CN1833755A

CN1833755A - Improved one-section variable pressure obsorbing gas separation method

Info

Publication number: CN1833755A
Application number: CN 200610056985
Authority: CN
Inventors: 宋宇文
Original assignee: Chengdu Tianli Chemical Engineering Technology Co Ltd
Current assignee: Chengdu Tianli Chemical Engineering Technology Co Ltd
Priority date: 2004-06-11
Filing date: 2004-06-11
Publication date: 2006-09-20
Anticipated expiration: 2024-06-11
Also published as: CN100423812C

Abstract

An improved one-segment variable-pressure adsorption method for separating gas is disclosed. The phase easy to adsorb and the phase difficult to adsorb are separated from each other to obtain relative products or the product both easy and difficult to adsorb. Such steps are performed in a cycle for its adsorption tower as adsorbing, uniformly lowering pressure at both ends, reversely lowering pressure, uniformly raising pressure at both ends and final rising of pressure.

Description

A kind of improved one-section variable pressure absorbing gas separation method

Technical field

The application is the applying date: on June 11st, 2004, application number: 200410046597.x, denomination of invention: the dividing an application of a kind of application for a patent for invention of improved one-section variable pressure absorbing gas separation method.The present invention relates to a kind of improved one-section variable pressure absorbing gas separation method, belong to transformation adsorbed gas separation field.

Background technology

We know, in the former transformation adsorbed gas isolation technics, no matter be easily absorption mutually the still difficult absorption of product (as transformation absorption system pure carbon dioxide) mutually product (as transformation absorption hydrogen producing technology) or not only needed to obtain product mutually but also need to obtain product (adsorb as transformation decarburization is used for urea production from synthetic-ammonia transformation gas) mutually from difficulty absorption from easy absorption, adsorption tower is when carrying out drop pressure ED, gaseous mixture all is to flow out from the top of adsorption tower another adsorption tower is boosted from the top, after all pressing end, the general emptying of gas in the adsorption tower, because adsorption tower bottom gas composition and unstripped gas are approaching after adsorption tower is all pressed end, can lose a lot of available gas like this, increase the cost of product.This class technology such as Chinese patent open CN1069708A, CN1146369A, CN1171285A etc., the present invention is the improvement to above-mentioned transformation adsorbed gas isolation technics, has reduced the loss of bottom available gas significantly, but also can save power consumption and investment.

The patent of invention content

It is reasonable to the purpose of this invention is to provide a kind of investment economy, and the improvement one-section variable pressure absorbing gas separation method that operating cost is lower makes it to have the advantage of compared with prior art saving operating cost, reduces the available gas loss of device to greatest extent.

The present invention is used for separating easy absorption phase and the difficult phase component that adsorbs from gaseous mixture, and product can be easily to adsorb phase component, also can be the difficult phase component that adsorbs, and can also be easily absorption phase and difficulty absorption phase component simultaneously.In the present invention, easily absorption is relative with difficult absorption mutually mutually, rather than it is absolute, with a kind of component is easily to adsorb phase component in certain mist, but may be difficult absorption phase component in another mist, even with a kind of component in a kind of mist, because the purpose difference that will reach, may be easily to adsorb phase component, it also might be difficult absorption phase component, in addition, said here easy absorption phase component and difficult absorption phase component may be one-components, also may be the summations of several components.For example, in synthetic-ammonia transformation gas, components such as hydrogen sulfide, organic sulfur, vaporous water, carbon dioxide, methane, carbon monoxide, nitrogen, oxygen, argon gas and hydrogen are arranged, when this gas is used to produce urea, four components such as hydrogen sulfide, organic sulfur, vaporous water and carbon dioxide are called easy absorption mutually, and six components such as methane, carbon monoxide, nitrogen, oxygen, argon gas and hydrogen are called difficult absorption phase component; When being used to produce the product hydrogen of 99.99V%, nine components such as hydrogen sulfide, organic sulfur, vaporous water, carbon dioxide, methane, carbon monoxide, nitrogen, oxygen and argon gas are called easy absorption phase component, and hydrogen is called difficult absorption phase component.Here, the nitrogen in the synthetic-ammonia transformation gas, when being used to produce urea, nitrogen is difficult absorption phase component; When being used to produce the product hydrogen of 99.99V%, nitrogen is easily to adsorb phase component, and methane, carbon monoxide and oxygen also are the same with nitrogen

Technical solution of the present invention is as follows:

The present invention is used for separating easily absorption phase and difficult absorption phase component from gaseous mixture, product can be easily to adsorb phase component, it also can be difficult absorption phase component, can also be simultaneously easily absorption mutually and difficult absorption phase component, pressure swing adsorption gas separation device adsorption tower experience absorption A, two ends drop pressure 2ED ', reverse step-down BD, two ends boost pressure 2ER ', the final FR processing step that boosts successively in a cycle period.

After adsorption tower absorption A step, increase forward drop pressure ED step, after the boost pressure 2ER ' step of two ends, increase reverse boost pressure ER step simultaneously.

After the reverse step-down BD of adsorption tower step, increase and vacuumize the VC step.

Increase easily absorption phase displacement step P ' after the drop pressure 2ED ' step of adsorption tower two ends, increase the ER ' step of boosting simultaneously after reverse step-down BD step, the gas that boosts is replaced the outlet mist of P ' step from adsorption tower.

Increase easily absorption phase displacement step P ' after the drop pressure 2ED ' step of adsorption tower two ends, increase the ER ' step of boosting simultaneously after vacuumizing the VC step, the gas that boosts is replaced the outlet mist of P ' step from adsorption tower.

After the drop pressure 2ED ' step of adsorption tower two ends, increase along putting the PP step, increase after the reverse step-down BD of adsorption tower step simultaneously and clean the P step, the gas that cleans the P step directly stores adsorption tower along the surge tank V of putting PP step gas from being in along putting the adsorption tower of PP step or coming from.

Adsorption tower is forward increasing along putting PP1 step and the suitable PP2 step of putting after the drop pressure ED step, adsorption tower is increasing cleaning P1 step and is cleaning the P2 step after putting the BD step simultaneously, the gas that adsorption tower cleans the P1 step directly stores adsorption tower along the surge tank V1 of putting PP2 step gas from being in along putting the adsorption tower of PP2 step or coming from, and the gas that adsorption tower cleans the P2 step directly stores adsorption tower along the surge tank V2 of putting PP1 step gas from being in along putting the adsorption tower of PP1 step or coming from.

Adsorption tower is forward increasing along putting the PP1 step after the drop pressure ED step, along putting PP2 step and the suitable PP3 step of putting, adsorption tower is increasing cleaning P1 step after putting the BD step simultaneously, clean the P2 step and clean the P3 step, the gas that adsorption tower cleans the P1 step directly stores adsorption tower along the surge tank V3 of putting PP3 step gas from being in along putting the adsorption tower of PP3 step or coming from, the gas that adsorption tower cleans the P2 step directly stores adsorption tower along the surge tank V4 of putting PP2 step gas from being in along putting the adsorption tower of PP2 step or coming from, and the gas that adsorption tower cleans the P3 step directly stores adsorption tower along the surge tank V5 of putting PP1 step gas from being in along putting the adsorption tower of PP1 step or coming from.

Adsorption tower is when carrying out the equal pressure drop in two ends, and the equal pressure drop gas below 50% enters the adsorption tower that another carries out equal voltage rise from the bottom of adsorption tower.

Adsorption tower is when carrying out the equal pressure drop in two ends, and 15～20% equal pressure drop gas enters the adsorption tower that another carries out equal voltage rise from the bottom of adsorption tower.

The present invention is used for separating easily absorption phase and difficult absorption phase component from gaseous mixture, product can be easily to adsorb phase component, it also can be difficult absorption phase component, can also be easily absorption phase and difficult absorption phase component simultaneously, the gas of the reverse step-down one BD1 step of adsorption tower return another adsorption tower from the bottom to the adsorption tower 2ER1 that boosts, pressure swing adsorption gas separation device adsorption tower experience absorption A successively in a cycle period, drop pressure ED, reverse step-down one BD1, reverse step-down two BD2, the contrary venting body 2ER1 that boosts, reverse boost pressure ER, the FR processing step finally boosts.

After the reverse step-down two BD2 steps of adsorption tower, increase and vacuumize the VC step.

The present invention is used for separating easily absorption phase and difficult absorption phase component from gaseous mixture, product can be easily to adsorb phase component, it also can be difficult absorption phase component, can also be easily absorption phase and difficult absorption phase component simultaneously, displacement P ' step the gas that comes out from the adsorption tower top returns another adsorption tower and carries out the substitution gas ER ' that boosts from the top to adsorption tower, pressure swing adsorption gas separation device adsorption tower experience absorption A successively in a cycle period, drop pressure ED, displacement P ', reverse step-down BD, the substitution gas ER ' that boosts, reverse boost pressure ER, the FR processing step finally boosts.

The present invention is used for separating easily absorption phase and difficult absorption phase component from gaseous mixture, product can be easily to adsorb phase component, it also can be difficult absorption phase component, can also be simultaneously easily absorption mutually and difficult absorption phase component, the pressure swing adsorption gas separation device adsorption tower in a cycle period successively experience absorption A, two ends drop pressure 2ED ', vacuumize VC, two ends boost pressure 2ER ', the final FR processing step that boosts.

