CN1178715A - Method and apparatus for treating gas through adsorption with variable production flow speed - Google Patents
Method and apparatus for treating gas through adsorption with variable production flow speed Download PDFInfo
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- CN1178715A CN1178715A CN 97118028 CN97118028A CN1178715A CN 1178715 A CN1178715 A CN 1178715A CN 97118028 CN97118028 CN 97118028 CN 97118028 A CN97118028 A CN 97118028A CN 1178715 A CN1178715 A CN 1178715A
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- adsorber
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- recompression
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Abstract
The present invention relates to a process that carries out a cycle on a monoadsorber (1). The adsorber connectes, on the one hand, to at least one container (2, 3) via a line (8, 10) fitted with a variable-opening valve (9, 11) and, on the other hand, to a reversible compression/pumping machine coupled to a speed variator (5). Application ot the invention in particular to the production of oxygen at a variable flow rate from atmospheric air.
Description
The present invention relates to a kind of method by pressure-swing adsorption processing gas, its transformation scope is for being higher than atmospheric high circulating pressure to subatmospheric low circulating pressure.Relate in particular to a kind of method of from atmosphere, producing oxygen.
The object of the present invention is to provide a kind of method and apparatus, this method and apparatus can make a single stage adsorption device, or one group of adsorber is used under the very big situation of production change in flow, especially for use in requiring within a certain period of time, make nominal flow rate be varied to the situation of low-speed running, make the round-robin peak pressure remain on steady state value as far as possible simultaneously.
Based on above-mentioned purpose, theme of the present invention is a kind of method by pressure-swing adsorption processing gas, and its transformation scope is characterized in that for being higher than atmospheric high circulating pressure to subatmospheric low circulating pressure:
Use an adsorber, be connected with at least one container and a reversible compressor/pump on it;
Carry out a circulation in adsorber, this circulation comprises the production phase, comprises the regeneration stage of a purifying step that the counterflow pump in this stage makes circulating pressure reduce to low pressure and comprises a maximum back and the recompression stage of stream recompression step; With
In the production phase, in the process of purifying step and last recompression step, when producing flow velocity and reduce (or increase) to the bigger value D of second variation from initial value DN, the rotating speed of machine just reduces (or increase), just correspondingly minimizing (or increasing) of flow section in the production phase by the product gas of adsorber discharge, thereby production phase, purifying step and the time length that recompresses step at last just increase (or minimizing).
Another theme of the present invention is a kind of equipment that aforesaid method is implemented.According to an aspect of of the present present invention, this equipment comprises:
One adsorber, its end that is called outlet links to each other with at least one container via a pipeline that has the valve of adjustable open degree.
One reversible compressor/pump, it links to each other with the other end (inlet) of adsorber.
One variator that is connected with reversible compressor/pump.
Embodiments of the invention are described by non-limiting description referring now to accompanying drawing, wherein:
Fig. 1 is the synoptic diagram of oxygen production equipment of the present invention;
Fig. 2 is the synoptic diagram that equipment shown in Figure 1 is finished round-robin embodiment, and this equipment moves under the rated speed situation;
Fig. 3 is and the corresponding synoptic diagram of Fig. 2 to represent the rotating speed of reversible favourable turn;
Fig. 4 and Fig. 5 be respectively with Fig. 2 and the corresponding synoptic diagram of Fig. 3, just equipment moves under the low speed situation.
Facility shown in Figure 1 is used for producing oxygen-rich air from atmosphere, or unpurified oxygen, (for simplicity, being called oxygen), and its purity is generally between 90%～95%.
In the embodiment shown, whole set of installation mainly comprises 1, two container 2 of a single stage adsorption device and 3, one reversible leafy compressor/pump 4, Roots type preferably, the variator 5 that is connected with machine 4, and an ECU 6.The outlet 7 of adsorber 1 (promptly via this outlet gas being drained) is connected with container 2 via a pipeline 8 that has the valve 9 of adjustable open degree.Outlet 7 also is connected with container 3 via another pipeline 10 that has the valve 11 of adjustable open degree.
In two inlet/outlets of machine 4, one of them mouthful directly is connected with the inlet 12 of adsorber, inlet 12 be positioned at adsorber with the outlet 7 relative the other ends.Another mouthful directly communicates with atmosphere.Here " directly ", refer to and be on relevant pipeline, not establish valve.
