Process and system for the production of ethylene carbonate and/or ethylene glycol

Patent metadata

Field	Value
Publication number	US-12006299-B2
Application number	US-202017637197-A
Country	US
Kind code	B2
Filing date	Sep 1, 2020
Priority date	Sep 5, 2019
Publication date	Jun 11, 2024
Grant date	Jun 11, 2024

Abstract

The invention relates to a process for producing ethylene carbonate and/or ethylene glycol, which comprises the following steps: a) supplying an overhead absorber stream withdrawn from an absorber to a vapor-liquid separator to yield an aqueous bottoms stream and a recycle gas stream; b) supplying an aqueous process stream comprising one or more impurities to a distillation apparatus to yield an overhead impurities stream and a purified aqueous process stream, wherein the aqueous process stream supplied to the distillation apparatus comprises at least a portion of the aqueous bottoms stream withdrawn from the vapor-liquid separator, wherein the overhead impurities stream is supplied to a condenser and is cooled to a temperature in the range of from 5 to 95° C., wherein the cooled overhead impurities stream is split into a reflux stream which is recycled to the distillation apparatus and an overhead impurities stream; and further steps c) and d).

First claim

We claim:

1. Process for the production of ethylene carbonate and/or ethylene glycol comprising:
a) supplying an overhead absorber stream (10) withdrawn from an absorber (6) to a vapor-liquid separator (12) to yield an aqueous bottoms stream (15) and a recycle gas stream (13);
b) supplying an aqueous process stream (17) comprising one or more impurities to a distillation apparatus (19) to yield an overhead impurities stream (22) and a purified aqueous process stream (21), wherein the aqueous process stream (17) supplied to the distillation apparatus (19) comprises at least a portion of the aqueous bottoms stream (15) withdrawn from the vapor-liquid separator (12), wherein the overhead impurities stream (22) is supplied to a condenser (45) and is cooled to a temperature in the range of from 5 to 95° C., wherein the cooled overhead impurities stream (22) is split into a reflux stream (22a) which is recycled to the distillation apparatus (19) and an overhead impurities stream (22b);
c) supplying at least a portion of the purified aqueous process stream (21) and an ethylene oxide product stream (4) to the absorber; and
d) contacting the ethylene oxide product stream (4) with the purified aqueous process stream (21) in the absorber in the presence of one or more carboxylation and hydrolysis catalysts to yield a fat absorbent stream (8) comprising ethylene carbonate and/or ethylene glycol.

2. Process according to claim 1 , wherein the aqueous process stream (17) is supplied to a preheater (36) prior to supplying the aqueous process stream (17) to the distillation apparatus (19) and wherein the preheater (36) is positioned at a minimum distance to the inlet (18) of the distillation apparatus (19) and/or wherein the preheater (36) has a minimum volume.

3. Process according to claim 2 , wherein the aqueous process stream (17) is supplied to a flash vessel (37) prior to supplying the aqueous process stream (17) to the preheater (36).

4. Process according to claim 2 , wherein the aqueous process stream (17) supplied to the preheater (36) additionally comprises at least a portion of an overhead dehydrator stream (33) withdrawn from a dehydrator (30).

5. Process according to claim 1 , wherein the one or more impurities are selected from the group consisting of: formaldehyde, acetaldehyde, 2,3-epoxy-1,4-dioxane, 1,3-dioxolane, 1,4-dioxane, 2-methyl-1,3-dioxolane, 2-methoxy ethanol, 2,2′-bis-1,3-dioxolane, 2-chloromethyl-1,3-dioxolane, 2-chloroethanol, and a combination thereof.

6. Process according to claim 2 , wherein the preheater (36) is heated via heat integration with a hot process stream (43) withdrawn from a separator (39).

7. Process according to claim 1 , wherein heat is supplied to the distillation apparatus (19) using a reboiler (44), and wherein the reboiler (44) is heated by heat integration with a hot process stream (43) withdrawn from a separator (39).

8. Process according to claim 1 , further comprising:
e) supplying at least a portion of the fat absorbent stream (8) to one or more finishing reactors (26) to yield a finishing reactor product stream (28), and
f) supplying at least a portion of the finishing reactor product stream (28) to a dehydrator (30) to yield a dehydrator bottom stream (31) and an overhead dehydrator stream (33).

9. Process according to claim 8 further comprising:
g) supplying at least a portion of the dehydrator bottom stream (31) to a separator (39) to yield a glycol product stream (41) and a hot process stream (43); and
h) supplying at least a portion of the hot process stream (43) to the absorber (6).

10. System for the production of ethylene carbonate and/or ethylene glycol, wherein the system comprises:
an absorber (6) comprising one or more carboxylation and hydrolysis catalysts, at least two inlets and at least two outlets, wherein a first inlet (5) of the absorber (6) is fluidly connected to an outlet (3) of an ethylene oxide reactor (2);
a vapor-liquid separator (12) comprising an inlet and an outlet, wherein the inlet (11) of the vapor-liquid separator (12) is fluidly connected to a first outlet (9) of the absorber (6);
a distillation apparatus (19) comprising an inlet (18), an outlet (20) and an outlet (22),
wherein the outlet (20) of the distillation apparatus (19) is fluidly connected to a second inlet (23) of the absorber (6) and the outlet (22) of the distillation apparatus (19) is fluidly connected to a sub-cooling condenser (45); and
optionally a preheater (36) comprising an inlet and an outlet, wherein the inlet of the preheater (36) is fluidly connected to the outlet (14) of the vapor-liquid separator (12) and

wherein the outlet of the preheater (36) is fluidly connected to the inlet (18) of the distillation apparatus (19).

11. System according to claim 10 further comprising:
a flash vessel (37) comprising an inlet and an outlet, wherein the inlet of the flash vessel (37) is fluidly connected to the outlet (14) of the vapor-liquid separator (12) and wherein the outlet of the flash vessel (37) is fluidly connected to the inlet of the preheater (36).

Assignees

• Shell Oil Co
• Shell Usa Inc

Inventors

• Black Jesse Raymond
• Bastings Roel Guillaume Hubertus Leonardus
• Dekkers Mark Albert Petrus

Classifications

• C07C29/80

  by distillation · CPC title

• C07C29/76

  by physical treatment · CPC title

• C07C29/106 Primary

  of oxiranes · CPC title

• B01D3/148 Primary

  in combination with at least one evaporator · CPC title

• C07C31/202

  Ethylene glycol · CPC title