Be filled with activated alumina and Kiselgel A in the adsorption tower, activated alumina is seated in the adsorption tower bottom, and Kiselgel A is seated in adsorption tower top.

The adsorbent that loads from down to up in the adsorption tower is followed successively by activated alumina and molecular sieve or activated alumina, active carbon and molecular sieve.

Description of drawings

Fig. 1 is the processing step working procedure table of the embodiment of the invention 1 adsorption tower.

Fig. 2 is the process chart of the embodiment of the invention 1.

The specific embodiment

Gaseous mixture of the present invention can be synthetic-ammonia transformation gas, synthetic ammonia relief gas, synthesis gas, water-gas, natural gas, semiwater gas, blast furnace gas, Device in Gas, cracking dry gas, associated gas and oily gas making etc., also can be other arbitrary mist.

The present invention adopts improved one-section variable pressure absorbing gas separation method, the method is used for separating easily absorption phase and difficult absorption phase component from gaseous mixture, product can be easily to adsorb phase component, it also can be difficult absorption phase component, can also be easily absorption phase and difficult absorption phase component simultaneously, each adsorption tower of pressure-swing absorption apparatus experiences following steps successively in a circulation.

(1) absorption A

Gaseous mixture is sent into the adsorption tower charging aperture that is in adsorption step, part in the adsorbents adsorb gaseous mixture in the adsorption tower is easily adsorbed phase component, the difficulty of absorption absorption phase component and the easy absorption of part phase component do not flow out from the port of export and enter next workshop section or emptying, As time goes on, the total amount of adsorbent easy absorption phase component constantly increases, when the adsorbents adsorb said components is saturated, stop air inlet, this moment, absorption finished.

(2) drop pressure ED forward

After absorption finished, difficult absorption phase component concentration was higher in the interior dead space gas of adsorption tower, and this part difficult absorption phase component need be recycled.The gradation of dead space gas is discharged from adsorption tower outlet and is entered this section and finished the corresponding adsorption tower of evacuation step and boost, and gas of every row is just all pressed once, and along with the increase of all pressing number of times, the easy absorption phase component concentration in adsorption tower exit constantly increases.All press number of times to finish the easy absorption phase component concentration decision in adsorption tower exit, back by adsorptive pressure and absorption.

(3) two ends drop pressure 2ED '

After absorption A finishes, higher and the easy absorption of difficult absorption phase component concentration phase component concentration is lower in the interior dead space gas of adsorption tower, this part difficult absorption phase component need be recycled on the one hand, easily adsorbing phase component concentration on the other hand in the adsorption tower needs to improve, for this reason, must emit the gas in the adsorption tower and carry out depressurization desorption.The gradation of dead space gas enters the corresponding adsorption tower of finishing regeneration step from the discharge of adsorption tower two ends and boosts, gas of every row, just all press once, along with the increase of all pressing number of times, the easy absorption phase component concentration in exit, adsorption tower two ends constantly increases, and difficult simultaneously absorption phase component obtains recycling.When carrying out above-mentioned drop pressure at every turn, adsorption tower can carry out at two ends up and down simultaneously, also can be earlier from the adsorption tower top drop pressure forward, later stage before drop pressure balance is forward carried out reverse drop pressure to same adsorption tower simultaneously, purpose is to improve easily to adsorb phase component concentration in the adsorption tower and reclaim difficult absorption phase component, can also carry out forward drop pressure earlier, before the two pressure tower balances, stop forward drop pressure, and then carry out reverse drop pressure, the previous case can improve the adsorbent utilization rate.When carrying out the two ends drop pressure, the gas of emitting from the bottom should be less than the gas of emitting from the top.Adsorption tower of the present invention two ends drop pressure 2ED ' step and common adsorption tower drop pressure ED step are different, common adsorption tower drop pressure ED step gas is to emit from the port of export of adsorption tower, be the said forward drop pressure of the present invention, emit and adsorption tower of the present invention two ends drop pressure 2ED ' gas is import and export two ends from adsorption tower.

After adsorption tower is finished absorption A step, before all press several times and also can adopt forward drop pressure ED, then all press several times or all press for the last time and adopt two ends drop pressure 2ED ', after drop pressure finished, product easily adsorbs phase component concentration still can satisfy production requirement.

(4) displacement P '

After forward drop pressure ED or two ends drop pressure 2ED ' end, enter from adsorption tower bottom with easy absorption phase component product and to replace difficult absorption phase component in the tower, reaching the purpose of purify easy absorption phase component product, the displacement P ' step gas that comes out from the adsorption tower top returns another adsorption tower and carries out the substitution gas ER ' that boosts from the top to adsorption tower.

(5) reverse step-down BD

After two ends drop pressure 2ED ' or displacement P ' ends, send easily adsorbing phase component in the adsorption tower into next workshop section, up to the pressure balance of next workshop section till, easily adsorb phase component or as product, or act as a fuel, also can emptying.

(6) reverse step-down one BD1

After forward drop pressure ED finishes, the absorption of the difficulty of adsorption tower inner bottom part emitted mutually enter surge tank and store, utilize the gas in the surge tank adsorption tower to be boosted again from the adsorption tower bottom, generally speaking, after reverse step-down one BD1 step is finished, easily absorption phase component concentration should be greater than 30V%, more preferably greater than 80V% in the adsorption tower bottom.。

(7) reverse step-down two BD2

After reverse step-down one BD1 finishes, with in the adsorption tower easily the absorption phase component send into next workshop section, up to the pressure balance of next workshop section till, easily adsorb phase component or as product, or act as a fuel, also can emptying.

(8) vacuumize VC

After reverse step-down BD or reverse step-down two BD2 finish, adsorbent easy absorption phase component is released with vavuum pump from the adsorption tower bottom and to send into next workshop section.

(9) the contrary 2ER1 that boosts that exits

Reverse step-down two BD2 or vacuumize after VC finishes, the gas that the reverse step-down one BD1 step of adsorption tower is emitted all return the adsorption tower port of export adsorption tower of finishing reverse step-down two BD2 or vacuumizing the VC step are boosted.Increase the available gas rate of recovery that this step can improve device.

(10) the displacement exit gas ER ' that boosts

Reverse step-down BD or vacuumize after VC finishes uses the displacement P ' step gas that comes out from another adsorption tower top to carry out the substitution gas ER ' that boosts from the top to adsorption tower.

(11) two ends boost pressure 2ER '

Contrary venting the boost ER ' or vacuumize after VC finishes of 2ER1 or displacement exit gas that boosts, the gas that utilizes this section two ends drop pressure 2ED ' step to discharge, enter adsorption tower from entrance end, make the adsorption tower pressure that progressively raises, two ends boost pressure 2ER ' equates with the number of times of two ends drop pressure 2ED '.The gas of each two ends boost pressure 2ER ' is from the two ends drop pressure 2ED ' gas of different adsorption towers.This section adsorption tower two ends boost pressure 2ER ' step and common boost pressure ER step are different, common adsorption tower boost pressure ER step gas is that the port of export from adsorption tower enters, and enters and this section adsorption tower two ends boost pressure 2ER ' step gas is import and export two ends from adsorption tower.

After adsorption tower is finished absorption A step, preceding all the pressure several times when adopting forward drop pressure ED, the boost pressure ER step gas of adsorption tower then enters from the port of export of adsorption tower, does not enter from entrance point.

(12) reverse boost pressure ER

After the boost pressure 2ER ' end of two ends, the gas that utilizes drop pressure step forward to discharge enters to finish from the port of export and contraryly puts BD or vacuumize C or clean the adsorption tower of P step, makes the adsorption tower pressure that progressively raises, and boost pressure equates with the number of times of drop pressure.The gas of each boost pressure is from the drop pressure gas of different adsorption towers.

(13) FR that finally boosts

After two ends boost pressure 2ER ' step finishes, utilize the adsorption tower that is in adsorption step to work off one's feeling vent one's spleen and adsorption tower is boosted, until being raised to adsorptive pressure from the top.

Embodiments of the invention 1:

This routine unstripped gas is a synthetic-ammonia transformation gas, comprises that with coal, natural gas, oil and other be the synthetic-ammonia transformation gas of raw material.

The conversion gas of present embodiment is composed as follows:

Component	H2	N2	CO2	CO	CH4	O2+Ar	Total sulfur	Water (vapour)
Component	H2	N2	CO2	CO	CH4	O2+Ar	Total sulfur	Water (vapour)	Concentration V%	46～60	0～22	10～30	≤1～28	1～2	≤0.8	150mg/Nm3	Saturated

Temperature :≤40 ℃

Pressure: 1.2MPa (G)

As shown in Figure 2, pressure-swing absorption apparatus by adsorption tower A～K totally 11 form, in the adsorption tower from down to up the adsorbent of filling be followed successively by activated alumina and Kiselgel A, move the absorption of single tower and all press program 9 times.Present embodiment is purified to carbon dioxide more than 98% (V), is used for urea synthesis, simultaneously in the hydrogen of Huo Deing, the nitrogen gas concentration lwevel less than 5% (V), to satisfy the needs of next step operation of synthetic ammonia.

