EP2867192A1 - Purification of a raw gas by hydrogenation - Google Patents
Purification of a raw gas by hydrogenationInfo
- Publication number
- EP2867192A1 EP2867192A1 EP13732475.2A EP13732475A EP2867192A1 EP 2867192 A1 EP2867192 A1 EP 2867192A1 EP 13732475 A EP13732475 A EP 13732475A EP 2867192 A1 EP2867192 A1 EP 2867192A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- raw gas
- gas
- hydrogenation
- reactor
- process according
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 32
- 238000000746 purification Methods 0.000 title description 4
- 239000007789 gas Substances 0.000 claims abstract description 108
- 238000000034 method Methods 0.000 claims abstract description 34
- 230000008569 process Effects 0.000 claims abstract description 34
- 239000000463 material Substances 0.000 claims abstract description 25
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 24
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 24
- 239000011593 sulfur Substances 0.000 claims abstract description 24
- 239000012535 impurity Substances 0.000 claims abstract description 19
- 150000001336 alkenes Chemical class 0.000 claims abstract description 11
- 238000004519 manufacturing process Methods 0.000 claims abstract description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 9
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 9
- 239000001301 oxygen Substances 0.000 claims abstract description 9
- 239000003463 adsorbent Substances 0.000 claims abstract description 3
- 239000002826 coolant Substances 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 238000001179 sorption measurement Methods 0.000 claims description 6
- 229910052802 copper Inorganic materials 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 5
- -1 steam Substances 0.000 claims description 4
- 238000009835 boiling Methods 0.000 claims description 3
- 239000011149 active material Substances 0.000 abstract description 4
- 150000001298 alcohols Chemical class 0.000 abstract description 2
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 31
- 229960005349 sulfur Drugs 0.000 description 15
- 235000001508 sulfur Nutrition 0.000 description 15
- 239000003054 catalyst Substances 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 230000015572 biosynthetic process Effects 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 239000000571 coke Substances 0.000 description 4
- 239000010949 copper Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 239000003502 gasoline Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 150000003464 sulfur compounds Chemical class 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 230000004913 activation Effects 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000011143 downstream manufacturing Methods 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical class [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-AKLPVKDBSA-N Sulfur-35 Chemical compound [35S] NINIDFKCEFEMDL-AKLPVKDBSA-N 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002006 petroleum coke Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/02—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/34—Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
Definitions
- the present invention is directed to purification of raw gas.
- the invention concerns removal of sul- fur by adsorption and oxygen and olefins by hydrogenation.
- Industrial raw gases arise typically from gasification of carbonaceous raw materials such as coal, oil petroleum coke, biomass and the like as a reformed hydrocarbon feed or as coke oven gas.
- such a raw gas is obtained by the gasification process or as an off gas from the production of coke, the so called coke oven gas.
- These gases contain hydrogen, which inter alia is a valuable reactant for use as alternative fuel or for use in the preparation of a number of bulk chemicals and of liquid or gaseous fuels.
- gasifier gas and coke oven gas may be em ⁇ ployed in the preparation of substitute natural gas (SNG) .
- a raw gas may also be converted into a liquid fuel, such as gasoline or diesel by the Fischer Tropsch process or by an oxygenate to gasoline process.
- Olefins are undesired because they may result in deactiva ⁇ tion of catalysts by carbon formation which may take place when heating a gas comprising olefins.
- Oxygen is similarly undesired because the presence of oxy ⁇ gen in downstream processes may be detrimental due to local hot-spots and oxidation of reduced catalysts.
- the raw gas may be a mixture of e.g. natural gas comprising sulfur and process tail gases comprising olefins being directed for downstream processing, such as tail gases from processes for synthesis of hydrocarbons by Fischer-Tropsch, methanol-to-gasoline, TIGAS and similar processes.
- olefins and oxygen together may be removed by hydro ⁇ genation over a hydrogenation catalyst, such cL S cL C3.talyst comprising one or more of Cu, Al ad Zn, while sulfur compounds may be adsorbed on said hydrogenation catalyst with ⁇ out influencing the catalytic activity.
- a hydrogenation catalyst such as cL S cL C3.talyst comprising one or more of Cu, Al ad Zn
- a temperature control may be im ⁇ portant, since increased temperatures due to the exothermal hydrogenation reaction may result in activation of exothermal reactions e.g. the exothermal production of CH 3 OH from 3 ⁇ 4 and CO on a catalyst comprising copper, methanation on a catalyst comprising nickel or Fischer Tropsch wax formation on a catalyst comprising iron.
- the latter may result in a further undesired heating of the reactor, in activating the exothermal reaction such as methanol production further, and possibly also in a catalyst deactivation due to sinter ⁇ ing of the catalyst. It may also be a desire to control the output temperature to avoid damage of downstream equipment.
