CN1789381A - Gas mixture enriched in hydrocarbon compound with two or more carbon atoms - Google Patents

Gas mixture enriched in hydrocarbon compound with two or more carbon atoms Download PDF

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Publication number
CN1789381A
CN1789381A CN 200510022376 CN200510022376A CN1789381A CN 1789381 A CN1789381 A CN 1789381A CN 200510022376 CN200510022376 CN 200510022376 CN 200510022376 A CN200510022376 A CN 200510022376A CN 1789381 A CN1789381 A CN 1789381A
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gas
adsorption
tower
valve
adsorption tower
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张剑锋
刘丽
石江
刘照利
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Sichuan Tianyi Science and Technology Co Ltd
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Sichuan Tianyi Science and Technology Co Ltd
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Priority to CN 200510022376 priority Critical patent/CN1789381A/en
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Abstract

The invention discloses the mixture gas of rich containing C2 or above C2 hydrocarbons, solving the problems that it is not direct to use, side effect is heavy and the cost is high. In the mixture gas, the content of ethylene, ethane, propylene and propane are rich, and they can be directly entered in ethylene catalytic cracker. The invention first detailedly determines the components and contents of mixture gas.

Description

A kind of C that is rich in 2And C 2The gas mixture of above hydro carbons
Technical field
The present invention relates to a kind of C of being rich in 2And C 2The gas mixture of above hydro carbons more particularly, relates to the catalytic cracked dry gas of heavy oil catalytically cracking equipment or coker and coking dry gas is carried out the C that is rich in that processing such as transformation absorption, wet desulphurization decarburization, dehydrogenation deoxidation, aluminum oxide and molecular sieve drying obtain 2The gas mixture of above hydro carbons.
Background technology
Catalytic cracked dry gas is the tail gas that refinery catalyzed cracking processing oil produces, and wherein contains 15%~20% left and right sides ethene.The existing catalytic cracking throughput of China is 9,300 ten thousand tons/year at present, and about 4,140,000 tons of the annual catalytic cracked dry gas of producing wherein contains 110,000 tons of alkane components such as 730,000 tons of ethene, 720,000 tons in ethane, 110,000 tons of propylene, 40,000 tons of butylene, propane, butane.Because of there not being industrialized recovery technology, domestic plant catalytic cracking dry gas is used as industrial fuel gas, domestic fuel gas substantially, or the torch of setting fire burns, and causes the serious wasting of resources.Along with developing rapidly of China petroleum refining industry crude oil deep processing, the catalytic cracked dry gas of by-product and coking dry gas are also rolling up, and how to make full use of this part valuable industrial chemicals, develop new comprehensive utilization process, improve the comprehensive benefit of refinery, caused people's common concern.
What adopt at most in the large-scale petroleum chemical industry at present is separation by deep refrigeration.
Patent CN99124686.1 " method of separating and reclaiming ethylene and device thereof from catalytic cracked dry gas " utilizes in the catalytic cracked dry gas each gaseous fraction of ethene and other different with the combination degree of water, at first separate and remove not and water bonded gaseous fraction, the ethene that is discharged is reclaimed in fractionation step by step under decompression or heated condition or decompression and heating condition then.
CN92112397.3 " process for separating ethene by catalytic cracking and dry gas adsorption " has announced a kind of like this technology, promptly the catalytic cracked dry gas that removes sour gas and water is passed through C 2And C 3Component can be removed C by effective isolating acticarbon bed 3Component has been removed C 3Dry gas enter to ethene have high-adsorption-capacity and optionally sieve adsorpting bed select ethylene adsorption.And adopt the method that combines with decompression that heats up or reduce pressure or heat up to carry out desorption, reclaim ethene.
The patent CN92109983.5 method of separating hydrocarbon " a kind of from catalytic cracked dry gas " has announced a kind of like this technology, promptly separates hydrogen in the dry gas with membrane separation process earlier, poor hydrogen dry gas is separated again obtaining hydro carbons subsequently with Deep Cooling Method.
