CN100400142C - Stripped gas method for recovering C2 and higher carbon content hydrocarbon constituent - Google Patents
Stripped gas method for recovering C2 and higher carbon content hydrocarbon constituent Download PDFInfo
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- CN100400142C CN100400142C CNB2005101293693A CN200510129369A CN100400142C CN 100400142 C CN100400142 C CN 100400142C CN B2005101293693 A CNB2005101293693 A CN B2005101293693A CN 200510129369 A CN200510129369 A CN 200510129369A CN 100400142 C CN100400142 C CN 100400142C
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Abstract
The present invention discloses a method for recovering C2 and hydrocarbon constituents above the C2 from dry gas. In the method, the dry gas is orderly and repeatedly processed by a pressure swing adsorption step comprises adsorption, reverse releasing, evacuation and final pressure increasing for separating the C2 and the hydrocarbon components above the C2. Gas processed by the pressure swing absorption step is orderly processed by at least the steps of wet desulphurization, refine desulphurization and deoxidation to be purified, and then, mixed gas containing the C2 and the hydrocarbon constituents above the C2 is obtained. In the C2 and the hydrocarbon components above the C2 recovered by the method, the sulfur content is less than 0.1 ppm, and the oxygen content is less than 1 ppm, so the C2 and the hydrocarbon components above the C2 accord with the using standard of downstream ethylene devices.
Description
Technical field
The present invention relates to a kind of method that reclaims the valuable gases component of from mist, separating, purify, specifically, relate to a kind of from dry gas, separate to reclaim be rich in C
2And C
2The method of above hydrocarbon component.
Background technology
Contain abundant ethene, ethane and C in the coking dry gas from the catalytic cracked dry gas of heavy oil catalytically cracking equipment, coking plant
2Basic chemical raw materials resources such as above hydrocarbon component, the past does not burn in vain because of there being industrialized recovery technology to be used as fuel.At present to C in the dry gas
2And C
2The concentrated recovery technology of above hydrocarbon component mainly contains separation by deep refrigeration, middle cold oil absorption and separation method and adsorption method of separation.The above two are because operation easier is big, and investment, operating cost is higher, the not obvious wide popularization and application of failing of economic benefit; Adsorption method of separation, especially transformation absorption (PSA) method is simple to operate because of it, and cost of equipment is low, becomes the cost-effective separation method that domestication factory extensively adopts.The C that reclaims in the existing dry gas pressure swing adsorption technique
2And C
2In the above hydrocarbon component because impurity content height such as sulfide, oxygen, in subsequent applications, these impurity easily make catalyst activity reduce, even poisoning loses activity, influence ordinary production, thereby the ethene hypothermia distillation device that can not enter downstream factory purify to reclaim ethene, propylene and ethane cracking furnace raw material ethane, propane etc., thereby limited ethene, ethane and the C that reclaims from dry gas
2The range of application of above hydrocarbon component.
Summary of the invention
At above-mentioned the deficiencies in the prior art, the technical problem to be solved in the present invention provides a kind of from dry gas recovery C
2And C
2The method of above hydrocarbon component is through the C of this method recovery
2And C
2(V/V) sulfur content is less than 0.1ppm in the above hydrocarbon component, and oxygen content is less than 1ppm, thereby meets the use standard of downstream ethylene unit.
For solving the problems of the technologies described above, method of the present invention is, make described dry gas circulate at least successively experience by absorption, contrary put, find time and the transformation adsorption step formed of finally boosting to wherein C
2And C
2Above hydrocarbon component separates, and experiences wet desulphurization, smart desulfurization and deoxygenation step more successively at least through the gas after the transformation absorption and purifies, and obtains to be rich in C
2And C
2The gaseous mixture of above hydrocarbon component.
Dry gas is through behind the isolation of purified of above-mentioned steps, sulfur content wherein is less than 0.1ppm, oxygen content is less than 1ppm, the charge gas compressor that can enter the downstream ethylene unit enters hypothermia distillation device through pressurization with after removing carbon dioxide and water, purifies and reclaims ethene and propylene and pyrolysis furnace raw material ethane and propane etc.
The optimization of above-mentioned steps can comprise the dearsenification step to remove the impurity arsenic hydride between wet desulphurization and smart desulfurized step; Can comprise essence between wet desulphurization and the dearsenification step and take off the liquid step, remove the liquid mist that produces in the amine mist carried secretly in the gas or other wet desulphurization mode; Further and then optimization can be carried out water washing and take off liquid wet desulphurization after, and then carry out essence and take off liquid, and promptly first amine mist in the gas or liquid mist are diluted removes, and takes off the life-span of adsorbent in the liquid step to improve essence.
Alkali cleaning carbon dioxide removal and drying steps are promptly carried out in further optimization after deoxygenation step successively, and the content of carbon dioxide and water is further reduced.Ethene and propylene and ethane cracking furnace raw material ethane and propane etc. are reclaimed in the hypothermia distillation device purification that then can directly enter the ethylene plant through the dry gas after desulfurization, deoxidation, carbon dioxide removal and the dehydration.Can contain the dealkalize step between alkali cleaning carbon dioxide removal and the drying steps, remove after the alkali cleaning residual alkali mist in the gas; Also can contain the water washing dealkalize between alkali cleaning carbon dioxide removal and the dealkalize step, with the concentration of alkali mist in the diluent gas.Described drying steps can adopt the alternating temperature absorption method to carry out drying, also can comprise keen-witted and capable dry step after the alternating temperature adsorption dry step, further to remove water.
And then above-mentioned water washing also can carry out moisture from step after taking off liquid, alkali cleaning carbon dioxide removal and water washing dealkalize step, to remove water smoke.
Now dry gas of the present invention is reclaimed C
2And C
2Alternative each step division is as follows in the method for above hydrocarbon component:
During operation, dry gas can remove high-boiling-point impurity through the cooling driers condensation earlier, be that carbon number is at the hydrocarbon component more than 5, and then enter pressure-swing absorption apparatus, at least successively circulation experience absorption, contraryly put, find time, the step of finally boosting, remove the impurity composition that hydrogen the dry gas, methane, oxygen, nitrogen, carbon monoxide etc. are difficult for adsorbing at adsorbent from absorption waste gas and discharge system, C
2And C
2Above hydrocarbon components etc. easily absorbed component are adsorbed agent absorption.From contrary put with exhaust obtain with ethene, ethane and C
2Above hydrocarbon component is half a main product gas, in order to increase ethene, ethane and C in the half product gas
2The concentration of above hydrocarbon component can directly return 10%～80% against putting with exhaust or returning adsorbent bed is replaced against putting with exhaust after pressurization.The gas of emitting from the adsorption tower port of export in the displacement step of transformation absorption is called displacement waste gas, inevitably can give off some half product gas from displacement waste gas in this replacement process.In order to increase ethene, ethane and C in the half product gas simultaneously
2The rate of recovery of above hydrocarbon component can increase by 1 stage pressure swing adsorption apparatus half product gas component in the displacement waste gas is reclaimed.Be that pressure swing adsorption system comprises 2 sections of 1 section of transformation absorption and transformation absorption, they are made of at least two adsorption towers that are filled with adsorbent respectively, each adsorption tower circulate at least successively experience absorption, displacement, contraryly put, find time, the step of finally boosting, and the displacement waste gas of 1 section of transformation absorption enters 2 sections of transformation absorption as unstripped gas; Entering transformation absorption after further the optimization displacement waste gas that also transformation can be adsorbed 1 section of 2 sections displacement waste gas and transformation absorption mixes adsorbs for 2 sections again.