Draw all-product line 13 from container 3, under meter 14 is used for measuring the flow velocity by all-product line 13 gas that transports.Under meter 14 passes to ECU 6 to the signal of the measured flow velocity of representative, and ECU 6 passes to variator 5 and valve 9 and valve 11 to signal.The information that relies on this signal to transmit is regulated the rotating speed of machine 4, and the open degree of valve 9 and valve 11, and this point will be described in detail hereinafter.
Rely on described equipment, in adsorber 1, realize circulation as shown in Figure 2, so that produce oxygen at nominal flow rate DN.Loop cycle T can be one minute to several minutes.In the present embodiment, T=90 second.Among Fig. 2, be that abscissa is an ordinate with absolute pressure P with time t, the line of band arrow is represented to come in and go out in the kinestate and the point of destination of the gas of adsorber.
Referring now to Fig. 1 to Fig. 3, the embodiment of a complete cycle is described.This circulates between two ultimate pressures and changes, and is referred to as high pressure or peak pressure PM, and its pressure is roughly in normal atmosphere and 2 * 10
5Between the Pa, more definite, 1 to 1.6 * 10
5Between the Pa, and low pressure or minimum pressure p
m, its pressure is roughly 0.2～6.5 * 10
5Between the Pa.
Circulation comprises following several successive step:
(a) from t=0 to t
1(=20S) utilizes processed ambient air to carry out recompression step last and stream, and in this step, machine 4 is used as compressor and turns round with its rated speed VN (Fig. 3).Valve 9 and valve 11 are closed, and pressure increases to high pressure P M nearly by an intermediate pressure PI;
(b) from t
1To t
2(=30S) almost is isobaric production stage, and pressure remains on high circulating pressure PM.In this step, machine 4 still is taken as compressor with speed VN running, and valve 11 is opened, and product gas (impure oxygen) drains into container 3 via the outlet 7 of adsorber;
(c) from t
2To t
3(=40S) is first and flow depressurization step, makes pressure reduce to an Intermediate High Pressure, and its pressure is higher than PI.Valve 11 is closed in this step, and valve 9 is opened, and like this, will in fact contain the mixture of the product gas that will produce to some extent, drains into container 2 by the outlet 7 of adsorber.
In this step, adopt a reduction of speed gradient R earlier
1, and then adopt a rightabout accelerating gradient R
2(Fig. 3), machine 4 being changed turns to.The slope of these two gradients can be identical, also can be different.At t
3The place, the rotating speed of machine 4 is-VN;
(d) from t
3To t
4(=70S), purifying step makes pressure reduce to low pressure Pm by counterflow pump.In this step, the gas that is rich in high absorbability component (nitrogen and impurity) is extracted with the mode of the adverse current inlet 12 from adsorber, is discharged in the ambient atmosphere.And in this step, machine 4 is used as vacuum pump with speed one VN running, and valve 9 and valve 11 are all closed;
(e) from t
4To t
5(=80S), the adverse current elution/drawing step of product gas, this step almost is at the inferior row of compressing into of low pressure Pm.In this step, the open degree of valve 11 is different from the open degree in the production phase (b), and the product gas that is come out by container 3 enters adsorber with reflux type, relies on machine 4 to rotate with the speed of a VN and realizes synchronous adverse current suction;
(f) from t
5To T, utilize the gas that discharges from equalizing reservoir 2 to carry out the recompression of first adverse current, make pressure rise to intermediate pressure PI.In this step, valve 11 is closed, and valve 9 is opened, but its open degree is different from first and flows the open degree of depressurization step (c).Like this, the outlet 7 via adsorber enters as adverse current by the gas of container 2.And, in this step, adopt a deceleration gradient R earlier
3, adopt a rightabout accelerating gradient R then
4(Fig. 3), machine 4 is changed once more turn to, the slope of these two gradients can be identical, also can be different.At the T place, the rotating speed of machine 4 is+VN.
Step (b) has constituted the production phase of adsorber, and step (c) (d) and (e) has constituted the regeneration stage of adsorber, step (f) and (a) constituted recompression stage of adsorber.
