CA1070249A - Suppression of cos formation in molecular sieve purification of hydrocarbon streams - Google Patents
Suppression of cos formation in molecular sieve purification of hydrocarbon streamsInfo
- Publication number
- CA1070249A CA1070249A CA229,314A CA229314A CA1070249A CA 1070249 A CA1070249 A CA 1070249A CA 229314 A CA229314 A CA 229314A CA 1070249 A CA1070249 A CA 1070249A
- Authority
- CA
- Canada
- Prior art keywords
- molecular sieve
- per cent
- suppression
- zeolite
- formation
- 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.)
- Expired
Links
Classifications
-
- 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
- B01D53/02—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
-
- 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
- C07C7/13—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers by molecular-sieve technique
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Water Supply & Treatment (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
SUPPRESSION OF COS FORMATION
IN MOLECULAR SIEVE PURIFICATION OF
HYDROCARBON GAS STREAMS
ABSTRACT OF DISCLOSURE
In the process for purifying hydrocarbon gas streams containing hydrogen sulfide and carbon dioxide as impurities by contact thereof with zeolitic molecular sieve adsorbents to selectively adsorb the impurities, the formation of carbonyl sulfide by the zeolite catalyzed reaction of H2S with CO2 is greatly suppressed by employing as the selective adsorbent certain cation forms of molecu-lar sieve zeolites which contain from 0.7 to 3 weight per cent adsorbed water.
S P E C I F I C A T I O N
IN MOLECULAR SIEVE PURIFICATION OF
HYDROCARBON GAS STREAMS
ABSTRACT OF DISCLOSURE
In the process for purifying hydrocarbon gas streams containing hydrogen sulfide and carbon dioxide as impurities by contact thereof with zeolitic molecular sieve adsorbents to selectively adsorb the impurities, the formation of carbonyl sulfide by the zeolite catalyzed reaction of H2S with CO2 is greatly suppressed by employing as the selective adsorbent certain cation forms of molecu-lar sieve zeolites which contain from 0.7 to 3 weight per cent adsorbed water.
S P E C I F I C A T I O N
Description
~ ~7 ~ 2 49 The present invention relates in general to the purification o~ hydrocarbon gas streams containing as impuriti~s H2S and C02, and more particularly to process whereby H2S is selectively adsorbed from such hydrocarbon gas streams using zeolitic molecular sie~es having minimal catalytic activity with respect to reaction between H2S
and C02 to form COS.
The gas phase trea~ments of hydrocarbon feedstocks, particularly natural gas, to remove H2S and other ~mpurities by selective adsorption and absorption techniques is well known. Natural gas, for example, commonly contains water, hydrogen sulfide7 carbon dioixide, plus other sulfur com-pounds and heavier hydrocarbons in various concentrations depending upon its source. The end use of the natural gas dictates which impurities must be removed and the extent of that removal When the gas is tv be transported by pipeline, ~here are specifications for its water and corrosive sulfur, as hydrogen sulfide, contents. Trans-mission and some other end uses do not require removal of carbon dioxide except in those instances where a mlnimum heating value needs to be met. Natural gas feed to a liquifaction unit requires much more thorough clean-up to protect against solids ~ormation by water and carbon dioxide in the cryogenic equipment.
The æelective adsorption character of molecular sieve has been quite ideal for these purifications for the
and C02 to form COS.
The gas phase trea~ments of hydrocarbon feedstocks, particularly natural gas, to remove H2S and other ~mpurities by selective adsorption and absorption techniques is well known. Natural gas, for example, commonly contains water, hydrogen sulfide7 carbon dioixide, plus other sulfur com-pounds and heavier hydrocarbons in various concentrations depending upon its source. The end use of the natural gas dictates which impurities must be removed and the extent of that removal When the gas is tv be transported by pipeline, ~here are specifications for its water and corrosive sulfur, as hydrogen sulfide, contents. Trans-mission and some other end uses do not require removal of carbon dioxide except in those instances where a mlnimum heating value needs to be met. Natural gas feed to a liquifaction unit requires much more thorough clean-up to protect against solids ~ormation by water and carbon dioxide in the cryogenic equipment.
