US20160346761A1 - Processes for removing contaminants from a dehydrogenation effluent - Google Patents
Processes for removing contaminants from a dehydrogenation effluent Download PDFInfo
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- US20160346761A1 US20160346761A1 US14/727,246 US201514727246A US2016346761A1 US 20160346761 A1 US20160346761 A1 US 20160346761A1 US 201514727246 A US201514727246 A US 201514727246A US 2016346761 A1 US2016346761 A1 US 2016346761A1
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- regenerant
- stream
- effluent
- zone
- gas
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- 238000000034 method Methods 0.000 title claims abstract description 74
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 39
- 239000000356 contaminant Substances 0.000 title claims description 19
- 239000012492 regenerant Substances 0.000 claims abstract description 154
- 239000007789 gas Substances 0.000 claims abstract description 80
- 239000003463 adsorbent Substances 0.000 claims abstract description 61
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 37
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 33
- 238000004140 cleaning Methods 0.000 claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000002594 sorbent Substances 0.000 claims abstract description 18
- 150000001805 chlorine compounds Chemical class 0.000 claims abstract description 5
- 239000003054 catalyst Substances 0.000 claims description 27
- 229930195733 hydrocarbon Natural products 0.000 claims description 23
- 150000002430 hydrocarbons Chemical class 0.000 claims description 23
- 239000004215 Carbon black (E152) Substances 0.000 claims description 17
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 17
- 239000007787 solid Substances 0.000 claims description 15
- 230000001172 regenerating effect Effects 0.000 claims description 11
- 238000001816 cooling Methods 0.000 claims description 9
- 150000001336 alkenes Chemical class 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 6
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 6
- 229910044991 metal oxide Inorganic materials 0.000 claims description 4
- 150000004706 metal oxides Chemical class 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- 230000003197 catalytic effect Effects 0.000 abstract description 8
- 230000008929 regeneration Effects 0.000 description 16
- 238000011069 regeneration method Methods 0.000 description 16
- 239000003518 caustics Substances 0.000 description 14
- 238000001179 sorption measurement Methods 0.000 description 13
- 239000001257 hydrogen Substances 0.000 description 9
- 229910052739 hydrogen Inorganic materials 0.000 description 9
- 238000011027 product recovery Methods 0.000 description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 description 6
- 239000008188 pellet Substances 0.000 description 6
- 239000012876 carrier material Substances 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 229910052717 sulfur Inorganic materials 0.000 description 5
- 239000011593 sulfur Substances 0.000 description 5
- 239000002737 fuel gas Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 3
- 239000012188 paraffin wax Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 150000004763 sulfides Chemical class 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N Propene Chemical compound CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 150000004679 hydroxides Chemical class 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 150000003464 sulfur compounds Chemical class 0.000 description 2
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 1
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 238000010923 batch production Methods 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000002939 deleterious effect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- VDQVEACBQKUUSU-UHFFFAOYSA-M disodium;sulfanide Chemical compound [Na+].[Na+].[SH-] VDQVEACBQKUUSU-UHFFFAOYSA-M 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hcl hcl Chemical compound Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000003100 immobilizing effect Effects 0.000 description 1
- 229910052809 inorganic oxide Inorganic materials 0.000 description 1
- 229910052741 iridium Inorganic materials 0.000 description 1
- GKOZUEZYRPOHIO-UHFFFAOYSA-N iridium atom Chemical compound [Ir] GKOZUEZYRPOHIO-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052976 metal sulfide Inorganic materials 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- IHYNKGRWCDKNEG-UHFFFAOYSA-N n-(4-bromophenyl)-2,6-dihydroxybenzamide Chemical compound OC1=CC=CC(O)=C1C(=O)NC1=CC=C(Br)C=C1 IHYNKGRWCDKNEG-UHFFFAOYSA-N 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 230000001151 other effect Effects 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- -1 propane to propene Chemical class 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 239000010948 rhodium Substances 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- HYHCSLBZRBJJCH-UHFFFAOYSA-M sodium hydrosulfide Chemical compound [Na+].[SH-] HYHCSLBZRBJJCH-UHFFFAOYSA-M 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/345—Regenerating or reactivating using a particular desorbing compound or mixture
- B01J20/3458—Regenerating or reactivating using a particular desorbing compound or mixture in the gas phase
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- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
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- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
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- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0462—Temperature swing adsorption
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- B01J20/34—Regenerating or reactivating
- B01J20/3433—Regenerating or reactivating of sorbents or filter aids other than those covered by B01J20/3408 - B01J20/3425
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
- C07C5/333—Catalytic processes
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24F—AIR-CONDITIONING; AIR-HUMIDIFICATION; VENTILATION; USE OF AIR CURRENTS FOR SCREENING
- F24F3/00—Air-conditioning systems in which conditioned primary air is supplied from one or more central stations to distributing units in the rooms or spaces where it may receive secondary treatment; Apparatus specially designed for such systems
- F24F3/12—Air-conditioning systems in which conditioned primary air is supplied from one or more central stations to distributing units in the rooms or spaces where it may receive secondary treatment; Apparatus specially designed for such systems characterised by the treatment of the air otherwise than by heating and cooling
- F24F3/14—Air-conditioning systems in which conditioned primary air is supplied from one or more central stations to distributing units in the rooms or spaces where it may receive secondary treatment; Apparatus specially designed for such systems characterised by the treatment of the air otherwise than by heating and cooling by humidification; by dehumidification
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- B01D2253/10—Inorganic adsorbents
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- B01D2253/1124—Metal oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D2257/308—Carbonoxysulfide COS
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40043—Purging
- B01D2259/4005—Nature of purge gas
- B01D2259/40056—Gases other than recycled product or process gas
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- B01D2259/40086—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by using a purge gas
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- B01D2259/402—Further details for adsorption processes and devices using two beds
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
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Definitions
- This invention relates generally to processes for removing contaminants from a dehydrogenation effluent, and more particularly to processes for removing sulfur compounds from same, and even more particularly to processes for treating a regenerant gas used with an adsorbent used to remove sulfur compounds.
- Catalytic dehydrogenation can be used to convert paraffins to the corresponding olefin, e.g., propane to propene, or butane to butene.
- U.S. Pat. No. 5,481,060 discloses an exemplary dehydrogenation process.
- the process includes a reactor section, a catalyst regeneration section, and a product recovery section.
- the product recovery system includes various zones to remove one or more contaminants from an effluent from the reaction section.
- the effluent from the reactor section typically passes through a chloride removal section. After chloride removal, the treated effluent is passed to a reactor effluent dryer system (RED) for drying and further purification, including removal of water and hydrogen sulfide (H 2 S).
- a reactor effluent dryer (RED) system includes two or more adsorbent beds arranged in a typical thermal swing adsorption (TSA) system.
