US2018148260A1PendingUtilityA1
Selective Hydrogenation Using a Flow Index
Assignee: CHEVRON PHILLIPS CHEMICAL CO LPPriority: Nov 16, 2015Filed: Jan 23, 2018Published: May 31, 2018
Est. expiryNov 16, 2035(~9.3 yrs left)· nominal 20-yr term from priority
Inventors:Joseph Bergmeister, IiiTin-Tack Peter CheungZongxuan HongTimothy O. OdiCharles D. NolidinThomas J. GonzalesJennifer L. NillDavid W. Dockter
B65G 1/0492B65G 1/10B65G 47/57B65G 1/1373B65G 1/137B65G 1/065Y10S901/01B65G 1/1378B65G 1/045B65G 1/1371B65G 1/127C10G 45/32C10G 2400/24C10G 2400/20C10G 70/02C10G 69/06C10G 9/00C07C 5/09B01J 2219/24B01J 2219/00306C07C 4/04C07C 5/05C07C 2521/04B01J 19/24B01J 19/245
44
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Claims
Abstract
A process includes hydrogenating, in a reaction zone, a highly unsaturated hydrocarbon received from a hydrocarbon stream to yield a product having an unsaturated hydrocarbon, the hydrogenating step occurring in the presence of a hydrogenation catalyst which has a selectivity for conversion of the highly unsaturated hydrocarbon to the unsaturated hydrocarbon of about 90 mol % or greater based on the moles of the highly unsaturated hydrocarbon which are converted to the product, the hydrogenating step occurring in a reaction zone under conditions which include a flow index (I F ) in a range of about 0.09 to about 35, wherein the I F is defined as: I F = F × [ CO ] V , wherein F is the flow rate of the hydrocarbon stream into the reaction zone in units of kg/h, [CO] is the concentration of carbon monoxide in the hydrocarbon stream in units of mol %, and V is the volume of the reaction zone in units of ft 3 .
Claims
exact text as granted — not AI-modifiedWhat is claimed is:
1 . A process comprising:
hydrogenating, in a reaction zone, a highly unsaturated hydrocarbon received from a hydrocarbon stream to yield a product comprising an unsaturated hydrocarbon, wherein the hydrogenating occurs in the presence of a hydrogenation catalyst which has a selectivity for conversion of the highly unsaturated hydrocarbon to the unsaturated hydrocarbon of about 90 mol % or greater based on the moles of the highly unsaturated hydrocarbon which are converted to the product, wherein the highly unsaturated hydrocarbon comprises acetylene, and wherein the unsaturated hydrocarbon comprises ethylene, and wherein the hydrogenation catalyst further comprises one or more inorganic supports, and wherein the hydrogenating in the reaction zone occurs under conditions comprising a flow index (I F ) in a range of about 0.09 to about 35, wherein the I F is defined as:
I
F
=
F
×
[
CO
]
V
,
wherein F is the flow rate of the hydrocarbon stream into the reaction zone in units of kg/h, [CO] is the concentration of carbon monoxide in the hydrocarbon stream in units of mol %, and V is the volume of the reaction zone in units of ft 3 .
2 . The process of claim 1 wherein the hydrogenation catalyst further comprises palladium.
3 . The process of claim 1 wherein the hydrogenation catalyst further comprises phosphorus.
4 . The process of claim 1 wherein the hydrogenation catalyst further comprises one or more phosphorus compounds.
5 . The process of claim 1 wherein the hydrogenation catalyst further comprises a Group 1B metal.
6 . The process of claim 1 wherein the hydrogenation catalyst further comprises silver.
7 . The process of claim 1 wherein the hydrogenation catalyst further comprises fluorine.
8 . The process of claim 1 wherein the hydrogenation catalyst further comprises or one or more fluoride compounds.
9 . The process of claim 1 wherein the hydrogenation catalyst further comprises sulfur.
10 . The process of claim 1 wherein the hydrogenation catalyst further comprises or one or more sulfur compounds.
11 . The process of claim 1 wherein the hydrogenation catalyst further comprises one or more alkali metals.