The æelective adsorption character of molecular sieve has been quite ideal for these purifications for the
- 2 - ~
~ D-9153 ~O~QZ~
reason that the order of adsorption selectivity is~
H20 ? H2S > C02 > CH4. Thus when crude natural gas is passed through a molecular sieve adsorbent bed, the impuri-~ies adsorb in zones and it is possible to adsorb only the water, or water and H2S, or H20, H2S ~nd C0~ to any desired extent.
It has been found, however, tha~ when both H2S
and C02 are present in the feedstock, COS is frequently : present in the product gas, i.e. after treatment in a ~ :
molecular sieve purification unit, in higher concentrations than in the feed. This is apparently due to the fact that the molecular sieve serves as a catalyst for the reaction.
2 2 > 2 and also due to the fact ~hat the COS, once produced in the adsorption bed is not retained therein as an impurity adsorbate because of its low polarity and low boiling point compared with the same properties of the other impurity i~
mo~ecules present.
Accordingly, it is the principal object of the : ~
present invention to provide a means to suppress the ;~:
formation of COS when sweetening hydrocarbon gas streams ~.
containing both H2S and C02 using molecular sieve adsorbents.
This object, we have found7 is accomplished in the process wherein a hydrocarbon stream containing H2S
~ and C02 is contacted in the vapor phase at a temperature of from 60 to 120F and a pressure of 200 to 1200 psia. with a molecular sieve adsorbent to selectively adsorb H2S and : - 3 - : :
~ ~7~ Z ~ 9 C2 and thereafter recovering a hydrocarbon product having a decreased concentration of H2S, by the improvement which comprises utilizing as the said molecular sieve adsorbent a crystalline zeolite having a pore diameter of at least 5 Angstroms, at least 45 per cent of the framework aluminum atoms thereof being associated with at least one species of alkaline earth metal cation having an atomic number less than 56, preferably calclum, and containing in the adsorbed state thereon rom 0.7 to 3 weight per cent water.
Although the preferred feedstock for treatment in accordance with the present process is CO2 - containing sour natural gas, any hydrocarbon of mixture of hydro-; carbons containing H2S and C02 which is in the vapor s~ate at a temperature within the range of 60F to 120F and a pressur~ of from 200 to 1200 psia and w~ich is less strongly adsorbed than ~I2S is suitably treated. The preferred natural gas feeds~ock contains 9 in addition to methane, water in an~ concentration up to saturation, ~p to 5 mole per cent H2S, from 0.5 to 55 mole per cent CO2 and not more than 25 mole per cen~ hydrocarbons having more than one carbon atom. Commonly such hydrocarbon feedstock~
will also contain organic sulfur compounds such as mer-captans.
; The drawing is a schematic flow diagram showing a three bed process system suitably employed in the practice of the present process~
. !
_ 4 _ , ~.
.. ... .. . .. .. . .
~ 0'70'~ ~ ~
The molecular ~ie~e zeolite adsorbent can be any naturally occurring or synthetic cr~stalline zeoli~e which contains at least 45 equivalent per cent beryllium, magnesium, calcium, or strontium cations or mixtures of any two or more of suoh cations and which has in this ca~ion form a pore dlameter of at least 5 Angstroms. The calcium cation forms of zeolite A and zeolite X as deined in U.S.PO 2,882,243 and U.S.P. 2,883,244 respect~vely, have been found to ha~e especially low catalytic activity with .
respect to the reaction of H2S and CO~ and are particularly preferred in the present process. Other suitable zeolites :~
include the calcium cation forms of mordPnite, chabazite, faujasite and zeolites Y disclosed in U.S.P. 3,130,007;
zeolite T disclosed in U.S.P. 2,950,952; zeolite L dis- ::
closed in U.S.P. 3,216~789; and zeolite disclosed in `~
Canadian Patent No. 993,432, issued July 20, 1976. .