- adsorbent bed(s) in adsorption step starts to breakthrough the contaminants
- the bed(s) on adsorbent mode is switched to regeneration mode and the freshly regenerated bed(s) are placed in adsorption mode.
- the beds are switched between adsorption and regeneration modes to provide for continuous purification of the process stream.
- Regeneration of the adsorbents is accomplished by purging the beds with a regenerant stream such as an inert gas, net gas, or vaporized hydrocarbon stream, at elevated temperature to desorb the impurities and water to rejuvenate or regenerate the adsorbent and prepare it for a fresh adsorption step.
- a regenerant stream such as an inert gas, net gas, or vaporized hydrocarbon stream
- the spent regenerant gas is typically cooled down and passed to a collection drum to remove heavier hydrocarbons (formed in the reactor through side reactions), such as polynuclear aromatics.
- the cooled gas is then passed into a regenerant gas scrubber, and, after being cleaned, depending on the composition of the regenerant gas, the regenerant gas may be used as fuel gas.
- the regenerant gas scrubber typically contains circulating caustic solution (sodium hydroxide (NaOH)) in which the hydrogen sulfide (H 2 S) is converted into sodium sulfide (Na 2 S) and sodium bisulfide (NaHS). Both of these sulfide compounds are toxic and presents environmental problems.
- the caustic solution is considered spent at approximately 70% utilization. The disposal of the spent caustic solution is costly and creates handling problems.
- the caustic solution has to be continuously replaced, the operating costs associated with constantly supplying caustic and disposing of same can be very large.
- KOH solid potassium hydroxide
- regenerant gas in a sulfur recovery unit (SRU) which utilizes the Claus catalytic process which converts hydrogen sulfide to elemental sulfur.
- SRU sulfur recovery unit
- This treatment of the regenerant gas without utilizing caustic is possible for large facilities processing hydrogen sulfide containing waste streams from different units.
- the dehydrogenation units are typically part of a petrochemical complexes which rarely have an SRU.
- the petrochemical complexes typically resort to utilizing caustic.
- One or more processes have been invented in which a solid adsorbent is used to remove sulfide compounds from the spent regenerant gas stream.
- the present invention may be broadly characterized as providing a process for producing a reusable regenerant gas stream by: compressing a reactor effluent from a catalyst dehydrogenation process to provide a compressed effluent; removing chlorides from the compressed effluent in a chloride removal zone to provide a treated effluent; removing water and hydrogen sulfide from the treated effluent in a dryer zone to provide a dryer output stream, the dryer zone having at least one vessel comprising a regenerable adsorbent; regenerating the regenerable adsorbent in the dryer zone with a regenerant gas stream to provide a spent regenerant gas stream, the spent regenerant stream including water and hydrogen sulfide; and, removing the hydrogen sulfide from the spent regenerant gas stream in a regenerant cleaning zone to provide a cleaned regenerant stream, the regenerant cleaning zone including one or more vessels having a sorbent configured to remove hydrogen sulfide from the spent regenerant gas.
- regenerating the regenerable adsorbent further comprises cooling the regenerable adsorbent. It is contemplated that the regenerable adsorbent is cooled with the cleaned regenerant stream.
- the process further includes cooling the cleaned regenerant stream to provide a cooled regenerant stream. It is contemplated that the process also includes removing contaminants from the cooled regenerant stream. It is further contemplated that the contaminants are removed from the regenerant stream by cooling. It is also contemplated that the process includes recycling the cooled regenerant stream to the dryer zone as the regenerant gas stream.
- the regenerant cleaning zone comprises at least two vessels.
- the regenerant cleaning zone comprises two vessels operated in a lead-lag configuration. It is contemplated that at least one vessel is used as a heat exchanger to provide heat or remove heat from a stream of gas including regenerant. It is further contemplated that the heat exchanger cools the cleaned regenerant stream to provide a cooled regenerant stream.
- the present invention may be broadly characterized as providing a process for removing contaminants from a reactor effluent of a catalyst dehydrogenation process by: dehydrogenating a hydrocarbon feed in a dehydrogenation reaction zone under dehydrogenation reaction conditions in the presence of a dehydrogenation catalyst to form a reactor effluent; compressing the reactor effluent to provide a compressed effluent; removing chloride contaminants from the compressed effluent in a chloride removal zone to provide a treated effluent; removing water and hydrogen sulfide from the treated effluent in a dryer zone to provide a dryer output stream including olefins and unconverted paraffins, the dryer zone having at least one vessel comprising a regenerable adsorbent; regenerating the regenerable adsorbent in the dryer zone with a regenerant gas stream to provide a spent regenerant stream, the spent regenerant stream including water and hydrogen sulfide; and, removing the hydrogen
- the process includes separating the dryer output stream in a product separator into a vapor stream and a liquid stream, the liquid stream comprising an olefin product stream.
- the regenerant gas stream comprises a portion of the reactor effluent.
- the dehydrogenation reaction zone comprises a plurality of reactors, and wherein the regenerant gas stream comprises an effluent stream.
- the process further includes compressing the cleaned regenerant gas stream to provide a compressed regenerant gas; and passing the compressed regenerant gas to a water removal vessel to remove water, heavy hydrocarbons, or both from the compressed regenerant gas.
- the process further includes passing the compressed regenerant gas to the product separator. It is further contemplated that the process also includes combining the compressed regenerant gas with the compressed effluent. It is contemplated that the process also includes combining the compressed regenerant gas with the treated effluent.
- the sorbent in the regenerant cleaning zone comprises a solid adsorbent including a metal oxide on a support.
- the regenerant cleaning zone comprises at least two vessels arranged in a lead-lag configuration.
- the present invention maybe broadly characterized as providing a process for cleaning a regenerant stream by: regenerating a regenerable adsorbent with a regenerant gas stream to provide a spent regenerant stream, the spent regenerant stream including water and hydrogen sulfide; removing the hydrogen sulfide from the spent regenerant stream in a regenerant cleaning zone to provide a cleaned regenerant stream, the regenerant cleaning zone including one or more vessels having a solid adsorbent including a metal oxide on a support configured to selectively immobilize hydrogen sulfide; and, regenerating a regenerable adsorbent with at least a portion of the cleaned regenerant stream.
- FIGURE depicts a process flow diagram of an exemplary process according to one or more embodiments of the present invention.
- a solid adsorbent is used to remove sulfide compounds from the spent regenerant gas stream.
- the use of the adsorbent addresses the environmental concerns because some adsorbents can be recycled or at least more easily disposed compared to the caustic solution or solid hydroxide pellets. Additionally, the cost of supplying and disposing of the adsorbent is believed to be considerably less than the same costs associated with the caustic solution or solid hydroxide pellets. Finally, some of the processes provide for the recycling of a cleaned regenerant gas to the dryer section as opposed to being used as a fuel gas.
