GB2162194A - Process for removing carbonyl sulphide from liquid hydro-carbon feedstocks - Google Patents
Process for removing carbonyl sulphide from liquid hydro-carbon feedstocks Download PDFInfo
- Publication number
- GB2162194A GB2162194A GB08518304A GB8518304A GB2162194A GB 2162194 A GB2162194 A GB 2162194A GB 08518304 A GB08518304 A GB 08518304A GB 8518304 A GB8518304 A GB 8518304A GB 2162194 A GB2162194 A GB 2162194A
- Authority
- GB
- United Kingdom
- Prior art keywords
- nickel
- absorbent material
- feedstock
- weight
- liquid hydrocarbon
- 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.)
- Granted
Links
- 239000007788 liquid Substances 0.000 title claims abstract description 30
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 29
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title claims abstract description 25
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 23
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 title claims description 9
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims abstract description 76
- 239000000463 material Substances 0.000 claims abstract description 34
- 230000002745 absorbent Effects 0.000 claims abstract description 33
- 239000002250 absorbent Substances 0.000 claims abstract description 33
- 229910052759 nickel Inorganic materials 0.000 claims abstract description 33
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 20
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 20
- 238000000746 purification Methods 0.000 claims abstract description 9
- 229910000480 nickel oxide Inorganic materials 0.000 claims abstract description 6
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000002245 particle Substances 0.000 claims description 6
- 239000007791 liquid phase Substances 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 description 8
- 238000006116 polymerization reaction Methods 0.000 description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 5
- 239000012535 impurity Substances 0.000 description 5
- 238000011282 treatment Methods 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- GIAFURWZWWWBQT-UHFFFAOYSA-N 2-(2-aminoethoxy)ethanol Chemical compound NCCOCCO GIAFURWZWWWBQT-UHFFFAOYSA-N 0.000 description 2
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 229910000431 copper oxide Inorganic materials 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000002685 polymerization catalyst Substances 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 description 1
- 239000005751 Copper oxide Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- WGLPBDUCMAPZCE-UHFFFAOYSA-N Trioxochromium Chemical compound O=[Cr](=O)=O WGLPBDUCMAPZCE-UHFFFAOYSA-N 0.000 description 1
- IJCVBMSXIPFVLH-UHFFFAOYSA-N [C].S=O Chemical compound [C].S=O IJCVBMSXIPFVLH-UHFFFAOYSA-N 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 229910000423 chromium oxide Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- LVTYICIALWPMFW-UHFFFAOYSA-N diisopropanolamine Chemical compound CC(O)CNCC(C)O LVTYICIALWPMFW-UHFFFAOYSA-N 0.000 description 1
- 229940043276 diisopropanolamine Drugs 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910000008 nickel(II) carbonate Inorganic materials 0.000 description 1
- ZULUUIKRFGGGTL-UHFFFAOYSA-L nickel(ii) carbonate Chemical compound [Ni+2].[O-]C([O-])=O ZULUUIKRFGGGTL-UHFFFAOYSA-L 0.000 description 1
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 1
- 229920001223 polyethylene glycol Polymers 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 239000008262 pumice Substances 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- -1 silico-aluminas Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 150000004763 sulfides Chemical class 0.000 description 1
- UWHCKJMYHZGTIT-UHFFFAOYSA-N tetraethylene glycol Chemical compound OCCOCCOCCOCCO UWHCKJMYHZGTIT-UHFFFAOYSA-N 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
- 239000011787 zinc oxide Substances 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Gas Separation By Absorption (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A process for the purification of liquid hydrocarbon feedstocks containing propylene and containing from 1 to 70 ppm of COS, consists in passing the feedstock over an absorbent material comprising nickel deposited on a support, the nickel being present in the form of nickel oxide and in the form of metallic nickel, and the quantity of metallic nickel being between 35 to 70% by weight of the total nickel.