Patent CN90109803.5 " the ethylbenzene process process is produced in the reaction of rare ethene and benzene ", CN93115961.X " rare ethene is produced the methyl-ethyl benzene processing method with the toluene reaction " are to use the direct and benzene of the catalytic cracked dry gas that contains rare ethene or toluene hydrocarbonylation system ethylbenzene or to methyl-ethyl benzene.
CN96109121.5 " process for producing dichloroethane by direct chloration of ethylene in catalytic cracking dry gas " has announced a kind of like this technology, is raw material with the ethene in the catalytic cracked dry gas promptly, in cleaner with dry gas dehydration, take off H 2Behind the S, in liquid ethylene dichloride reactor is housed, mix,, react under 0~3MPa condition at-10~250 ℃ with chlorine.Reacted gas condenses into liquid through cooling with wherein ethylene dichloride, separate with unreacted rare gas element making it, again with reactor in liquid mixing, mixture obtains the product ethylene dichloride after rectifying in distillation tower.
More than utilize in the technology, describedly utilize in isolated hydrogen of mode institute or the hydrocarbon and the impurity such as removing sulfide, arsenic, oxygen, carbide that is untreated, thereby in the application of reality, can cause a lot of problems, such as poisoning of catalyst follow-up use;
Perhaps, because ethene not being carried out enrichment handles, the amount that enters gas volume, tail gas (mainly being gas except that ethene and unreacted ethene in the catalytic cracked dry gas) amount of reactive system and the reactant of taking out of with tail gas (benzene, toluene etc.), solvent is all than higher, and operation energy consumption is higher relatively.And owing to need to use special catalyzer and corresponding process matched therewith, equipment cost and early investment are higher, and this makes the application of catalytic cracked dry gas and coking dry gas be restricted.
Summary of the invention
Goal of the invention of the present invention is intended to overcome above-mentioned prior art shortcoming, to dry gas by desulfurization, decarburization, dearsenification, deoxidation, go out the absorption of high-boiling-point impurity and transformation, obtain a kind of C of being rich in 2And C 2The gas mixture of above hydro carbons, this gas mixture can directly enter the ethylene catalyst cracking unit and be used.
The C that is rich in of the present invention 2And C 2The gas mixture of above hydro carbons mainly comprises following component (V%):
Ethene 7.0~70
Ethane 20~70
Propane 1.0~30
Propylene 1.0~30
i-C 4 0.2~3
n-C 4 0.1~10
i-C 4 0.1~10
n-C 4 0.1~10
f-C 4 0.1~10
C 5 0.5~10
Hydrogen≤0.2
Oxygen≤1ppm
Nitrogen≤2.0
Methane≤15
~carbonoxide≤0.3
Carbonic acid gas≤1ppm
As≤ 5ppb
Sulfide≤0.1ppm
Moisture≤1ppm
The preparation method of this gas mixture is made up of following steps:
Remove high-boiling-point impurity
From the catalytic cracked dry gas and the coking dry gas of heavy oil catalytically cracking equipment or coker, composition sees Table 1, removes high-boiling-point impurity through cooling driers.
Transformation adsorbing and removing hydrogen, methane, oxygen, nitrogen, carbon monoxide
Gas after cooling driers removes high-boiling-point impurity enters pressure-swing absorption apparatus, removes the impurity composition that hydrogen the dry gas, methane, oxygen, nitrogen, carbon monoxide etc. are difficult for adsorbing at sorbent material from absorption waste gas and discharges system as other purposes.From contrary put with draws air obtain to be rich in ethene, ethane and C 3The product gas of above hydrocarbon component is in order to increase ethene, ethane and C in the product gas 3The concentration of above hydrocarbon component, the contrary of backflow 10%~80% put and draws air pressurization rear substitution adsorption bed.In order to increase the rate of recovery of product gas simultaneously, can increase by 1 stage pressure swing adsorption apparatus the product component in the displacement waste gas is reclaimed.
