified by the following equation.

(expression)

Figure 112016001074711-pat00002

(? 1 is the first SC value, Z F is the target gas concentration of the separation target gas, and? 1 is the selectivity of the first gas separation membrane module or the second gas separation membrane module)

Claim 2 SC value (θ 2) and through the adjustment is possible to control the overall permeability recovery (R tot) of the gas recovery apparatus of claim 2 SC value (θ 2) is set by the following equation.

(expression)

Figure 112016001074711-pat00003

R 1 is the recovery rate of the first gas separation membrane module, θ 1 is the first SC value, e 1 is the second SC value, θ 1 is the second SC value, Δ R is R tot -R 1 , R tot is the total recovery rate of the high permeable gas recovery device, Is the concentration of the first gas separation membrane module, and e 2 is the degree of concentration of the second gas separation membrane module)

Wherein the first compression tank further comprises a first compression tank and a second compression tank for supplying the mixed gas of the separation target gas and the second permeation gas to the first gas separation membrane module at a specific supply pressure, Supplies the first residual gas to the second gas separation membrane module at a specific supply pressure, and the supply pressure of the first compression tank and the supply pressure of the second compression tank are set to be the same. The supply pressure P of the first compression tank and the supply pressure P of the second compression tank may be calculated by the following equations.

(expression)

Figure 112016001074711-pat00004

(P is the flow rate of the supply pressure, v is a real-time variation supply gas of the first compression tank and the second compression tank in which real-time setting, v o is the flow rate of the first feed gas, P o is the first compression tank and the second compression tank Of the initial supply pressure)

A highly permeable gas recovery method according to the present invention comprises a first gas separation membrane module and a second gas separation membrane module, separating an injection gas into a first permeation gas and a first residual gas through a first gas separation membrane module, The gas separation membrane module separates the first residual gas into a second permeable gas and a second residual gas, and the first gas separation membrane module is supplied with a separation target gas and a second transmission gas containing a high permeable target gas to be recovered , The first gas separation membrane module separates the injected gas into a first permeable gas and a first residual gas in accordance with a first SC value (? 1 ), and the second gas separation membrane module separates the first residual gas into a second a second permeate gas and a second residue, and the gas separated by the second transmission target of claim 1 SC value so that the gas concentration is consistent with the target gas concentration in the separated target gas in the gas (θ 2) in accordance with the SC value (θ 2) specific And the target gas concentration of the first permeable gas So that the temperature is kept constant.

The highly permeable gas recovery apparatus and method according to the present invention has the following effects.

It is possible to increase the recovery rate of the highly permeable target gas contained in the separation target gas through the repeated gas separation process using the first gas separation membrane module and the second gas separation membrane module.

In addition, when the second permeable gas separated by the second gas separation membrane module is mixed with the separation target gas and supplied to the first gas separation membrane module, the target gas concentration of the second permeation gas and the target gas concentration of the separation target gas It is possible to keep the target gas concentration of the first transparent gas constant by specifying the first SC value (? 1 ). At the same time, selective control of the overall recovery rate is possible through adjustment of the second SC value (? 2 ).

1 is a configuration diagram of a highly permeable gas recovery device according to an embodiment of the present invention;

The present invention provides a technique for recovering a high permeability target gas contained in a gas to be separated by using a gas separation membrane module.

In the present invention, the 'gas to be separated' may be a gas mixture of various kinds (or a mixture of gases having various molecular sizes), such as a mixture of natural gas, air, methane and hydrogen. The term 'target gas' refers to a specific high permeable gas having a relatively small molecular size contained in the gas to be separated. For example, carbon dioxide in natural gas, nitrogen in air, hydrogen in a mixture of methane and hydrogen May correspond to the target gas.

Also, the 'gas to be separated' may be defined as a mixture of a high permeable gas and a low permeable gas. A high permeable gas means a gas having a small molecular size and a high probability of permeating the pores of the gas separation membrane module, The permeable gas means a gas having a small molecular size and a low probability of permeating the pores of the gas separation membrane module. Alternatively, the highly permeable gas may be a gas that is likely to be a permeable gas that permeates the pores of the gas separation membrane module, and the low permeable gas may be a gas that is likely to be a residual gas that remains in the gas separation membrane module. It is natural that the target gas concentration in the residual gas is higher than the target gas concentration in the residual gas.

The present invention provides a technique capable of selectively controlling the recovery rate of the target gas while maintaining the concentration of the recovered target gas constant while recovering the target gas contained in the separation target gas.