Conversion gas enters adsorption tower from the bottom, adsorbent in the adsorption tower optionally adsorbs the components such as water, organic sulfur, inorganic sulfur and carbon dioxide in the conversion gas successively, and components such as the carbon monoxide of Xi Fu partial CO 2 and difficult absorption, methane, nitrogen, hydrogen are not discharged from the port of export and entered next workshop section.Adsorption tower experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, 2E4D ' all falls in two ends four, 2E5D ' all falls in two ends five, 2E6D ' all falls in two ends six, 2E7D ' all falls in two ends seven, 2E8D ' all falls in two ends eight, 2E9D ' all falls in two ends nine, the reverse step-down BD of product carbon dioxide, two ends nine all rise 2E9R ', two ends eight all rise 2E8R ', two ends seven all rise 2E7R ', two ends six all rise 2E6R ', two ends five all rise 2E5R ', two ends four all rise 2E4R ', two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, adsorption tower is the product carbon dioxide at the gas that product carbon dioxide step-down BD step obtains, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon dioxide, carbon monoxide and methane.Be example with the A tower now, contrast Fig. 1 and Fig. 2 illustrate the processing step of present embodiment pressure-swing absorption apparatus adsorption tower in a cyclic process:

(1) absorption A

At this moment, the A tower has been finished the FR step of finally boosting, open sequencing valve 1A, 2A, conversion gas enters adsorption tower A through pipeline G11, in adsorption tower A, adsorbent optionally adsorbs the water in the conversion gas successively, organic sulfur, component such as inorganic sulfur and carbon dioxide, Xi Fu partial CO 2 and be difficult for the carbon monoxide of absorption not, methane, nitrogen, components such as hydrogen flow out through sequencing valve 2A from the port of export and enter next workshop section, As time goes on, adsorbent water, the total amount of component such as organic sulfur and inorganic sulfur and carbon dioxide constantly increases, when the adsorbents adsorb said components is saturated, stop air inlet, this moment, absorption finished, and closed sequencing valve 1A, 2A, gas concentration lwevel is controlled at 5% (V) in working off one's feeling vent one's spleen.

(2) the equal voltage drop step in the two ends first time is called for short two ends one and all falls 2E1D '

After absorption finishes,

open sequencing valve

3A, 3C, 11A and 11C, the gas in the A tower enters the C tower through pipeline G13 and G111 the C tower is carried out boost pressure in two ends (being called for short 2E1R '), after A and C pressure tower are in a basic balance, closes sequencing valve 3A, 11C.

(3) the equal voltage drop step in the two ends second time is called for short two ends two and all falls 2E2D '

After 2E1D ' end all falls in two ends one, open sequencing valve 4A, 4D and 11D, gas in the A tower enters the D tower through pipeline G14 and G111 the D tower is carried out two ends secondary boost pressure (being called for short 2E2R '), after A and D pressure tower are in a basic balance, closes sequencing valve 4D, 11A and 11D.

(4) the equal voltage drop step in two ends for the third time is called for short two ends three and all falls 2E3D '

After 2E2D ' end all falls in two ends two,

open sequencing valve

4E, 12A and 12E, gas in the A tower enters the E tower through pipeline G14 and G112 the E tower is carried out three boost pressures in two ends (being called for short 2E3R '), after A and E pressure tower are in a basic balance, closes sequencing

valve

4A, 4E and 12E.

(5) the 4th equal voltage drop step in two ends are called for short two ends four and all fall 2E4D '

After 2E3D ' end all falls in two ends three, open sequencing valve 5A, 5F and 12F, gas in the A tower enters the F tower through pipeline G15 and G112 the F tower is carried out four boost pressures in two ends (being called for short 2E4R '), after A and F pressure tower are in a basic balance, closes sequencing

valve

5F, 12A and 12F.

(6) the 5th equal voltage drop step in two ends are called for short two ends five and all fall 2E5D '

After 2E4D ' end all falls in two ends four, open sequencing valve 5G, 13A and 13G, gas in the A tower enters the G tower through pipeline G15 and G113 the G tower is carried out five boost pressures in two ends (being called for short 2E5R '), after A and G pressure tower are in a basic balance, closes sequencing valve 5A, 5G and 13G.

(7) the 6th equal voltage drop step in two ends are called for short two ends six and all fall 2E6D '

After 2E5D ' end all falls in two ends five, open sequencing valve 6A, 6H and 13H, gas in the A tower enters the H tower through pipeline G16 and G113 the H tower is carried out six boost pressures in two ends (being called for short 2E6R '), after A and H pressure tower are in a basic balance, closes sequencing valve 6H, 13A and 13H.

(8) the 7th equal voltage drop step in two ends are called for short two ends seven and all fall 2E7D '

After 2E6D ' end all falls in two ends six, open sequencing valve 6I, 8A and 8I, gas in the A tower enters the I tower through pipeline G16 and G18 the I tower is carried out seven boost pressures in two ends (being called for short 2E7R '), after A and I pressure tower are in a basic balance, closes sequencing valve 6A, 6I and 8I.

(9) the 8th equal voltage drop step in two ends are called for short two ends eight and all fall 2E8D '

After 2E7D ' end all falls in two ends seven, open sequencing valve 7A, 7J and 8J, gas in the A tower enters the J tower through pipeline G17 and G18 the J tower is carried out eight boost pressures in two ends (being called for short 2E8R '), after A and J pressure tower are in a basic balance, closes sequencing valve 7J, 8A and 8J.

(10) the 9th equal voltage drop step in two ends are called for short two ends nine and all fall 2E9D '

After 2E8D ' end all falls in two ends eight, open sequencing valve 7K, 9A and 9K, gas in the A tower enters the K tower through pipeline G17 and G19 the K tower is carried out nine boost pressures in two ends (being called for short 2E9R '), after A and K pressure tower are in a basic balance, closes sequencing valve 7A, 7K and 9K.

After 2E9D ' end all fell in two ends nine, phase component concentration was easily adsorbed greater than 80V% in the adsorption tower top; Phase component concentration is easily adsorbed greater than 85V% in the adsorption tower bottom.

(11) the reverse step-down BD of product carbon dioxide

After 2E9D ' end all falls in two ends nine, open sequencing valve KV-14a earlier, product carbon dioxide intermediate buffering jar V9 is put in product carbon dioxide step-down in the A tower, when the pressure of A tower during near V9 pressure, close sequencing valve KV14a, open sequencing valve KV14 again, product carbon dioxide buffer jar V8 is put in the product carbon dioxide step-down in the A tower, when the pressure of A tower during, close sequencing valve KV-14 near V8 pressure.

(12) the 9th equal voltage rise steps in two ends are called for short two ends nine and all rise 2E9R '

After the reverse step-down BD of product carbon dioxide finishes, open sequencing valve 7A, 7B, 9A and 9B, gas in the B tower enters the A tower through pipeline G19 and G17 the A tower is carried out nine boost pressures in two ends (being called for short 2E9R '), after A and B pressure tower are in a basic balance, closes sequencing valve 7B, 9A and 9B.

(13) the 8th equal voltage rise steps in two ends are called for short two ends eight and all rise 2E8R '

After two ends nine all rise 2E9R ' end, open sequencing valve 7A, 7C, 8A and 8C, gas in the C tower enters the A tower through pipeline G17 and G18 the A tower is carried out eight boost pressures in two ends (being called for short 2E8R '), after A and C pressure tower are in a basic balance, close sequencing valve 7A,, 7C and 8C.

(14) the 7th equal voltage rise steps in two ends are called for short two ends seven and all rise 2E7R '

After two ends eight all rise 2E8R ' end, open sequencing valve 6A, 6D and 8D, gas in the D tower enters the A tower through pipeline G16 and G18 the A tower is carried out seven boost pressures in two ends (being called for short 2E7R '), after A and D pressure tower are in a basic balance, closes sequencing valve 6D, 8A and 8D.

(15) six equal voltage rise steps in two ends are called for short two ends six and all rise 2E6R '

After two ends seven all rise 2E7R ' end, open sequencing valve 6E, 13A and 13E, gas in the E tower enters the A tower through pipeline G16 and G113 the A tower is carried out six boost pressures in two ends (being called for short 2E6R '), after A and E pressure tower are in a basic balance, closes sequencing valve 6A, 6E and 13E.

(16) the 5th equal voltage rise steps in two ends are called for short two ends five and all rise 2E5R '

After two ends six all rise 2E6R ' end, open sequencing valve 5A, 5F and 13F, gas in the F tower enters the A tower through pipeline G15 and G113 the A tower is carried out five boost pressures in two ends (being called for short 2E5R '), after A and F pressure tower are in a basic balance, closes sequencing valve 5F, 13A and 13F.

(17) the 4th equal voltage rise steps in two ends are called for short two ends four and all rise 2E4R '

After two ends five all rise 2E5R ' end, open sequencing valve 5G, 12A and 12G, gas in the G tower enters the A tower through pipeline G15 and G112 the A tower is carried out four boost pressures in two ends (being called for short 2E4R '), after A and G pressure tower are in a basic balance, closes sequencing valve 5A, 5G and 12G.