In the above-mentioned pressure swing adsorption method, in the once circulation of each adsorption tower, all to experience absorption, contrary put, find time, the step of finally boosting, and according to adsorptive pressure, reclaim process conditions such as absorption phase product purity requirement, can to equal pressure drop, all the voltage rise step reasonably accept or reject, arrangement and number of times setting.Promptly also can comprise the equal voltage drop step of one or many at least, and after evacuation step, be right after the equal voltage rise of one or many at least in absorption with between strideing suddenly; All voltage drop step can be right after after the adsorption step, also can be right after after including the step of displacement and carry out.Each adsorption tower all will experience identical step, and each tower just staggers in time mutually, so that device is continuous, stable operation.
The half product gas that transformation absorption obtains enters the wet desulphurization unit after by compressor pressurizes, removes hydrogen sulfide, carbon dioxide sour gas in the half product gas.The wet desulphurization decarburization comprises that monoethanolamine (EA), methylethanolamine (MEA) and methyl diethanolamine (MDEA) amine washes method, is solvent with EA, MEA, MDEA promptly, absorbs sour gas, reaches the purpose that removes hydrogen sulfide, carbon dioxide; Except that above-mentioned amine is washed the method, also can adopt the wet desulphurization that contains phthalein cyanogen cobalt (PDS) catalyst, remove hydrogen sulfide and amounts of carbon dioxide, remove remaining carbon dioxide by alkali cleaning again in subsequent step or the application.Gas after the wet desulphurization decarburization can enter the water washing liquid taking-off tower, to the amine mist in the gas or liquid mist dilute remove after, and enter smart defluid device again, utilize at least a in active carbon, coke and the activated alumina adsorbents of loading in the smart defluid device, remove the amine mist or the impurity such as liquid mist and water smoke that after washing, remain in the product gas.
Half product gas after purifying can enter and be filled with the dearsenicator dearsenification that contains the cupric oxide Hydrodearsenic Catalyst, and arsenic content is less than 5ppb in the later half product gas of process dearsenicator.The half product gas that comes out through dearsenicator enters and is filled with the active carbon is the desulfurizing agent of carrier, or to be filled with the active carbon be the desulfurizing agent of carrier and the smart desulfurizing tower of two kinds of desulfurizing agents of ferric oxide desulfurizer, and sulfide in the half product gas is comprised that hydrogen sulfide and organosulfur compound are removed to less than 0.1ppm.
Half product gas after the desulfurization enters deoxidation reactor, can use the CNA-538 type of the dehydrogenation catalyst of manganese oxide, the dehydrogenation catalyst of cupric, the dehydrogenation catalyst that contains noble metal or Sichuan Tianyi Science ﹠ Technology Co., Ltd's production and sales or CNA-520 type dehydrogenation catalyst and this amphitypy dehydrogenation catalyst to be used in combination in deoxidation reactor and carry out deoxygenation.Hydrogen and oxygen water generation reaction in first product gas of catalyst, thus make oxygen in the half product gas less than 1ppm.
Half product gas after the deoxidation can remove carbon dioxide through the alkali absorption tower.In the alkali absorption tower, the reaction of carbon dioxide and NaOH generates sodium acid carbonate and sodium carbonate, makes in the half product gas carbon dioxide content less than 1ppm.The half product gas that comes out in the alkali absorption tower can enter water washing dealkalize tower and the alkali lye of carrying secretly in the gas is diluted remove, and at least a dealkalize tower in being filled with active carbon, coke and activated alumina adsorbents again, remove impurity such as the alkali mist that after washing, remains in the product gas and water smoke.Half product gas carries out drying more then, makes water content in the half product gas less than 1ppm.Can enter the filling drier when dry and be the alternating temperature adsorbent equipment of at least a or CNA-421 type drier that Sichuan Tianyi Science ﹠ Technology Co., Ltd produces in activated alumina, silica gel, active carbon, the molecular sieve, remove the water in the half product gas.Product gas after alternating temperature adsorption dry also can enter the smart drying tower that is filled with molecular sieve, with the continous-stable of guaranteeing to dehydrate step and water content less than 1ppm.
As shown in Figure 5, above-mentioned alternating temperature adsorption dry device is made up of at least 2 drying tower and heaters that are filled with the CNA-421 type drier that at least a or Sichuan Tianyi Science ﹠ Technology Co., Ltd produces in activated alumina, silica gel, active carbon, the molecular sieve desiccant.One of them tower is in adsorption step, in adsorption step, half product gas enters drying tower, the drier that loads in the drying tower adsorbs the water in the half product gas, removing half product gas output drying tower behind the water becomes the product gas of this device, and meanwhile another drying tower is in the thermal regeneration step of drier.In the thermal regeneration step, with returning part after drying product gas or water content less than the hydrogen of 1ppm, nitrogen, methane, ethene, ethane, propane, propylene, butane, butylene or by two or more mist that constitutes of these components, after heater via is heated to 100 ℃～400 ℃, enter the drying tower that is in the thermal regeneration step from the port of export of drying tower product gas, under higher temperature, be adsorbed on the water in the drier, from drier, desorb with the arrival end outflow drying tower of regeneration gas, when regeneration temperature is higher, can increase the cold blowing step to reduce the temperature of regeneration back drying tower and drier from drying tower half product gas.The cold blowing gas of cold blowing step be returning part after drying product gas or water content less than the hydrogen of 1ppm, nitrogen, methane, ethene, ethane, propane, propylene, butane, butylene or by two or more mist that constitutes of these components.If adsorptive pressure and thermal regeneration step pressure differ to, the buck or boost step can be set before entering regeneration step, and after regeneration step is finished, be provided with and boost or depressurization step.If being used for the regeneration gas of thermal regeneration drier forms different with product gas, in order to guarantee that purity of product gas also can replace drying tower by returning part product gas behind thermal regeneration, remain in regeneration gas component on the drier to the influence of product makings amount with elimination.