Description
SPECIFICATION
Process for removing carbonyl sulphide from liquid hydrocarbon feedstocks
The present invention relates to a process for removing the sulphur, present in the form of carbon oxysulphide or carbonyl sulphide, from liquid hydrocarbons, in particular from hydrocarbon feedstocks containing propylene.
In refineries, the treatment of liquid hydrocarbons to remove or convert the impurities therein requires complex and expensive processes. Various sulphur compounds constitute the usual impurities which it is often desired to remove, the compounds being hydrogen sulphide, mercaptans and, in particular, carbonyl sulphide.
It is common in industrial practice to reduce the sulphur content by treating the hydrocarbons in the gaseous state. A widely accepted practice consists in using diethanolamine, diisopropanolamine, monoethanolamine and tetraethylene glycol to remove the sulphides from combustible gases in the gaseous state. It is also known that those solvents can be used to treat hydrocarbons in the liquid state.
However, when those solvents are used to extract the impurities from hydrocarbons in the liquid state, it is not possible to reduce the content of carbonyl sulphide, hereafter referred to as COS for the sake of simplicity, to less than 5 ppm.
It is also known that recently developed propylene polymerization processes are using increasingly efficient catalysts. However, those catalysts are extremely sensitive to all polar impurities such as COS, for example, which has a dipole moment of 0.736 Debye. When using those polymerization processes, it is therefore important to purify the feedstock so that the residual content of the impurities is extremely low.
With the conventional processes, which treat feedstocks capable of initially containing from 30 to 70 ppm of COS, a residual COS content of from 10 to 20 ppm is achieved after purification.
It has already been proposed to treat liquid hydrocarbon feedstocks, containing propylene, with 2-(2aminoethoxy)ethanol, known as diglycolamine, in order to remove the COS. However, although the residual content obtained is low, being of the order of ppm, it is still not sufficient to satisfy the conditions of polymerizations using very active Ziegler-type catalysts.
In addition to the treatment technique using liquid-liquid contact, treatments involving liquid-solid contact have also been proposed.
Those latter types of treatment have the advantage of restricting the risks of contamination of the propylene which is subsequently to be polymerized, which contamination would make it necessary to have a second absorber.
It has already been proposed to use a solid material consisting of a porous inert support having a large specific surface area, such as silica gel, pumice or Mg silicate and oxides of Cd, Zn, Ni and Co, over which the liquefied feedstock is passed, leading to a residual COS content of less than 1 ppm in the feedstock.
It has also been proposed to use absorbents composed of iron oxide, copper oxide or copper and chromium oxide on a support of high specific surface area, such as active charcoal or alumina, so as to reduce the COS content of the liquid hydrocarbons from 50 to 60 ppm in the initial feedstock to about 0.5 ppm.
However, although that COS content is already very low, it is still not sufficient to allow propylene which is purified in this way to be sent to a polymerization unit which uses very active Ziegler catalysts.
It has also been proposed to treat the feedstocks by passing them over basic ion exchange resins at ambient temperature. Nevertheless, the residual COS content which is obtained is also of the order of ppm, which is too high to carry out the polymerization in the presence of the latest generation of polymerization catalysts.
It has also been proposed to use zinc oxide which has been deposited on an alumina support, but that type of catalyst is not sufficiently active to be able to remove the COS down to residual contents below 30 ppb.
Consequently, there is a need for a process which makes it possible to desulphurize liquid hydrocarbon feedstocks containing propylene and other oelfins, and in particular to remove the COS from such feedstocks, until the residual COS content does not exceed 30 ppb, so that the new generation of propylene polymerization catalysts are not poisoned too quickly.
The present invention relates to a process for the purification of liquid hydrocarbon feedstocks which makes it possible to satisfy the above-mentioned criteria.
Also, the present invention relates to a purification process which makes it possible to remove the COS from liquid hydrocarbon feedstocks containing propylene, so that the residual COS content is less than 30 ppb.
