Use of phosphorus modified molecular sieves in conversion of organics to olefins

1. A process of making light olefins from an oxygen containing, halogenide containing or sulphur containing organic feedstock, comprising:

selecting a zeolite in the H + or NH 4 + form that has an initial Si:Al atomic ratio of 100 or less, wherein the zeolite is an MFI or MEL;

steaming the zeolite at a temperature ranging from 480° C. to 760° C. for 0.01-200 hours;

after steaming, leaching the zeolite with an aqueous acid solution at conditions effective to remove a substantial part of Al from the zeolite;

after leaching, introducing phosphorus (P) to the zeolite with an aqueous solution containing a source of P at conditions effective to introduce at least 0.05 wt % to 7 wt % of P, obtaining a first P modified zeolite;

contacting the oxygen containing, halogenide containing, or sulphur containing organic feedstock in a first reactor with a first catalyst comprising the first P modified zeolite at conditions effective to convert at least a portion of the feedstock to form a first reactor effluent comprising light olefins and a heavy hydrocarbon fraction;

sending the first reactor effluent to a first fractionator and separating the light olefins from the heavy hydrocarbon fraction in the first fractionator, wherein the light olefins from the first fractionator comprise ethylene and propylene, and wherein the separated light olefins are recovered;

contacting the separated heavy hydrocarbon fraction in a second reactor with a second catalyst made from a second P modified zeolite, wherein the second P modified zeolite catalyst is the same as the first P modified zeolite catalyst, at conditions effective to convert at least a portion of the heavy hydrocarbon fraction to light olefins; and

sending the second reactor effluent to a second fractionator and separating the light olefins from the heavy hydrocarbon fraction in the second fractionator, wherein the separated light olefins from the second fractionator comprise ethylene and propylene.

2. The process of claim 1 , wherein the first P modified zeolite has been made without direct addition of an organic template, and wherein the selected zeolite is steamed with a 5 to 100% stream volume, a pressure at from 10 to 100 kPa, and in the presence of 0 to 95% of an inert gas for 0.05 to 200 hours.

3. The process of claim 1 , wherein the second P modified zeolite has an initial Si:Al atomic ratio of 100 or less, and wherein the oxygen containing, halogenide containing, or sulphur containing organic feedstock that contacts the first catalyst is obtained from one or more of oil, coal, tar sand, shale, hydrocarbon residues, biomass, organic waste, natural gas, methanol, or methanol from a production of synthesis gas.

4. The process of claim 1 , wherein steaming the selected zeolite dealuminates the selected zeolite, and wherein the selected zeolite has an initial Si:Al atomic ratio ranging from 4-30.

5. The process of claim 1 , further comprising a step of dealumination of the second P modified zeolite by steaming, followed by a leaching step.

6. The process of claim 1 , wherein the first P modified zeolite is subjected to a washing step, a drying step, or a combination thereof prior to calcining.

7. The process of claim 1 , wherein the first catalyst and the second catalyst are different.

8. The process of claim 1 , wherein the second P modified zeolite is made by a process comprising:

selecting an MFI zeolite in the H + or NH 4 + form that has an initial Si:Al atomic ratio of 100 or less;

steaming the selected MFI zeolite at a temperature ranging from 480° C. to 760° C. for 0.01-200 h; and

after steaming, leaching the selected MFI zeolite with an aqueous acid solution at conditions effective to remove an amount of Al from the selected MFI zeolite before introducing P into the selected MFI zeolite and calcining the selected MFI zeolite.

9. The process of claim 8 , wherein the second P modified zeolite is subjected to a washing step, a drying step, or a combination thereof after P is added and prior to calcining.

10. The process of claim 8 , wherein the light olefins are recovered from the second fractionator;

wherein heavy hydrocarbons having 4 or more carbon atoms from the second reactor and second fractionator are recycled to the second reactor and are mixed with heavy hydrocarbons from an additional first reactor effluent that has been separated from the light olefin fraction by the first fractionator; and

wherein the heavy hydrocarbons from the first and second fractionators are sent to the second reactor for additional processing.

11. The process of claim 8 , wherein the heavy hydrocarbons from the second fractionator having 4 or more carbon atoms are sent to a third fractionator to remove and recover a heavy hydrocarbon stream comprising C 6 + hydrocarbons prior to recycling a separated C 4 -C 5 fraction from the third fractionator to the second reactor; and

wherein separated C 4 -C 5 fraction from the third fractionator is recycled with heavy hydrocarbons from an additional effluent from the first reactor that has been separated from the light olefin fraction by the first fractionator, and wherein the heavy hydrocarbons from the first and second fractionators are sent to the second reactor for additional proceeding.

12. The process of claim 10 , wherein in order to adjust a propylene to ethylene production ratio for the process, ethylene is recycled to the second reactor; and

wherein the recycled ethylene is from a source selected from the first fractionator, the second fractionator, from both the first fractionator and the second fractionator, or from a common recovery section.