Dry gas of the present invention passes through after above-mentioned transformation absorption, wet desulphurization, smart desulfurization and the deoxygenation step successively, the C that makes recovery
2And C
2(V/V) sulfur content is less than 0.1ppm in the above hydrocarbon component, and oxygen content has realized the reasonable processing to the dry gas of oil plant discharging less than 1ppm, thereby reaches the standard of utilizing of ethylene plant, downstream, and then provides a cover useful technological process.When solveing the technical problem, the domestic scholar of having once proposed to annotate earlier the sulphur deoxidation, and then desulfurization, but this process need to be only applicable to the expensive dehydrogenation catalyst of presulfurization, thereby had limited the utilization of above-mentioned dehydrogenation catalyst commonly used at present.In addition, dehydrogenation catalyst commonly used can meet the standard of utilizing of ethylene plant, downstream with oxygen removal below 1ppm, and it is used in the deoxygenation of the dry gas of component complexity, domesticly yet there are no relevant report and application.From the following embodiment that we carry out as can be seen, process provided by the invention has not only solved the technical problem that is proposed, and has the operability of practice.
By the optimization of above-mentioned technology as can be seen, through after a series of dearsenification, carbon dioxide removal and the dehydration, the content of the arsenic in the dry gas, carbon dioxide and water can be respectively less than 5ppb, 1ppm and 1ppm, its impurity content further reduces, purity and added value improve, and more help the further utilization of downstream factory.
Below the present invention is further detailed explanation for the embodiment by the specific embodiment.But this should be interpreted as that the scope of the above-mentioned theme of the present invention only limits to following embodiment.Do not breaking away under the above-mentioned technological thought situation of the present invention, various replacements or change according to ordinary skill knowledge and customary means are made include within the scope of the invention.
Description of drawings
Fig. 1 is a transformation adsorption step process flow diagram in the embodiment of the invention 1;
Fig. 2 is a transformation adsorption step process flow diagram in the embodiment of the invention 2;
Fig. 3 is the embodiment of the invention 3 technological process block-diagrams;
Fig. 4 is a transformation adsorption step process flow diagram in the embodiment of the invention 3;
Fig. 5 is an alternating temperature adsorption dry process schematic flow sheet in the embodiment of the invention 3.
The specific embodiment
Present embodiment is for to reclaim C from the oil plant catalytic cracked dry gas
2And C
2The method of above hydrocarbon component, catalytic cracked dry gas treating capacity 5000Nm
3/ h, pressure 0.55MPa, 40 ℃ of temperature, its gas componant is formed as shown in table 1:
Table 1 catalytic cracked dry gas becomes to be grouped into (V/V)
| Form | H 2 | O 2 | N 2 | CH 4 | CO | CO 2 | C 2H 4 | C 2H 6 | C 3H 6 | C 3H 8 | C 4 | C 5 | H 2S |
| Content % | 25.8 | 0.3 | 9.1 | 30 | 0.9 | 1.5 | 13.5 | 12 | 4.2 | 0.8 | 0.8 | 1.1 | 50ppm |
C in the table
4Expression contains the hydrocarbon gas of 4 carbon atoms, as normal butane, iso-butane, isobutene, n-butene, anti-butylene; C
5 +Expression contains the hydrocarbon gas of 5 and 5 above carbon atoms.
At first adopt C in the pressure swing adsorption method concentrating and separating catalytic cracked dry gas in the present embodiment
2And C
2Above hydrocarbon component, the C of pressure swing adsorption method concentrating and separating
2And C
2Above hydrocarbon component and then successively through PDS wet desulphurization unit, smart desulfurization unit and chemical reaction deacidification unit.
Psa unit by 6 adsorption towers that respectively are filled with the CNA-716 type adsorbent of 15 cubic metres of Sichuan Tianyi Science ﹠ Technology Co., Ltd's production and sales, 1 50 cubic metres contraryly put jar, 1 50 cubic metres half product gas blending tanks, 1 20 cubic metres of displacement gas surge tank, 1 displacement gas compressor, 1 half product air compressor, 2 vavuum pumps and corresponding pipeline and sequencing valve be formed by connecting.Each cyclic process of each tower experience absorption A, displacement RP, all pressure drop ED, contraryly put D, the V that finds time, all voltage rise ER, final seven steps of FR of boosting, each tower operation sequential, gauge pressure see Table 2:
Table 2PSA work schedule table
During the pressure swing adsorption system operation, by the switch of computer by certain each sequencing valve of programme-control.Be example now with adsorption tower A, each processing step of narration PSA operation:
Absorption A: open sequencing valve KV1A and KV2A, enter adsorption tower A through valve KV1A, adsorbents adsorb C in bed from the catalytic cracked dry gas of catalytic cracking unit
2H
4, C
2H
6And C
2Above hydrocarbon components etc. are absorbed component easily, and H
2, O
2, N
2, CO, CH
4Discharge from adsorption tower A top by valve KV2A as absorption waste gas Deng being difficult for absorbed component.After adsorption time arrived, shut off valve KV1A and KV2A stopped absorption, and another adsorption tower that this moment, dry gas entered after finally boosting adsorbs.
Displacement RP: open sequencing valve KV3A and KV4A, come self-converse put with the absorption of finding time to obtain mutually half product gas enter adsorption tower A through half product gas blending tank 5, displacement gas compressor 10, displacement gas surge tank 6, the adsorbent bed of finishing adsorption step is replaced, to improve the content of absorption phase component.Impurity that is displaced and portion C
2H
4, C
2H
6And C
2Above hydrocarbon component is discharged from adsorption tower A top by valve KV4A as displacement waste gas.After time swap arrived, shut off valve KV3A and KV4A stopped displacement.
Equal pressure drop ED: open sequencing valve KV7A and KV7D, the adsorption tower A that finishes after the absorption all presses with the adsorption tower D that finishes after finding time, and after two adsorption column pressures were in a basic balance, shut off valve KV7A finished the equal pressure drop of adsorption tower A.
The contrary D of putting: open sequencing valve KV8A, the adsorbent bed that equal voltage drop step is finished is discharged the absorption phase component, reduces adsorption tower A pressure.Contrary venting enters the contrary jar 1 of putting through valve KV8A, enters half product gas blending tank 5 through manual modulation valve HV1 again.After adsorption tower A pressure is reduced to normal pressure, shut off valve KV8A, contrary putting finished.