The wet desulphurization decarburization
The half product gas that transformation absorption obtains enters wet desulphurization decarburization unit after by compressor pressurizes and removes sour gas such as hydrogen sulfide in the half product gas, carbonic acid gas, usually the wet desulphurization decarburization is that MDEA (methyldiethanolamine) amine absorbs, and MEA (Mono Methyl Ethanol Amine) amine absorbs and the PDS desulfurization.Gas after the wet desulphurization decarburization enters water wash column, remove and enter essence behind the liquid impurity of carrying secretly in the gas and take off the amine device, utilize smart gac or the sorbent materials such as coke or activated alumina that take off the filling in the amine device to remove the impurity such as water smoke that after washing, remain in the product gas.
Dearsenification
Product gas after purifying enters and is filled with the dearsenicator that contains cupric oxide, and the cupric oxide reaction in dearsenicator in hydrogen arsenide and the dearsenic agent generates copper arsenide.( ), arsenic content is less than 5ppb in the later half product gas of process dearsenicator.
Smart desulfurization
The half product gas that comes out through dearsenicator enters and is filled with ferric oxide and is the smart thionizer of the desulfurizing agent of carrier with the gac, and sulfide (comprising hydrogen sulfide and organosulfur compound) in the half product gas is removed to less than 0.1ppm.
Deoxidation
Half product gas after the desulfurization enters deoxidation reactor, and in deoxidation reactor, on the dehydrogenation catalyst that is loaded with palladium, platinum or palladium and platinum, thereby hydrogen in the half product gas and oxygen water generation reaction make oxygen in the half product gas less than 1ppm.
Decarbonation
Half product gas after the deoxidation removes carbonic acid gas through the alkali absorption tower.The reaction of carbonic acid gas and sodium hydroxide generates sodium bicarbonate and yellow soda ash and makes in the half product gas carbon dioxide content less than 1ppm in the alkali absorption tower.
Wherein the reaction of Fa Shenging is:
Dry
The half product gas that comes out in the alkali absorption tower enters water wash column and removes the alkali lye of carrying secretly in the gas.Dealkalize tower through being filled with sorbent materials such as gac or coke or activated alumina removes impurity such as remaining in water smoke in the product gas after washing and enters the alternating temperature adsorption unit that is filled with siccative and removes water in the half product gas again, makes water-content in the half product gas less than 1ppm.Siccative is at least a in activated alumina, silica gel, gac, the molecular sieve.
Drying obtains the product gas that composition as shown in table 1 is formed.
I-C in the table 4, n-C 4, i-C 4 =, n-C 4 =, f-C 4 =Represent Trimethylmethane, normal butane, iso-butylene, n-butene, anti-butylene respectively, down together.
Table 1 coking dry gas and product pneumatolytic are grouped into (volume percent)
Air-flow The coking dry gas Product gas
Form H 2 5.0%~30% ≤0.2%
O 2 0.05%~5% ≤1ppm
N 2 3.0%~25% ≤2.0%
CH 4 20%~55% ≤15%
CO 0.1%~5% ≤0.3%
CO 2 0.1%~5% ≤1ppm
C 2H 4 3.0%~15% 7.0%~76%
C 2H 6 8.0%~20% 20%~89%
C 3H 8 0.5%~10% 1.0%~70%
C 3H 6 0.5%~10% 1.0%~70%
i-C 4 0.1%~1.0% 0.2%~3%
n-C 4 0.01%~1.0% 0.1%~70%
i-C 4 0.01%~1.0% 0.1%~70%
n-C 4 0.01%~1.0% 0.1%~70%
f-C 4 0.01%~1.0% 0.1%~70%
C 5 0.1%~5% 0.5%~70%
Above-mentioned alternating temperature adsorption dry unit is made up of at least 2 at least a adsorption tower and well heaters that are filled with in activated alumina, silica gel, gac, the molecular sieve.One of them tower is in adsorption step, and in adsorption step, half product gas enters drying tower, and the siccative that loads in the drying tower adsorbs the water in the half product gas, removes the product gas that half product gas output drying tower behind the water becomes this device.Meanwhile another adsorption tower is in the thermal regeneration step, if adsorptive pressure and thermal regeneration step pressure differ to, before entering regeneration step and after step-down and pressurising step can be arranged, if regeneration gas is different from product gas to guarantee that purity of product gas also can return product gas drying tower is replaced behind thermal regeneration.In the thermal regeneration step, be heated to 100 ℃~400 ℃ exit end less than hydrogen, nitrogen or other gas heater vias of 1ppm and enter the drying tower that is in the thermal regeneration step with returning part product gas or water-content after drying from drying tower product gas, the water that is adsorbed under higher temperature in the siccative desorbs from siccative with the inlet end outflow drying tower of resurgent gases from drying tower half product gas, can increase the cold blowing step to reduce the temperature of regeneration after drying tower and siccative when regeneration temperature is higher.The cold blowing gas of cold blowing step be returning part after drying product gas or water-content less than hydrogen, nitrogen or other gas of 1ppm.