(18) the equal voltage rise step in two ends for the third time is called for short two ends three and all rises 2E3R '

After two ends four all rise 2E4R ' end,

open sequencing valve

4A, 4H and 12H, gas in the H tower enters the A tower through pipeline G14 and G112 the A tower is carried out three boost pressures in two ends (being called for short 2E3R '), after A and H pressure tower are in a basic balance, closes

sequencing valve

4H, 12A and 12H.

(19) the equal voltage rise step in the two ends second time is called for short two ends two and all rises 2E2R '

After two ends three all rise 2E3R ' end, open sequencing valve 4I, 11A and 11I, gas in the I tower enters the A tower through pipeline G14 and G111 the A tower is carried out two ends secondary boost pressure (being called for short 2E2R '), after A and I pressure tower are in a basic balance, closes sequencing valve 4A, 4I and 11I.

(20) the equal voltage rise step in the two ends first time is called for short two ends one and all rises 2E1R '

After two ends two all rise 2E2R ' end, open sequencing valve 3A, 3J and 11J, gas in the J tower enters the A tower through pipeline G13 and G111 the A tower is carried out boost pressure in two ends (being called for short 2E1R '), after A and J pressure tower are in a basic balance, closes sequencing valve 3J, 11A and 11J.

(21) FR that finally boosts

Sequencing valve KV-12 is opened after all rising 2E1R ' end in two ends one, utilizes the adsorption tower that is in adsorption step to work off one's feeling vent one's spleen and boosts from the top to the A tower, when the A pressure tower rises near adsorptive pressure, closes sequencing valve KV-12,3A.So far, the A tower has been finished a circulation, can enter next circulation again.B～K adsorption tower is the same with the circulation step of A tower, just staggers mutually on the time, sees Fig. 1 and Fig. 3.

The present embodiment result is 98% (V) for the product carbon dioxide purity, and carbon dioxide, hydrogen, nitrogen and the carbon monoxide rate of recovery are greater than 99.7% (V), and gas concentration lwevel is less than 5% (V) in product hydrogen, the nitrogen, and ton ammonia power consumption 2 is spent (instrument and electric consumption on lighting).

For present embodiment, adopt particular adsorbent combination of the present invention, under the identical situation of other condition (adsorptive pressure is 1.2MPa (G), conversion gas composition and temperature, sorption cycle time, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span), the investment of decarburization original equipment can save 8%.

Embodiments of the invention 2:

Condition such as the conversion gas composition of present embodiment, temperature, adsorbent kind, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span and embodiment 1 are in full accord, the adsorptive pressure of present embodiment is 1.8MPa (G), and the discharge pressure of product carbon dioxide is 0.005MPa.

Pressure-swing absorption apparatus is made up of 12 adsorption towers, move single tower absorption and all press program 10 times, the present embodiment pressure-swing absorption apparatus is purified to carbon dioxide more than 98% (V), be used for urea synthesis, gas concentration lwevel is less than 3V%, to satisfy the needs of next step operation in the hydrogen of adsorption tower upper end outlet, the nitrogen.

Adsorption tower experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, 2E4D ' all falls in two ends four, 2E5D ' all falls in two ends five, 2E6D ' all falls in two ends six, 2E7D ' all falls in two ends seven, 2E8D ' all falls in two ends eight, 2E9D ' all falls in two ends nine, 2E10D ' all falls in two ends ten, the reverse step-down BD of product carbon dioxide, two ends ten all rise 2E10R ', two ends nine all rise 2E9R ', two ends eight all rise 2E8R ', two ends seven all rise 2E7R ', two ends six all rise 2E6R ', two ends five all rise 2E5R ', two ends four all rise 2E4R ', two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, pressure-swing absorption apparatus is the product carbon dioxide at the gas that the reverse step-down BD of product carbon dioxide step obtains, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is 98% (V) for the product carbon dioxide purity, and carbon dioxide, hydrogen, nitrogen and the carbon monoxide rate of recovery are greater than 99.8% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen, the nitrogen; Ton ammonia power consumption 2 degree (instrument and electric consumption on lighting).

For present embodiment, adopt particular adsorbent combination of the present invention, under the identical situation of other condition (adsorptive pressure is 1.8MPa (G), conversion gas composition and temperature, sorption cycle time, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span), the investment of decarburization original equipment can save 9%.

Embodiments of the invention 3:

Condition such as the conversion gas composition of present embodiment, temperature, adsorbent kind, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span and embodiment 1 are in full accord, the adsorptive pressure of present embodiment is 3.0MPa (G), and the discharge pressure of product carbon dioxide is 0.005MPa.

Pressure-swing absorption apparatus is made up of 12 adsorption towers, move single tower absorption and all press program 10 times, the present embodiment pressure-swing absorption apparatus is purified to carbon dioxide more than 98% (V), be used for urea synthesis, gas concentration lwevel is less than 2V%, to satisfy the needs of next step operation in the hydrogen of adsorption tower upper end outlet, the nitrogen.

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, 2E4D ' all falls in two ends four, 2E5D ' all falls in two ends five, 2E6D ' all falls in two ends six, 2E7D ' all falls in two ends seven, 2E8D ' all falls in two ends eight, 2E9D ' all falls in two ends nine, 2E10D ' all falls in two ends ten, the reverse step-down BD of product carbon dioxide, two ends ten all rise 2E10R ', two ends nine all rise 2E9R ', two ends eight all rise 2E8R ', two ends seven all rise 2E7R ', two ends six all rise 2E6R ', two ends five all rise 2E5R ', two ends four all rise 2E4R ', two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, pressure-swing absorption apparatus is the product carbon dioxide at the gas that the reverse step-down BD of product carbon dioxide step obtains, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is 98% (V) for the product carbon dioxide purity, and carbon dioxide, hydrogen, nitrogen and the carbon monoxide rate of recovery are greater than 99.8% (V), and gas concentration lwevel is less than 2% (V) in product hydrogen, the nitrogen, and ton ammonia power consumption 2 is spent (instrument and electric consumption on lighting).

For present embodiment, adopt particular adsorbent combination of the present invention, under the identical situation of other condition (adsorptive pressure is 3.0MPa (G), conversion gas composition and temperature, sorption cycle time, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span), the investment of decarburization original equipment can save 9%.

Embodiments of the invention 4:

Condition such as the conversion gas composition of present embodiment, temperature, adsorbent kind, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span and embodiment 1 are in full accord, and the adsorptive pressure of present embodiment is 1.5MPa (G).

Pressure-swing absorption apparatus is made up of 5 adsorption towers, moves single tower absorption and all presses program 3 times, and gas concentration lwevel is less than 0.2V%, to satisfy the needs of next step operation in the hydrogen of present embodiment pressure-swing absorption apparatus adsorption tower upper end outlet, the nitrogen.

Experience absorption A, two ends one all fall 2E1D ', two ends two and all fall 2E2D ', two ends three and all fall 2E3D ', reverse step-down BD, two ends three and all rise 2E3R ', two ends two and all rise 2E2R ', two ends one and all rise 2E1R ', the final FR pressure swing adsorption technique step of boosting the adsorption tower of pressure-swing absorption apparatus successively in a cycle period, pressure-swing absorption apparatus is in the gas emptying of reverse step-down BD step, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product, wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is that hydrogen, nitrogen and the carbon monoxide rate of recovery improve 2V% than traditional pressure swing adsorption decarbonization technology, and gas concentration lwevel is less than 0.2V% in product hydrogen, the nitrogen, and ton ammonia power consumption 2 is spent (instrument and electric consumption on lighting).

For present embodiment, adopt particular adsorbent combination of the present invention, under the identical situation of other condition (adsorptive pressure is 1.5MPa (G), conversion gas composition and temperature, sorption cycle time, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span), the investment of decarburization original equipment can save 9%.

Embodiments of the invention 5:

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, one all falls E1D, two all fall E2D, three all fall E3D, four all fall E4D, five all fall E5D, six all fall E6D, seven all fall E7D, eight all fall E8D, nine all fall E9D, 2E10D ' all falls in two ends ten, the reverse step-down BD of product carbon dioxide, two ends ten all rise 2E10R ', nine all rise E9R, eight all rise E8R, seven all rise E7R, six all rise E6R, five all rise E5R, four all rise E4R, three all rise E3R, two all rise E2R, one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, pressure-swing absorption apparatus is the product carbon dioxide at the gas that the reverse step-down BD of product carbon dioxide step obtains, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is 98% (V) for the product carbon dioxide purity, and carbon dioxide, hydrogen, nitrogen and the carbon monoxide rate of recovery are greater than 99.7% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen, the nitrogen, and ton ammonia power consumption 2 is spent (instrument and electric consumption on lighting).

Embodiments of the invention 6:

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, one all falls E1D, two all fall E2D, 2E3D ' all falls in two ends three, reverse step-down BD, two ends three all rise 2E3R ', two all rise E2R, one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, adsorption tower is at every turn when carrying out the equal pressure drop in two ends, 15～20% equal pressure drop gas enters the adsorption tower that another carries out equal voltage rise from the bottom of adsorption tower, pressure-swing absorption apparatus is in the gas emptying of reverse step-down BD step, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

Embodiments of the invention 7:

Condition such as the conversion gas composition of present embodiment, temperature, adsorbent kind, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span and embodiment 1 are in full accord, the adsorptive pressure of present embodiment is 0.6MPa (G), and the discharge pressure of product carbon dioxide is 0.005MPa.