That is, in collecting the target gas contained in the target gas to be separated by using the two gas separation membrane modules, that is, the first gas separation membrane module and the second gas separation membrane module, the first gas separation membrane module, And the recovery rate of the target gas recovered through the first permeable gas can be selectively controlled.

Specifically, in order to keep the target gas concentration contained in the first permeable gas constant, the target gas concentration of the second permeable gas (separated by the second gas separation membrane module) and the target gas concentration of the separation target gas coincide with each other A technique of setting the first SC value (? 1 ) so as to be as large as possible. In addition, a technique of selectively controlling the recovery rate of the target gas recovered through the first permeable gas through the control of the second SC value (? 2 ) is presented.

On the other hand, if the target gas concentration of the second transparent gas differs from the target gas concentration of the gas to be separated, the target gas concentration contained in the injected gas (the gas to be separated + the second permeable gas) supplied to the first gas separation membrane module is The target gas concentration in the first permeable gas can not be kept constant even if the first SC value of the first gas separation membrane module is specified.

Hereinafter, a highly permeable gas recovery apparatus and method according to an embodiment of the present invention will be described in detail with reference to the drawings.

1, a highly permeable gas recovery apparatus according to an embodiment of the present invention includes a separating gas supply unit 110, a gas mixing unit 120, a first gas separation membrane module 140, a second gas separation membrane module 170, a first SC regulator 150, and a second SC regulator 180.

The separation target gas supply unit 110 serves to supply a separation target gas, which is a mixture of various kinds of gases, and the separation target gas includes a target gas having high permeability. The target gas is a gas to be recovered through the first gas separation membrane module 140 and the second gas separation membrane module 170 and refers to a specific high permeability gas having a relatively small molecular size contained in the gas to be separated , For example, carbon dioxide in natural gas, nitrogen in air, hydrogen in a mixture of methane and hydrogen may be the target gas.

The gas mixing unit 120 serves to mix a target gas to be separated from the target gas supply unit 110 and a second permeable gas separated by the second gas separation membrane module 170, The mixed gas of the two permeation gases is supplied to the first gas separation membrane module 140.

The first gas separation membrane module 140 separates the injected gas into a first permeable gas and a first residual gas. The first gas separation membrane module 140 may be formed of a first gas permeable gas and a first gas permeable gas using a gas molecular size difference, Separate into residual gas.

The first gas separation membrane module 140 (and the second gas separation membrane module 170) is a collection of membrane assemblies in the form of a hollow or flat membrane having pores formed on the surface thereof. The high permeable gas having a relatively small molecular size, And a relatively low permeable gas having a relatively large molecular size remains in the interior of the separator without passing through the pores.

Since the target gas is a specific high permeability gas having a small molecular size, there is a high probability that the target gas will be contained in the permeable gas. Is contained in the residual gas. The reason why the highly permeable target gas can not permeate the pores of the gas separation membrane module and is included in the residual gas is that the pore size is not uniform due to the characteristics of the gas separation membrane module. In other words, it can be explained that the permeability of the target gas in the permeability of the gas permeating the pores of the gas separator module is smaller than the permeability of the other gas in the waste gas, so that the possibility of remaining in the gas separator module is high. The object of the present invention is to recover not only the target gas included in the transparent gas but also the target gas contained in the residual gas.

The first residual gas of the first gas separation membrane module 140 is supplied to the second gas separation membrane module 170 to recover the target gas contained in the residual gas as well as the target gas contained in the permeation gas, 2 gas separator module 170 separates the first residual gas into a second permeable gas and a second residual gas as an injector. The second permeable gas separated by the second gas separation membrane module 170 is supplied to the first gas separation membrane module 140 via the gas mixing part 120 and is separated into the first permeable gas and the first residual gas again Through the same repetitive cycling process, the recovery rate of the target gas can be increased.

On the other hand, the flow rate of each of the permeated gas and the residual gas separated by the gas separation membrane module is determined by the SC value (stage cut) controlled by the SC regulator. That is, the first gas separation membrane module 140 separates the injected gas into the first permeable gas and the first residual gas according to the first SC value (? 1 ) set by the first SC regulator 150, The membrane module 170 separates the injected gas into a second permeable gas and a second residual gas in accordance with the second SC value (? 2 ) set by the second SC regulator 180.