V finds time: open sequencing valve KV6A, find time by the adsorbent bed after 81 pairs of contrary putting of vavuum pump, the gas that vavuum pump 81 is extracted out mixes mutually with contrary venting, after 11 pressurizations of half product air compressor, export as half product gas, another part enters displacement gas surge tank 6 as displacement gas after 10 pressurizations of displacement gas compressor, retrieval system is replaced.Find time to finish shut off valve KV6A.
Equal voltage rise ER: open valve KV7D and KV7A, the adsorption tower A of the evacuation step of finishing and the adsorption tower D that finishes after the displacement step all press, and after two adsorption column pressures were in a basic balance, shut off valve KV7D and KV7A finished the equal voltage rise of adsorption tower A.
FR finally boosts: open sequencing valve KV5A, by manual modulation valve HV3, utilize absorption waste gas that the adsorption tower A that finishes equal voltage rise step is boosted, make it to reach adsorptive pressure, shut off valve KV5A prepares to enter adsorption step.
So far, the institute of adsorption tower A in one-period all is finished in steps, and begins to enter next time circulation, and the performed step of other 5 adsorption towers is identical with adsorption tower A, just staggers mutually in time.
1500Nm from the psa unit acquisition
3/ h half product gas, be forced into 0.6Mpa through half product air compressor, be cooled to 42 ℃ through cooler again, enter the PDS absorption tower that is filled with 1.0 meters of 20 meters high stainless steel Pall ring fillers, tower diameter from the bottom to top, contain 50ppm PDS catalyst from the upper end spray of adsorption tower, the absorbent solution that contains sodium carbonate 8%, 10 tons/hour of solution spraying amounts.Hydrogen sulfide in the catalysis drying gas is absorbed solution and absorbs, and obtains the gas of hydrogen sulfide less than 5ppm from the upper end gas vent on absorption tower.This gas enters from the lower end and is filled with 5 cubic metres of iron oxide fine desulfurizers and 5 cubic metres is the smart desulfurizing tower of the desulfurizing agent of carrier with the active carbon, and the sulfide in the half product gas is removed to below the 0.1ppm.Half product gas heater via after smart desulfurization is heated to 250 ℃, enter the deoxidation reactor of the CNA-538 type dehydrogenation catalyst that is filled with 1.0 cubic metres of Sichuan Tianyi Science ﹠ Technology Co., Ltd's production and sales, oxygen and H-H reaction generate water in deoxidation reactor, and oxygen is removed to below the 1ppm.
The purified gas of the above-mentioned a plurality of cell processing of process is as the product gas of this device, component is as shown in table 3, can enter the charge gas compressor inlet of ethylene plant, downstream ethylene unit, mix with ethene cracking gas through pressurization again after the back device removes carbon dioxide and water, enter low temperature separation unit recovery ethene, propylene and ethane cracking furnace raw material ethane, propane etc.
The product pneumatolytic is grouped into (V/V) behind the table 3 catalytic cracked dry gas isolation of purified
| Form | H 2 | O 2 | N 2 | CH 4 | CO | CO 2 | C 2H 4 | C 2H 6 | C 3H 6 | C 3H 8 | C 4 | C 5 | Total S |
| Content % | 0.01 | ≤ 1ppm | 1.0 | 8.63 | 0.19 | 4.34 | 38.3 | 26.8 | 12.4 | 2.68 | 2.68 | 2.97 | ≤ 0.1ppm |
The coking dry gas flow is 12000Nm
3/ h, pressure 0.7Mpa, 30 ℃ of temperature, its constituent content such as table 4, enter by transformation adsorbed gas separative element, MEA desulfurization carbon dioxide removal unit, water washing take off liquid unit, moisture from the unit, essence takes off the coking dry gas isolation of purified that liquid unit, dearsenification unit, smart desulfurization unit and hydrogenation deoxidation reactor unit constitute and reclaims C
2And C
2Above hydrocarbon component device.
Table 4 coking dry gas becomes to be grouped into (V/V)
| Form | H 2 | O 2 | N 2 | CH 4 | C 2H 4 | C 2H 6 | C 3H 8 | C 3H 6 | i-C 4 | n-C 4 | n-C 4 - | H 2S | As |
| Content % | 4.90 | 0.64 | 3.24 | 52.97 | 3.32 | 19.21 | 9.21 | 5.03 | 0.54 | 0.47 | 0.46 | 0.01 | 0.5ppm |
I-C in the table
4, n-C
4, n-C
4 =Represent iso-butane, normal butane, n-butene respectively.
At first transformation adsorbed gas separative element is with the C in the coking dry gas
2And C
2Above hydrocarbon component concentrating and separating obtains half product gas.Psa unit by 8 CNA-625 type adsorbents that respectively are filled with 40 cubic metres of Sichuan Tianyi Science ﹠ Technology Co., Ltd's production and sales adsorption tower, 1 80 cubic metres contrary puts jar, 1 80 cubic metres half product gas blending tanks, 1 80 cubic metres of displacement gas surge tank, 2 displacement gas compressors, 2 half product air compressors, 6 vavuum pumps and corresponding pipeline and sequencing valve are formed by connecting.Fig. 2 is seen in the technological process of pressure-swing absorption apparatus, and time-scale sees Table 5.
Table 5 PSA work schedule table
During the pressure swing adsorption system operation, by the switch of computer by certain each sequencing valve of programme-control.Be example now with adsorption tower A, each processing step of narration PSA operation:
Absorption A: open sequencing valve KV1A and KV2A, enter adsorption tower A through valve KV1A, adsorbents adsorb C in bed from the coking dry gas of coking plant
2H
4, C
2H
6And C
2Above hydrocarbon components etc. are absorbed component easily, and H
2, O
2, N
2, CO, CH
4Discharge from adsorption tower A top by valve KV2A as absorption waste gas Deng being difficult for absorbed component.After adsorption time arrived, shut off valve KV1A and KV2A stopped absorption, and another adsorption tower that this moment, dry gas entered after finally boosting adsorbs.
Equal pressure drop E1D once: open sequencing valve KV5A and KV5E, the adsorption tower A that finishes after the absorption all presses with the adsorption tower E that finishes the equal voltage rise of secondary, and after two adsorption column pressures were in a basic balance, shut off valve KV5A and KV5E finished once all pressure drops of adsorption tower A.
The equal pressure drop E2D of secondary: open sequencing valve KV7A and KV7F, finish once after all pressure drops adsorption tower A with finish the adsorption tower F that finds time and all press, after two adsorption column pressures were in a basic balance, shut off valve KV7A and KV7F finished the equal pressure drop of secondary of adsorption tower A.