The purification process of the present invention for removing the COS from liquid hydrocarbon feedstocks including propylene and containing from 1 to 70 ppm of COS, comprises passing the liquid hydrocarbon feedstocks over an absorbent material comprising nickel deposited on a support, the nickel being present in the form of nickel oxide and in the form of metallic nickel, and the quantity of metallic nickel being from 35 to 70% by weight of the total nickel.
It has been found, unexpectedly, that by passing a liquid hydrocarbon feedstock, in the preferred case a propylene feedstock intended for polymerization, over an absorbent material consisting of from 40 to 70% by weight of nickel deposited on a support representing from 60 to 30% by weight of the absorbent material, the nickel being present to the extent of from 35 to 70% by weight in the form of metallic nickel, the purified feedstock obtained corresponds to the purity conditions required for polymerization in the presence of the latest generation of Ziegler catalyst, i.e. the feedstock has a COS content not exceeding 30 ppb.
Silica, silico-aluminas, alumina, keiselguhr and other similar materials can be used as the support on which the nickel is deposited.
The nickel can be deposited on the support by any of the methods which are well known to those skilled in the art, for example by dissolving nickel nitrate in water, mixing the solution with the support and precipitating the nickel, for example in the form of nickel carbonate, and then washing, drying and calcining the precipitate. The nickel deposited in this way is then partially reduced by means of hydrogen so as to form metallic nickel in a quantity of from 35 to 70% of the total quantity of nickel deposited, the remainder being in the form of nickel oxide.
In general, the size of the nickel crystallites after reduction is from 10 to 200A. The size of the nickel crystallites depends inter alia on the degree of reduction which is carried out. In fact, if the degree of reduction is increased, the size of the crystallites is increased but the absorbent material obtained no longer has such good properties. On the other hand, if the degree of reduction is too low, the crystallites still have good dimensions but the quantity of nickel available in this case is too small to ensure successful purification of the feedstock.
The specific surface area of the absorbent material obtained after reduction is generally from 100 to 200 mCg.
The particle size of the absorbent material depends in particular on the pressure loss which is allowed in the reactor. It has been noted, however, that it is advantageous to use the absorbent material in finely divided form. In general, the particle size of the material does not exceed about 3 mm and is most frequently from 1 to 2.5 mm.
In general, the liquid hydrocarbon feedstocks treated contain more than 75% of propylene, more particularly up to from 85 to 99% of propylene, the COS content normally being of the order of from 1 to 10 ppm. If feedstocks having a higher COS content, i.e. up to 500 ppm, are to be treated, they are first subjected to a treatment with an aminated solvent, such as monoethanolamine, so as to reduce the COS content to an appropriate value, i.e. less than 70 ppm.
In one embodiment of the process of the present invention, the liquid hydrocarbon feedstock containing propylene is passed over the absorbent material of the present invention at a temperature generally of from O"C to 902C and at a sufficient pressure to keep the medium in the liquid phase.
The liquid hourly space velocity, or LHSV, at which the feedstock is passed over is generally from 0.1 to 20 and preferably from 0.2 to 15.
The examples which follow are given in order to provide a better illustration of the process of the present invention, but without thereby restricting its scope.
Example 1
A liquid hydrocarbon feedstock containing 99% of propylene and having a residual COS content of 2.7 ppm was passed over an absorbent material consisting of 43.3% by weight of silica as the support, on which nickel was deposited, the nickel being present in the form of NiO to the extent of 34 wt % and in the form of metallic Ni to the extent of 22.7 wt %.
Before reduction, the absorbent material contained about 49% by weight of nickel.
The absorbent material was finely divided so as to give an average particle size of about 1 mm and the specific surface area of the absorbent material was 145 m2/g.
The feedstock was passed over the absorbent material at ambient temperature, at a sufficient pressure to keep the feedstock in the liquid phase, and at an LHSV of 5.
A sample of the purified feedstock was taken and the COS content determined. The COS content was 18 ppb.
Example 2
Liquid hydrocarbon feedstocks containing 99% of propylene and having different residual COS contents were passed over the same absorbent material as in Example 1.