When the target gas concentration in the second permeable gas and the target gas concentration in the target gas to be separated are different from each other as the second permeable gas is included in the injection gas of the first gas separation membrane module 140, Even if the first SC value of the first gas separation membrane module 140 is specified by changing the concentration of the target gas contained in the injected gas (the separation target gas + the second transmission gas) supplied to the first residual gas 140, The gas concentration can not be kept constant.

In order to increase the target gas recovery rate by using the first gas separation membrane module 140 and the second gas separation membrane module 170, in order to maintain the target gas concentration in the first permeation gas constant, The gas concentration and the target gas concentration of the gas to be separated must be matched. To satisfy this, the first SC value (θ 1 ) should be specified by the following equation. For reference, the SC value (?) Means the ratio of permeate flow rate (F p ) to the inlet gas flow rate (F f ) (θ = F p / F f ), and the selectivity ( A = P A / P B ) of the permeability (P A ) of the high permeable gas to the permeability (P B ) of the permeable gas.

(Equation 1)

Figure 112016001074711-pat00005

( 1 is the first SC value, Z F is the target gas concentration of the separation target gas,? 1 is the selectivity of the first gas separation membrane module, and? 2 is the selectivity of the second gas separation membrane module)

When the selectivities of the first gas separation membrane module 140 and the second gas separation membrane module 170 are the same, the first SC value? 1 is specified by the following expression (2).

(Equation 2)

Figure 112016001074711-pat00006

(? 1 is the first SC value, Z F is the target gas concentration of the separation target gas, and? 1 is the selectivity of the first gas separation membrane module or the second gas separation membrane module)

As described above, the present invention increases the recovery rate of the target gas through the repetitive gas separation process using the first gas separation membrane module 140 and the second gas separation membrane module 170, 1 ) is determined as in Equation ( 1 ) or (2), the target gas concentration in the first permeable gas can be kept constant by matching the target gas concentration of the second permeable gas with the target gas concentration of the gas to be separated. In addition, the present invention provides a configuration capable of selectively controlling the recovery rate by adjusting the second SC value (? 2 ).

In order to selectively regulate the recovery rate (R tot ) of the highly permeable gas recovery apparatus according to the present invention, the second SC value ([theta] 2 ) is controlled as shown in Equation 3 below.

(Equation 3)

Figure 112016001074711-pat00007

R 1 is the recovery rate of the first gas separation membrane module, θ 1 is the first SC value, e 1 is the second SC value, θ 1 is the second SC value, Δ R is R tot -R 1 , R tot is the total recovery rate of the high permeable gas recovery device, Is the concentration of the first gas separation membrane module, and e 2 is the degree of concentration of the second gas separation membrane module)

In the formula 3, the enrichment of (e), as referring to a non-(e = w / Z F) of the injected gas in the target gas concentration (Z F) compared to the transmission target gas concentration (w) of the base, e 1 is injected into the gas Means a ratio of a target gas concentration of the first permeable gas to a target gas concentration of the second permeable gas (the gas to be separated + the second permeable gas), e 2 denotes a ratio of the target gas concentration of the second permeable gas Means the ratio of the target gas concentration.

In Equation 3, R is the recovery rate of the target gas recovered through the gas separation membrane module, and R is expressed as the product of the SC value (?) And the degree of concentration (e) (R =? Furthermore, R tot is a first gas separation membrane module 140 and the second means the full recovery of high permeability gas recovery apparatus according to the invention comprises a gas separation membrane module (170), R tot is the following equation 4 And the second SC value from Equation (4) can be summarized as a function of ΔR as shown in Equation (3).

(Equation 4)

Figure 112016001074711-pat00008

(R tot is high permeability gas full recovery of the recovery unit, R 1 is a first gas separation membrane recovery of modules, R 2 is a second recovery rate of the gas separation membrane module, e 1 is a concentration of the first gas separation membrane module, e 2 is The concentration of Cr in the second gas separation membrane module is 1 -? 1 ? E 1 , and R tot - R 1 is? R)

(= R tot- R 1 ) can be controlled by adjusting the second SC value (? 2 ) as the second SC value (? 2 ) is arranged as shown in Equation (3) The total recovery R tot of the highly permeable gas recovery device according to the invention.

The first gas separation membrane module 140, the second gas separation membrane module 170, the first gas separation membrane module 170, the first gas separation membrane module 170, and the second gas separation membrane module 170, which constitute the highly permeable gas recovery device of the present invention, The SC regulator 150 and the second SC regulator 180 have been described above. However, in the above-described configuration, the first gas separator module 140 and the second gas separator module 170 are repeatedly used for gas separation Second, by specifying the first SC value (? 1 ) as shown in Equation ( 1 ) or (2), the target gas concentration of the second permeable gas and the target gas concentration of the target gas are made to coincide with each other 1, the target gas concentration in the permeable gas can be maintained constant. Third, the total recovery (R tot ) of the highly permeable gas recovery apparatus according to the present invention can be controlled through adjustment of the second SC value (θ 2 ) It becomes possible to selectively control.