Displacement RP: open sequencing valve KV3A and KV4A, come self-converse put with the absorption of finding time to obtain mutually half product gas enter adsorption tower A through half product gas blending tank 5, displacement gas compressor bank 10, displacement gas surge tank 6, the adsorbent bed of finishing the equal pressure drop of secondary is replaced, to improve the content of absorption phase component.Impurity that is displaced and portion C
2H
4, C
2H
6And C
2Above hydrocarbon component is discharged from adsorption tower A top by valve KV4A as displacement waste gas.After time swap arrived, shut off valve KV3A and KV4A stopped displacement.
The contrary D of putting: open sequencing valve KV8A, the adsorbent bed that displacement step is finished is discharged the absorption phase component, reduces adsorption tower A pressure.Contrary venting enters the contrary jar 1 of putting through valve KV8A, enters half product gas blending tank 5 through manual modulation valve HV1 again.After adsorption tower A pressure is reduced to normal pressure, shut off valve KV8A, contrary putting finished.
V finds time: open sequencing valve KV6A, find time by the adsorbent bed after 8 pairs of contrary putting of vavuum pump group, the gas that vavuum pump group 8 is extracted out mixes mutually with contrary venting, output after 11 pressurizations of half product air compressor group, a part is exported as half product gas, another part enters displacement gas surge tank 6 as displacement gas, and retrieval system is replaced.Find time to finish shut off valve KV6A.
The equal voltage rise E2R of secondary: open sequencing valve KV7A and KV7D, the adsorption tower A that finishes after finding time all presses with the adsorption tower D that finishes once equal pressure drop, and after two adsorption column pressures were in a basic balance, shut off valve KV7A and KV7D finished the equal voltage rise of secondary of adsorption tower A.
Equal voltage rise E1R once: open sequencing valve KV5A and KV5E, the adsorption tower A that finishes after the equal voltage rise of secondary all presses with the adsorption tower E that finishes absorption, and after two adsorption column pressures were in a basic balance, shut off valve KV5A and KV5E finished once all voltage rises of adsorption tower A.
FR finally boosts: continue open valve KV5A, by manual modulation valve HV3, utilize absorption waste gas that the adsorption tower A that finishes equal voltage rise step is boosted, make it to reach adsorptive pressure, prepare to enter adsorption step.
So far, the institute of adsorption tower A in one-period all is finished in steps, and begins to enter next time circulation, and the performed step of other 7 adsorption towers is identical with adsorption tower A, just staggers mutually in time.
4000Nm from the psa unit acquisition
3/ h half product gas, be forced into 1.2Mpa through half product air compressor, be cooled to 40 ℃ through cooler again, enter from the bottom to top and be filled with 15 meters high ceramic Pall ring fillers, the MEA absorption tower that tower diameter is 0.6 meter, spray the MEA solution of concentration 15% from the upper end of adsorption tower, 15 tons/hour of MEA solution spraying amounts.Hydrogen sulfide in the coking dry gas, carbon dioxide are absorbed by MEA solution, obtain the gas of hydrogen sulfide less than 5ppm from the upper end gas vent on MEA absorption tower.This gas enters 0.6 meter of tower diameter from the lower end, be filled with the water washing liquid taking-off tower of 5 meters high ceramic Pall ring fillers, spray into deionized water from the upper end of water washing liquid taking-off tower, 10 tons/hour of spray flux obtain to remove through water washing half product gas of the amine mist of carrying secretly in the semi-finished product gas at the upper end of water wash column gas vent.This half product gas enters the smart liquid taking-off tower that is filled with 10 cubic metres of activated aluminas behind 10 cubic metres of separator separating liquid impurity, separate and remove minor amount of water and MEA solution impurity.The half product gas heater via that obtains is heated to 50 ℃, enters the dearsenicator that is filled with 20 cubic metres of Hydrodearsenic Catalysts again, and the arsenide in the half product gas is removed to below the 5ppb.Half product gas after dearsenification enters from the lower end and is filled with 10 cubic metres is the smart desulfurizing tower of the desulfurizing agent of carrier with the active carbon, and the sulfide in the half product gas is removed to below the 0.1ppm.This half product gas heater via is heated to 250 ℃, enters the deoxidation reactor of the CNA-520 type dehydrogenation catalyst that is filled with 1 cubic metre of Sichuan Tianyi Science ﹠ Technology Co., Ltd's production and sales again.Oxygen and H-H reaction generate water in deoxidation reactor, gas after the deoxidation is used as the product gas of this device, become to be grouped into as shown in table 7, this product gas can be transported to the charge gas compressor inlet of ethylene unit, after pressurization, removing carbon dioxide and water, enter that low temperature separation unit is used to reclaim ethene, propylene and as hydrocarbon components such as the ethane of pyrolysis furnace raw material, propane.
The product pneumatolytic is grouped into (V/V) behind the table 6 coking dry gas isolation of purified
| Form | H 2 | O 2 | N 3 | CH 4 | C 3H 4 | C 3H 4 | C 3H 4 | C 3H 4 | i-C 4 | n-C 4 | 1-C 4 - | Total S | As |
| Content % | 0.02 | 1ppm | 0.07 | 5.76 | 7.39 | 46.76 | 23.69 | 12.39 | 1.45 | 1.26 | 1.21 | ≤0.1ppm | 5ppb |
Embodiment 3
Oil plant catalytic cracked dry gas flow 25000Nm
3/ h, pressure 0.60MPa, 30 ℃ of its gas componants of temperature are formed as shown in table 7:
Table 7 catalytic cracked dry gas becomes to be grouped into (V/V)
| Form | H 2 | O 2 | N 2 | CH 4 | CO | CO 2 | C 2H 4 | C 2H 6 | C 3H 6 | C 3H 8 | C 4 | C 5 - | H 2S | As | H 2O |
| Content % | 25.3 | 0.3 | 9.1 | 30 | 0.9 | 1.5 | 13.5 | 12 | 4.2 | 0.8 | 0.8 | 1.1 | 30ppm | 2ppm | 0.5 |
Present embodiment catalytic cracked dry gas separating purifying device as shown in Figure 3, by psa unit, MDEA desulfurization carbon dioxide removal unit, water washing take off liquid unit, moisture from the unit, essence take off liquid unit, dearsenification unit, smart desulfurization unit, hydrogenation deoxidation reactor unit, alkali cleaning carbon dioxide removal unit, water washing dealkalize unit, moisture from the unit, dealkalize unit, alternating temperature adsorption dry unit and keen-witted and capable dry unit constitute.