- the present invention will be described in relation to a catalytic dehydrogenation process, it is believed that the processes of treating a regenerant gas stream are applicable to many additional processes, including other processes for the dehydrogenation.
- the present invention is applicable in any of such processes in which the reaction effluent includes a hydrogen sulfide.
- a typical arrangement for a catalytic dehydrogenation unit 10 is shown.
- the catalytic dehydrogenation unit 10 includes a reactor section 12 , a catalyst regeneration section 14 , and a product recovery section 16 .
- the reactor section 12 may include one or more reactors 18 a , 18 b , 18 c , 18 d .
- four reactors 18 a , 18 b , 18 c , 18 d are included in the reactor section 12 . This is merely a preferred arrangement.
- a hydrocarbon feed 20 including hydrocarbons and hydrogen is initially heated in a heat exchanger 22 via indirect heat exchange with a reactor effluent (discussion below) from the reactor section 12 .
- the hydrocarbon feed 20 normally passes through a preheater 24 to further increase the temperature of the feed components to form a preheated feed 26 before it enters the reactors 18 a , 18 b , 18 c , 18 d where it is contacted with the dehydrogenation catalyst.
- the temperature of a dehydrogenation effluent 28 a from the first reactor 18 a is less than the temperature of the preheated feed 26 . Accordingly, before being passed to a second reactor 18 b , the dehydrogenation effluent 28 a from the first reactor 18 a may be passed to an interstage heater 30 a to raise the temperature to a desired inlet temperature for the second reactor 18 b.
- the second reactor 18 b will produce a second dehydrogenation effluent 28 b which may be passed to an interstage heater 30 b , to raise the temperature to a desired inlet temperature for a third reactor 18 c .
- the third reactor 18 c will provide a third dehydrogenation effluent 28 c which may be passed to an interstage heater 30 c , to raise the temperature to a desired inlet temperature for a fourth reactor 18 d .
- the number of reactors can be different than the depicted embodiment.
- a reactor effluent 28 b comprising a net reactor effluent 28
- the heat exchanger 22 may be passed to the heat exchanger 22 to allow for heat to be exchanged with the hydrocarbon feed 20 (discussed above).
- the net reactor effluent 28 may then be passed to the product recovery section 16 (discussed in more detail below).
- the dehydrogenation reaction is a highly endothermic reaction which is typically effected at low (near atmospheric) pressure conditions.
- the precise dehydrogenation temperature and pressure employed in the dehydrogenation reaction zone will depend on a variety of factors, such as the composition of the paraffinic hydrocarbon feedstock, the activity of the selected catalyst, and the hydrocarbon conversion rate.
- dehydrogenation conditions include a pressure of from about 0 MPa (0 bar) to about 3.5 MPa (35 bars) and a temperature of from about 480° C. (900° F.) to about 760° C. (1400° F.).
- the hydrocarbon feed 20 is typically charged to the reactors 18 a , 18 b , 18 c , 18 d and contacted with the catalyst contained therein at an LHSV of from about 1 to about 10.
- Hydrogen principally recycle hydrogen
- Preferred dehydrogenation conditions include a pressure of from about 0 MPa (0 bar) to about 0.5 MPa (5 bars) and a temperature of from about 540° C. (1000° F.) to about 705° C. (1300° F.), a hydrogen-to-hydrocarbon mole ratio of from about 0.1 to about 2, and an LHSV of less than 4.
- the dehydrogenation reaction may utilize a catalyst 34 which moves through the series of reactors 18 a , 18 b , 18 c , 18 d .
- a spent catalyst 36 may be passed from the last reactor 18 d to the catalyst regeneration section 14 .
- the catalyst regeneration section 14 typically includes a reactor 38 where coke on the spent catalyst 36 is burned off and the catalyst may go through a reconditioning step.
- a regenerated catalyst 40 may be sent back to the first reactor 18 a as the catalyst 34 . Additionally, fresh catalyst may also be added (not shown).
- the dehydrogenation may use any suitable dehydrogenation catalyst.
- preferred suitable catalyst comprises a Group VIII noble metal component (e.g., platinum, iridium, rhodium, and palladium), an alkali metal component, and a porous inorganic carrier material.
- the catalyst may also contain promoter metals which advantageously improve the performance of the catalyst.
- the porous carrier material should be relatively refractory to the conditions utilized in the reactor section 12 and may be chosen from those carrier materials which have traditionally been utilized in dual function hydrocarbon conversion catalysts.
- a preferred porous carrier material is a refractory inorganic oxide, with the most preferred an alumina carrier material.
- the particles are usually spheroidal and have a diameter of from about 1.6 to about 3.2 mm (about 1/16 to about 1 ⁇ 8inch), although they may be as large as about 6.4 mm (about 1 ⁇ 4 inch).
- Operation of the reactor section 12 will produce a mixture of hydrogen and hydrocarbons. Normally, a portion of the hydrocarbons will include an equilibrium mixture of the desired olefin and its alkane precursor.
- the reactor effluent 28 from the reactor section 12 passes to the product recovery section 16 .
- the product recovery section 16 removes hydrogen from the reactor effluent 28 and may recover it in high purity for recycle to the reactor section 12 . Separation steps for the removal of hydrogen will normally include cooling and compressing with subsequent cooling and flashing in a separation vessel. Such methods for the separation of hydrogen and light gases are well known by those skilled in the art.
- the net reactor effluent 28 is compressed in a compressor 42 to provide a compressed effluent 44 .
- the compressed effluent 44 may be introduced directly into a chloride removal zone 46 , as shown, or may be passed through a cooler or heater to adjust the temperature of the compressed effluent 44 , to a temperature that is above the dew point temperature of the compressed effluent stream 44 at the particular process conditions.
- the temperature of the chloride removal zone 46 is between about 75 to 250° C. (about 167 to 482° F.), more preferably between about 75 to 177° C. (about 167 to about 351° F.), and most preferably between about 93 to 157° C. (about 199 to 315° F.).
- chloride chlorinated species
- HCl hydrochloric acid
- RCl organic chlorides
- trace chloride contaminants Such compounds are referred to herein as trace chloride contaminants.
- Example deleterious effects from untreated trace chloride contaminants include corrosion, poisoning of downstream catalysts, and other effects.
- the product recovery section 16 in typical catalytic dehydrogenation unit includes a process for removal of trace chloride contaminants.
- chloride present in the compressed effluent 44 is adsorbed with an adsorbent to provide a treated effluent 48 .
- An exemplary chloride removal zone 46 is discussed in more detail in U.S. Pat. No. 2014/0378725, the entirety of which is incorporated herein by reference.
- the treated effluent 48 may then be passed to a dryer zone 50 .
- the dryer zone 50 may be a reactor effluent dryer system (RED) for drying and purification, including water and hydrogen sulfide (H 2 S) removal.