Meanwhile, the high permeable gas recovery apparatus according to an embodiment of the present invention may further include a first compression tank 130 and a second compression tank 160 in addition to the above-described components.

The first compression tank 130 and the second compression tank 160 are provided at the front ends of the first gas separation membrane module 140 and the second gas separation membrane module 170 respectively and include a first gas separation membrane module 140, 2 gas separation membrane module 170, as shown in FIG. In the case of the first compression tank 130, the injection gas, that is, the mixture gas of the separation target gas and the second permeation gas is compressed and supplied to the first gas separation membrane module 140. In the case of the second compression tank 160, That is, the first residual gas, and supplies the compressed gas to the second gas separation membrane module 170.

On the other hand, the gas to be separated supplied from the gas supply part 110 to be separated is set to be supplied at a constant flow rate, but the characteristics that change in real time due to various factors such as equipment condition, temperature, And when the flow rate of the gas to be separated is changed, the flow rate of the permeated gas and the residual gas separated by the first gas separation membrane module 140 and the second gas separation membrane module 170 are affected. That is, when the flow rate of the gas to be separated is changed, the flow rate of the permeated gas and the residual gas can not be maintained constant.

It is necessary to change the supply pressure of the injection gas injected into the first gas separation membrane module 140 and the second gas separation membrane module 170 in accordance with the change in the flow rate of the separation target gas . Specifically, the supply pressure P of the first compression tank 130 and the second compression tank 160 can be set as shown in the following Equation 5 in order to correspond to the change in the flow rate of the separation target gas. That is, if the change occurs in the flow rate of the separated target gas, the non-flow rate of the separation target gas (v / v o), the first supply pressure (P o), the first compression tank 130 and the second compression tank (160 multiplied by the ) Is set. At this time, the supply pressure of the first compression tank 130 and the supply pressure of the second compression tank 160 are set to be the same.

A supply pressure control unit may be further provided to control the supply pressure of the first compression tank 130 and the supply pressure of the second compression tank 160 according to a change in the flow rate of the separation target gas, The supply pressure of the first compression tank 130 and the supply pressure of the second compression tank 160 can be set using the equation 5 by checking the change in the flow rate of the gas.

(Equation 5)

Figure 112016001074711-pat00009

(P is the flow rate, v o is the flow rate of the first separate target gas, P o of the real-time setting first supply pressure of the compression tank (130) and the second compression tank 160 that is, v is separated in real time variable target gas comprises a The first supply pressure of the first compression tank 130 and the second compression tank 160)

The highly permeable gas recovery apparatus according to the embodiment of the present invention has been described above. Next, a highly permeable gas recovery method according to an embodiment of the present invention will be described. The highly permeable gas recovery method according to one embodiment of the present invention proceeds under the structure of the apparatus of FIG. 1, that is, the highly permeable gas recovery apparatus according to an embodiment of the present invention.

First, the first SC value (? 1 ) is specified as shown in Equation ( 1 ) or (2) so that the target gas concentration of the second transparent gas and the target gas concentration of the gas to be separated coincide with each other. When the selectivities of the first gas separation membrane module 140 and the second gas separation membrane module 170 are different from each other, the first SC value (? 1 ) of Equation 1 is applied, and the first gas separation membrane module When the selectivity of the two gas separation membrane modules 170 is the same, the first SC value (? 1 ) of Equation 2 is applied.

In order to specify the first SC value (? 1 ) as described above and to selectively control the overall recovery (R tot ) of the highly permeable gas recovery apparatus according to an embodiment of the present invention, a second SC value θ 2 ) is set as shown in Equation 3. As the second SC value ([theta] 2 ) is summarized as a function of [Delta] R as in Equation 3, selective control of the total recovery rate R tot is possible through adjustment of the second SC value ([theta] 2 ).

In this manner, the target gas recovery process using the first gas separation membrane module 140 and the second gas separation membrane module 170 proceeds with the first SC value? 1 and the second SC value? 2 set .

