Liquid phase distillate dewaxing
Hydrocarbon feeds can be hydrotreated in a continuous gas-phase environment and then dewaxed in a liquid-continuous reactor. The liquid-continuous reactor can advantageously be operated in a manner that avoids the need for a hydrogen recycle loop. A contaminant gas can be added to the hydrogen input for the liquid-continuous reactor to modify the hydrogen consumption in the reactor.
1. A method for producing a dewaxed distillate product, comprising:
contacting a feedstock having a T95 boiling point of about 440° C. or less with a hydrotreating catalyst under effective hydrotreating conditions in a hydrotreatment reactor comprising a continuous gas phase to produce a hydrotreated effluent;
separating the hydrotreated effluent into at least a hydrotreated liquid product having a cloud point and a gas-phase product comprising H 2 and H 2 S;
mixing the hydrotreated liquid product with a hydrogen-containing stream and at least a portion of the gas-phase product to produce a hydrotreated dewaxing input stream comprising an H 2 S content of about 0.1 mol % to 10 mol % of a total gas content in the hydrotreated dewaxing input; and
contacting the hydrotreated dewaxing input stream with a dewaxing catalyst under effective catalytic dewaxing conditions in a liquid-continuous reactor to form a dewaxed effluent comprising a dewaxed distillate product having a reduced level of aromatics saturation compared to a level of aromatics saturation under otherwise identical dewaxing conditions but with H 2 S content below about 0.1 mol %,
wherein the liquid-continuous reactor comprises a gas phase that is less than about 10% of the reactor volume and the dewaxed effluent has a cold flow property that is at least about 9° F. (about 5° C.) less than a corresponding cold flow property of the feedstock, and wherein the cold flow property comprises one or more of a cloud point, a pour point, and a cold filter plugging point.
2. The method of claim 1 , wherein a ratio of the hydrogen-containing stream to the at least a portion of the gas-phase product is adjusted to reduce the hydrogen consumption in the liquid-continuous reactor to about 20 Nm 3 /m 3 or less.
3. The method of claim 1 , wherein at least a portion of the dewaxed effluent from the liquid-continuous reactor is recycled and mixed with the hydrotreated liquid product prior to said mixing with the hydrogen-containing stream.
4. The method of claim 1 , wherein at least a portion of the dewaxed effluent from the liquid-continuous reactor is mixed with a second hydrogen-containing stream and recycled as an input stream to the liquid-continuous reactor.
5. The method of claim 1 , wherein the contacting in the liquid continuous reactor comprises:
removing at least a portion of the hydrotreated dewaxing input stream from the liquid-continuous reactor;
dissolving hydrogen in the removed portion; and
passing the removed portion containing the dissolved hydrogen back into the liquid-continuous reactor.
6. The method of claim 1 , wherein the effective catalytic dewaxing conditions include a temperature from about 500° F. (about 260° C.) to about 750° F. (about 399° C.), a total pressure from about 200 psig (about 1.4 MPag) to about 2250 psig (about 15.5 MPag), and an LHSV from about 0.2 hr −1 to about 15 hr −1 .
7. The method of claim 1 , wherein effective hydrotreating conditions include a temperature from about 500° F. (about 260° C.) to about 800° F. (about 425° C.), a total pressure from about 200 psig (about 1.4 MPag) to about 3000 psig (about 20.7 MPag), an LHSV from about 0.2 hr −1 to about 15 hr −1 , and a hydrogen treat gas rate from about 500 scf/bbl (about 85 Nm 3 /m 3 ) to about 10000 scf/bbl (about 1700 Nm 3 /m 3 ).
8. The method of claim 1 , wherein the dewaxing catalyst comprises a molecular sieve and a supported metal, wherein the molecular sieve comprises ZSM-5, ZSM-22, ZSM-23, ZSM-35, ZSM-48, or a combination thereof.
9. The method of claim 1 , further comprising:
separating the hydrotreated effluent into at least a hydrotreated liquid product, a first gas-phase product, and a second gas-phase product, wherein said first and second gas-phase product comprise at least H 2 and H 2 S;
providing the first gas-phase product for mixing with the hydrotreated liquid product;
recovering hydrogen from the second gas-phase product; and
recycling the recovered hydrogen.