As shown in Figure 4, the present embodiment psa unit is by transformation absorption 1 section (PSA-1) and 2 sections (PSA-2) formations of transformation absorption.PSA-1 by the adsorption tower of 10 CNA-625 types that respectively are filled with 56 cubic metres of Sichuan Tianyi Science ﹠ Technology Co., Ltd's production and sales and two kinds of adsorbents of CNA-716 type, 1 contraryly put jar, 1 half product gas blending tank, 1 displacement off-gas buffer tank, 10 vavuum pumps and corresponding pipeline and sequencing valve be formed by connecting.PSA-2 by the adsorption tower of 6 CNA-625 types that respectively are filled with 10 cubic metres of Sichuan Tianyi Science ﹠ Technology Co., Ltd's production and sales and two kinds of adsorbents of CNA-716 type, 1 contraryly put jar, 1 half product gas blending tank, 4 vavuum pumps and corresponding pipeline and sequencing valve be formed by connecting.This two-stage pressure swing adsorption apparatus is shared 1 half product gas blending tank, 1 displacement gas surge tank, 3 displacement gas compressors and 3 half product air compressors in addition.
PSA-1 is in when operation, and every tower circulates each time all that experience absorption A, displacement RP, fall all that E1D, two all falls E2D, contraryly puts D, the V that finds time, two all rises E2R, and all rises E1R, final nine steps of FR of boosting, and its program operation sequential sees Table 8:
Table 8 PSA-1 work schedule table
Be subjected to the restriction of margin, the E in the table in the expression symbol of equal pressure drop and all voltage rises is omitted; The gauge pressure of the third line value is unlisted in the table, and this value is respectively: 0.60,0.55,0.30,0.05,0.02 ,-0.08,0.05,0.30,0.59, and units MPa.
Be example now with adsorption tower A among the PSA-1, each processing step of narration PSA-1 operation:
Absorption A: open sequencing valve KV1A and KV2A, enter adsorption tower A from the catalytic cracked dry gas outside the battery limit (BL), adsorbent is to C in bed
2H
4, C
2H
6And C
2Above hydrocarbon components etc. easily absorbed component adsorb, and H
2, O
2, N
2, CO, CH
4Discharge from adsorption tower A top by valve KV2A as absorption waste gas Deng being difficult for absorbed component.After adsorption time arrived, shut off valve KV1A and KV2A stopped absorption, and another adsorption tower that this moment, dry gas entered after finally boosting adsorbs.
Displacement RP: open sequencing valve KV3A and KV4A, come self-converse put with the absorption of finding time to obtain mutually product gas enter adsorption tower A through half product gas blending tank 5, displacement gas compressor bank 10, displacement gas surge tank 6, the adsorbent bed of finishing attached step is replaced, to improve the content of absorption phase component.Impurity that is displaced and portion C
2H
4, C
2H
6And C
2Above hydrocarbon component is discharged from adsorption tower A top by valve KV4A as displacement waste gas, enters displacement off-gas buffer tank 7, as the unstripped gas of PSA-2.After time swap arrived, shut off valve KV3A and KV4A stopped displacement.
One all falls E1D: open sequencing valve KV5A and KV5G, the adsorption tower A that finishes after the displacement all presses with finishing two adsorption tower G after all rising, and after two adsorption column pressures were in a basic balance, shut off valve KV5A finished one of adsorption tower A and all falls.
Two all fall E2D: open sequencing valve KV7A and KV7H, the gas in the adsorption tower A enters adsorption tower H, and finishes the adsorption tower H that finds time and carries out isostasy, and after two adsorption column pressures were in a basic balance, shut off valve KV7A and KV7H finished two of adsorption tower A and all fall.
The contrary D of putting: open sequencing valve KV8A, reduce adsorption tower A pressure.Contrary venting enters the contrary jar 1 of putting through valve KV8A, enter half product gas blending tank 2 and enter half product gas blending tank 5 through manual modulation valve HV1 again, when adsorption column pressure is reduced to gauge pressure 0.05Mpa, open sequencing valve KV9, the contrary gas of putting directly enters half product gas blending tank 2 and half product gas blending tank 5 by KV8A by KV9.After adsorption tower A pressure is reduced to normal pressure, shut off valve KV8A, KV9, contrary putting finished.
V finds time: open sequencing valve KV6A, find time by the adsorbent bed after 81 pairs of contrary putting of 5 vavuum pump groups, the gas that vavuum pump group 81 is extracted out mixes mutually with contrary venting, enter half product gas blending tank 2 and half product gas blending tank 5, a part is as the 11 pressurization back outputs of half product gas, half product air compressor group, and another part is as displacement gas retrieval system after 10 pressurizations of displacement gas compressor bank.Find time to finish shut off valve KV6A.
Two all rise E2R: open valve KV7D and KV7A, gas enters adsorption tower A in the adsorption tower D, finishes an adsorption tower D who all falls and finishes the adsorption tower A that finds time and carry out isostasy, when two pressure towers equate substantially, close KV7D and KV7A valve, finish two of adsorption tower A and all rise.
One all rises E1R: open valve KV5A and KV5E, and finish two adsorption tower A after all rising and all press with the adsorption tower E that finishes after the absorption, after two adsorption column pressures were in a basic balance, shut off valve KV5E finished one of adsorption tower A and all rises.
FR finally boosts: continue open valve KV5A, by manual modulation valve HV3, utilize absorption waste gas that the adsorption tower A that finishes equal voltage rise step is boosted, make it to reach adsorptive pressure, prepare to enter adsorption step.
So far, the institute of adsorption tower A in one-period all is finished in steps, and begins to enter next time circulation, and the performed step of other nine adsorption towers is identical with adsorption tower A, just staggers mutually in time, carries out continuously with the assurance separation process.
Each adsorption column pressure is cyclically-varying with the variation of processing step, and according to the practical operation situation, adsorptive pressure can suitably be adjusted, then other step pressure is corresponding changes.
PSA-2 is in when operation, each tower each cyclic process experience absorption A, displacement RP, all pressure drop ED, contraryly put D, the V that finds time, all voltage rise ER, final seven steps of FR of boosting, each tower operation sequential, gauge pressure see Table 9:
Table 9 PSA-2 work schedule table
Be example now with adsorption tower K, each processing step of narration PSA-2 operation:
Absorption A: open sequencing valve KV1K and KV2K, enter adsorption tower K through valve KV1K, adsorbing separation C in bed by displacement off-gas buffer tank 7 from the displacement waste gas of PSA-1
2H
4, C
2H
6And C
2Above hydrocarbon components etc. are absorbed component easily, and H
2, O
2, N
2, CO, CH
4Discharge from adsorption tower K top by valve KV2K as absorption waste gas Deng being difficult for absorbed component.After adsorption time arrived, shut off valve KV1K and KV2K stopped absorption, replaced another adsorption tower that waste gas enters after finally boosting this moment and adsorbed.