Specifically, a separation target gas containing a target gas with high permeability is supplied from the separation target gas supply unit 110 to the gas mixing unit 120, and the gas mixing unit 120 separates the separation target gas and the second gas separation membrane module 170, and the mixture gas of the separation target gas and the second permeation gas is supplied to the first compression tank 130. The first permeation gas and the second permeation gas are mixed with each other. Only the gas to be separated is supplied to the first compression tank 130 because the second permeable gas of the second gas separation membrane module 170 is not supplied to the gas mixing portion 120 during the initial operation.

The first compression tank 130 compresses the mixed gas to a predetermined pressure and injects the mixed gas into the first gas separation membrane module 140. It is necessary to vary the supply pressure of the injection gas injected into the first gasket separation membrane module 140 in accordance with the change in the flow rate of the separation target gas in order to cope with the change in the flow rate of the separation target gas. The supply pressure P is set as shown in the above-mentioned equation (5). The supply pressure of the second compression tank 160, which will be described later, is also set equal to the supply pressure of the first compression tank 130.

The injected gas injected into the first gasketing membrane module 140 at a constant supply pressure P is separated into the first permeable gas and the first residual gas by the first gasketing membrane module 140. At this time, the flow rate of the first permeable gas and the flow rate of the first residual gas are determined by the first SC value (? 1 ) specified as shown in Equation 1 or 2, and the first SC value? 1 ) is presumed to match the target gas concentration of the second permeable gas with the target gas concentration of the gas to be separated. As the first SC value (? 1 ) is specified so that the target gas concentration of the second transparent gas and the target gas concentration of the separation target gas are specified, the concentration of the target gas recovered through the first transparent gas can be maintained constant .

The first residual gas separated by the first gas separation membrane module 140 is supplied to the second compression tank 160 and the second compression tank 160 is supplied with the same supply pressure as the supply pressure of the first compression tank 130. [ The first residual gas is injected into the second gas separation membrane module 170 under pressure.

The second gas separation membrane module 170 separates the injected first residual gas into a second permeable gas and a second residual gas. At this time, the flow rate of the second permeable gas and the flow rate of the second residual gas are determined by the set second SC value (? 2 ). Also, as the second SC value (? 2 ) is summarized as a function of? R as in Equation (3), selective control of the total recovery rate (R tot ) is possible through adjustment of the second SC value? 2 .

The second permeable gas separated by the second gas separation membrane module 170 is supplied to the gas mixing unit 120 and the second permeable gas and the gas to be separated are mixed in the gas mixing unit 120. Then, the mixed gas of the second permeable gas and the separation target gas is supplied to the first gas separation membrane module 140 through the first compression tank 130, and the target gas recovery process is repeatedly performed as described above.

110: separating gas supply unit 120: gas mixing unit
130: first compression tank 140: first gas separation membrane module
150: first SC regulator 160: second compression tank
170: Second gas separation membrane module 180: Second SC regulator

Claims (11)

A separation target gas supply unit for supplying a separation target gas containing a highly permeable target gas to be recovered;
A gas mixing unit for mixing the object gas to be separated and the second transparent gas;
A first gas separation membrane module for separating a mixed gas of a gas to be separated and a second transparent gas into a first transparent gas and a first residual gas in accordance with a first SC value (? 1 ) set; And
And a second gas separation membrane module for separating the first residual gas into a second permeable gas and a second residual gas in accordance with a second SC value (&thetas; 2 )
The second transparent substrate is supplied to the gas mixing portion,
It is possible to specify the first SC value (? 1 ) so that the target gas concentration of the second transparent gas coincides with the target gas concentration of the gas to be separated, thereby maintaining the target gas concentration of the first transparent gas constant,
The target gas is a specific high permeability gas having a relatively small molecular size contained in the gas to be separated,
Wherein the overall recovery (R tot ) of the high permeable gas recovery device is controllable by adjusting the second SC value (? 2 ), and the second SC value (? 2 ) is set by the following equation Permeable gas recovery device.
(expression)
Figure 112018001732927-pat00019

R 1 is the recovery rate of the first gas separation membrane module, θ 1 is the first SC value, e 1 is the second SC value, θ 1 is the second SC value, Δ R is R tot -R 1 , R tot is the total recovery rate of the high permeable gas recovery device, Is the concentration of the first gas separation membrane module, and e 2 is the degree of concentration of the second gas separation membrane module)
The apparatus of claim 1, wherein the first SC value (θ 1 ) is specified by the following equation:
(expression)