- raw gas shall comprise any gas in which the combined concentration of hydrogen and carbon oxides is at least 60%.
- the present disclosure relates to a pro ⁇ cess for hydrogenation of a raw gas feed, said process com ⁇ prising the steps of a) reacting the raw gas in the presence of a material being catalytically active in hydrogenation of oxygen and/or olefins, and being an adsorbent of 3 ⁇ 4S, and b) withdrawing a heated purified gas wherein said raw gas comprises at least 10 ppb, preferably at least 20 ppb, and most preferably at least 50 ppb of a sulfur impurity such as 3 ⁇ 4S or COS, and at least 0.1%, preferably at least 0.2% and most preferably at least 0.5% by volume of one or more further impurities taken from the group of O2 and C n H2 n , and wherein the temperature of the catalytically active material is sufficiently high to en ⁇ sure that the concentration of the sulfur impurity and said one or more further impurities in said purified gas is less than half the concentration in said raw gas.
- the material used for capture of sulfur compounds may be the hydrogenation catalyst if it comprises a sulfur binding material known to the skilled person, such as compositions comprising ZnO.
- the hydrogenation process is carried out in a reactor cooled by a cooling medium with the associated benefit.
- the cooling medium is the raw gas, steam, water or another heat transfer medium with the associated benefit of being able to transfer heat to other pro- cess stages, such as preheating the raw gas e.g. to at least 60°C while the reactor temperature is maintained at a low level such that undesired exothermal reactions such as formation of methanol from CO and 3 ⁇ 4 are not activated.
- the raw gas further comprises less than 5% 3 ⁇ 40. The presence of water allows the reaction forming 3 ⁇ 4S and CO 2 from COS and 3 ⁇ 40, but an excessive pres ⁇ ence of water may shift the adsorption equilibrium
- the cooling medium is boiling water
- the heated purified gas is withdrawn at a tempera ⁇ ture below 250°C with the associated benefit of the maximum temperature of the heated purified gas being well con- trolled due to the invariability of the boiling point.
- the heated purified gas is with ⁇ drawn at a temperature below 220°C, preferably below 200°C, and even more preferably below 180°C with the associated effects of protecting equipment and catalysts and avoiding activation of undesired reactions.
- the material being catalytically active in hydrogenation comprises at least one active ele ⁇ ment chosen from the group consisting of Cu, Al, and ZnO, with the associated benefit of providing a material having a high hydrogenation activity.
- the sum of the volumetric concen ⁇ tration of CO and 3 ⁇ 4 in said raw gas is at least 60% with the associated benefit of providing a synthesis gas suita ⁇ ble for production of synthethic natural gas or for use as a feed to a Fischer-Tropsh process or for a liquid fuel production such as a TIGAS process or a methanol produc ⁇ tion.
- the process further comprises con ⁇ tacting the raw gas with an additional sulfur capture mate ⁇ rial, which may be arranged outside the heat exchange sec ⁇ tion of the reactor.
- an additional sulfur capture mate ⁇ rial which may be arranged outside the heat exchange sec ⁇ tion of the reactor.
- the raw gas, the cooling medium and the raw gas are configured to flow in co-flow with the as- sociated benefit of an improved control of runaway tempera ⁇ tures which applies especially to varying inlet tempera ⁇ tures or varying compositions.
- the raw gas, the cooling medium and the raw gas are configured to flow in counter flow with the associated benefit of an efficient cooling of the reaction while maintaining a reduced temperature of the catalytical- ly active material, which is especially relevant in case of high concentrations of the compounds to be hydrogenated .
- the raw gas is pre-heated by an ex ⁇ ternal heat source, such as a steam heat exchange, an elec ⁇ trical heating or a heat exchange with a warm process stream prior to hydrogenation with the associated benefit of being able to adjust the raw gas temperature to the op ⁇ timal value.
- an ex ⁇ ternal heat source such as a steam heat exchange, an elec ⁇ trical heating or a heat exchange with a warm process stream prior to hydrogenation with the associated benefit of being able to adjust the raw gas temperature to the op ⁇ timal value.
- the pre-heating may be made upstream or downstream the cooling of the reactor.