Pressure-swing absorption apparatus is made up of 10 adsorption towers, moves single tower absorption and all presses program 8 times, and gas concentration lwevel is less than 3V%, to satisfy the needs of next step operation in the hydrogen of present embodiment pressure-swing absorption apparatus adsorption tower upper end outlet, the nitrogen.

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, 2E4D ' all falls in two ends four, 2E5D ' all falls in two ends five, 2E6D ' all falls in two ends six, 2E7D ' all falls in two ends seven, 2E8D ' all falls in two ends eight, vacuumize VC, two ends eight all rise 2E8R ', two ends seven all rise 2E7R ', two ends six all rise 2E6R ', two ends five all rise 2E5R ', two ends four all rise 2E4R ', two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, pressure-swing absorption apparatus is the product carbon dioxide at the gas that vacuumizes the acquisition of VC step, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is 98% (V) for the product carbon dioxide purity, and carbon dioxide, hydrogen, nitrogen and the carbon monoxide rate of recovery are greater than 99.6% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen, the nitrogen, and ton ammonia power consumption 100 is spent.

For present embodiment, adopt particular adsorbent combination of the present invention, under the identical situation of other condition (adsorptive pressure is 0.6MPa (G), conversion gas composition and temperature, sorption cycle time, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span), the investment of decarburization original equipment can save 9%.

Embodiments of the invention 8:

Condition such as the conversion gas composition of present embodiment, temperature, adsorbent kind, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span and embodiment 1 are in full accord, the adsorptive pressure of present embodiment is 1.2MPa (G), and the discharge pressure of product carbon dioxide is 0.005MPa.

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, 2E4D ' all falls in two ends four, 2E5D ' all falls in two ends five, 2E6D ' all falls in two ends six, 2E7D ' all falls in two ends seven, 2E8D ' all falls in two ends eight, the reverse step-down BD of product carbon dioxide, vacuumize VC, two ends eight all rise 2E8R ', two ends seven all rise 2E7R ', two ends six all rise 2E6R ', two ends five all rise 2E5R ', two ends four all rise 2E4R ', two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, pressure-swing absorption apparatus is the product carbon dioxide at the reverse step-down BD of product carbon dioxide with the gas that vacuumizes the acquisition of VC step, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is 98% (V) for the product carbon dioxide purity, and carbon dioxide, hydrogen, nitrogen and the carbon monoxide rate of recovery are greater than 99.8% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen, the nitrogen, and ton ammonia power consumption 70 is spent.

For present embodiment, adopt particular adsorbent combination of the present invention, under the identical situation of other condition (adsorptive pressure is 1.2MPa (G), conversion gas composition and temperature, sorption cycle time, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span), the investment of decarburization original equipment can save 9%.

Embodiments of the invention 9:

Condition such as the conversion gas composition of present embodiment, temperature, adsorbent kind, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span and embodiment 1 are in full accord, and the adsorptive pressure of present embodiment is 0.6MPa (G).

Pressure-swing absorption apparatus is made up of 6 adsorption towers, moves single tower absorption and all presses program 3 times, and gas concentration lwevel is less than 0.2V%, to satisfy the needs of next step operation in the hydrogen of present embodiment pressure-swing absorption apparatus adsorption tower upper end outlet, the nitrogen.

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, reverse step-down BD, two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, pressure-swing absorption apparatus is in the gas emptying of reverse step-down BD step, adsorption tower is at every turn when carrying out the equal pressure drop in two ends, 15～20% equal pressure drop gas enters the adsorption tower that another carries out equal voltage rise from the bottom of adsorption tower, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is that hydrogen, nitrogen and the carbon monoxide rate of recovery improve 2V% than traditional pressure swing adsorption decarbonization technology, and gas concentration lwevel is less than 0.2V% in product hydrogen, the nitrogen, and ton ammonia power consumption 95 is spent.

For present embodiment, adopt particular adsorbent combination of the present invention, (adsorptive pressure is 0.6MPa in other condition

(G), conversion gas composition and temperature, sorption cycle time, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span) under the identical situation, the investment of decarburization original equipment can save 9%.

Embodiments of the invention 10:

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, one all falls E1D, two all fall E2D, 2E3D ' all falls in two ends three, reverse step-down BD, vacuumize VC, two ends three all rise 2E3R ', two all rise E2R, one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, adsorption tower is at every turn when carrying out the equal pressure drop in two ends, 15～20% equal pressure drop gas enters the adsorption tower that another carries out equal voltage rise from the bottom of adsorption tower, pressure-swing absorption apparatus is in reverse step-down BD step and the gas emptying that vacuumizes VC, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

Embodiments of the invention 11:

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, one all falls E1D, two all fall E2D, three all fall E3D, four all fall E4D, five all fall E5D, six all fall E6D, 2E7D ' all falls in two ends seven, 2E8D ' all falls in two ends eight, the reverse step-down BD of product carbon dioxide, vacuumize VC, two ends eight all rise 2E8R ', two ends seven all rise 2E7R ', six all rise E6R, five all rise E5R, four all rise E4R, three all rise E3R, two all rise E2R, one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, pressure-swing absorption apparatus is the product carbon dioxide at the reverse step-down BD of product carbon dioxide with the gas that vacuumizes the acquisition of VC step, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

Embodiment result is 98% (V) for the product carbon dioxide purity, and carbon dioxide, hydrogen, nitrogen and the carbon monoxide rate of recovery are greater than 99.8% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen, the nitrogen, and ton ammonia power consumption 70 is spent.

Embodiments of the invention 12:

Pressure-swing absorption apparatus is made up of 13 adsorption towers, moves single tower absorption and all presses program 8 times, and gas concentration lwevel is less than 3V%, to satisfy the needs of next step operation in the hydrogen of present embodiment pressure-swing absorption apparatus adsorption tower upper end outlet, the nitrogen.

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, 2E4D ' all falls in two ends four, 2E5D ' all falls in two ends five, 2E6D ' all falls in two ends six, 2E7D ' all falls in two ends seven, 2E8D ' all falls in two ends eight, displacement P ', reverse step-down BD, vacuumize VC, the displacement gas ER ' that boosts, two ends eight all rise 2E8R ', two ends seven all rise 2E7R ', two ends six all rise 2E6R ', two ends five all rise 2E5R ', two ends four all rise 2E4R ', two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, pressure-swing absorption apparatus is the product carbon dioxide at reverse step-down BD with the gas that vacuumizes the acquisition of VC step, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is 98% (V) for the product carbon dioxide purity, and carbon dioxide, hydrogen, nitrogen and the carbon monoxide rate of recovery are greater than 99.8% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen, the nitrogen, and ton ammonia power consumption 110 is spent.

Embodiments of the invention 13:

Pressure-swing absorption apparatus is made up of 15 adsorption towers, move single tower absorption and all press program 10 times, the present embodiment pressure-swing absorption apparatus is purified to carbon dioxide more than 99.99% (V), be used for urea synthesis, gas concentration lwevel is less than 3V%, to satisfy the needs of next step operation in the hydrogen of adsorption tower upper end outlet, the nitrogen.

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, 2E4D ' all falls in two ends four, 2E5D ' all falls in two ends five, 2E6D ' all falls in two ends six, 2E7D ' all falls in two ends seven, 2E8D ' all falls in two ends eight, 2E9D ' all falls in two ends nine, 2E10D ' all falls in two ends ten, displacement P ', the reverse step-down BD of product carbon dioxide, the displacement gas ER ' that boosts, two ends ten all rise 2E10R ', two ends nine all rise 2E9R ', two ends eight all rise 2E8R ', two ends seven all rise 2E7R ', two ends six all rise 2E6R ', two ends five all rise 2E5R ', two ends four all rise 2E4R ', two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, pressure-swing absorption apparatus is the product carbon dioxide at the gas that the reverse step-down BD of product carbon dioxide step obtains, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is 99.99% (V) for the product carbon dioxide purity, and carbon dioxide, hydrogen, nitrogen and the carbon monoxide rate of recovery are greater than 99.8% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen, the nitrogen, and ton ammonia power consumption 2 is spent.

Embodiments of the invention 14:

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, one all falls E1D, two all fall E2D, three all fall E3D, four all fall E4D, five all fall E5D, 2E6D ' all falls in two ends six, 2E7D ' all falls in two ends seven, 2E8D ' all falls in two ends eight, displacement P ', reverse step-down BD, vacuumize VC, the displacement gas ER ' that boosts, two ends eight all rise 2E8R ', two ends seven all rise 2E7R ', two ends six all rise 2E6R ', five all rise E5R, four all rise E4R, three all rise E3R, two all rise E2R, one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, pressure-swing absorption apparatus is the product carbon dioxide at reverse step-down BD with the gas that vacuumizes the acquisition of VC step, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is 98% (V) for the product carbon dioxide purity, and carbon dioxide, hydrogen, nitrogen and the carbon monoxide rate of recovery are greater than 99.8% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen, the nitrogen, and ton ammonia power consumption 100 is spent.