The nickel containing absorbent material had a nickel content of about 49% by weight. The absorbent material was finely divided so as to give an average particle size of about 1 mm. The specific area of the absorbent material was about 145 m2/g.
The feedstocks were passed over the nickel containing material under various operating conditions, which are specified in Table 1.
The pressure was 14 bars. As can be seen from the results, the purified feedstocks each had a COS content lower than 30 ppb, even when the feed contains water, which is known to be detrimental.
TABLE I
LHSV Temperature of H20 content COS
the bed (0C) (ppm) in out
ppm ppb
4.95 20 13 1.8 22
5.05 25 8 4.5 20
4.8 23 8 3.1 18
9.3 16 14 1.85 15
15.05 15 14 1.3 24
Example 3
Liquid hydrocarbon feedstocks containing 95.6% propylene, 3.8% propane and 0.6% C4, the water content of each of which was less than 10 ppm, and having different residual COS contents were passed over the same absorbent as described in Examples 1 and 2. This example is given to illustrate the activity of the catalyst over a long period of time.
The feedstocks were passed at a pressure of 14 bar over a bed of nickel containing 2 litres of absorbent material.
The other operating conditions such as LHSV and the temperature of the bed are specified in Table II.
TABLE II
Day Temperature of LHSV COS the bed { C) in out
ppm ppb
1 14 9.4 2.8 25
5 9 9.3 1.4 23
12 6 9.7 4.2 21
19 7 9.7 2.55 20
25 10 9.7 3.0 11
34 7 9.75 1.9 16
39 2 9.85 1.85 23
52 9 9.6 0.85 20
58 3 10.15 0.8 22
68 11 9.65 2.2 20
82 6 9.75 1.95 15
88 1 9.8 0.8 15
This example shows that even after 88 days the activity of the catalyst is always very high.
Claims (11)
1. A process for the purification of a liquid hydrocarbon feedstock including propylene and containing from 1 to 70 ppm of COS, in order to remove the carbonyl sulphide therefrom, which process comprises passing the liquid hydrocarbon feedstock over an absorbent material comprising nickel which is deposited on a support, the nickel being present in the form of nickel oxide and in the form of metallic nickel, and the quantity of metallic nickel being from 35 to 70% by weight of the total nickel content.
2. A process according to Claim 1, wherein the absorbent material consists of from 40 to 70% by weight of nickel which is deposited on the support which constitutes from 60 to 30% by weight of the absorbent material, the nickel being present to the extent of from 35 to 70% by weight in the form of metallic nickel, and the remainder of the nickel being in the form of nickel oxide.
3. A process according to Claim 1 or Claim 2, wherein the specific surface area of the absorbent material is from 100 to 200 m2/g.
4. A process according to any one of Claims 1 to 3, wherein the absorbent material is finely divided and the particle size of the absorbent material does not exceed 3 mm.
5. A process according to Claim 4, wherein the particle size of the absorbent material is from 1 to 2.5 mm.
6. A process according to any foregoing Claim, wherein the liquid hydrocarbon feedstock is passed over the absorbent material at a temperature of from 0 C to 900C, at a sufficient pressure to keep the feedstock in the liquid phase, and at a liquid hourly space velocity of from 0.1 to 20.
7. A process according to Claim 6, wherein the liquid hourly space velocity is from 0.2 to 15.
8. A process according to any foregoing Claim, wherein the liquid hydrocarbon feedstock contains more than 75% propylene.
9. A process for the purification of a liquid hydrocarbon feedstock containing more than 95% propylene and containing from 1 to 70 ppm of carbonyl sulphide, in order to remove the carbonyl sulphide therefrom, which process comprises passing the feedstock over an absorbent material consisting of from 40 to 70% by weight of nickel which is deposited on a support which constitutes 60 to 30% by weight of the absorbent material, the nickel being present to the extent of from 35 to 70% by weight in the form of metallic nickel and the remainder of the nickel being in the form of nickel oxide, the absorbent material having a specific surface area of from 100 to 200 mVg, the feedstock being passed over the absorbent
material at a temperature of from 0 C to 900C and at a sufficient pressure to keep the feedstock in the
liquid phase, and at an LHSV of from 0.1 to 20.