The required water loading on the zeolite ad- -sorbent is readily at~ained by any conventional means. In cyclic continuous operation in which an adsorbent bed is : :
periodically desorbed by means of a hot purge gas, commonly a portion of the purified product gas, it i~ convenient to j ::
inject water vapor into that purge gas stream in appro~
priate amounts such that after desorption and cool down of the bed is complete the requisite water loading remalns :
on the bed.
: ~' -: .
-5- .
,... .
- ~- .. , : ~ -~7~ 9 The following example is illu~trative of the present process:
Example 1.
(a) With refer~nce to the drawing, a natural gas feedstock having the following composi~ion wa~ employed in the proce~s, CH4 ..... .....95. mole ~/O
2 .106 "
C~2 ~ 3.
H2S ..... ~. .006 "
1~ the drawing it i5 to be under~tood that each of the three ad~orbent beds shown are ~quivalent and:each i~ turn would~ in conventional operation, undergo ~he step~ of adsorption9 hot purge desorp~ion and cool-down in prepara-: tion for the nexe cycle of the same three stepsO For simplicity the~var~ou~ valves~ manifolds, pump~, etc.
ordinarily used in this conventional ~hree~bed type of oparation have been omitted. The drawing show~ the sim~
taneous operation in each of the three b~ds.
.
The sforesald feedstock i9 ~ed at a pressure 1045 psia through line lO to ad~orb~r 12 which contains : as the ad~orbent z~olite A havlng 80 aquivalen~ per cent .. . .
calcium cations and 20 equivalent par cent aodium catlons ..
and cont~ining 2.6 weigh~-% ad~orbed H2O, Adsorber 12 is .
operated during t~i~ adsorption st~p at 92~F. The efluent rom the adsorber 20 i~ es3entiall~ pure me~h~ne, In due courae a~ ad~orpticn fr~nt for each o~ tha component~ ~20g . 6 .
, ~ 0~ 2 ~9 H2S and C02 are formed in the adsorber with H20 front being closest to the ingress end of the bed and the C02 front being nearest the egress end of the bed. Since in this embodiment it is the purpose to remove only the H2S, the C2 front is permitted tG break through the egress end o~
he adsorber and comingle with the product methane which is in the main removed from the system through line 14.
A portion of the product methane is continuously passed through line 16 to ~he top of adsorber 18 which at the beginning of the adsorption stroke in adsorber 12 had just finished being hot purge desorbed and con~ains essentially H~S - free product methane. The adsorber is at a tempera~
ture of 500F. The purified methane entering adsorber 18 is at a temperature of 92F. and in its passage through adsorber 18 cools that adsorber until a temperature of 125F. is reached. The thus heated gas leaving bed 18 is passed through line 20, furnace 22 where the temperature is raised to 550F., and line 24 into adsorber 26 which a~ the -~
beginning of the adsorption fill stroke in adsorber 12 has just completed a downward adsorption ~11 stroke u~ing feedstock of the same composition as i8 currentl~ be~ng in~roduced through line-10, The water con~ent of the purge gas fr~m furnace 22 is in~ected with water through line 28 to rai~e the water vapor content to 00185 mole per cent.
Tha desorbate stream from adsorber 26 which contains the H20 and H2S previously adsorbed is fed through line 30 to sulfur recovery unit 32. Stack gases are passed from the 070 Z ~ 9 ~tem through line 34 and sulfur collected from line 36.
The COS content o~ the product methane leaving the system through line 14 is less than 8 ppm, (b) Using the same procedure, feedstock and appara~us as set orth in part (a) above, except that ~he zeolite adsorbent in adsorber 12 contained less than 0,~7 weight-%
adsorbed H20, the COS content of ~he product methane leavlng the system ~hrough line 14 is about 45 ppm.
- 8 - :
'
~ D-9153 ~O~QZ~
reason that the order of adsorption selectivity is~
H20 ? H2S > C02 > CH4. Thus when crude natural gas is passed through a molecular sieve adsorbent bed, the impuri-~ies adsorb in zones and it is possible to adsorb only the water, or water and H2S, or H20, H2S ~nd C0~ to any desired extent.