- An example reactor effluent dryer (RED) system includes two or more adsorbent vessels arranged in a typical thermal swing adsorption (TSA) system. While one or more adsorbent vessels is in adsorption mode to purify and dehydrate the process stream, the other vessel(s) are in regeneration mode. When the adsorbent vessel(s) in the adsorption step starts to break through the contaminants, the vessel(s) on adsorbent mode is switched to regeneration mode and the freshly regenerated vessel (s) are placed in adsorption mode. The vessels are switched between adsorption and regeneration modes to provide for continuous purification of the treated effluent 48 .
- TSA process is well known to those skilled in the art.
- Desorption of the hydrogen sulfide and regeneration of the adsorbents is accomplished by purging the beds with a regenerant gas stream 52 such as an inert gas, net gas, or vaporized hydrocarbon stream, at elevated temperature to desorb the impurities and water to rejuvenate the adsorbent and prepare it for a fresh adsorption step.
- a spent regenerant gas 54 including the impurities removed from the adsorbents, is passed to a regenerant cleaning zone 56 (discussed in more detail below).
- a dryer output stream 58 may be heated in a heat exchanger 60 and then separated in a product separator 62 .
- a gas stream 64 from the product separator 62 may be expanded in expander 66 .
- the vapor stream from the expander 66 may be and separated into a recycle hydrogen stream 68 and a net separator gas stream 70 .
- the recycle hydrogen stream 68 may be combined with the hydrocarbon feed 20 .
- a liquid stream 74 which includes the olefin product and unconverted paraffin, from the product separator 62 may be sent for further processing, where the desired olefin product is recovered and the unconverted paraffin is recycled to the reactor section 12 .
- the regenerant cleaning zone 56 includes one or more vessels 76 a , 76 b each having a sorbent configured to remove hydrogen sulfide from the spent regenerant gas 54 , preferably by immobilizing hydrogen sulfide.
- the spent regenerant gas 54 may be introduced, after exiting the dryer zone 50 , to the regenerant cleaning zone 56 comprising, in an embodiment, two fixed bed vessels 76 a , 76 b operated in lead-lag configuration.
- the vessels 76 a , 76 b serve also as heat exchangers to provide for a regenerant gas stream with a reduced or lower temperature that can be utilized during the regeneration operation of the dryer zone 50 .
- the duration of the regeneration/cooling cycles can be adjusted to keep a certain temperature profile in the regenerant cleaning zone 56 .
- the regenerated adsorbent bed in the vessels 76 a , 76 b may be still cooled down by fresh regenerant 78 which passes into the regenerant cleaning zone 56 through the vessels 76 a , 76 b or by a cleaned regenerant stream 80 that has been cooled.
- the adsorbent is capable of operating at high temperatures similar to these applied to RED regeneration.
- the adsorbent preferably has a high sulfur capacity and, most preferably also a low reactivity and ability to handle the contaminants present in the spent regenerant, mostly hydrogen sulfide (H 2 S) and carbonyl sulfide (COS), to a very low residual concentration.
- the sulfur capacity of the adsorbent at the typical regeneration temperatures of the RED beds may exceeds 200 Kg/m 3 without any detrimental effects on the hydrocarbon feed.
- the sorbent may comprise a zinc oxide (ZnO) containing composite adsorbent, GB-280, available from UOP LLC of Des Plaines, Ill., is an example of the sorbent suitable for this invention.
- ZnO zinc oxide
- the sulfur containing compounds will chemically react with the metal in the adsorbent to form metal sulfide. Additionally, all of the carbonyl sulfide may be fully converted by the metal on the adsorbent.
- the spent sorbent is preferably not hazardous and can be recycled.
- the adsorbents comprises another high capacity metal absorbents, such as manganese or iron.
- the sorbent comprises porous shaped particles with a median particle size of between 0.5-12 mm.
- the contacting of the sorbent and the spent regenerant gas 54 can be carried out in a batch or continuous process.
- the sorbent can be present as a fixed bed, moving bed or radial flow bed and may have a bulk density between 200-2000 kg/m 3 .
- the spent regenerant gas 54 can be flowed in an upflow or downflow direction, with upflow being generally preferred for liquid feeds.
- the spent regenerant gas 54 flow can be either co-current or counter-current.
- Adsorption conditions generally include a temperature of about ambient to about 80° C.
- the temperature may be between 250 to 290° C. (482 to 554° F.).
- the concentration of hydrogen sulfide in the spent regenerant gas 54 may be between 1 to 10,000 ppm, and will most likely vary within that range throughout the process. As will be appreciated these conditions are merely exemplary.
- the sorbent After a certain amount of time, which time depends on the concentration of contaminants, the size of the bed and the space velocity, the sorbent will be substantially spent, i.e. has adsorbed an amount of contaminant(s) such that the level of contaminant in the purified stream is above an acceptable level. At this time, the sorbent is removed and replaced with fresh sorbent. The spent sorbent can be regenerated by means well known in the art and then placed back on service.
- the lead-lag bed configuration of the regenerant cleaning zone 56 is merely a preferred embodiment whereas the lag vessel would have sufficient residual sulfur capacity while the lead vessel may be cooled down and re-charged with fresh adsorbent.
- the removed spent adsorbent may be recycled or otherwise disposed of.
- the cleaned regenerant stream 80 or stream including some fresh regenerant 78 may be passed a hydrocarbon removal zone 82 , for removing of any heavy hydrocarbons.
- a dryer 84 such as a knockout drum or vessel with an adsorbent may be utilized for removal of any water from the cleaned regenerant stream 80 to provide a purified regenerant stream 86 .
- the purified regenerant stream 86 may be passed to in various different configurations. For example, the purified regenerant stream 86 may be compressed and recycled back to the dryer zone 50 to be used as the regenerant gas 52 .
- the regenerant gas 52 may comprise a portion of the reactor effluent 28 , or a portion of the effluent streams 28 a , 28 b , 28 c , 28 d from one of the reactors 18 a , 18 b , 18 c , 18 d .
- the purified regenerant stream 86 may be combined with one of the effluent streams 28 a , 28 b , 28 c , 28 d or passed to product separator 62 , for example by being combined with the dryer output stream 58 .
- the purified regenerant stream 86 may be compressed and combined with the compressed effluent 44 .
- a regenerant gas is cleaned or further purified by cooling.
- spent regenerant gas 54 is cleaned in a cleaning zone 56 .
- the cleaning zone 56 may comprise solid adsorbent configured to selectively adsorb immobilize hydrogen sulfide.
- the cleaned regenerant gas 80 may be is used in a closed or semi-closed loop in which it is recycled and reused to regenerate the regenerable adsorbent. Make-up or fresh regenerant gas may be added as needed throughout the process.
- Various contemplated regenerant gases include nitrogen, saturated hydrocarbons, and natural gas.
- the various processes according to the present invention allow for the use of caustic may be eliminated or minimized.