10. A process for the purification of a liquid hydrocarbon feedstock substantially as hereinbefore described in any one of Examples 1 to 3.
11. Purified hydrocarbon feedstocks having a low carbonyl sulphide content whenever obtained by a process as claimed in any one of Claims 1 to 10.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| LU85487A LU85487A1 (en) | 1984-07-27 | 1984-07-27 | PROCESS FOR PURIFYING LIQUID HYDROCARBON FEEDSTOCKS |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| GB8518304D0 GB8518304D0 (en) | 1985-08-29 |
| GB2162194A true GB2162194A (en) | 1986-01-29 |
| GB2162194B GB2162194B (en) | 1988-05-05 |
Family
ID=19730298
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB08518304A Expired GB2162194B (en) | 1984-07-27 | 1985-07-19 | Process for removing carbonyl sulphide from liquid hydro-carbon feedstocks |
Country Status (16)
| Country | Link |
|---|---|
| JP (1) | JPS6176425A (en) |
| KR (1) | KR930011063B1 (en) |
| AT (1) | AT393132B (en) |
| AU (1) | AU4535885A (en) |
| BE (1) | BE902942A (en) |
| DE (1) | DE3526153C2 (en) |
| ES (1) | ES8608463A1 (en) |
| FR (1) | FR2568262B1 (en) |
| GB (1) | GB2162194B (en) |
| IT (1) | IT1187696B (en) |
| LU (1) | LU85487A1 (en) |
| MX (1) | MX168045B (en) |
| NL (1) | NL194334C (en) |
| NO (1) | NO173782C (en) |
| PT (1) | PT80877B (en) |
| SU (1) | SU1447274A3 (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0302771A1 (en) * | 1987-08-07 | 1989-02-08 | Institut Français du Pétrole | Process for the simultaneous removal of arsenic and carbon oxysulfide from a cut of unsaturated hydrocarbons in the liquid phase |
| EP0308569A1 (en) * | 1987-09-24 | 1989-03-29 | Fina Research S.A. | Process for removing arsine from light olefin-containing hydrocarbon feedstocks |
| CN1053883C (en) * | 1993-09-20 | 2000-06-28 | 芬娜研究有限公司 | Process for the removal of arsine carbonyl sulphide from hydrocarbon feedstocks containing light olefin(s) |
| WO2005028403A1 (en) * | 2003-09-23 | 2005-03-31 | Engelhard Corporation | Process for the removal of sulfur compounds from hydrocarbon feedstocks |
| EP2199269A1 (en) | 2008-12-22 | 2010-06-23 | Total Petrochemicals Research Feluy | Method to purify olefin-containing hydrocarbon feedstocks |
| US7780846B2 (en) | 2004-09-01 | 2010-08-24 | Sud-Chemie Inc. | Sulfur adsorbent, desulfurization system and method for desulfurizing |
| US8323603B2 (en) | 2004-09-01 | 2012-12-04 | Sud-Chemie Inc. | Desulfurization system and method for desulfurizing a fuel stream |
| WO2014009159A3 (en) * | 2012-07-13 | 2014-03-06 | Evonik Industries Ag | Sulfur adsorption upstream of oligomerization plants |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE1004214A3 (en) * | 1990-03-23 | 1992-10-13 | Fina Research | Process to remove loads of hydride antimony oil liquids |
| US5324420A (en) * | 1990-07-27 | 1994-06-28 | Exxon Chemical Patents Inc. | Sulfur removal from hydrocarbons with nickel containing catalyst |
| ATE165803T1 (en) * | 1993-09-15 | 1998-05-15 | Fina Research | METHOD FOR POLYMERIZING OLEFINS |