It has been found, however, tha~ when both H2S
and C02 are present in the feedstock, COS is frequently : present in the product gas, i.e. after treatment in a ~ :
molecular sieve purification unit, in higher concentrations than in the feed. This is apparently due to the fact that the molecular sieve serves as a catalyst for the reaction.
2 2 > 2 and also due to the fact ~hat the COS, once produced in the adsorption bed is not retained therein as an impurity adsorbate because of its low polarity and low boiling point compared with the same properties of the other impurity i~
mo~ecules present.
Accordingly, it is the principal object of the : ~
present invention to provide a means to suppress the ;~:
formation of COS when sweetening hydrocarbon gas streams ~.
containing both H2S and C02 using molecular sieve adsorbents.
This object, we have found7 is accomplished in the process wherein a hydrocarbon stream containing H2S
~ and C02 is contacted in the vapor phase at a temperature of from 60 to 120F and a pressure of 200 to 1200 psia. with a molecular sieve adsorbent to selectively adsorb H2S and : - 3 - : :
~ ~7~ Z ~ 9 C2 and thereafter recovering a hydrocarbon product having a decreased concentration of H2S, by the improvement which comprises utilizing as the said molecular sieve adsorbent a crystalline zeolite having a pore diameter of at least 5 Angstroms, at least 45 per cent of the framework aluminum atoms thereof being associated with at least one species of alkaline earth metal cation having an atomic number less than 56, preferably calclum, and containing in the adsorbed state thereon rom 0.7 to 3 weight per cent water.
Although the preferred feedstock for treatment in accordance with the present process is CO2 - containing sour natural gas, any hydrocarbon of mixture of hydro-; carbons containing H2S and C02 which is in the vapor s~ate at a temperature within the range of 60F to 120F and a pressur~ of from 200 to 1200 psia and w~ich is less strongly adsorbed than ~I2S is suitably treated. The preferred natural gas feeds~ock contains 9 in addition to methane, water in an~ concentration up to saturation, ~p to 5 mole per cent H2S, from 0.5 to 55 mole per cent CO2 and not more than 25 mole per cen~ hydrocarbons having more than one carbon atom. Commonly such hydrocarbon feedstock~
will also contain organic sulfur compounds such as mer-captans.
; The drawing is a schematic flow diagram showing a three bed process system suitably employed in the practice of the present process~
. !
_ 4 _ , ~.
.. ... .. . .. .. . .
~ 0'70'~ ~ ~
The molecular ~ie~e zeolite adsorbent can be any naturally occurring or synthetic cr~stalline zeoli~e which contains at least 45 equivalent per cent beryllium, magnesium, calcium, or strontium cations or mixtures of any two or more of suoh cations and which has in this ca~ion form a pore dlameter of at least 5 Angstroms. The calcium cation forms of zeolite A and zeolite X as deined in U.S.PO 2,882,243 and U.S.P. 2,883,244 respect~vely, have been found to ha~e especially low catalytic activity with .
respect to the reaction of H2S and CO~ and are particularly preferred in the present process. Other suitable zeolites :~
include the calcium cation forms of mordPnite, chabazite, faujasite and zeolites Y disclosed in U.S.P. 3,130,007;
zeolite T disclosed in U.S.P. 2,950,952; zeolite L dis- ::
closed in U.S.P. 3,216~789; and zeolite disclosed in `~
Canadian Patent No. 993,432, issued July 20, 1976. .
The required water loading on the zeolite ad- -sorbent is readily at~ained by any conventional means. In cyclic continuous operation in which an adsorbent bed is : :
periodically desorbed by means of a hot purge gas, commonly a portion of the purified product gas, it i~ convenient to j ::
inject water vapor into that purge gas stream in appro~
priate amounts such that after desorption and cool down of the bed is complete the requisite water loading remalns :
on the bed.
: ~' -: .
-5- .
,... .
- ~- .. , : ~ -~7~ 9 The following example is illu~trative of the present process:
Example 1.
(a) With refer~nce to the drawing, a natural gas feedstock having the following composi~ion wa~ employed in the proce~s, CH4 ..... .....95. mole ~/O
2 .106 "
C~2 ~ 3.