Embodiments of the invention 15:

Pressure-swing absorption apparatus is made up of 7 adsorption towers, moves single tower absorption and all presses program 2 times, and gas concentration lwevel is less than 0.2V%, to satisfy the needs of next step operation in the hydrogen of present embodiment pressure-swing absorption apparatus adsorption tower upper end outlet, the nitrogen.

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, along putting PP1, along putting PP2, along putting PP3, the contrary BD of putting, clean P1, clean P2, clean P3, two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, directly go to clean by Flow-rate adjustment and finish the adsorption tower that cleans the P2 step along putting gaseous mixture that the PP1 step emits, the impurity that adsorbs on its adsorbent is desorbed, directly go to clean by Flow-rate adjustment and finish the adsorption tower that cleans the P1 step along putting gaseous mixture that the PP2 step emits, directly go to clean by Flow-rate adjustment and finish the contrary adsorption tower of BD step of putting along putting gaseous mixture that the PP3 step emits, the impurity that adsorbs on its adsorbent is desorbed, adsorption tower is at every turn when carrying out the equal pressure drop in two ends, 15～20% equal pressure drop gas enters the adsorption tower that another carries out equal voltage rise from the bottom of adsorption tower, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is that hydrogen, nitrogen and the carbon monoxide rate of recovery improve 2V% than traditional pressure swing adsorption decarbonization technology, and gas concentration lwevel is less than 0.2V% in product hydrogen, the nitrogen, and ton ammonia power consumption 2 is spent.

For present embodiment, adopt particular adsorbent combination of the present invention, under the identical situation of other condition (adsorptive pressure is 0.6MPa (G), conversion gas composition and temperature, sorption cycle time, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span), the investment of decarburization original equipment can save 7%.

Embodiments of the invention 16:

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, one all falls E1D, 2E2D ' all falls in two ends two, along putting PP1, along putting PP2, along putting PP3, the contrary BD of putting, clean P1, clean P2, clean P3, two ends two all rise 2E2R ', one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, directly go to clean by Flow-rate adjustment and finish the adsorption tower that cleans the P2 step along putting gaseous mixture that the PP1 step emits, the impurity that adsorbs on its adsorbent is desorbed, directly go to clean by Flow-rate adjustment and finish the adsorption tower that cleans the P1 step along putting gaseous mixture that the PP2 step emits, directly go to clean by Flow-rate adjustment and finish the contrary adsorption tower of BD step of putting along putting gaseous mixture that the PP3 step emits, the impurity that adsorbs on its adsorbent is desorbed, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product, adsorption tower is at every turn when carrying out the equal pressure drop in two ends, 15～20% equal pressure drop gas enters the adsorption tower that another carries out equal voltage rise from the bottom of adsorption tower, wherein also contains a spot of carbon monoxide and methane.

Embodiments of the invention 17:

Condition such as the conversion gas composition of present embodiment, temperature, adsorbent kind, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span and embodiment 1 are in full accord, the adsorptive pressure of present embodiment is 1.0MPa (G), and the discharge pressure of product carbon dioxide is 0.005MPa.

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, one all falls E1D, two all fall E2D, three all fall E3D, four all fall E4D, five all fall E5D, six all fall E6D, seven all fall E7D, eight all fall E8D, nine all fall E9D, ten all fall E10D, reverse step-down one BD1, reverse step-down two BD2, the contrary venting body 2ER1 that boosts, ten all rise E10R, nine all rise E9R, eight all rise E8R, seven all rise E7R, six all rise E6R, five all rise E5R, four all rise E4R, three all rise E3R, two all rise E2R, one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, contrary venting body boosts the gas of 2ER1 step from the reverse step-down one BD1 gas of another or same adsorption tower, pressure-swing absorption apparatus is the product carbon dioxide at the gas that reverse step-down two BD2 steps obtain, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

Embodiments of the invention 18:

Condition such as the conversion gas composition of present embodiment, temperature, adsorbent kind, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span and embodiment 1 are in full accord, the adsorptive pressure of present embodiment is 0.7MPa (G), and the discharge pressure of product carbon dioxide is 0.005MPa.

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, one all falls E1D, two all fall E2D, three all fall E3D, four all fall E4D, five all fall E5D, six all fall E6D, seven all fall E7D, eight all fall E8D, nine all fall E9D, ten all fall E10D, reverse step-down one BD1, reverse step-down two BD2, vacuumize VC, the contrary venting body 2ER1 that boosts, ten all rise E10R, nine all rise E9R, eight all rise E8R, seven all rise E7R, six all rise E6R, five all rise E5R, four all rise E4R, three all rise E3R, two all rise E2R, one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, contrary venting body boosts the gas of 2ER1 step from the reverse step-down one BD1 gas of another or same adsorption tower, pressure-swing absorption apparatus is the product carbon dioxide at reverse step-down two BD2 steps and the gas that vacuumizes the VC acquisition, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is 98% (V) for the product carbon dioxide purity, and carbon dioxide, hydrogen, nitrogen and the carbon monoxide rate of recovery are greater than 99.7% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen, the nitrogen, and ton ammonia power consumption 100 is spent.

Embodiments of the invention 19:

Pressure-swing absorption apparatus is made up of 15 adsorption towers, move single tower absorption and all press program 10 times, the present embodiment pressure-swing absorption apparatus is purified to carbon dioxide more than 98% (V), be used for urea synthesis, gas concentration lwevel is less than 3V%, to satisfy the needs of next step operation in the hydrogen of adsorption tower upper end outlet, the nitrogen.

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, one all falls E1D, two all fall E2D, three all fall E3D, four all fall E4D, five all fall E5D, six all fall E6D, seven all fall E7D, eight all fall E8D, nine all fall E9D, ten all fall E10D, displacement P ', the reverse step-down BD of product carbon dioxide, the displacement gas ER ' that boosts, ten all rise E10R, nine all rise E9R, eight all rise E8R, seven all rise E7R, six all rise E6R, five all rise E5R, four all rise E4R, three all rise E3R, two all rise E2R, one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, pressure-swing absorption apparatus is the product carbon dioxide at the gas that reverse step-down two BD2 steps obtain, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

Embodiments of the invention 20:

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, one all falls E1D, two all fall E2D, three all fall E3D, four all fall E4D, five all fall E5D, six all fall E6D, seven all fall E7D, eight all fall E8D, nine all fall E9D, ten all fall E10D, displacement P ', the reverse step-down BD of product carbon dioxide, vacuumize VC, the displacement gas ER ' that boosts, ten all rise E10R, nine all rise E9R, eight all rise E8R, seven all rise E7R, six all rise E6R, five all rise E5R, four all rise E4R, three all rise E3R, two all rise E2R, one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, contrary venting body boosts the gas of 2ER1 step from the reverse step-down one BD1 gas of another or same adsorption tower, pressure-swing absorption apparatus is the product carbon dioxide at reverse step-down two BD2 steps and the gas that vacuumizes the VC acquisition, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

Embodiments of the invention 21:

This routine unstripped gas is hydrogeneous gaseous mixture, as light oil gas making, synthetic-ammonia transformation gas, synthesis gas, gas and synthetic ammonia purge, methanol synthetic discharged gas delayed, semiwater gas, water-gas and cracking dry gas etc.

The light oil gas making of present embodiment is composed as follows:

Component

H2

CO2

CO

CH4

O2+Ar

Total sulfur

Water (vapour)

Concentration V%

69～72

15～20

≤2～6

3～7

≤0.8

150mg/Nm3

Saturated

Temperature :≤40 ℃

Pressure: 2.0MPa (G)

The adsorbent that loads from down to up in the adsorption tower is followed successively by activated alumina and molecular sieve or activated alumina, active carbon and molecular sieve or activated alumina, Kiselgel A and molecular sieve; In the hydrogeneous gaseous mixture, hydrogen is difficult absorption phase component, and the component beyond the hydrogen is easily to adsorb phase component.

Pressure-swing absorption apparatus is made up of 6 adsorption towers, moves single tower absorption and all presses program 4 times.

Adsorption tower experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, 2E4D ' all falls in two ends four, reverse step-down BD, two ends four all rise 2E4R ', two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, adsorption tower is at every turn when carrying out the equal pressure drop in two ends, 15～20% equal pressure drop gas enters the adsorption tower that another carries out equal voltage rise from the bottom of adsorption tower, and adsorption tower is in the gas emptying or its usefulness of reverse step-down BD step.

The present embodiment result be density of hydrogen greater than 99.9% (V), hydrogen recovery rate improves 2V% than traditional transformation absorption hydrogen producing technology.

Embodiments of the invention 22:

Condition such as the unstripped gas composition of present embodiment, temperature, adsorbent kind, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span and embodiment 21 are in full accord, and the adsorptive pressure of present embodiment is 2.0MPa (G).

Adsorption tower in a cycle period successively experience absorption A, all fall E1D, two and all fall E2D, three and all fall E3D, two ends four and all fall 2E4D ', reverse step-down BD, two ends four and all rise 2E4R ', three and all rise E3R, two and all rise E2R, and all rise E1R, the final FR pressure swing adsorption technique step of boosting, adsorption tower is at every turn when carrying out the equal pressure drop in two ends, 15～20% equal pressure drop gas enters the adsorption tower that another carries out equal voltage rise from the bottom of adsorption tower, and adsorption tower is in the gas emptying or its usefulness of reverse step-down BD step.