- the disposable adsorbent addresses the environmental concerns because some adsorbents are easier to dispose of compared to the caustic solution or solid hydroxide pellets. Additionally, the cost of supplying and disposing of the adsorbent is believed to be considerably less than the same costs associated with the caustic solution or solid hydroxide pellets. Finally, some of the processes provide for the recycling of a cleaned regenerant gas to the dryer section as opposed to being used as a fuel gas.
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Abstract
Description
- This invention relates generally to processes for removing contaminants from a dehydrogenation effluent, and more particularly to processes for removing sulfur compounds from same, and even more particularly to processes for treating a regenerant gas used with an adsorbent used to remove sulfur compounds.
- Catalytic dehydrogenation can be used to convert paraffins to the corresponding olefin, e.g., propane to propene, or butane to butene. U.S. Pat. No. 5,481,060 discloses an exemplary dehydrogenation process. In a typical arrangement for a catalytic dehydrogenation, the process includes a reactor section, a catalyst regeneration section, and a product recovery section. The product recovery system includes various zones to remove one or more contaminants from an effluent from the reaction section.
- For example, the effluent from the reactor section typically passes through a chloride removal section. After chloride removal, the treated effluent is passed to a reactor effluent dryer system (RED) for drying and further purification, including removal of water and hydrogen sulfide (H2S). An exemplary reactor effluent dryer (RED) system includes two or more adsorbent beds arranged in a typical thermal swing adsorption (TSA) system.
- As is known, in a TSA, while one or more adsorbent beds is operated in adsorption mode to purify and dehydrate the process stream, the other bed(s) are operated in regeneration mode. When the adsorbent bed(s) in the adsorption step starts to breakthrough the contaminants, the bed(s) on adsorbent mode is switched to regeneration mode and the freshly regenerated bed(s) are placed in adsorption mode. The beds are switched between adsorption and regeneration modes to provide for continuous purification of the process stream. Regeneration of the adsorbents is accomplished by purging the beds with a regenerant stream such as an inert gas, net gas, or vaporized hydrocarbon stream, at elevated temperature to desorb the impurities and water to rejuvenate or regenerate the adsorbent and prepare it for a fresh adsorption step. The TSA process is well known to those skilled in the art.
- After desorbing and/or regenerating the regenerable adsorbed in the RED, the spent regenerant gas is typically cooled down and passed to a collection drum to remove heavier hydrocarbons (formed in the reactor through side reactions), such as polynuclear aromatics. The cooled gas is then passed into a regenerant gas scrubber, and, after being cleaned, depending on the composition of the regenerant gas, the regenerant gas may be used as fuel gas.
- The regenerant gas scrubber typically contains circulating caustic solution (sodium hydroxide (NaOH)) in which the hydrogen sulfide (H2S) is converted into sodium sulfide (Na2S) and sodium bisulfide (NaHS). Both of these sulfide compounds are toxic and presents environmental problems. In addition, the caustic solution is considered spent at approximately 70% utilization. The disposal of the spent caustic solution is costly and creates handling problems. Furthermore, since the caustic solution has to be continuously replaced, the operating costs associated with constantly supplying caustic and disposing of same can be very large. The use of solid potassium hydroxide (KOH) pellets placed in a vessel may not address these problem because of operational difficulties associated with the solid particles, and the continue problems associated with spent material disposal.
- Alternatively, it is known to treat regenerant gas in a sulfur recovery unit (SRU) which utilizes the Claus catalytic process which converts hydrogen sulfide to elemental sulfur. This treatment of the regenerant gas without utilizing caustic is possible for large facilities processing hydrogen sulfide containing waste streams from different units. However, the dehydrogenation units are typically part of a petrochemical complexes which rarely have an SRU. Thus, the petrochemical complexes typically resort to utilizing caustic.
- Therefore, there remains a need for an effective and efficient process for treating a spent regenerant gas that does not utilize a caustic solution or solid hydroxide salt pellets and that does not require an SRU. It would also be desirable to have such a process that allows for the regenerant gas to be recycled instead of being used as fuel gas.
- One or more processes have been invented in which a solid adsorbent is used to remove sulfide compounds from the spent regenerant gas stream.
- In a first aspect of the present invention, the present invention may be broadly characterized as providing a process for producing a reusable regenerant gas stream by: compressing a reactor effluent from a catalyst dehydrogenation process to provide a compressed effluent; removing chlorides from the compressed effluent in a chloride removal zone to provide a treated effluent; removing water and hydrogen sulfide from the treated effluent in a dryer zone to provide a dryer output stream, the dryer zone having at least one vessel comprising a regenerable adsorbent; regenerating the regenerable adsorbent in the dryer zone with a regenerant gas stream to provide a spent regenerant gas stream, the spent regenerant stream including water and hydrogen sulfide; and, removing the hydrogen sulfide from the spent regenerant gas stream in a regenerant cleaning zone to provide a cleaned regenerant stream, the regenerant cleaning zone including one or more vessels having a sorbent configured to remove hydrogen sulfide from the spent regenerant gas.
- In various embodiments of the present invention, regenerating the regenerable adsorbent further comprises cooling the regenerable adsorbent. It is contemplated that the regenerable adsorbent is cooled with the cleaned regenerant stream.
- In some embodiments of the present invention, the process further includes cooling the cleaned regenerant stream to provide a cooled regenerant stream. It is contemplated that the process also includes removing contaminants from the cooled regenerant stream. It is further contemplated that the contaminants are removed from the regenerant stream by cooling. It is also contemplated that the process includes recycling the cooled regenerant stream to the dryer zone as the regenerant gas stream.
- In at least one embodiment of the present invention, the regenerant cleaning zone comprises at least two vessels.
- In one or more embodiments of the present invention, the regenerant cleaning zone comprises two vessels operated in a lead-lag configuration. It is contemplated that at least one vessel is used as a heat exchanger to provide heat or remove heat from a stream of gas including regenerant. It is further contemplated that the heat exchanger cools the cleaned regenerant stream to provide a cooled regenerant stream.
- In a second aspect of the present invention, the present invention may be broadly characterized as providing a process for removing contaminants from a reactor effluent of a catalyst dehydrogenation process by: dehydrogenating a hydrocarbon feed in a dehydrogenation reaction zone under dehydrogenation reaction conditions in the presence of a dehydrogenation catalyst to form a reactor effluent; compressing the reactor effluent to provide a compressed effluent; removing chloride contaminants from the compressed effluent in a chloride removal zone to provide a treated effluent; removing water and hydrogen sulfide from the treated effluent in a dryer zone to provide a dryer output stream including olefins and unconverted paraffins, the dryer zone having at least one vessel comprising a regenerable adsorbent; regenerating the regenerable adsorbent in the dryer zone with a regenerant gas stream to provide a spent regenerant stream, the spent regenerant stream including water and hydrogen sulfide; and, removing the hydrogen sulfide from the spent regenerant stream in a regenerant cleaning zone to provide a cleaned regenerant stream, the regenerant cleaning zone including one or more vessels having a sorbent configured to remove hydrogen sulfide from the spent regenerant gas.