10. The method of claim 1 , wherein the hydrotreated dewaxing input stream has an H 2 S content from about 0.5 mol % to about 10 mol % of the total gas in the hydrotreated dewaxing input stream.
11. The method of claim 1 , wherein the dewaxed effluent has an aromatics content of at least about 50% of an aromatics content of the hydrotreated effluent.
12. A method for producing a dewaxed distillate product, comprising:
providing a feedstock having a cloud point of at least about 15° F. (about −4° C.), having a T95 boiling point of about 440° C. or less, and having a first aromatics content;
contacting the feedstock with a hydrotreating catalyst under effective hydrotreating conditions in a hydrotreatment reactor comprising a continuous gas phase to produce a hydrotreated effluent;
separating the hydrotreated effluent into at least a hydrotreated liquid product and a gas-phase product comprising H 2 and H 2 S;
mixing the hydrotreated liquid product with a hydrogen containing stream and at least a portion of the gas-phase product to form a hydrotreated dewaxing input stream comprising an H 2 S content of about 0.1 mol % to 10 mol % of a total gas content in the hydrotreated dewaxing input; and
contacting the hydrotreated dewaxing input stream with a dewaxing catalyst under effective catalytic dewaxing conditions in a liquid-continuous reactor to form a dewaxed effluent comprising a dewaxed distillate product having a reduced level of aromatics saturation compared to a level of aromatics saturation under otherwise identical dewaxing conditions but with H 2 S content below about 0.1 mol %,
wherein the liquid-continuous reactor comprises a gas phase that is less than about 10% of the reactor volume, the dewaxed effluent has a second aromatics content that is at least about 50% of the first aromatics content, and the dewaxed effluent has a cloud point that is at least about 9° F. (5° C.) lower than the cloud point of the feedstock.
13. The method of claim 12 , wherein the second aromatics content is at least about 65% of the first aromatics content.
14. The method of claim 12 , wherein the effective catalytic dewaxing conditions include a temperature from about 500° F. (about 260° C.) to about 750° F. (about 399° C.), a total pressure from about 200 psig (about 1.4 MPag) to about 2250 psig (about 15.5 MPag), and an LHSV from about 0.2 hr −1 to about 15 hr −1 .
15. The method of claim 12 , wherein the effective hydrotreating conditions include a temperature from about 500° F. (about 260° C.) to about 800° F. (about 425° C.), a total pressure from about 200 psig (about 1.4 MPag) to about 3000 psig (about 20.7 MPag), an LHSV from about 0.2 hr −1 to about 15 hr −1 , and a hydrogen treat gas rate from about 500 scf/bbl (about 85 Nm 3 /m 3 ) to about 10000 scf/bbl (about 1700 Nm 3 /m 3 ).
16. The method of claim 12 , wherein the hydrotreated dewaxing input stream has an H 2 S content from about 0.5 mol % to about 10 mol % of the total gas in the hydrotreated dewaxing input stream.
17. The method of claim 12 , wherein the dewaxing catalyst comprises ZSM-23, ZSM-48, ZSM-5, or a combination thereof.
18. The method of claim 12 , further comprising:
separating the hydrotreated effluent into at least a hydrotreated liquid product, a first gas-phase product and a second gas-phase product wherein said first and second gas-phase product comprise at least H 2 and H 2 S;
providing the first gas-phase product for mixing with the hydrotreated liquid product;
recovering hydrogen from the second gas-phase product; and
recycling the recovered hydrogen.
19. The method of claim 12 , wherein the contacting in the liquid-continuous reactor comprises:
removing at least a portion of the hydrotreated dewaxing input stream from the liquid-continuous reactor;
dissolving hydrogen in the removed portion; and
passing the removed portion containing the dissolved hydrogen back into the liquid-continuous reactor.
20. The method of claim 2 , wherein hydrotreated effluent has an aromatics content of at least about 10 wt %.