Embodiments of the invention 23:

Condition such as the unstripped gas composition of present embodiment, temperature, adsorbent kind, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span and embodiment 21 are in full accord, and the adsorptive pressure of present embodiment is 0.6MPa (G).

Experience absorption A, falls all that E1D, two falls all that E2D, three falls all that E3D, two ends four all fall 2E4D ', reverse step-down BD, vacuumize VC to adsorption tower successively in a cycle period, two ends four all rise 2E4R ', three and all rise E3R, two and all rise E2R, and all rise E1R, the final FR pressure swing adsorption technique step of boosting, adsorption tower is at every turn when carrying out the equal pressure drop in two ends, 15～20% equal pressure drop gas enters the adsorption tower that another carries out equal voltage rise from the bottom of adsorption tower, and adsorption tower is used in reverse step-down BD step and the gas emptying that vacuumizes the VC step or its.

Embodiments of the invention 24:

Adsorption tower experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, 2E4D ' all falls in two ends four, reverse step-down BD, two ends four all rise 2E4R ', two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, adsorption tower is at every turn when carrying out the equal pressure drop in two ends, 15～20% equal pressure drop gas enters the adsorption tower that another carries out equal voltage rise from the bottom of adsorption tower, and adsorption tower is used in reverse step-down BD step and the gas emptying that vacuumizes the VC step or its.

Embodiments of the invention 25:

Pressure-swing absorption apparatus is made up of 7 adsorption towers, moves single tower absorption and all presses program 2 times.

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, one all falls E1D, 2E2D ' all falls in two ends two, along putting PP1, along putting PP2, along putting PP3, the contrary BD of putting, clean P1, clean P2, clean P3, two ends two all rise 2E2R ', one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, directly go to clean by Flow-rate adjustment and finish the adsorption tower that cleans the P2 step along putting gaseous mixture that the PP1 step emits, the impurity that adsorbs on its adsorbent is desorbed, directly go to clean by Flow-rate adjustment and finish the adsorption tower that cleans the P1 step along putting gaseous mixture that the PP2 step emits, directly go to clean by Flow-rate adjustment and finish the contrary adsorption tower of BD step of putting along putting gaseous mixture that the PP3 step emits, the impurity that adsorbs on its adsorbent is desorbed, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product, adsorption tower is at every turn when carrying out the equal pressure drop in two ends, 15～20% equal pressure drop gas enters the adsorption tower that another carries out equal voltage rise from the bottom of adsorption tower, and adsorption tower is in the gas emptying or its usefulness of reverse step-down BD step and cleaning P step.

Embodiments of the invention 26:

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, along putting PP1, along putting PP2, along putting PP3, the contrary BD of putting, clean P1, clean P2, clean P3, two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, directly go to clean by Flow-rate adjustment and finish the adsorption tower that cleans the P2 step along putting gaseous mixture that the PP1 step emits, the impurity that adsorbs on its adsorbent is desorbed, directly go to clean by Flow-rate adjustment and finish the adsorption tower that cleans the P1 step along putting gaseous mixture that the PP2 step emits, directly go to clean by Flow-rate adjustment and finish the contrary adsorption tower of BD step of putting along putting gaseous mixture that the PP3 step emits, the impurity that adsorbs on its adsorbent is desorbed, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product, adsorption tower is at every turn when carrying out the equal pressure drop in two ends, 15～20% equal pressure drop gas enters the adsorption tower that another carries out equal voltage rise from the bottom of adsorption tower, and adsorption tower is in the gas emptying or its usefulness of reverse step-down BD step and cleaning P step.

Embodiments of the invention 27:

The gaseous mixture of present embodiment is composed as follows:

Component	H2	CO2	CO	CH4	O2+Ar	Total sulfur	Water (vapour)
Component	H2	CO2	CO	CH4	O2+Ar	Total sulfur	Water (vapour)	Concentration V%	45～65	10～18	≤20～28	0.2～2	≤0.8	150mg/Nm3	Saturated

Temperature :≤40 ℃

Pressure: 2.0MPa (G)

Pressure-swing absorption apparatus is made up of 13 adsorption towers, move single tower absorption and all press program 11 times, the adsorbent that loads from down to up in the adsorption tower is followed successively by activated alumina and Kiselgel A, the present embodiment pressure-swing absorption apparatus is concentrated to carbon dioxide more than 96% (V), gas concentration lwevel is less than 3V%, to satisfy the needs of next step methyl alcohol synthetic (single alcohol) operation in the hydrogen of adsorption tower upper end outlet and the carbon monoxide.

Adsorption tower experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, 2E4D ' all falls in two ends four, 2E5D ' all falls in two ends five, 2E6D ' all falls in two ends six, 2E7D ' all falls in two ends seven, 2E8D ' all falls in two ends eight, 2E9D ' all falls in two ends nine, 2E10D ' all falls in two ends ten, 2E11D ' all falls in two ends 11, the reverse step-down BD of carbon dioxide, two ends 11 all rise 2E11R ', two ends ten all rise 2E10R ', two ends nine all rise 2E9R ', two ends eight all rise 2E8R ', two ends seven all rise 2E7R ', two ends six all rise 2E6R ', two ends five all rise 2E5R ', two ends four all rise 2E4R ', two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, the gaseous mixture that the adsorption tower outlet is discharged is mainly hydrogen and carbon monoxide, wherein also contains a spot of methane.

The present embodiment result is 96% (V) for carbon dioxide purity, and the hydrogen and the carbon monoxide rate of recovery are greater than 99.6% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen and the carbon monoxide, and methyl alcohol power consumption 2 per ton is spent.

For present embodiment, adopt particular adsorbent combination of the present invention, under the identical situation of other condition (adsorptive pressure is 2.0MPa (G), conversion gas composition and temperature, sorption cycle time, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span), the investment of decarburization original equipment can save 9%.

Embodiments of the invention 28:

Condition such as the unstripped gas composition of present embodiment, temperature, adsorbent kind, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span and embodiment 27 are in full accord, and the adsorptive pressure of present embodiment is 2.0MPa (G).

Adsorption tower experiences absorption A successively in a cycle period, one all falls E1D, two all fall E2D, three all fall E3D, four all fall E4D, five all fall E5D, six all fall E6D, seven all fall E7D, eight all fall E8D, nine all fall E9D, ten all fall E10D, 2E11D ' all falls in two ends 11, the reverse step-down BD of carbon dioxide, two ends 11 all rise 2E11R ', ten all rise E10R, nine all rise E9R, eight all rise E8R, seven all rise E7R, six all rise E6R, five all rise E5R, four all rise E4R, three all rise E3R, two all rise E2R, one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, the gaseous mixture that the adsorption tower outlet is discharged is mainly hydrogen and carbon monoxide, wherein also contains a spot of methane.

Embodiments of the invention 29:

Condition such as the unstripped gas composition of present embodiment, temperature, adsorbent kind, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span and embodiment 27 are in full accord, and the adsorptive pressure of present embodiment is 0.7MPa (G).

Pressure-swing absorption apparatus is made up of 12 adsorption towers, move single tower absorption and all press program 9 times, the adsorbent that loads from down to up in the adsorption tower is followed successively by activated alumina and Kiselgel A, the present embodiment pressure-swing absorption apparatus is concentrated to carbon dioxide more than 93% (V), gas concentration lwevel is less than 3V%, to satisfy the needs of next step methyl alcohol synthetic (single alcohol) operation in the hydrogen of adsorption tower upper end outlet and the carbon monoxide.

Adsorption tower experiences absorption A successively in a cycle period, one all falls E1D, two all fall E2D, three all fall E3D, four all fall E4D, five all fall E5D, six all fall E6D, seven all fall E7D, eight all fall E8D, 2E9D ' all falls in two ends nine, the reverse step-down BD of carbon dioxide, vacuumize VC, two ends nine all rise 2E9R ', eight all rise E8R, seven all rise E7R, six all rise E6R, five all rise E5R, four all rise E4R, three all rise E3R, two all rise E2R, one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, the gaseous mixture that the adsorption tower outlet is discharged is mainly hydrogen and carbon monoxide, wherein also contains a spot of methane.

The present embodiment result is 93% (V) for carbon dioxide purity, and the hydrogen and the carbon monoxide rate of recovery are greater than 99.2% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen and the carbon monoxide, and methyl alcohol power consumption 15～20 per ton is spent.

Embodiments of the invention 30:

Adsorption tower experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, 2E4D ' all falls in two ends four, 2E5D ' all falls in two ends five, 2E6D ' all falls in two ends six, 2E7D ' all falls in two ends seven, 2E8D ' all falls in two ends eight, 2E9D ' all falls in two ends nine, the reverse step-down BD of carbon dioxide, vacuumize VC, two ends nine all rise 2E9R ', two ends eight all rise 2E8R ', two ends seven all rise 2E7R ', two ends six all rise 2E6R ', two ends five all rise 2E5R ', two ends four all rise 2E4R ', two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, the gaseous mixture that the adsorption tower outlet is discharged is mainly hydrogen and carbon monoxide, wherein also contains a spot of methane.