- In various embodiments of the present invention, the process includes separating the dryer output stream in a product separator into a vapor stream and a liquid stream, the liquid stream comprising an olefin product stream. It is contemplated that the regenerant gas stream comprises a portion of the reactor effluent. It is also contemplated that the dehydrogenation reaction zone comprises a plurality of reactors, and wherein the regenerant gas stream comprises an effluent stream. It is contemplated that the process further includes compressing the cleaned regenerant gas stream to provide a compressed regenerant gas; and passing the compressed regenerant gas to a water removal vessel to remove water, heavy hydrocarbons, or both from the compressed regenerant gas. It is also contemplated that the process further includes passing the compressed regenerant gas to the product separator. It is further contemplated that the process also includes combining the compressed regenerant gas with the compressed effluent. It is contemplated that the process also includes combining the compressed regenerant gas with the treated effluent.
- In some embodiments of the present invention, the sorbent in the regenerant cleaning zone comprises a solid adsorbent including a metal oxide on a support.
- In one or more embodiments of the present invention, the regenerant cleaning zone comprises at least two vessels arranged in a lead-lag configuration.
- In a third aspect of the present invention, the present invention maybe broadly characterized as providing a process for cleaning a regenerant stream by: regenerating a regenerable adsorbent with a regenerant gas stream to provide a spent regenerant stream, the spent regenerant stream including water and hydrogen sulfide; removing the hydrogen sulfide from the spent regenerant stream in a regenerant cleaning zone to provide a cleaned regenerant stream, the regenerant cleaning zone including one or more vessels having a solid adsorbent including a metal oxide on a support configured to selectively immobilize hydrogen sulfide; and, regenerating a regenerable adsorbent with at least a portion of the cleaned regenerant stream.
- Additional aspects, embodiments, and details of the invention, all of which may be combinable in any manner, are set forth in the following detailed description of the invention.
- One or more exemplary embodiments of the present invention will be described below in conjunction with the following drawing FIGURE, in which:
- The FIGURE depicts a process flow diagram of an exemplary process according to one or more embodiments of the present invention.
- As mentioned above, various processes have been invented in which a solid adsorbent is used to remove sulfide compounds from the spent regenerant gas stream. The use of the adsorbent addresses the environmental concerns because some adsorbents can be recycled or at least more easily disposed compared to the caustic solution or solid hydroxide pellets. Additionally, the cost of supplying and disposing of the adsorbent is believed to be considerably less than the same costs associated with the caustic solution or solid hydroxide pellets. Finally, some of the processes provide for the recycling of a cleaned regenerant gas to the dryer section as opposed to being used as a fuel gas.
- With these general principles in mind, one or more embodiments of the present invention will be described with the understanding that the following description is not intended to be limiting.
- While the present invention will be described in relation to a catalytic dehydrogenation process, it is believed that the processes of treating a regenerant gas stream are applicable to many additional processes, including other processes for the dehydrogenation. The present invention is applicable in any of such processes in which the reaction effluent includes a hydrogen sulfide. As shown in the FIGURE, a typical arrangement for a
catalytic dehydrogenation unit 10 is shown. Thecatalytic dehydrogenation unit 10 includes areactor section 12, acatalyst regeneration section 14, and aproduct recovery section 16. Thereactor section 12 may include one ormore reactors reactors reactor section 12. This is merely a preferred arrangement. - In an exemplary embodiment, a
hydrocarbon feed 20 including hydrocarbons and hydrogen is initially heated in aheat exchanger 22 via indirect heat exchange with a reactor effluent (discussion below) from thereactor section 12. Following heating, thehydrocarbon feed 20 normally passes through apreheater 24 to further increase the temperature of the feed components to form apreheated feed 26 before it enters thereactors - Since the dehydrogenation reaction is endothermic, the temperature of a
dehydrogenation effluent 28 afrom thefirst reactor 18 a is less than the temperature of thepreheated feed 26. Accordingly, before being passed to asecond reactor 18 b, thedehydrogenation effluent 28 a from thefirst reactor 18 a may be passed to aninterstage heater 30 a to raise the temperature to a desired inlet temperature for thesecond reactor 18 b. - Similarly, the
second reactor 18 b will produce asecond dehydrogenation effluent 28 b which may be passed to aninterstage heater 30 b, to raise the temperature to a desired inlet temperature for athird reactor 18 c. Likewise, thethird reactor 18 c will provide athird dehydrogenation effluent 28 c which may be passed to aninterstage heater 30 c, to raise the temperature to a desired inlet temperature for afourth reactor 18 d. As will be appreciated, the number of reactors can be different than the depicted embodiment. After the last reactor (in this example, thefourth reactor 18 d), areactor effluent 28 b, comprising anet reactor effluent 28, may be passed to theheat exchanger 22 to allow for heat to be exchanged with the hydrocarbon feed 20 (discussed above). Thenet reactor effluent 28 may then be passed to the product recovery section 16 (discussed in more detail below). - The dehydrogenation reaction is a highly endothermic reaction which is typically effected at low (near atmospheric) pressure conditions. The precise dehydrogenation temperature and pressure employed in the dehydrogenation reaction zone will depend on a variety of factors, such as the composition of the paraffinic hydrocarbon feedstock, the activity of the selected catalyst, and the hydrocarbon conversion rate. In general, dehydrogenation conditions include a pressure of from about 0 MPa (0 bar) to about 3.5 MPa (35 bars) and a temperature of from about 480° C. (900° F.) to about 760° C. (1400° F.).