The present invention adopts a series of processing such as transformation absorption, wet desulphurization decarburization, dehydrogenation deoxidation, aluminum oxide and molecular sieve drying, obtains a kind of C of being rich in 2The gas mixture of above hydro carbons, not only hydro carbons has been carried out enrichment, and sulfide, arsenic, oxygen, carbon monoxide, carbonic acid gas, moisture equal size are all very low in the prepared gas mixture, can not cause its poisoning to employed a lot of catalyzer in the petroleum chemical industry.
This gas mixture can directly enter the ethylene catalyst cracking unit and be used, and produces great economic benefit.
This gas mixture can further be isolated ethene and be used for derived product such as synthesizing styrene, ethylene dichloride, oxyethane, and other part can be used as the raw material of cracking of ethylene, thereby the hydro carbons in catalytic cracked dry gas and the coking dry gas is recycled fully.
Any prior art, the gas mixture after all dry gas not being reclaimed was made concrete sign, and distinguishing feature of the present invention is to have characterized this gas mixture first.
Description of drawings
Fig. 1 is a dry gas concentrating ethylene schematic flow sheet;
Fig. 2 is a pressure-swing absorption apparatus process flow diagram in the embodiment of the invention 1;
Fig. 3 is a pressure-swing absorption apparatus process flow diagram in the embodiment of the invention 2;
Fig. 4 is a pressure-swing absorption apparatus process flow diagram in the embodiment of the invention 3;
Fig. 5 is the device schematic flow sheet of drying process in the embodiment of the invention 3.
Embodiment
Embodiment 1
Present embodiment is for to reclaim C from the refinery catalytic cracked dry gas 2And C 2The method of above hydrocarbon component, catalytic cracked dry gas treatment capacity 5000Nm 3/ h, pressure 0.55MPa, 40 ℃ of temperature, its gaseous constituent is formed as shown in table 2:
Table 2 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, Trimethylmethane, iso-butylene, 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 process concentrating and separating catalytic cracked dry gas in the present embodiment 2And C 2Above hydrocarbon component, the C of pressure swing adsorption process concentrating and separating 2And C 2Above hydrocarbon component and then absorb the decarbonation unit, dehydrate the unit through PDS wet desulphurization unit, smart desulfurization unit, dearsenification and chemical reaction deacidification unit, alkali successively.