Displacement RP: open sequencing valve KV3K and KV4K, come self-converse put with the absorption of finding time to obtain mutually product gas enter adsorption tower K through half product gas blending tank 5, displacement gas compressor bank 10, displacement gas surge tank 6, the adsorbent bed of finishing adsorption step is replaced, to improve the content of absorption phase component.Impurity that is displaced and portion C
2H
4, C
2H
6And C
2Above hydrocarbon component is discharged from adsorption tower K top by valve KV4K as displacement waste gas, enters displacement off-gas buffer tank 7 and further reclaims.After time swap arrived, shut off valve KV3K and KV4K stopped displacement.
Equal pressure drop ED: open sequencing valve KV5K and KV5N, the adsorption tower K that finishes after the displacement all presses with the adsorption tower N that finishes after finding time, and after two adsorption column pressures were in a basic balance, shut off valve KV5K finished the equal pressure drop of adsorption tower K.
The contrary D of putting: open sequencing valve KV8K, reduce adsorption tower K pressure.Contrary venting enters the contrary jar 3 of putting through valve KV8K, enter half product gas blending tank 4 and half product gas blending tank 5 through manual modulation valve HV2 again, when adsorption column pressure is reduced to gauge pressure 0.05Mpa, open sequencing valve KV10, the contrary gas of putting directly enters half product gas blending tank 4 and half product gas blending tank 5 by KV8K by KV10.After adsorption tower K pressure is reduced to gauge pressure 0.01Mpa, shut off valve KV8K, contrary putting finished.
V finds time: open sequencing valve KV6K, find time by the adsorbent bed after 91 pairs of contrary putting of 2 vavuum pump groups, the gas that vavuum pump group 91 is extracted out mixes mutually with contrary venting, a part is as the output after 11 pressurizations of half product air compressor group of half product gas, and another part is as displacement gas retrieval system after 10 pressurizations of displacement gas compressor bank.Find time to finish shut off valve KV6K.
Equal voltage rise ER: open valve KV5N and KV5K, the adsorption tower N after finishing the adsorption tower K after finding time and finishing absorption all presses, and after two adsorption column pressures were in a basic balance, shut off valve KV5N finished the equal voltage rise of adsorption tower K.
FR finally boosts: continue open valve KV5K, by manual modulation valve HV4, utilize absorption waste gas that the adsorption tower K that finishes equal voltage rise step is boosted, make it to reach adsorptive pressure, prepare to enter adsorption step.
So far, the institute of adsorption tower K in one-period all is finished in steps, and begins to enter next time circulation, and the performed step of other 5 adsorption towers is identical with adsorption tower K, just staggers mutually in time.
6000Nm from the psa unit acquisition
3/ h half product gas, be forced into 3.5Mpa through half product air compressor, be cooled to 35 ℃ through cooler again, enter from the bottom to top by being filled with 21 meters high stainless steel Pall ring fillers, the MDEA absorption tower that tower diameter is 1.0 meters, spray the MDEA solution of content 12% from the upper end of adsorption tower, 25 tons/hour of MDEA solution spraying amounts.Hydrogen sulfide in the catalytic cracked dry gas, carbon dioxide are absorbed by MDEA solution, obtain the gas of hydrogen sulfide from the upper end gas vent on MDEA absorption tower less than 6ppm, enter 0.8 meter of tower diameter again from the lower end, the water washing liquid taking-off tower that filling stainless steel Pall ring packed height is 6 meters.Spray into deionized water from the upper end of water wash column, obtain to remove half product gas of the amine mist of carrying secretly the semi-finished product gas through water washing from the upper end gas vent of water wash column.This half product gas enters the activated alumina that is filled with 10 cubic metres of 1: 1 volume ratios and the smart liquid taking-off tower of acticarbon again behind separator separating liquid impurity, separate and remove minor amount of water and MDEA solution impurity.The half product gas heater via that obtains is heated to 80 ℃, enters the dearsenicator that is filled with 25 cubic metres of Hydrodearsenic Catalysts again, and the arsenide in the half product gas is removed to below the 5ppb.Half product gas after dearsenification enters from the lower end and is filled with 5 cubic metres of iron oxide fine desulfurizers and 5 cubic metres is the smart desulfurizing tower of the desulfurizing agent of carrier with the active carbon, and the sulfide in the half product gas is removed to below the 0.1ppm.This gas heater via is heated to 200 ℃, enters the CNA-538 type that is filled with 1.5 cubic metres of Sichuan Tianyi Science ﹠ Technology Co., Ltd's production and sales and the deoxidation reactor of CNA-520 type dehydrogenation catalyst again, and both volume ratios are 1: 2.Oxygen and H-H reaction generate water in deoxidation reactor, and oxygen is removed to below the 1ppm.Gas after the deoxidation, the carbon dioxide in the NaOH absorbing and removing half product gas in the alkali absorption tower is to 1ppm.The gas that removes behind the carbon dioxide enters 0.8 meter of tower diameter from the lower end, the water washing dealkalize tower that filling stainless steel Pall ring packed height is 5 meters, spray into deionized water from the upper end of water wash column, obtain to remove half product gas of the alkali mist of carrying secretly the semi-finished product gas through water washing from the upper end gas vent of water wash column.This half product gas enters the dealkalize tower that is filled with 10 cubic metres of acticarbons again behind separator separating liquid impurity, separate and remove minor amount of water and aqueous slkali impurity.The most later half product gas enters the drier that respectively is filled with the CNA-421 type drier of 20 cubic metres of Sichuan Tianyi Science ﹠ Technology Co., Ltd's production and sales by two successively, and the alternating temperature adsorption dry unit that constitutes of a series of sequencing valves and pipeline and the keen-witted and capable dry unit Jiang Shui that is filled with the CNA-131 type drier of 10 cubic metres of Sichuan Tianyi Science ﹠ Technology Co., Ltd's production and sales are removed to below the 1ppm.
As shown in Figure 5, existing is example with drying tower A, each processing step of narration alternating temperature adsorption dry operation, and during the operation of alternating temperature absorbing unit, can be by the switch of computer by certain each sequencing valve of programme-control.
Absorption: open sequencing valve KV1A and KV2A, valve KV1A from half product gas self-desiccation tower lower end of dealkalize tower enters drying tower A, the contained humidity adsorbents adsorb in the tower that is dried in the half product gas, the valve KV2A of dry purified gas self-desiccation tower upper end discharges and enters keen-witted and capable dry unit.Water content in purified gas surpasses 1ppm, and shut off valve KV1A and KV2A stop absorption.Half product gas entered drying tower B and adsorbed this moment.
Heating: open sequencing valve KV4A, KV3A and KV5, enter the regeneration gas heater from the regeneration gas outside the battery limit (BL) through valve KV5, regeneration gas after the heating enters through valve KV4A adsorbs saturated drying tower A, be attracted to moisture on the adsorbent through heating, discharge the battery limit (BL) with the valve KV3A of regeneration gas self-desiccation tower lower end.When regeneration gas port of export temperature rises to 150 ℃, shut off valve KV5 and regeneration gas heater stop heating.