- The
hydrocarbon feed 20 is typically charged to thereactors - The dehydrogenation reaction may utilize a
catalyst 34 which moves through the series ofreactors catalyst 36 may be passed from thelast reactor 18 d to thecatalyst regeneration section 14. Thecatalyst regeneration section 14 typically includes a reactor 38 where coke on the spentcatalyst 36 is burned off and the catalyst may go through a reconditioning step. A regeneratedcatalyst 40 may be sent back to thefirst reactor 18 a as thecatalyst 34. Additionally, fresh catalyst may also be added (not shown). - The dehydrogenation may use any suitable dehydrogenation catalyst. Generally, preferred suitable catalyst comprises a Group VIII noble metal component (e.g., platinum, iridium, rhodium, and palladium), an alkali metal component, and a porous inorganic carrier material. The catalyst may also contain promoter metals which advantageously improve the performance of the catalyst. The porous carrier material should be relatively refractory to the conditions utilized in the
reactor section 12 and may be chosen from those carrier materials which have traditionally been utilized in dual function hydrocarbon conversion catalysts. A preferred porous carrier material is a refractory inorganic oxide, with the most preferred an alumina carrier material. The particles are usually spheroidal and have a diameter of from about 1.6 to about 3.2 mm (about 1/16 to about ⅛inch), although they may be as large as about 6.4 mm (about ¼ inch). - Operation of the
reactor section 12 will produce a mixture of hydrogen and hydrocarbons. Normally, a portion of the hydrocarbons will include an equilibrium mixture of the desired olefin and its alkane precursor. - The
reactor effluent 28 from thereactor section 12 passes to theproduct recovery section 16. As will be discussed in more detail below, theproduct recovery section 16 removes hydrogen from thereactor effluent 28 and may recover it in high purity for recycle to thereactor section 12. Separation steps for the removal of hydrogen will normally include cooling and compressing with subsequent cooling and flashing in a separation vessel. Such methods for the separation of hydrogen and light gases are well known by those skilled in the art. - In the
product recovery section 16, thenet reactor effluent 28 is compressed in acompressor 42 to provide acompressed effluent 44. The compressedeffluent 44 may be introduced directly into achloride removal zone 46, as shown, or may be passed through a cooler or heater to adjust the temperature of the compressedeffluent 44, to a temperature that is above the dew point temperature of thecompressed effluent stream 44 at the particular process conditions. In an example embodiment, the temperature of thechloride removal zone 46 is between about 75 to 250° C. (about 167 to 482° F.), more preferably between about 75 to 177° C. (about 167 to about 351° F.), and most preferably between about 93 to 157° C. (about 199 to 315° F.). - As will be appreciated by those of ordinary skill in the art, the use of organic chloride used to condition paraffin dehydrogenation catalysts typically results in undesirable chlorinated species (chloride) compounds, such as hydrochloric acid (HCl) and organic chlorides (RCl), in the
net reactor effluent 28. Such compounds are referred to herein as trace chloride contaminants. Example deleterious effects from untreated trace chloride contaminants include corrosion, poisoning of downstream catalysts, and other effects. Accordingly, theproduct recovery section 16 in typical catalytic dehydrogenation unit includes a process for removal of trace chloride contaminants. - In the
chloride removal zone 46, chloride present in the compressedeffluent 44 is adsorbed with an adsorbent to provide a treatedeffluent 48. An exemplarychloride removal zone 46 is discussed in more detail in U.S. Pat. No. 2014/0378725, the entirety of which is incorporated herein by reference. The treatedeffluent 48 may then be passed to adryer zone 50. - The
dryer zone 50 may be a reactor effluent dryer system (RED) for drying and purification, including water and hydrogen sulfide (H2S) removal. An example reactor effluent dryer (RED) system includes two or more adsorbent vessels arranged in a typical thermal swing adsorption (TSA) system. While one or more adsorbent vessels is in adsorption mode to purify and dehydrate the process stream, the other vessel(s) are in regeneration mode. When the adsorbent vessel(s) in the adsorption step starts to break through the contaminants, the vessel(s) on adsorbent mode is switched to regeneration mode and the freshly regenerated vessel (s) are placed in adsorption mode. The vessels are switched between adsorption and regeneration modes to provide for continuous purification of the treatedeffluent 48. The TSA process is well known to those skilled in the art. - Desorption of the hydrogen sulfide and regeneration of the adsorbents is accomplished by purging the beds with a
regenerant gas stream 52 such as an inert gas, net gas, or vaporized hydrocarbon stream, at elevated temperature to desorb the impurities and water to rejuvenate the adsorbent and prepare it for a fresh adsorption step. A spentregenerant gas 54, including the impurities removed from the adsorbents, is passed to a regenerant cleaning zone 56 (discussed in more detail below). - From the
dryer zone 50, adryer output stream 58 may be heated in aheat exchanger 60 and then separated in aproduct separator 62. Agas stream 64 from theproduct separator 62 may be expanded inexpander 66. After exchanging heat in theheat exchanger 60 with thedryer output stream 58, the vapor stream from theexpander 66 may be and separated into arecycle hydrogen stream 68 and a netseparator gas stream 70. Therecycle hydrogen stream 68 may be combined with thehydrocarbon feed 20. - A
liquid stream 74, which includes the olefin product and unconverted paraffin, from theproduct separator 62 may be sent for further processing, where the desired olefin product is recovered and the unconverted paraffin is recycled to thereactor section 12. - Returning to the
dryer zone 50, as discussed above, in contrast to the prior art processes in which a caustic solution, solid hydroxide salt, or an SRU is used to clean the spentregenerant gas 54, in the processes of the present invention, theregenerant cleaning zone 56 includes one ormore vessels regenerant gas 54, preferably by immobilizing hydrogen sulfide. - The spent
regenerant gas 54 may be introduced, after exiting thedryer zone 50, to theregenerant cleaning zone 56 comprising, in an embodiment, two fixedbed vessels vessels dryer zone 50. For example, in regenerant heater operation, the duration of the regeneration/cooling cycles can be adjusted to keep a certain temperature profile in theregenerant cleaning zone 56. The regenerated adsorbent bed in thevessels fresh regenerant 78 which passes into theregenerant cleaning zone 56 through thevessels regenerant stream 80 that has been cooled. - It is desired that the adsorbent is capable of operating at high temperatures similar to these applied to RED regeneration. In addition, the adsorbent preferably has a high sulfur capacity and, most preferably also a low reactivity and ability to handle the contaminants present in the spent regenerant, mostly hydrogen sulfide (H2S) and carbonyl sulfide (COS), to a very low residual concentration. The sulfur capacity of the adsorbent at the typical regeneration temperatures of the RED beds may exceeds 200 Kg/m3 without any detrimental effects on the hydrocarbon feed.
- The sorbent may comprise a zinc oxide (ZnO) containing composite adsorbent, GB-280, available from UOP LLC of Des Plaines, Ill., is an example of the sorbent suitable for this invention. As will be appreciated, the sulfur containing compounds will chemically react with the metal in the adsorbent to form metal sulfide. Additionally, all of the carbonyl sulfide may be fully converted by the metal on the adsorbent. The spent sorbent is preferably not hazardous and can be recycled. It is also contemplated that the adsorbents comprises another high capacity metal absorbents, such as manganese or iron. Preferably, the sorbent comprises porous shaped particles with a median particle size of between 0.5-12 mm.