H2S ..... ~. .006 "
1~ the drawing it i5 to be under~tood that each of the three ad~orbent beds shown are ~quivalent and:each i~ turn would~ in conventional operation, undergo ~he step~ of adsorption9 hot purge desorp~ion and cool-down in prepara-: tion for the nexe cycle of the same three stepsO For simplicity the~var~ou~ valves~ manifolds, pump~, etc.
ordinarily used in this conventional ~hree~bed type of oparation have been omitted. The drawing show~ the sim~
taneous operation in each of the three b~ds.
.
The sforesald feedstock i9 ~ed at a pressure 1045 psia through line lO to ad~orb~r 12 which contains : as the ad~orbent z~olite A havlng 80 aquivalen~ per cent .. . .
calcium cations and 20 equivalent par cent aodium catlons ..
and cont~ining 2.6 weigh~-% ad~orbed H2O, Adsorber 12 is .
operated during t~i~ adsorption st~p at 92~F. The efluent rom the adsorber 20 i~ es3entiall~ pure me~h~ne, In due courae a~ ad~orpticn fr~nt for each o~ tha component~ ~20g . 6 .
, ~ 0~ 2 ~9 H2S and C02 are formed in the adsorber with H20 front being closest to the ingress end of the bed and the C02 front being nearest the egress end of the bed. Since in this embodiment it is the purpose to remove only the H2S, the C2 front is permitted tG break through the egress end o~
he adsorber and comingle with the product methane which is in the main removed from the system through line 14.
A portion of the product methane is continuously passed through line 16 to ~he top of adsorber 18 which at the beginning of the adsorption stroke in adsorber 12 had just finished being hot purge desorbed and con~ains essentially H~S - free product methane. The adsorber is at a tempera~
ture of 500F. The purified methane entering adsorber 18 is at a temperature of 92F. and in its passage through adsorber 18 cools that adsorber until a temperature of 125F. is reached. The thus heated gas leaving bed 18 is passed through line 20, furnace 22 where the temperature is raised to 550F., and line 24 into adsorber 26 which a~ the -~
beginning of the adsorption fill stroke in adsorber 12 has just completed a downward adsorption ~11 stroke u~ing feedstock of the same composition as i8 currentl~ be~ng in~roduced through line-10, The water con~ent of the purge gas fr~m furnace 22 is in~ected with water through line 28 to rai~e the water vapor content to 00185 mole per cent.
Tha desorbate stream from adsorber 26 which contains the H20 and H2S previously adsorbed is fed through line 30 to sulfur recovery unit 32. Stack gases are passed from the 070 Z ~ 9 ~tem through line 34 and sulfur collected from line 36.
The COS content o~ the product methane leaving the system through line 14 is less than 8 ppm, (b) Using the same procedure, feedstock and appara~us as set orth in part (a) above, except that ~he zeolite adsorbent in adsorber 12 contained less than 0,~7 weight-%
adsorbed H20, the COS content of ~he product methane leavlng the system ~hrough line 14 is about 45 ppm.
- 8 - :
'
Claims (2)
1. In the process wherein a hydrocarbon stream con-taining H2S and CO2 is contacted in the vapor phase at a temperature of from 60°F to 120°F and at a pressure of 200 to 1200 psia with a molecular sieve adsorbent to sel-ectively adsorb H2S whereby a hydrocarbon product is recovered having a decreased H2S content, the improvement which comprises utilizing as the said molecular sieve adsorbent a crystalline zeolite having a pore diameter of at least 5 Angstroms, at least 45 per cent of the framework aluminum atoms thereof being associated with at least one species of alkaline earth metal cation having an atomic number less than 56, and containing in the adsorbed state thereon from 0.7 to 3 weight per cent water.