12 . The process of claim 1 wherein the hydrogenation catalyst further comprises one or more alkaline earth metals.
13 . The process of claim 1 wherein the hydrogenation catalyst further comprises iodine.
14 . The process of claim 4 , wherein the phosphorus compound is an organophosphorus compound.
15 . The process of claim 2 , wherein the palladium is concentrated near the periphery of the catalyst and forms a palladium skin, wherein the skin has a thickness of from about 1 micron to about 3000 microns.
16 . The process of claim 2 , wherein the palladium is added by contacting the hydrogenation with an acidic solution comprising palladium.
17 . The process of claim 14 , wherein the organophosphorus compound comprises a methylphosphonate, a trifluorophosphate, or combinations thereof.
18 . The process of claim 8 , wherein the fluoride compound comprises a trifluoromethanesulfonate, a tetrafluoroborate, a trifluoromethylsulfonyl, a pentafluoroethyl, a trifluoromethylsulfonyl, or combinations thereof.
19 . The process of claim 10 , wherein the sulfur compound comprises an ethylsulfate, a methylsulfate, an octylsulfate, or combinations thereof.
20 . The process of claim 1 , wherein the selectivity is defined as:
S
=
100
×
(
UH
(
p
)
-
UH
(
f
)
HUH
(
f
)
-
HUH
(
p
)
)
where S is selectivity in mol %, UH(p) is moles of the unsaturated hydrocarbon in the product, UH(f) is moles of the unsaturated hydrocarbon in the hydrocarbon stream, HUH(f) is the moles of highly unsaturated hydrocarbon in the hydrocarbon stream, and HUH(p) is the moles of the highly unsaturated hydrocarbon in the product, wherein the reaction zone comprises a first stage and a second stage, and wherein the selectivity achieved in the first stage is greater than the selectivity achieved in the second stage.
21 . The process of claim 1 , further comprising:
cracking a feed stream to produce a cracked gas stream comprising the highly unsaturated hydrocarbon, carbon monoxide, and a saturated hydrocarbon.
22 . The process of claim 21 , further comprising:
fractionating the cracked gas stream to yield a C 3 − stream or a C 2 − stream comprising the highly unsaturated hydrocarbon, carbon monoxide, and about 90 mol % or greater of the saturated hydrocarbon contained in the cracked gas stream, wherein at least a portion of the highly unsaturated hydrocarbon in the C 3 − stream or the C 2 − stream is hydrogenated in the presence of the hydrogenation catalyst.
23 . The process of claim 1 , wherein the [CO] in the reaction zone is from about 0.0001 mol % to about 0.15 mol %.
24 . The process of claim 20 , wherein:
i) the first stage of the reaction zone and the second stage of the reaction zone are contained in a common vessel; or ii) the first stage of the reaction zone is a first reactor, the second stage of the reaction zone is a second reactor, and the first reactor and the second reactor are connected in series.
25 . A process comprising:
hydrogenating, in a reaction zone, a highly unsaturated hydrocarbon received from a hydrocarbon stream to yield a product comprising an unsaturated hydrocarbon, wherein the hydrogenating occurs in the presence of a hydrogenation catalyst which has a selectivity for conversion of the highly unsaturated hydrocarbon to the unsaturated hydrocarbon of about 90 mol % or greater based on the moles of the highly unsaturated hydrocarbon which are converted to the product, and wherein the hydrogenating in the reaction zone occurs under conditions comprising a flow index (I F ) in a range of about 0.09 to about 35, wherein the I F is defined as:
I
F
=
F
×
[
CO
]
V
,
wherein F is the flow rate of the hydrocarbon stream into the reaction zone in units of kg/h, [CO] is the concentration of carbon monoxide in the hydrocarbon stream in units of mol %, and V is the volume of the reaction zone in units of ft 3 , and
wherein the process comprises a first reactor and a second reactor in series, wherein a first effluent stream entering the first reactor enters at a first temperature, wherein the first temperature is from about 100° F. and about 250° F., and a second effluent stream enters the second reactor at a second temperature, wherein the second temperature is from about 110° F. to about 260° F.