Psa unit by 6 adsorption towers that respectively are filled with the CNA-716 type sorbent material 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 mixing tanks, 1 20 cubic metres of displacement gas surge tank, 1 displacement gas compressor, 1 half product air compressor, 2 vacuum pumps and corresponding pipeline and sequencing valve be formed by connecting.Each working cycle 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 3:
Table 3 PSA work schedule table
Cycle 1 2 3 4 5 6 7 8 9 10 11 12
Time (S) 300 300 30 270 600 30 270
Pressure (MPa) 0.55 0.55 0.22 0.02 -0.08 0.22 0.54
Adsorption tower A A RP ED D V ER FR
B ER FR A RP ED D V
C V ER FR A RP ED D V
D V ER FR A RP ED D
E ED D V ER FR A RP
F RP ED D V ER FR A
During the pressure swing adsorption system operation, by the switch of computer by certain each sequencing valve of time variable 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 from the catalytic cracked dry gas of catalytic cracking unit through valve KV1A, at bed internal adsorption agent absorption C 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 mixing tank 5, displacement gas compressor 10, displacement gas surge tank 6, the adsorption 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 adsorption 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 mixing 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 adsorption bed after 81 pairs of contrary putting of vacuum pump, the gas that vacuum 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 water 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 catalyzer from the upper end spray of adsorption tower, the absorbent solution that contains yellow soda ash 8%, 10 tons/hour of solution spraying amounts.Hydrogen sulfide in the gas is absorbed solution absorption, obtains the gas of hydrogen sulfide less than 5ppm from the upper end pneumatic outlet 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 thionizer of the desulfurizing agent of carrier with the gac, and the sulfide in the half product gas is removed to below the 0.1ppm.Product gas heater via after the desulfurization is heated to 80 ℃, enters the dearsenicator that is filled with 10 cubic metres of dearsenic agents again, and the arsenide in the half product gas is removed to below the 5ppb.Half product gas heater via after the dearsenification 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 carbonic acid gas in the sodium hydroxide absorbing and removing half product gas in the alkali absorption tower is to 1ppm.This half product gas enters the dealkalize tower that is filled with 10 cubic metres of acticarbons again behind water separator separating liquid impurity, separate and remove minor amount of water and alkaline solution impurity.The most later half product gas enters the moisture eliminator that respectively is filled with the CNA-421 type siccative of 7 cubic metres of Sichuan Tianyi Science ﹠ Technology Co., Ltd's production and sales by two successively, and the alternating temperature adsorption dry unit Jiang Shui of a series of sequencing valve and pipeline formation 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, and component is as shown in table 4, can be used for producing ethylbenzene and process for oxychlorination and produces ethylene dichloride and vinylchlorid.
The product pneumatolytic is grouped into (V/V) behind the table 4 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 H 2O As
Content % 0.01 ≤ 1ppm 1.0 8.63 0.19 ≤ 1ppm 38.3 26.8 12.4 2.68 2.68 2.97 ≤ 0.1p pm ≤ 1ppm ≤ 5ppb
Embodiment 2
The coking dry gas flow is 12000Nm 3/ h, pressure 0.7Mpa, 30 ℃ of temperature, its component concentration such as table 5 enter and take off liquid unit, water sepn unit, essence by transformation adsorbed gas separating unit, MEA desulfurization decarbonation unit, water washing and take off the coking dry gas isolation of purified that liquid unit, smart desulfurization unit and dearsenification unit hydrogenation deoxidation reactor unit constitute and reclaim C 2And C 2Above hydrocarbon component device.
Table 5 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 0.5 ppm
I-C in the table 4, n-C 4, n-C 4 =Represent Trimethylmethane, normal butane, n-butene respectively.
At first transformation adsorbed gas separating unit 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 sorbent materials 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 mixing tanks, 1 80 cubic metres of displacement gas surge tank, 2 displacement gas compressors, 2 half product air compressors, 6 vacuum pumps and corresponding pipeline and sequencing valve are formed by connecting.Fig. 3 is seen in the technical process of pressure-swing absorption apparatus, and time-scale sees Table 6.