Cold blowing: continue open valve KV4A, KV3A, open sequencing valve KV6 simultaneously, the valve KV4A through valve KV6, drying tower upper end enters the drying tower A of thermal regeneration without the regeneration gas that heats, and the valve KV3A of cold blowing regeneration off gases self-desiccation tower lower end discharges the battery limit (BL).When regeneration gas port of export temperature drops to 50 ℃, shut off valve KV6 and valve KV4A, KV3A stop cold blowing.Drying tower is finished regeneration, prepares to enter next adsorption cycle.
So far, the institute of drying tower A in one-period all is finished in steps, and begins to enter next time circulation, and the performed step of drying tower B is identical with it, just staggers mutually in time with the continuous output of assurance purified gas.
The purified gas of the above-mentioned a plurality of cell processing of process is as the product gas of this device, and component is as shown in table 10, and the low temperature separation unit that can directly enter ethylene unit reclaims ethene, third rare and pyrolysis furnace raw material ethane, the propane etc.
The product pneumatolytic is grouped into (V/V) behind the table 10 catalytic cracked dry gas isolation of purified
| Form | H 2 | O 2 | N 2 | CH 4 | CO | CO 2 | C 2H 4 | C 2H 6 | C 3H 6 | C 3H 8 | C 4 | C 5 - | Total S | As | H 2O |
| Content % | 0.05 | ≤ 1ppm | 1.05 | 9.0 | 0.2 | ≤ 1ppm | 40 | 28 | 13 | 2.8 | 2.8 | 3.1 | ≤ 0.1ppm | ≤ 5ppb | ≤ 1ppm |
Claims (11)
1. dry gas reclaims C
2And C
2The method of above hydrocarbon component, make described dry gas circulate at least successively experience by absorption, contrary put, find time and the transformation adsorption step formed of finally boosting to wherein C
2And C
2Above hydrocarbon component separates, and it is characterized in that, experiences wet desulphurization, smart desulfurization and deoxygenation step more successively at least through the gas after the transformation absorption and purifies, and obtains to be rich in C
2And C
2The gaseous mixture of above hydrocarbon component.
2. dry gas according to claim 1 reclaims C
2And C
2The method of above hydrocarbon component is characterized in that,
Also include the dearsenification step between described wet desulphurization and the smart desulfurized step.
3. dry gas according to claim 2 reclaims C
2And C
2The method of above hydrocarbon component is characterized in that,
Also include essence between described wet desulphurization and the dearsenification step and take off the liquid step.
4. dry gas according to claim 3 reclaims C
2And C
2The method of above hydrocarbon component is characterized in that,
Described wet desulphurization and essence are taken off and are also included water washing between the liquid step and take off the liquid step.
5. dry gas according to claim 1 reclaims C
2And C
2The method of above hydrocarbon component is characterized in that,
Also include alkali cleaning carbon dioxide removal and drying steps after the described deoxygenation step successively.
6. dry gas according to claim 4 reclaims C
2And C
2The method of above hydrocarbon component is characterized in that,
Also include alkali cleaning carbon dioxide removal and drying steps after the described deoxygenation step successively.
7. dry gas according to claim 6 reclaims C
2And C
2The method of above hydrocarbon component is characterized in that,
Also include the dealkalize step between described alkali cleaning carbon dioxide removal and the drying steps.
8. dry gas according to claim 7 reclaims C
2And C
2The method of above hydrocarbon component is characterized in that,
Also include water washing dealkalize step between described alkali cleaning carbon dioxide removal and the dealkalize step.
9. dry gas according to claim 8 reclaims C
2And C
2The method of above hydrocarbon component is characterized in that,
Described drying steps adopts the alternating temperature absorption method to carry out drying.
10. dry gas according to claim 9 reclaims C
2And C
2The method of above hydrocarbon component is characterized in that,
Also include keen-witted and capable dry step after the described alternating temperature adsorption dry step.
11. reclaim C according to each described dry gas in the claim 1 to 10
2And C
2The method of above hydrocarbon component, it is characterized in that, pressure swing adsorption system comprises 2 sections of 1 section of transformation absorption and transformation absorption in the described transformation adsorption step, they are made of at least two adsorption towers that are filled with adsorbent respectively, each adsorption tower circulate at least successively experience absorption, displacement, contraryly put, find time and the step of finally boosting, and the displacement waste gas of 1 section of transformation absorption enters 2 sections of transformation absorption as unstripped gas.
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| CN100364943C (en) * | 2006-08-25 | 2008-01-30 | 四川开元科技有限责任公司 | Pressure swing adsorption method of separating and recovering C3+ hydrocarbons from C3+ hydrocarbons contained mixture gas |
| CN101638584B (en) * | 2008-08-01 | 2013-01-02 | 中国石油化工股份有限公司 | Method for separating catalytic dry gas in refinery by using shallow cold oil absorption method |
| CN102463032A (en) * | 2010-11-04 | 2012-05-23 | 中国石油化工股份有限公司 | Treatment method of acid water head space gas |
| CN103450941B (en) * | 2012-05-30 | 2015-08-19 | 中国石油化工股份有限公司 | A kind of method of being produced ethylene cracking material by coking dry gas |
| CN102898267B (en) * | 2012-09-14 | 2014-06-04 | 四川天一科技股份有限公司 | Method for purifying and recovering light hydrocarbon components of C3 and above C3 in polypropylene exhaust |
| CN103752129A (en) * | 2013-09-25 | 2014-04-30 | 上海同利环境科技有限公司 | Device and process for separating and recycling non-methane total hydrocarbons and hydrogen gas from refinery dry gas |
| CN109609219B (en) * | 2019-01-17 | 2020-11-24 | 青岛华世洁环保科技有限公司 | Coking tail gas treatment method and device |
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| CN112574784A (en) * | 2020-11-05 | 2021-03-30 | 西南化工研究设计院有限公司 | Method for recovering hydrocarbon components with carbon number of 2 and carbon number of more than 2 in dry gas by adsorption absorption coupling process |
| CN112521245A (en) * | 2020-12-02 | 2021-03-19 | 西南化工研究设计院有限公司 | Method for producing high-purity ethylene |
| CN112374959B (en) * | 2020-12-02 | 2023-09-29 | 西南化工研究设计院有限公司 | Method for separating ethylene and ethane in catalytic dry gas |
| CN113899161B (en) * | 2021-10-12 | 2023-04-18 | 中石化石油工程技术服务有限公司 | Method for extracting ethane from natural gas |
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