26 . The process of claim 25 , wherein the selectivity is defined as:
S
=
100
×
(
UH
(
p
)
-
UH
(
f
)
HUH
(
f
)
-
HUH
(
p
)
)
where S is selectivity in mol %, UH(p) is moles of the unsaturated hydrocarbon in the product, UH(f) is moles of the unsaturated hydrocarbon in the hydrocarbon stream, HUH(f) is the moles of highly unsaturated hydrocarbon in the hydrocarbon stream, and HUH(p) is the moles of the highly unsaturated hydrocarbon in the product; and wherein the selectivity achieved in the second reactor is less than the selectivity achieved in the first reactor.
27 . The process of claim 25 further comprising:
cracking a feed stream to produce a cracked gas stream comprising the highly unsaturated hydrocarbon, carbon monoxide, and a saturated hydrocarbon.
28 . The process of claim 27 , further comprising:
fractionating the cracked gas stream to yield a C 3 − stream or a C 2 − stream comprising the highly unsaturated hydrocarbon, carbon monoxide, and about 90 mol % or greater of the saturated hydrocarbon contained in the cracked gas stream, wherein at least a portion of the highly unsaturated hydrocarbon in the C 3 − stream or the C 2 − stream is hydrogenated in the presence of the hydrogenation catalyst.
29 . The process of claim 25 , wherein the [CO] in the reaction zone is from about 0.0001 mol % to about 0.15 mol %.
30 . A process comprising:
hydrogenating, in a reaction zone, a highly unsaturated hydrocarbon received from a hydrocarbon stream to yield a product comprising an unsaturated hydrocarbon, wherein the hydrogenating occurs in the presence of a hydrogenation catalyst which has a selectivity for conversion of the highly unsaturated hydrocarbon to the unsaturated hydrocarbon of about 90 mol % or greater based on the moles of the highly unsaturated hydrocarbon which are converted to the product, and wherein the hydrogenating in the reaction zone occurs under conditions comprising a flow index (I F ) in a range of about 0.09 to about 35, wherein the I F is defined as:
I
F
=
F
×
[
CO
]
V
,
wherein F is the flow rate of the hydrocarbon stream into the reaction zone in units of kg/h, [CO] is the concentration of carbon monoxide in the hydrocarbon stream in units of mol %, and V is the volume of the reaction zone in units of ft 3 , and wherein the process comprises a first reactor and a second reactor in series, wherein the first reactor operates at a first temperature of from about 100° F. and about 250° F., and the second reactor operates at a second temperature of from about 110° F. to about 260° F.
31 . The process of claim 30 , wherein the selectivity is defined as:
S
=
100
×
(
UH
(
p
)
-
UH
(
f
)
HUH
(
f
)
-
HUH
(
p
)
)
where S is selectivity in mol %, UH(p) is moles of the unsaturated hydrocarbon in the product, UH(f) is moles of the unsaturated hydrocarbon in the hydrocarbon stream, HUH(f) is the moles of highly unsaturated hydrocarbon in the hydrocarbon stream, and HUH(p) is the moles of the highly unsaturated hydrocarbon in the product; and wherein the selectivity achieved in the second reactor is less than the selectivity achieved in the first reactor.
32 . The process of claim 30 , further comprising:
cracking a feed stream to produce a cracked gas stream comprising the highly unsaturated hydrocarbon, carbon monoxide, and a saturated hydrocarbon.
33 . The process of claim 32 , further comprising:
fractionating the cracked gas stream to yield a C 3 − stream or a C 2 − stream comprising the highly unsaturated hydrocarbon, carbon monoxide, and about 90 mol % or greater of the saturated hydrocarbon contained in the cracked gas stream, wherein at least a portion of the highly unsaturated hydrocarbon in the C 3 − stream or the C 2 − stream is hydrogenated in the presence of the hydrogenation catalyst.
34 . The process of claim 30 , wherein the [CO] in the reaction zone is from about 0.0001 mol % to about 0.15 mol %.Join the waitlist — get patent alerts
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