Table 6 PSA work schedule table
Cycle 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16
Time (S) 360 60 60 120 60 120 60 60 60
Pressure (Mpa) 0.7 0.43 0.18 0.18 0 -0.08 0.18 0.43 0.7
Adsorption tower A A E1D E2D RP D V E2R E1R FR
B E1R FR A E1D E2D RP D V E2R
C V E2R E1R FR A E1D E2D RP D V
D D V E2R E1R FR A E1D E2D RP
E RP D V E2R E1R FR A E1D E2D
F E1D E2D RP D V E2R E1R FR A
G A E1D E2D RP D V E2R E1R FR A
H A E1D E2D RP D V E2R E1R FR A
During the pressure swing adsorption system operation, by the switch of computer by certain each sequencing valve of time variable 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 from the coking dry gas of coker through valve KV1A, at bed internal adsorption agent absorption C 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 mixing tank 5, displacement gas compressor unit 10, displacement gas surge tank 6, the adsorption 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 adsorption 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 mixing 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 adsorption bed after 8 pairs of contrary putting of vacuum pump group, the gas that vacuum 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 water 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, carbonic acid gas be by the MEA solution absorption, obtains the gas of hydrogen sulfide less than 5ppm from the upper end pneumatic outlet 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 work in-process gas at the upper end of water wash column pneumatic outlet.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 water separator separating liquid impurity, separate and remove minor amount of water and MEA solution impurity.The half product gas that obtains enters from the lower end and is filled with 10 cubic metres is the smart thionizer of the desulfurizing agent of carrier with the gac, sulfide in the half product gas is removed to below the 0.1ppm, half product gas heater via after the desulfurization is heated to 50 ℃, enter the dearsenicator that is filled with 20 cubic metres of dearsenic agents again, the arsenide in the half product gas is removed to below the 5ppb.Half product gas heater via after the dearsenification 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, the gas after the deoxidation, and the carbonic acid gas in the sodium hydroxide absorbing and removing half product gas in the alkali absorption tower is to 1ppm.The gas that removes behind the carbonic acid gas 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 3 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 work in-process gas through water washing from the upper end pneumatic outlet of water wash column.This half product gas enters the dealkalize tower that is filled with 8 cubic metres of acticarbons again behind water separator separating liquid impurity, separate and remove minor amount of water and alkaline solution impurity.The most later half product gas enters the moisture eliminator that respectively is filled with the CNA-421 type siccative of 10 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 siccative of 10 cubic metres of Sichuan Tianyi Science ﹠ Technology Co., Ltd's production and sales are removed to below the 1ppm.Purify the product gas that gas after the dehydration is used as this device, become to be grouped into as shown in table 7, this product gas can be transported to that the ethene low temperature separation unit is used to reclaim ethene, propylene and as hydrocarbon components such as the ethane of pyrolyzer raw material, propane.
The product pneumatolytic is grouped into (V/V) behind the table 7 coking dry gas isolation of purified
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 l-C 4 CO 2 Total S H 2O As
Content % 0.02 ≤ 1ppm 0.07 5.76 7.39 46.76 23.69 12.39 1.45 1.26 1.21 ≤ 1ppm ≤ 0.1ppm ≤ 1ppm ≤ 5ppb
Embodiment 3
Refinery catalytic cracked dry gas flow 25000Nm 3/ h, pressure 0.60MPa, 30 ℃ of its gaseous constituents of temperature are formed as shown in table 8:
Table 8 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 separation purifier takes off liquid unit, water sepn unit, essence by psa unit, MDEA desulfurization decarbonation unit, water washing and takes off liquid unit, smart desulfurization unit, dearsenification unit, hydrogenation deoxidation reactor unit, alkali cleaning decarbonation unit, water washing dealkalize unit, water sepn unit, dealkalize unit, alternating temperature adsorption dry unit and keen-witted and capable dry unit and constitute.