- The contacting of the sorbent and the spent
regenerant gas 54 can be carried out in a batch or continuous process. The sorbent can be present as a fixed bed, moving bed or radial flow bed and may have a bulk density between 200-2000 kg/m3. When a fixed bed is used, the spentregenerant gas 54 can be flowed in an upflow or downflow direction, with upflow being generally preferred for liquid feeds. If a moving bed is used the spentregenerant gas 54 flow can be either co-current or counter-current. Further, when a fixed bed is used, multiple beds can be used and can be placed in one or more reactor vessel. Adsorption conditions generally include a temperature of about ambient to about 80° C. (176° F.), a pressure of about atmospheric to about 10,132 kPa (1,470 psi) and a contact time in which the gas hourly space velocity varies from about 500 to about 10,000 hr−1. In some embodiments, the temperature may be between 250 to 290° C. (482 to 554° F.). Furthermore, the concentration of hydrogen sulfide in the spentregenerant gas 54 may be between 1 to 10,000 ppm, and will most likely vary within that range throughout the process. As will be appreciated these conditions are merely exemplary. - After a certain amount of time, which time depends on the concentration of contaminants, the size of the bed and the space velocity, the sorbent will be substantially spent, i.e. has adsorbed an amount of contaminant(s) such that the level of contaminant in the purified stream is above an acceptable level. At this time, the sorbent is removed and replaced with fresh sorbent. The spent sorbent can be regenerated by means well known in the art and then placed back on service.
- The lead-lag bed configuration of the
regenerant cleaning zone 56 is merely a preferred embodiment whereas the lag vessel would have sufficient residual sulfur capacity while the lead vessel may be cooled down and re-charged with fresh adsorbent. The removed spent adsorbent may be recycled or otherwise disposed of. - The cleaned
regenerant stream 80 or stream including somefresh regenerant 78, may be passed ahydrocarbon removal zone 82, for removing of any heavy hydrocarbons. Additionally, adryer 84 such as a knockout drum or vessel with an adsorbent may be utilized for removal of any water from the cleanedregenerant stream 80 to provide apurified regenerant stream 86. Thepurified regenerant stream 86 may be passed to in various different configurations. For example, thepurified regenerant stream 86 may be compressed and recycled back to thedryer zone 50 to be used as theregenerant gas 52. In at least one embodiment, theregenerant gas 52 may comprise a portion of thereactor effluent 28, or a portion of the effluent streams 28 a, 28 b, 28 c, 28 d from one of thereactors purified regenerant stream 86 may be combined with one of the effluent streams 28 a, 28 b, 28 c, 28 d or passed toproduct separator 62, for example by being combined with thedryer output stream 58. Alternatively, thepurified regenerant stream 86 may be compressed and combined with the compressedeffluent 44. As will be appreciated, the order of compression and removal of water and other impurities from the cleanedregenerant stream 80 may be changed from the described embodiments. In at least one embodiment, a regenerant gas is cleaned or further purified by cooling. - In other embodiment of the present invention, spent
regenerant gas 54 is cleaned in acleaning zone 56. Thecleaning zone 56 may comprise solid adsorbent configured to selectively adsorb immobilize hydrogen sulfide. The cleanedregenerant gas 80 may be is used in a closed or semi-closed loop in which it is recycled and reused to regenerate the regenerable adsorbent. Make-up or fresh regenerant gas may be added as needed throughout the process. Various contemplated regenerant gases include nitrogen, saturated hydrocarbons, and natural gas. - In sum, by utilizing such a cleaning process for the regenerant gas, the various processes according to the present invention allow for the use of caustic may be eliminated or minimized. As discussed above, the disposable adsorbent addresses the environmental concerns because some adsorbents are easier to dispose of compared to the caustic solution or solid hydroxide pellets. Additionally, the cost of supplying and disposing of the adsorbent is believed to be considerably less than the same costs associated with the caustic solution or solid hydroxide pellets. Finally, some of the processes provide for the recycling of a cleaned regenerant gas to the dryer section as opposed to being used as a fuel gas.
- It should be appreciated and understood by those of ordinary skill in the art that various other components such as valves, pumps, filters, coolers, etc. were not shown in the drawings as it is believed that the specifics of same are well within the knowledge of those of ordinary skill in the art and a description of same is not necessary for practicing or understanding the embodiments of the present invention.
- While at least one exemplary embodiment has been presented in the foregoing detailed description of the invention, it should be appreciated that a vast number of variations exist. It should also be appreciated that the exemplary embodiment or exemplary embodiments are only examples, and are not intended to limit the scope, applicability, or configuration of the invention in any way. Rather, the foregoing detailed description will provide those skilled in the art with a convenient road map for implementing an exemplary embodiment of the invention, it being understood that various changes may be made in the function and arrangement of elements described in an exemplary embodiment without departing from the scope of the invention as set forth in the appended claims and their legal equivalents.
Claims (20)
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CN201680024695.4A CN107530614B (en) | 2015-06-01 | 2016-05-17 | Process for removing contaminants from dehydrogenation effluent |
ES16803971T ES2821978T3 (en) | 2015-06-01 | 2016-05-17 | Procedures for removing contaminants from a dehydrogenation effluent |
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RU2017137443A RU2662538C1 (en) | 2015-06-01 | 2016-05-17 | Methods of removing pollutants from outlet flow of dehydration |
US15/346,619 US9962682B2 (en) | 2015-06-01 | 2016-11-08 | Processes for removing contaminants from a dehydrogenation effluent |
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CN111170821A (en) * | 2019-08-26 | 2020-05-19 | 浙江卫星能源有限公司 | Propane dehydrogenation process involving catalyst regeneration and reactor double-on-line switching |
US20220041529A1 (en) * | 2020-08-04 | 2022-02-10 | Honeywell International Inc. | Propane/butane dehydrogenation complex with thermal oxidation system |
US11931686B1 (en) * | 2022-09-16 | 2024-03-19 | Carbon Capture Inc. | Carbon capture process utilizing inert gas medium to assist thermal desorption |
US12017984B2 (en) * | 2021-06-29 | 2024-06-25 | Honeywell International Inc. | Propane/butane dehydrogenation complex with thermal oxidation system |
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US9517447B1 (en) * | 2015-06-01 | 2016-12-13 | Uop Llc | Processes for removing contaminants from a dehydrogenation effluent |
KR101921190B1 (en) | 2017-01-18 | 2018-11-23 | 효성화학 주식회사 | Dehydrogenation method of alkane |
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CN111170821A (en) * | 2019-08-26 | 2020-05-19 | 浙江卫星能源有限公司 | Propane dehydrogenation process involving catalyst regeneration and reactor double-on-line switching |
WO2021036098A1 (en) * | 2019-08-26 | 2021-03-04 | 浙江卫星能源有限公司 | Propane dehydrogenation process involving catalyst regeneration and reactor double-online switching |
US20220041529A1 (en) * | 2020-08-04 | 2022-02-10 | Honeywell International Inc. | Propane/butane dehydrogenation complex with thermal oxidation system |
US12017984B2 (en) * | 2021-06-29 | 2024-06-25 | Honeywell International Inc. | Propane/butane dehydrogenation complex with thermal oxidation system |
US11931686B1 (en) * | 2022-09-16 | 2024-03-19 | Carbon Capture Inc. | Carbon capture process utilizing inert gas medium to assist thermal desorption |
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