When the oxygen demand by pipeline 13 reduces significantly, to produce flow velocity and reduce to D=α DN (α＜1) from rated value DN, this variation is detected by velocimeter 14, and ECU 6 has received relevant information.
ECU 6 act on simultaneously then variator 5 and valve 9 and valve 11 (open degree by open the position be converted to close the used time of position), so just can circulate by Fig. 4 and method change shown in Figure 5.
On the one hand, in the end recompress step (a), production stage (b), in purifying step (d) and this several stages of elution step (e), the rotating speed of machine 4 is owing to the effect of a factor R reduces.This point will be explained below.
Thereby, rotating speed by in step (a) and (b)+R.VN changes into by in step (d) with the R.VN (e).
On the other hand, step (a) (b), (d) and time length (e) prolonged, and the time length is the 1/R of former time length.On the contrary, first and time length of flowing depressurization step (c) and first adverse current recompression step (f) with move the used time by initial flow rate and do not compare and change.
Therefore, in step (c) with (f), the rotating speed of machine 4 is in the foregoing identical timed interval, and to-R.VN, vice versa by+R.VN transposing.So variator 5 is by changing gradient R ' successively
1, R '
2, R '
3, R '
4(Fig. 5) make machine deceleration and acceleration.
At last, in order to make machine keep-up pressure PM and Pm in low cruise, valve 9 and 11 open degree will correspondingly reduce in step (b) and (e).
Circulation shown in Figure 4 equally also comprises the step shown in Fig. 2 (a) and (f), but following relation is arranged:
Loop cycle: T '=T/ α
Step (a) is (d) and time length (e): t ' (b)
1, t '
2-t '
1, t '
4-t '
3, t '
5-t '
4, they equal corresponding specified duration of runs and multiply by coefficient 1/R.
Specifically, if in an embodiment to the demand ∝ DN of product gas, t wherein
3-t
2(=C)=T-t
5(=f)=10S:
R＝(T-20)/((T/α-20)。
As a kind of distortion, as among Fig. 1 shown in the with dashed lines, be provided with bypass pipe 15 at the two ends of valve 11, the valve 16 of an additional adjustable open degree is installed on the bypass pipe, valve 16 is by ECU 6 controls.Like this, open valve 11 or valve 16, open valve 16 or valve 11 in elution step (e) in the production phase (b).If do not establish bypass pipe 15, be inconsistent in the open degree of production phase (b) and elution stage (e) valve 11.As another distortion, use from the gas of container 3 and realize elution (step (e)), recompress (step (f)) to small part and be subjected to from the influence of the gas of container 2.
Specified speed that it should be noted that machine 4 can be according to turning to difference and difference, in any case above-mentioned formula all relates to two values, so that calculate the rotating speed of machine 4 under the low cruise situation.
Claims (10)
1, a kind of method by pressure-swing adsorption processing gas, its transformation scope is for being higher than atmospheric high circulating pressure (PM) to subatmospheric low circulating pressure (Pm), wherein:
One adsorber (1) is connected with a container (2,3) and a reversible compressor/pump (4) at least on it;
Carry out a circulation in adsorber, this circulation comprises the production phase (b), comprises the regeneration stage of a purifying step (d), and the counterflow pump in this stage makes circulating pressure reduce to low pressure, and the recompression stage (a) that comprises a last also stream recompression step;
At production phase (b), in the process in cleansing phase (d) and last recompression stage (a), when producing flow velocity and reduce (or increase) to the bigger value D of second variation from rated value DN, the rotating speed of machine (4) just reduces (or increase), just correspondingly minimizing (or increasing) of flow section in the production phase (b) by adsorber (1) expellant gas, thereby the production phase (b), the time length of purifying step (d) and last recompression step (a) just increases (or minimizing).
2, method according to claim 1 is characterized in that:
The regeneration stage comprise to small part be the final step (e) that the adverse current elution carried out under round-robin low pressure (Pm)/pump is inhaled, in this stage, the gas that is stored in first container (3) is sent into adsorber (1) with reflux type, and simultaneously, the gas in the adsorber is taken away in the mode of adverse current;
In above-mentioned steps (e), reduce (or increase) when above-mentioned second is worth D when producing flow velocity from above-mentioned first value DN, the rotating speed of machine (4), and be positioned at gas flow cross section between adsorber (1) and first container (3), also correspondingly reduce (or increase), thereby the time that elution/pump is inhaled and this step (e) is continued just increases (or minimizing).