( 1 is the first SC value, Z F is the target gas concentration of the separation target gas,? 1 is the selectivity of the first gas separation membrane module, and? 2 is the selectivity of the second gas separation membrane module)
The method according to claim 1, wherein the selection of the first gas separation membrane module and the selectivity of the second gas separation membrane module are the same,
Wherein the first SC value (&thetas; 1 ) is specified by the following equation.
(expression)
Figure 112018009736514-pat00011

(? 1 is a first SC value, Z F is a target gas concentration of a separation target gas,? 1 is a selectivity of the first gas separation membrane module or a selectivity of the second gas separation membrane module)
delete The apparatus of claim 1, further comprising a first compression tank and a second compression tank,
Wherein the first compression tank supplies the mixed gas of the separation target gas and the second permeation gas to the first gas separation membrane module at a specific supply pressure,
The second compression tank supplies the first residual gas to the second gas separation membrane module at a specific supply pressure,
Wherein the supply pressure of the first compression tank and the supply pressure of the second compression tank are set to be the same.
The high permeability gas recovery device according to claim 5, wherein the supply pressure (P) of the first compression tank and the supply pressure (P) of the second compression tank are calculated by the following equations.
(expression)
Figure 112016001074711-pat00013

(P is the flow rate of the supply pressure, v is a real-time variation supply gas of the first compression tank and the second compression tank in which real-time setting, v o is the flow rate of the first feed gas, P o is the first compression tank and the second compression tank Of the initial supply pressure)
The first gas separation membrane module and the second gas separation membrane module are configured to separate the injected gas into the first permeable gas and the first residual gas through the first gas separation membrane module, 2 permeable gas and a second residual gas, wherein the first gas separation membrane module is supplied with a separation target gas and a second transmission gas containing a high permeable target gas to be recovered,
The first gas separation membrane module separates the injected gas into a first permeable gas and a first residual gas according to a first SC value (? 1 )
The second gas separation membrane module separates the first residual gas into a second permeable gas and a second residual gas in accordance with the set second SC value (? 2 )
The first SC value? 2 is specified so that the target gas concentration of the second transparent gas coincides with the target gas concentration of the gas to be separated, so that the target gas concentration of the first transparent gas is kept constant,
The target gas is a specific high permeability gas having a relatively small molecular size contained in the gas to be separated,
Wherein the overall recovery (R tot ) of the high permeable gas recovery device is controllable by adjusting the second SC value (? 2 ), and the second SC value (? 2 ) is set by the following equation Permeable gas recovery method.
(expression)
Figure 112018001732927-pat00020

R 1 is the recovery rate of the first gas separation membrane module, θ 1 is the first SC value, e 1 is the second SC value, θ 1 is the second SC value, Δ R is R tot -R 1 , R tot is the total recovery rate of the high permeable gas recovery device, Is the concentration of the first gas separation membrane module, and e 2 is the degree of concentration of the second gas separation membrane module)
8. The method of claim 7, wherein the first SC value (? 1 ) is specified by the following equation.
(expression)
Figure 112016001074711-pat00014

( 1 is the first SC value, Z F is the target gas concentration of the separation target gas,? 1 is the selectivity of the first gas separation membrane module, and? 2 is the selectivity of the second gas separation membrane module)
The method as claimed in claim 7, wherein the selection of the first gas separation membrane module and the selectivity of the second gas separation membrane module are the same,
Wherein the first SC value (&thetas; 1 ) is specified by the following equation.
(expression)
Figure 112018009736514-pat00015

(? 1 is the first SC value, Z F is the target gas concentration of the separation target gas, and? 1 is the selectivity of the first gas separation membrane module or the second gas separation membrane module)
delete 8. The apparatus of claim 7, further comprising a first compression tank and a second compression tank,
The first compression tank supplies the mixture gas of the separation gas and the second permeation gas to the first gas separation membrane module at a specific supply pressure and the second compression tank supplies the first residual gas to the second gas separation membrane Module,
Wherein the supply pressure of the first compression tank and the supply pressure of the second compression tank are the same and are calculated by the following equation.
(expression)
Figure 112016001074711-pat00017

(P is the flow rate of the supply pressure, v is a real-time variation supply gas of the first compression tank and the second compression tank in which real-time setting, v o is the flow rate of the first feed gas, P o is the first compression tank and the second compression tank Of the initial supply pressure)
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Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2001062240A (en) 1999-08-27 2001-03-13 Air Liquide Japan Ltd Method and device for adjusting concentration of mixed gas

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2001062240A (en) 1999-08-27 2001-03-13 Air Liquide Japan Ltd Method and device for adjusting concentration of mixed gas

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