13. The process of claim 10 , wherein in order to adjust a propylene to ethylene ratio for the process, ethylene is recycled to the first reactor; and

wherein the recycled ethylene is from a source selected from the first fractionator, the second fractionator, from both the first fractionator and the second fractionator, or from a common recovery section.

14. The process of claim 8 , wherein the oxygen containing, halogenide containing, or sulphur containing organic feedstock is obtained from one or more of oil, coal, tar sand, shale, hydrocarbon residues, biomass, organic waste, natural gas, methanol, or methanol from a production of synthesis gas, and wherein the produced and separated ethylene is further polymerized with one or more comonomers.

15. The process of claim 8 , wherein the oxygen containing, halogenide containing, or sulphur containing organic feedstock is obtained from one or more of oil, coal, tar sand, shale, hydrocarbon residues, biomass, organic waste, natural gas, methanol, or methanol from a production of synthesis gas, and wherein the produced and separated propylene is further polymerized with one or more comonomers.

16. A process of making light olefins from an oxygen containing, halogenide containing, sulphur containing organic feedstock, comprising:

selecting a zeolite in the H + or NH 4 + form that has an initial Si:Al atomic ratio of 100 or less, wherein the zeolite is MFI or MEL;

steaming the zeolite at a temperature ranging from 480° C. to 760° C. for 0.01-200 hours:

after steaming, leaching the zeolite with an aqueous acid solution at conditions effective to remove a substantial part of Al from the zeolite;

after leaching, introducing phosphorus (P) to the zeolite with an aqueous solution containing a source of P at conditions effective to introduce at least 0.05 wt % to 7 wt % of P, obtaining a first P modified zeolite;

contacting the oxygen containing, halogenide containing, or sulphur containing organic feedstock in a XTO reactor having an inlet temperature of from 540° C. to 580° C. and an olefin partial pressure of from 0.1 to 2 bars with the first P modified zeolite conditions effective to convert at least a portion of the feedstock to form a XTO reactor effluent comprising light olefins and a heavy hydrocarbon fraction;

sending the XTO reactor effluent to a first fractionator and separating the light olefins from the heavy hydrocarbon fraction in the first fractionator, wherein the light olefins from the first fractionator comprise ethylene and propylene, and wherein the separated light olefins are recovered;

contacting the separated heavy hydrocarbon fraction in an OCP reactor having an inlet temperature of from 540° C. to 590° C., and olefin partial pressure of from 0.1 to 2 bars, and a LHSV of from 1 to 30 hr −1 , with

a second P modified zeolite, wherein the second P modified zeolite catalyst is the same as the first P modified zeolite catalyst, at conditions effective to convert at least a portion of the heavy hydrocarbon fraction to light olefins; and

sending the OCP reactor effluent to a second fractionator and separating the light olefins from the heavy hydrocarbon fraction in the second fractionator, wherein the separated light olefins from the second fractionator comprise ethylene and propylene.

17. The process of claim 16 , wherein the light olefins are recovered from the second fractionator;

wherein heavy hydrocarbons having 4 or more carbon atoms from the OCP reactor and second fractionator are recycled along with heavy hydrocarbons from an additional effluent from the XTO reactor that has been separated from the light olefin fraction by the first fractionator; and

wherein the heavy hydrocarbons from the XTO reactor and second fractionator are sent to the OCP reactor for additional processing.

18. The process of claim 16 , wherein the light olefins are recovered from the second fractionator;

wherein the heavy hydrocarbons having 4 or more carbon atoms from the second fractionator are sent to a third fractionator to remove a heavy hydrocarbon stream comprising C 6 + hydrocarbons prior to recycling a separated C 4 -C 5 fraction from the third fractionator to the OCP reactor;

wherein C 4 -C 5 fraction from the third fractionator is recycled with heavy hydrocarbons from an additional effluent from the XTO reactor that has been separated from the light olefin fraction by the first fractionator, and wherein the heavy hydrocarbons from the first and third fractionators are sent to the OCP reactor for additional processing; and

wherein the second P modified zeolite has an initial Si:Al atomic ratio of 100 or less.

19. The process of claim 1 , wherein the first catalyst and the second catalyst are the same.

20. The process of claim 1 , wherein the aqueous acid solution comprises:

an organic acid selected from a group consisting of citric acid, formic acid, oxalic acid, tartaric acid, malonic acid, succinic acid, glutaric acid, adipic acid, maleic acid, phthalic acid, isophthalic acid, fumaric acid, nitrilotriacetic acid, hydroxyethylenediaminetriacetic acid, ethylenediaminetetracetic acid, trichloroacetic acid, trifluoroacetic acid, a salt thereof, or combinations thereof; or

an inorganic acid selected from a group consisting of nitric acid, hydrochloric acid, methansulfuric acid, phosphoric acid, phosphonic acid, sulfuric acid, a salt thereof, or combinations thereof.

21. The process of claim 1 , wherein the selected zeolite is an MFI.

22. The process of claim 1 , wherein the selected zeolite is an MEL.