2. Process according to claim 1 wherein the hydro-carbon of the stream being treated is methane containing not greater than 5 mole per cent H2S from 0.5 to 55 mole per cent carbon dioxide, and the molecular sieve adsorbent is the calcium cation form of zeolite A having at least 45 equivalent per cent calcium cations.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US48663874A | 1974-07-08 | 1974-07-08 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1070249A true CA1070249A (en) | 1980-01-22 |
Family
ID=23932674
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA229,314A Expired CA1070249A (en) | 1974-07-08 | 1975-06-13 | Suppression of cos formation in molecular sieve purification of hydrocarbon streams |
Country Status (7)
| Country | Link |
|---|---|
| AU (1) | AU498733B2 (en) |
| CA (1) | CA1070249A (en) |
| DE (1) | DE2530091B2 (en) |
| FR (1) | FR2277798A1 (en) |
| GB (1) | GB1516202A (en) |
| IT (1) | IT1036464B (en) |
| NL (1) | NL7508072A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104291275A (en) * | 2013-07-15 | 2015-01-21 | 北京丰汉工程技术有限公司 | Method and system for recovering sulfur from acid gas in coal gasification process |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2654599C2 (en) * | 1976-12-02 | 1984-11-15 | Union Carbide Corp., New York, N.Y. | Process for purifying natural gas |
| DE3029187C2 (en) * | 1980-08-01 | 1986-04-17 | Bergwerksverband Gmbh, 4300 Essen | Process for removing hydrogen sulfide from oxygen-free or oxygen-containing gas mixtures |
| DE3306371A1 (en) * | 1983-02-24 | 1984-08-30 | Bergwerksverband Gmbh, 4300 Essen | METHOD FOR PRODUCING A METHANE-RICH GAS MIXTURE, ESPECIALLY FROM MINE GAS |
| US4830733A (en) * | 1987-10-05 | 1989-05-16 | Uop | Integrated process for the removal of sulfur compounds from fluid streams |
| GB8803767D0 (en) * | 1988-02-18 | 1988-03-16 | Ici Plc | Desulphurisation |
| FR2882941B1 (en) * | 2005-03-08 | 2007-12-21 | Inst Francais Du Petrole | PROCESS FOR PURIFYING NATURAL GAS BY ADSORPTING MERCAPTANS |
| US9144765B2 (en) | 2007-05-18 | 2015-09-29 | Shell Oil Company | Reactor system, an absorbent and a process for reacting a feed |
| US8193374B2 (en) | 2008-05-15 | 2012-06-05 | Shell Oil Company | Process for the preparation of alkylene carbonate and/or alkylene glycol |
| KR101633523B1 (en) | 2008-05-15 | 2016-06-24 | 셀 인터나쵸나아레 레사아치 마아츠샤피 비이부이 | Process for the preparation of an alkylene carbonate and an alkylene glycol |
-
1975
- 1975-06-13 CA CA229,314A patent/CA1070249A/en not_active Expired
- 1975-07-05 DE DE2530091A patent/DE2530091B2/en not_active Withdrawn
- 1975-07-07 IT IT68764/75A patent/IT1036464B/en active
- 1975-07-07 NL NL7508072A patent/NL7508072A/en unknown
- 1975-07-07 FR FR7521239A patent/FR2277798A1/en active Granted
- 1975-07-07 AU AU82799/75A patent/AU498733B2/en not_active Expired
- 1975-07-07 GB GB28489/75A patent/GB1516202A/en not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104291275A (en) * | 2013-07-15 | 2015-01-21 | 北京丰汉工程技术有限公司 | Method and system for recovering sulfur from acid gas in coal gasification process |
Also Published As
| Publication number | Publication date |
|---|---|
| DE2530091A1 (en) | 1976-01-29 |
| IT1036464B (en) | 1979-10-30 |
| FR2277798A1 (en) | 1976-02-06 |
| NL7508072A (en) | 1976-01-12 |
| AU498733B2 (en) | 1979-03-22 |
| GB1516202A (en) | 1978-06-28 |
| AU8279975A (en) | 1977-01-13 |
| FR2277798B1 (en) | 1979-05-11 |
| DE2530091B2 (en) | 1978-03-23 |
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Legal Events
| Date | Code | Title | Description |
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| MKEX | Expiry |