- a further aspect of the disclosure relates to a reactor for the production of a purified gas being configured to re ⁇ ceive a raw gas as heat exchange medium providing a heated raw gas, where said raw gas comprises at least 10 ppb, preferably at least 20 ppb, and most preferably at least 50 ppb of a sulfur impurity such as 3 ⁇ 4S or COS, and at least 0.1%, preferably at least 0.2%, and most preferably at least 0.5% by volume of a further impurity taken from the group of O 2 and C n H 2n , where the concentration of sulfur im- purity and said further impurity in said purified gas is less than half the concentration in said raw gas, and where said reactor is further configured to direct said heated raw gas to a material being catalytically active in the hydrogenation of olefins, oxygen or both, and having an adsorption capacity for sulfur, characterized in that said reactor is configured for the material being catalytically active to be in thermal contact with a cooling medium, such as steam, water or
- the reactor may be configured for the raw gas to contact the material being catalytically ac ⁇ tive in hydrogenation inside tubes with the cooling medium flowing on the outer side of the tubes. In a further embodiment the reactor may be configured for the raw gas to contact the material being catalytically ac ⁇ tive in hydrogenation on the outside of tubes with the cooling medium flowing on the inside of the tubes. In a further embodiment the reactor further comprises one or more zones of sulfur capture material.
- Fig. 1 illustrates a process according to a first embodi ⁇ ment of the disclosure
- Fig. 2 illustrates a process according to a second embodi- ment of the disclosure.
- Fig. 1 shows a specific embodiment of the disclosure, in which a raw gas 10 is fed as a heat exchange medium to a gas cooled reactor 15 and withdrawn as a first heated raw gas 20.
- the temperature of the heated raw gas may be fur- ther adjusted in an optional heat exchanger 25 providing a heated feed gas 30, having a temperature in the range 70- 170°C.
- the heated feed gas 30 is then directed to contact an optional first sulfur capture material comprising ZnO and being active in adsorption or chemisorption of sulfur 35, then further to contact a catalytic material, such as
- Cu, Al, or ZnO being active in hydrogenation 40, and finally to contact an optional second sulfur capture material comprising ZnO and being active in adsorption or chemisorption of sulfur 45, providing a heated purified gas 50.
- Fig. 2 shows a further embodiment of the disclosure in which the reactor is cooled by a steam medium.
- Water 60 is fed to a steam drum 65, from which water 70 is directed to the cooled reactor 40, in which the water is heated to steam 75, which is collected in the steam drum 65 from which it may be distributed in a steam line 80.
- a feed composition comprising 0.31% ox ⁇ ygen was hydrogenated .
- the feed gas of the first example was evaluated according to the prior art with hydrogenation in an adiabatic reactor.
- the product gas comprised 1.20% methanol, and the temperature out of the reactor was raised to 230°C.
- the feed gas of the first example was also evaluated ac ⁇ cording to the present disclosure with hydrogenation in a gas cooled reactor.
- the product gas comprised no methanol, and the temperature was due to the gas cooling maintained at 160°C.
- the feed gas of the second example was evaluated according to the prior art with hydrogenation in an adiabatic reactor.
- the product gas comprised 0.50% methanol, and the temperature out of the reactor was raised to 177°C.
- the feed gas of the second example was also evaluated ac ⁇ cording to the present disclosure with hydrogenation in a gas cooled reactor.
- the product gas comprised no methanol and the temperature was maintained at 160°C by means of gas cooling.
- Example 3 In a third example, a feed composition comprising 0.30% ox ⁇ ygen, 1.00% ethylene and 0.50% propylene was hydrogenated .
- the feed gas of the third example was evaluated according to the prior art with hydrogenation in an adiabatic reactor. In this case the product gas comprised 1.92% methanol, and the temperature out of the reactor was raised to 277°C.
- the feed gas of the third example was also evaluated ac ⁇ cording to the present disclosure with hydrogenation in a gas cooled reactor. In this case the product gas comprised no methanol and the temperature was maintained at 160°C by means of gas cooling.
- the effect of the pre ⁇ sent disclosure is an ability to control the temperature in the reactor such that the undesired production of methanol is avoided, and such that the outlet gas is maintained at a temperature of 160°C protecting the process materials.
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP13732475.2A EP2867192A1 (en) | 2012-06-29 | 2013-06-27 | Purification of a raw gas by hydrogenation |
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP2012002753 | 2012-06-29 | ||
EP13732475.2A EP2867192A1 (en) | 2012-06-29 | 2013-06-27 | Purification of a raw gas by hydrogenation |
PCT/EP2013/063481 WO2014001438A1 (en) | 2012-06-29 | 2013-06-27 | Purification of a raw gas by hydrogenation |
Publications (1)
Publication Number | Publication Date |
---|---|
EP2867192A1 true EP2867192A1 (en) | 2015-05-06 |
Family
ID=52780109
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP13732475.2A Withdrawn EP2867192A1 (en) | 2012-06-29 | 2013-06-27 | Purification of a raw gas by hydrogenation |
Country Status (1)
Country | Link |
---|---|
EP (1) | EP2867192A1 (en) |
-
2013
- 2013-06-27 EP EP13732475.2A patent/EP2867192A1/en not_active Withdrawn
Non-Patent Citations (1)
Title |
---|
See references of WO2014001438A1 * |
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