| RU2152421C1 (en) * | 1994-05-19 | 2000-07-10 | Мицуи Петрокемикал Индастриз Лтд. | METHOD OF PURIFICATION OF α-OLEFINS FOR POLYMERIZATION AND METHOD OF SYNTHESIS OF POLY-α-OLEFINS |
| EP2006012A1 (en) * | 2007-06-22 | 2008-12-24 | Total Petrochemicals Research Feluy | Process for the polymerisation of olefins |
| EP2006011A1 (en) * | 2007-06-22 | 2008-12-24 | Total Petrochemicals Research Feluy | Process for reducing carbon monoxide in olefin-containing hydrocarbon feedstocks |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE636323A (en) * | ||||
| US2756182A (en) * | 1955-01-12 | 1956-07-24 | Exxon Research Engineering Co | Desulfurization of hydrocarbons with an iron group carbonyl impregnated on an adsorbent |
| FR1483583A (en) * | 1965-06-19 | 1967-06-02 | Basf Ag | Process for the removal of carbon oxysulfide from liquid hydrocarbon mixtures |
| GB1240134A (en) * | 1968-11-27 | 1971-07-21 | British Petroleum Co | Desulphurisation process |
| DE2447910A1 (en) * | 1974-10-08 | 1976-04-22 | Basf Ag | Removal of sulphur cpds from gaseous of liquid hydrocarbons - by contact with basic carbonates of transition metals, reduced in hydrogen |
| LU85309A1 (en) * | 1984-04-13 | 1985-11-27 | Labofina Sa | PROCESS FOR REMOVING CARBONYL SULFIDE FROM LIQUID HYDROCARBON FEEDSTOCKS |
-
1984
- 1984-07-27 LU LU85487A patent/LU85487A1/en unknown
-
1985
- 1985-07-19 BE BE0/215384A patent/BE902942A/en not_active IP Right Cessation
- 1985-07-19 IT IT21650/85A patent/IT1187696B/en active
- 1985-07-19 GB GB08518304A patent/GB2162194B/en not_active Expired
- 1985-07-22 DE DE3526153A patent/DE3526153C2/en not_active Expired - Fee Related
- 1985-07-23 NL NL8502109A patent/NL194334C/en not_active IP Right Cessation
- 1985-07-24 NO NO852939A patent/NO173782C/en not_active IP Right Cessation
- 1985-07-24 FR FR8511344A patent/FR2568262B1/en not_active Expired
- 1985-07-25 AU AU45358/85A patent/AU4535885A/en not_active Abandoned
- 1985-07-26 SU SU853932563A patent/SU1447274A3/en active
- 1985-07-26 ES ES545570A patent/ES8608463A1/en not_active Expired
- 1985-07-26 MX MX206114A patent/MX168045B/en unknown
- 1985-07-26 PT PT80877A patent/PT80877B/en not_active IP Right Cessation
- 1985-07-26 AT AT2221/85A patent/AT393132B/en not_active IP Right Cessation
- 1985-07-26 JP JP60165615A patent/JPS6176425A/en active Granted
- 1985-07-27 KR KR1019850005461A patent/KR930011063B1/en not_active Expired - Fee Related
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0302771A1 (en) * | 1987-08-07 | 1989-02-08 | Institut Français du Pétrole | Process for the simultaneous removal of arsenic and carbon oxysulfide from a cut of unsaturated hydrocarbons in the liquid phase |
| FR2619120A1 (en) * | 1987-08-07 | 1989-02-10 | Inst Francais Du Petrole | PROCESS FOR THE JOINT ELIMINATION OF ARSENIC AND CARBON OXYSULFIDE FROM A CUP OF LIQUID PHASE UNSATURATED HYDROCARBONS |
| EP0308569A1 (en) * | 1987-09-24 | 1989-03-29 | Fina Research S.A. | Process for removing arsine from light olefin-containing hydrocarbon feedstocks |