Embodiments of the invention 31:

Pressure-swing absorption apparatus is made up of 12 adsorption towers, move single tower absorption and all press program 9 times, the adsorbent that loads from down to up in the adsorption tower is followed successively by activated alumina and Kiselgel A, the present embodiment pressure-swing absorption apparatus is concentrated to carbon dioxide more than 98% (V), gas concentration lwevel is less than 3V%, to satisfy the needs of next step methyl alcohol synthetic (single alcohol) operation in the hydrogen of adsorption tower upper end outlet and the carbon monoxide.

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, one all falls E1D, two all fall E2D, three all fall E3D, four all fall E4D, five all fall E5D, six all fall E6D, seven all fall E7D, eight all fall E8D, nine all fall E9D, 2E10D ' all falls in two ends ten, displacement P ', the reverse step-down BD of carbon dioxide, vacuumize VC, the displacement gas ER ' that boosts, two ends ten all rise 2E10R ', nine all rise E9R, eight all rise E8R, seven all rise E7R, six all rise E6R, five all rise E5R, four all rise E4R, three all rise E3R, two all rise E2R, one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, contrary venting body boosts the gas of 2ER1 step from the reverse step-down one BD1 gas of another or same adsorption tower, pressure-swing absorption apparatus is the product carbon dioxide at reverse step-down two BD2 steps and the gas that vacuumizes the VC acquisition, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is 98% (V) for carbon dioxide purity, and the hydrogen and the carbon monoxide rate of recovery are greater than 99.9% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen and the carbon monoxide, and methyl alcohol power consumption 20 per ton is spent.

Embodiments of the invention 32:

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, 2E4D ' all falls in two ends four, 2E5D ' all falls in two ends five, 2E6D ' all falls in two ends six, 2E7D ' all falls in two ends seven, 2E8D ' all falls in two ends eight, 2E9D ' all falls in two ends nine, 2E10D ' all falls in two ends ten, displacement P ', the reverse step-down BD of carbon dioxide, vacuumize VC, the displacement gas ER ' that boosts, two ends ten all rise 2E10R ', two ends nine all rise 2E9R ', two ends eight all rise 2E8R ', two ends seven all rise 2E7R ', two ends six all rise 2E6R ', two ends five all rise 2E5R ', two ends four all rise 2E4R ', two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, contrary venting body boosts the gas of 2ER1 step from the reverse step-down one BD1 gas of another or same adsorption tower, pressure-swing absorption apparatus is the product carbon dioxide at reverse step-down two BD2 steps and the gas that vacuumizes the VC acquisition, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

Embodiments of the invention 33:

Condition such as the unstripped gas composition of present embodiment, temperature, adsorbent kind, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span and embodiment 27 are in full accord, and the adsorptive pressure of present embodiment is 0.9MPa (G).

Pressure-swing absorption apparatus is made up of 13 adsorption towers, move single tower absorption and all press program 10 times, the adsorbent that loads from down to up in the adsorption tower is followed successively by activated alumina and Kiselgel A, the present embodiment pressure-swing absorption apparatus is concentrated to carbon dioxide more than 97% (V), gas concentration lwevel is less than 3V%, to satisfy the needs of next step methyl alcohol synthetic (single alcohol) operation in the hydrogen of adsorption tower upper end outlet and the carbon monoxide.

Adsorption tower experiences absorption A successively in a cycle period, 2E1D ' all falls in two ends one, 2E2D ' all falls in two ends two, 2E3D ' all falls in two ends three, 2E4D ' all falls in two ends four, 2E5D ' all falls in two ends five, 2E6D ' all falls in two ends six, 2E7D ' all falls in two ends seven, 2E8D ' all falls in two ends eight, 2E9D ' all falls in two ends nine, 2E10D ' all falls in two ends ten, vacuumize VC, two ends ten all rise 2E10R ', two ends nine all rise 2E9R ', two ends eight all rise 2E8R ', two ends seven all rise 2E7R ', two ends six all rise 2E6R ', two ends five all rise 2E5R ', two ends four all rise 2E4R ', two ends three all rise 2E3R ', two ends two all rise 2E2R ', two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting, the gaseous mixture that the adsorption tower outlet is discharged is mainly hydrogen and carbon monoxide, wherein also contains a spot of methane.

The present embodiment result is 97% (V) for carbon dioxide purity, and the hydrogen and the carbon monoxide rate of recovery are greater than 99.8% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen and the carbon monoxide, and methyl alcohol power consumption 20 per ton is spent.

Embodiments of the invention 34:

The adsorption tower of pressure-swing absorption apparatus experiences absorption A successively in a cycle period, one all falls E1D, two all fall E2D, three all fall E3D, four all fall E4D, five all fall E5D, six all fall E6D, seven all fall E7D, eight all fall E8D, nine all fall E9D, ten all fall E10D, reverse step-down one BD1, reverse step-down two BD2, vacuumize VC, the contrary venting body 2ER1 that boosts, ten all rise E10R, nine all rise E9R, eight all rise E8R, seven all rise E7R, six all rise E6R, five all rise E5R, four all rise E4R, three all rise E3R, two all rise E2R, one all rises E1R, the FR pressure swing adsorption technique step of finally boosting, contrary venting body boosts the gas of 2ER1 step from the reverse step-down one BD1 gas of another or same adsorption tower, the gaseous mixture that the adsorption tower outlet is discharged is mainly nitrogen, hydrogen product wherein also contains a spot of carbon monoxide and methane.

The present embodiment result is 97% (V) for the product carbon dioxide purity, and carbon dioxide, hydrogen, nitrogen and the carbon monoxide rate of recovery are greater than 99.8% (V), and gas concentration lwevel is less than 3% (V) in product hydrogen, the nitrogen, and ton ammonia power consumption 20 is spent.

For present embodiment, adopt particular adsorbent combination of the present invention, under the identical situation of other condition (adsorptive pressure is 0.7MPa (G), conversion gas composition and temperature, sorption cycle time, power-equipment performance, instrument and meter and control function, special-purpose sequencing valve and hydraulic system structure and life-span), the investment of decarburization original equipment can save 9%.

Embodiments of the invention 35:

This routine unstripped gas is an air.

The air of present embodiment is composed as follows:

Component	N2	O2	Ar	Water (vapour)
Component	N2	O2	Ar	Water (vapour)	Concentration V%	78	21	1	Saturated

Temperature :≤40 ℃

Pressure: 0.015MPa (G)

The adsorbent that loads from down to up in the pressure swing adsorption gas separation device adsorption tower is followed successively by activated alumina and and molecular sieve.Present embodiment is a pressure swing adsorption oxygen making device, contains in the air, and oxygen and argon gas are difficult absorption phase components, and nitrogen G﹠W (vapour) is easily to adsorb phase component.

Pressure swing adsorption oxygen making device is made up of 4 adsorption towers, moves single tower absorption and all presses program 1 time.

Experience absorption A, two ends one all fall 2E1D ', vacuumize VC adsorption tower successively in a cycle period, two ends one all rise 2E1R ', the FR pressure swing adsorption technique step of finally boosting.

The present embodiment result be oxygen concentration greater than 93% (V), oxygen recovery rate is than traditional handicraft high by 3.5% (V).

The invention is not restricted to above-mentioned range applications, can be applicable to all and from gaseous mixture, obtain easily to adsorb the phase product or from gaseous mixture, obtain the difficult phase product that adsorbs, also be applied to all acquisitions simultaneously from gaseous mixture easily absorption phase product and the difficult product mutually that adsorbs.Easy absorption of the present invention can be a component with difficult absorption mutually mutually, also can be more than one component.

Claims

1, a kind of improved one-section variable pressure absorbing gas separation method, it is characterized in that the method is used for separating easily absorption phase and difficult absorption phase component from gaseous mixture, product can be easily to adsorb phase component, it also can be difficult absorption phase component, can also be simultaneously easily absorption mutually and the displacement P ' step gas that comes out from the adsorption tower top of difficult absorption phase component return another adsorption tower and carry out the substitution gas ER ' that boosts, pressure swing adsorption gas separation device adsorption tower experience absorption A successively in a cycle period from the top to adsorption tower, drop pressure ED, displacement P ', reverse step-down BD, the substitution gas ER ' that boosts, reverse boost pressure ER, the FR processing step finally boosts.

2, a kind of improved one-section variable pressure absorbing gas separation method according to claim 1 is characterized in that increase vacuumizes the VC step after the reverse step-down BD of adsorption tower step.

3, a kind of improved one-section variable pressure absorbing gas separation method according to claim 1 and 2 is characterized in that being filled with in the adsorption tower activated alumina and Kiselgel A, and activated alumina is seated in the adsorption tower bottom, and Kiselgel A is seated in adsorption tower top.

4, a kind of two-section totally recovering pressure swing adsorption gas separating method according to claim 1 and 2 is characterized in that the adsorbent that loads from down to up in the adsorption tower is followed successively by activated alumina and molecular sieve or activated alumina, active carbon and molecular sieve.