Process for the production of ethylene oxide
An ethylene oxide (EO) production process for the epoxidation of ethylene comprising: contacting an inlet feed gas with a catalyst having a fluoride-mineralized alpha-alumina carrier, silver, a rhenium promoter, and one or more alkali metal promoters. At a cumulative EO production cumEO 1 of at least 0.2 kton EO/m 3 catalyst, the process is operating at a reaction temperature T 1 and with the inlet feed gas having an optimum overall catalyst chloriding effectiveness value Cl eff 1 to produce EO with an EO production parameter value EO 1 ; and the process is subsequently operated such that at a cumulative EO production cumEO X , cumEO X is at least 0.6 kton EO/m 3 catalyst greater than cumEO 1 , the reaction temperature has an increased value T X to maintain EO production parameter EO 1 whilst the optimum overall catalyst chloriding effectiveness value of the inlet feed gas Cl eff X is controlled such that the ratio of Cl eff X /Cl eff 1 is from 0.8 to 1.2.
1 . A process for the epoxidation of ethylene comprising:
contacting an inlet feed gas comprising ethylene, oxygen and one or more reaction modifiers consisting of organic chlorides with an epoxidation catalyst comprising a carrier, and having silver, a rhenium promoter, and one or more alkali metal promoters deposited thereon;
wherein the inlet feed gas has an overall catalyst chloriding effectiveness value (Cl eff ) represented by the formula:—
Cl
eff
=
(
0.1
*
[
MC
]
+
[
EC
]
+
2
*
[
EDC
]
+
[
VC
]
)
(
0.002
*
[
CH
4
]
+
[
C
2
H
6
]
+
0.01
*
[
C
2
H
4
]
)
(
I
)
wherein [MC], [EC], [EDC], and [VC] are the concentrations in ppmv of methyl chloride (MC), ethyl chloride (EC), ethylene dichloride (EDC), and vinyl chloride (VC), respectively, and [CH 4 ], [C 2 H 6 ] and [C 2 H 4 ] are the concentrations in mole percent of methane, ethane, and ethylene, respectively, in the inlet feed gas;
wherein at an initial cumulative ethylene oxide production cumEO 1 of at least 0.2 kton ethylene oxide/m 3 catalyst, said process is operating at a reaction temperature having a value T 1 and with the inlet feed gas having an optimum overall catalyst chloriding effectiveness value of Cl eff1 to produce ethylene oxide with an ethylene oxide production parameter at a target value EO 1 ; and characterised in that the carrier is a fluoride-mineralized alpha-alumina carrier and said process is subsequently operated such that at a cumulative ethylene oxide production cumEO x , wherein cumEO x is at least 0.6 kton ethylene oxide/m 3 catalyst greater than cumEO 1 , the reaction temperature has an increased value T x to maintain said ethylene oxide production parameter at the target value EO 1 whilst the optimum overall catalyst chloriding effectiveness value of the inlet feed gas Cl effx is controlled such that the ratio of Cl effx /Cl eff1 is in the range of from 0.8 to 1.2, wherein the value T1 is the reaction temperature when the ethylene oxide production is at cumEO1, and wherein the value Tx is greater than the value T1 by at least 3° C.
2 . The process of claim 1 , wherein cumEO 1 is at least 0.25 kton ethylene oxide/m 3 catalyst.
3 . The process of claim 1 , wherein cumEO x is at least 0.8 kton ethylene oxide/m 3 catalyst greater than cumEO 1 .
4 . The process of claim 1 , wherein the ratio of Cl effx /Cl eff1 is in the range of from 0.9 to 1.1.
5 . The process of claim 1 , wherein as cumulative ethylene oxide production increases from cumEO 1 to cumEO x , the ratio of Cl effx /Cl eff1 is maintained throughout the period of said increase in the range of from 0.8 to 1.2.
6 . The process of claim 1 , wherein as cumulative ethylene oxide production increases from cumEO 1 to reach its final value of cumEO x at the end of catalyst life, the ratio of Cl effx /Cl eff1 is maintained throughout the entire life of the catalyst in the range of from 0.8 to 1.2.
7 . The process of claim 1 , wherein the reaction temperature T 1 is at a value in the range of from 180 to 260° C.
8 . The process of claim 1 , wherein the reaction temperature T x is at a value in the range of from 200 to 300° C.
9 . The process of claim 1 , wherein the ethylene oxide production parameter, EO 1 , is work rate and EO 1 is selected from in the range of from 50 to 600 kg of ethylene oxide per m 3 of catalyst per hour.
10 . The process of claim 1 , wherein the inlet feed gas further comprises carbon dioxide in a concentration of from 0.10 mole-% to 10 mole-%, relative to the total inlet feed gas.
11 . The process of claim 1 , wherein one or more reaction modifiers are selected from methyl chloride, ethyl chloride, ethylene dichloride, vinyl chloride, and combinations thereof.
12 . The process of claim 1 , wherein the one or more alkali metal promoters are selected from the group consisting of lithium, sodium, potassium, rubidium, cesium, and a combination thereof.
13 . The process of claim 1 , wherein the epoxidation catalyst further comprises one or more co-promoters selected from the group consisting of sulfur, phosphorus, boron, tungsten, molybdenum, chromium, and a combination thereof.
14 . The process of claim 1 , wherein the epoxidation catalyst comprises:
a first co-promoter selected from the group consisting of sulfur, phosphorus, boron, and a combination thereof; and
a second co-promoter selected from the group consisting of tungsten, molybdenum, chromium, and a combination thereof.
15 . The process of claim 1 , wherein the epoxidation catalyst further comprises a further metal selected from the group consisting of beryllium, magnesium, calcium, strontium, barium, titanium, hafnium, zirconium, vanadium, thallium, thorium, tantalum, niobium, gallium, germanium, manganese, and a combination thereof.
16 . The process of claim 1 , wherein the fluoride-mineralized alpha-alumina carrier has a surface area in the range of from 0.1 to 10 m 2 /g relative to the weight of the fluoride-mineralized alpha-alumina carrier, as measured in accordance with the B.E.T. method.
17 . The process of claim 1 , wherein the fluoride-mineralized alpha-alumina carrier has a particulate matrix having a lamellar or platelet-type morphology.
18 . The process as claimed in claim 17 , wherein the lamellar or platelet-type morphology is such that particles having in at least one direction a size greater than 0.1 micrometer have at least one substantially flat major surface.
19 . The process of claim 1 , further comprising:
reacting at least a portion of the ethylene oxide produced with at least one reagent selected from the group consisting of: water, an alcohol, carbon dioxide and an amine to form ethylene glycol, an ethylene glycol ether, ethylene carbonate and ethanolamine, respectively.