| AU654260B2 (en) * | 1987-09-24 | 1994-11-03 | Labofina S.A. | Process for removing arsine |
| CN1053883C (en) * | 1993-09-20 | 2000-06-28 | 芬娜研究有限公司 | Process for the removal of arsine carbonyl sulphide from hydrocarbon feedstocks containing light olefin(s) |
| TWI403361B (en) * | 2003-09-23 | 2013-08-01 | Engelhard Corp | Process for the removal of sulfur compounds from hydrocarbon feedstocks |
| RU2370481C2 (en) * | 2003-09-23 | 2009-10-20 | БАСФ КАТАЛИСТС ЭлЭлСи | Method of removing sulphur compounds from hydrocarbon material |
| CN102643154A (en) * | 2003-09-23 | 2012-08-22 | 英格哈得公司 | Process for the removal of sulfur compounds from hydrocarbon feedstocks |
| WO2005028403A1 (en) * | 2003-09-23 | 2005-03-31 | Engelhard Corporation | Process for the removal of sulfur compounds from hydrocarbon feedstocks |
| EP2463260A3 (en) * | 2003-09-23 | 2014-01-08 | BASF Corporation | Process for the removal of sulfur compounds from hydrocarbon feedstocks |
| US9011675B2 (en) | 2003-09-23 | 2015-04-21 | Basf Corporation | Process for the removal of sulfur compounds from hydrocarbon feedstocks |
| US7780846B2 (en) | 2004-09-01 | 2010-08-24 | Sud-Chemie Inc. | Sulfur adsorbent, desulfurization system and method for desulfurizing |
| US8323603B2 (en) | 2004-09-01 | 2012-12-04 | Sud-Chemie Inc. | Desulfurization system and method for desulfurizing a fuel stream |
| EP2199269A1 (en) | 2008-12-22 | 2010-06-23 | Total Petrochemicals Research Feluy | Method to purify olefin-containing hydrocarbon feedstocks |
| WO2010072789A1 (en) | 2008-12-22 | 2010-07-01 | Total Petrochemicals Research Feluy | Method to purify olefin-containing hydrocarbon feedstocks |
| US10493438B2 (en) | 2008-12-22 | 2019-12-03 | Total Research & Technology Feluy | Method to purify olefin-containing hydrocarbon feedstocks |
| WO2014009159A3 (en) * | 2012-07-13 | 2014-03-06 | Evonik Industries Ag | Sulfur adsorption upstream of oligomerization plants |
Also Published As
| Publication number | Publication date |
|---|---|
| ES8608463A1 (en) | 1986-07-16 |
| AT393132B (en) | 1991-08-26 |
| NO173782C (en) | 1994-02-02 |
| JPH0552294B2 (en) | 1993-08-05 |
| NL194334B (en) | 2001-09-03 |
| DE3526153A1 (en) | 1986-01-30 |
| PT80877B (en) | 1987-11-30 |
| IT8521650A0 (en) | 1985-07-19 |
| NO852939L (en) | 1986-01-28 |
| DE3526153C2 (en) | 1995-03-09 |
| AU4535885A (en) | 1986-01-30 |
| LU85487A1 (en) | 1986-02-12 |
| JPS6176425A (en) | 1986-04-18 |
| NL194334C (en) | 2002-01-04 |
| KR930011063B1 (en) | 1993-11-20 |
| ATA222185A (en) | 1991-01-15 |
| ES545570A0 (en) | 1986-07-16 |
| MX168045B (en) | 1993-04-29 |
| GB8518304D0 (en) | 1985-08-29 |
| FR2568262B1 (en) | 1988-04-01 |
| BE902942A (en) | 1986-01-20 |
| GB2162194B (en) | 1988-05-05 |
| IT1187696B (en) | 1987-12-23 |
| KR860001177A (en) | 1986-02-24 |
| PT80877A (en) | 1985-08-01 |
| NO173782B (en) | 1993-10-25 |
| NL8502109A (en) | 1986-02-17 |
| SU1447274A3 (en) | 1988-12-23 |
| FR2568262A1 (en) | 1986-01-31 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PCNP | Patent ceased through non-payment of renewal fee |
Effective date: 20040719 |