3, method according to claim 1 and 2 is characterized in that:
The regeneration stage comprises first and flow depressurization step (e), and in this step, gas flows into second container (2) from adsorber, and the recompression stage comprises the recompression step (f) of first adverse current, and the gas source of use is in this container;
Reduce (or increase) to the above-mentioned second value D when producing flow velocity from the above-mentioned first value DN, first and flow depressurization step (c) and first adverse current to recompress the time that step (f) continued almost constant.
4, according to the described method of claim 3, it is characterized in that:
First and flow in depressurization step (c) and first adverse current recompression step (f), turning to of reversible favourable turn device (4) changes;
When the production flow velocity reduces (or increase) to the second value D from above-mentioned initial value DN, the deceleration gradient of reversible favourable turn device and accelerating gradient (R
1To R
4) slope in Umklapp process, change.
5, according to claim 3 or 4 described methods, it is characterized in that: first and flow in depressurization step (c) and first adverse current recompression step (f), when the production flow velocity reduced (or increase) to second value D from the above-mentioned first value DN, the gas flow cross section that is positioned between adsorber (1) and second container (2) was almost constant.
6, a kind of equipment by pressure-swing adsorption processing gas, its transformation scope comprises for being higher than between atmospheric high circulating pressure (PM) and the subatmospheric low circulating pressure (pm):
One adsorber (1), its end (7) that is called outlet is via a valve (9 with adjustable open degree; 11) pipeline (8; 10) with at least one container (2; 3) link to each other;
One reversible compressor/pump (4), the other end (12) of it and adsorber, promptly inlet links to each other;
One variator (5) that is connected with reversible compressor/pump.
7, equipment according to claim 6 is characterized in that the outlet (7) of adsorber (1) also has the valve (11 that can regulate open degree via one; 9) second pipeline (10; 8) link to each other with second container (3).
8,, it is characterized in that above-mentioned route (10) has bypass pipe (15) in adjustable open degree valve (11) two ends cross-over connection, is equipped with another valve that can regulate open degree (16) on the bypass pipe (15) according to claim 6 or 7 described equipment.
9,, it is characterized in that it comprises that one is used for coordinating the action of joint each valve of control (9,11,16) and the unit (6) of variator (5) according to any described equipment in the claim 6 to 8.
10, equipment according to claim 9 is characterized in that unit (6) is established to be used for adjusting the deceleration gradient of reversible favourable turn device (4) and the slope (R of accelerating gradient
1～R
4) equipment, these slopes are functions of the rotating speed that applies of variator (5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 97118028 CN1178715A (en) | 1996-07-30 | 1997-07-30 | Method and apparatus for treating gas through adsorption with variable production flow speed |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR9609592 | 1996-07-30 | ||
| CN 97118028 CN1178715A (en) | 1996-07-30 | 1997-07-30 | Method and apparatus for treating gas through adsorption with variable production flow speed |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1178715A true CN1178715A (en) | 1998-04-15 |
Family
ID=5174625
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 97118028 Pending CN1178715A (en) | 1996-07-30 | 1997-07-30 | Method and apparatus for treating gas through adsorption with variable production flow speed |
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| Country | Link |
|---|---|
| CN (1) | CN1178715A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101721880A (en) * | 2008-10-20 | 2010-06-09 | 太平洋联合工业公司 | Vsa gas concentrator using a reversing blower |
| CN101797465B (en) * | 2010-02-02 | 2012-07-25 | 陕西高芯超滤膜科技有限责任公司 | Pressure-reduction zero-emission energy-saving gas dewatering device |
-
1997
- 1997-07-30 CN CN 97118028 patent/CN1178715A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101721880A (en) * | 2008-10-20 | 2010-06-09 | 太平洋联合工业公司 | Vsa gas concentrator using a reversing blower |
| CN101797465B (en) * | 2010-02-02 | 2012-07-25 | 陕西高芯超滤膜科技有限责任公司 | Pressure-reduction zero-emission energy-saving gas dewatering device |
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