The present embodiment psa unit is as shown in Figure 4 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 sorbent materials of CNA-716 type, 1 contraryly put jar, 1 half product gas mixing tank, 1 displacement off-gas buffer tank, 10 vacuum 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 sorbent materials of CNA-716 type, 1 contraryly put jar, 1 half product gas mixing tank, 4 vacuum pumps and corresponding pipeline and sequencing valve be formed by connecting.This two-stage pressure swing adsorption apparatus is shared 1 half product gas mixing 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 run sequential sees Table 9:
Table 9 PSA-1 work schedule table
Cycle 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20
Time (S) 300 200 50 50 50 200 50 50 50
Adsorption tower A A RP 1D 2D D V 2R 1R FR
B 1R FR A RP 1D 2D D V 2R
C V 2R 1R FR A RP 1D 2D D V
D V 2R 1R FR A RP 1D 2D D
E D V 2R 1R FR A RP 1D 2D
F 1D 2D D V 2R 1R FR A RP
G RP 1D 2D D V 2R 1R FR A RP
H RP 1D 2D D V 2R 1R FR A
I A RP 1D 2D D V 2R 1R FR A
J A RP 1D 2D D V 2R 1R FR A
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), in the agent of bed internal adsorption to C 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 mixing tank 5, displacement gas compressor unit 10, displacement gas surge tank 6, the adsorption bed of finishing adsorption step is replaced, to improve the content of absorption phase component.Impurity that is displaced and portion C 2H 1, 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 pressure equalization, 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 mixing tank 2 and enter half product gas mixing 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 mixing tank 2 and half product gas mixing 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 adsorption bed after 81 pairs of contrary putting of 5 vacuum pump groups, the gas that vacuum pump group 81 is extracted out mixes mutually with contrary venting, enter half product gas mixing tank 2 and half product gas mixing tank 5, 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 unit.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 pressure equalization, 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 sepn process.
Each adsorption column pressure is periodical change with the variation of processing step, and according to the actually operating situation, adsorptive pressure can suitably be adjusted, then other step pressure is corresponding changes.
PSA-2 is in when operation, each tower each working cycle 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 10:
Table 10 PSA-2 work schedule table
Cycle 1 2 3 4 5 6 7 8 9 10 11 12
Time (S) 300 300 30 270 600 30 270
Pressure (MPa) 0.55 0.55 0.22 0.02 -0.08 0.22 0.54
Adsorption tower K A RP ED D V ER FR
L ER FR A RP ED D V
M V ER FR A RP ED D V
N V ER FR A RP ED D
O ED D V ER FR A RP
P RP ED D V ER FR A
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 by displacement off-gas buffer tank 7 through valve KV1K from the displacement waste gas of PSA-1, in bed internal adsorption separation of C 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 mixing tank 5, displacement gas compressor unit 10, displacement gas surge tank 6, the adsorption 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 mixing tank 4 and half product gas mixing 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 mixing tank 4 and half product gas mixing 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 adsorption bed after 91 pairs of contrary putting of 2 vacuum pump groups, the gas that vacuum 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 unit.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 water 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, carbonic acid gas are by the MDEA solution absorption, obtain the gas of hydrogen sulfide from the upper end pneumatic outlet 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 work in-process gas through water washing from the upper end pneumatic outlet 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 water separator separating liquid impurity, separate and remove minor amount of water and MDEA solution impurity.The half product gas that obtains enters from the lower end and is filled with 5 cubic metres of iron oxide fine desulfurizers and 5 cubic metres is the smart thionizer of the desulfurizing agent of carrier with the gac, and the sulfide in the half product gas is removed to below the 0.1ppm.Product gas heater via after the desulfurization is heated to 80 ℃, enters the dearsenicator that is filled with 25 cubic metres of dearsenic agents again, and the arsenide in the half product gas is removed to below the 5ppb.This gas heater via of half product gas after the dearsenification is heated to 200 ℃, enter 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, 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 carbonic acid gas in the sodium hydroxide absorbing and removing half product gas in the alkali absorption tower is to 1ppm.The gas that removes behind the carbonic acid gas 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 work in-process gas through water washing from the upper end pneumatic outlet of water wash column.This half product gas enters the dealkalize tower that is filled with 10 cubic metres of acticarbons again behind water separator separating liquid impurity, separate and remove minor amount of water and alkaline solution impurity.The most later half product gas enters the moisture eliminator that respectively is filled with the CNA-421 type siccative 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 siccative 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 time variable 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 exsiccant 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 resurgent gases well heater from the resurgent gases outside the battery limit (BL) through valve KV5, resurgent gases after the heating enters through valve KV4A adsorbs saturated drying tower A, be attracted to moisture on the sorbent material through heating, discharge the battery limit (BL) with the valve KV3A of resurgent gases self-desiccation tower lower end.When resurgent gases exit end temperature rises to 150 ℃, shut-off valve KV5 and resurgent gases well 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 resurgent gases that heats, and the valve KV3A of cold blowing regeneration off gases self-desiccation tower lower end discharges the battery limit (BL).When resurgent gases exit end 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 11, and the low temperature separation unit that can directly enter ethylene unit reclaims ethene, third rare and cracking stock ethane, the propane etc.
The product pneumatolytic is grouped into (V/V) behind the table 11 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 (3)

1, a kind of C that is rich in 2And C 2The gas mixture of above hydro carbons, it is characterized in that this mixed gas by volume per-cent mainly comprise following component:
Ethene 7.0~70
Ethane 20~70
Propane 1.0~30
Propylene 1.0~30
And,
Hydrogen≤0.2
Oxygen≤1ppm
Nitrogen≤2.0
Methane≤15
Carbon monoxide≤0.3
Carbonic acid gas 1ppm
As≤5ppb
Sulfide≤0.1ppm
Moisture≤1ppm.
2. a kind of C that is rich in according to claim 1 2And C 2The gas mixture of above hydro carbons is characterized in that in this gas mixture that by volume per-cent also contains:
i-C 4 0.2~3
n-C 4 0.1~10
i-C 4= 0.1~10
n-C 4= 0.1~10
f-C 4= 0.1~10。
3. a kind of C that is rich in according to claim 1 and 2 2And C 2The gas mixture of above hydro carbons, it is characterized in that this gas mixture by volume per-cent also contain:
C 5 0.5~10。
CN 200510022376 2005-12-23 2005-12-23 Gas mixture enriched in hydrocarbon compound with two or more carbon atoms Pending CN1789381A (en)

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103450941A (en) * 2012-05-30 2013-12-18 中国石油化工股份有限公司 Method for producing ethylene cracking raw material from coking dry gas
CN103566706A (en) * 2012-08-10 2014-02-12 张天来 System and method for removing oxygen-contained compounds in mixed C4 hydrocarbons
CN109609219A (en) * 2019-01-17 2019-04-12 青岛华世洁环保科技有限公司 A kind of coking method for treating tail gas and device
CN109364691B (en) * 2018-10-17 2021-06-04 四川天采科技有限责任公司 Asymmetric desorption method for simultaneously recovering adsorption phase and non-adsorption phase components by PSA
CN113024344A (en) * 2019-12-25 2021-06-25 惠生工程(中国)有限公司 Resource treatment method for producing ethylbenzene by using alkylation tail gas after preparation of styrene from refinery dry gas

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103450941A (en) * 2012-05-30 2013-12-18 中国石油化工股份有限公司 Method for producing ethylene cracking raw material from coking dry 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
CN103566706A (en) * 2012-08-10 2014-02-12 张天来 System and method for removing oxygen-contained compounds in mixed C4 hydrocarbons
CN109364691B (en) * 2018-10-17 2021-06-04 四川天采科技有限责任公司 Asymmetric desorption method for simultaneously recovering adsorption phase and non-adsorption phase components by PSA
CN109609219A (en) * 2019-01-17 2019-04-12 青岛华世洁环保科技有限公司 A kind of coking method for treating tail gas and device
CN113024344A (en) * 2019-12-25 2021-06-25 惠生工程(中国)有限公司 Resource treatment method for producing ethylbenzene by using alkylation tail gas after preparation of styrene from refinery dry gas

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