# US 2021/0277313 A1 · Heating and cooling system for high pressure processing system

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- Number: US 2021/0277313 A1
- Document ID: US20210277313A1
- Status: Published application
- Kind: A1
- Application number: 16/491,715
- Filed: 2018-03-06
- Published: 2021-09-09
- Earliest claimed: 2017-03-07
- Assignees: Steeper Energy Aps
- Applicants: Steeper Energy Aps
- Inventors: Steen Brummerstedt IVERSEN; Andrew IRONSIDE; Claus Uhrenholt JENSEN
- Web page: https://patentgrep.com/patent/US20210277313A1

## CPC

- C10G 3/42: {Catalytic treatment}
- C10J 3/78: High-pressure apparatus
- C10G 1/02: by distillation
- C10G 1/08: with moving catalysts
- C10G 2300/1011: Biomass
- C10G 2300/4006: Temperature
- C10J 2300/0926: Slurries comprising bio-oil or bio-coke, i.e. charcoal, obtained, e.g. by fast pyrolysis of biomass
- C10J 2300/0986: Catalysts
- Y02P 20/129: Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
- Y02P 30/20: using bio-feedstock
- C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10J: PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES (synthesis gas from liquid or gaseous hydrocarbons C01B; underground gasification of minerals E21B43/295); CARBURETTING AIR OR OTHER GASES
- Y02P: CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS

## Abstract

The invention relates to a method of heating and cooling a feed mixture in a continuous high pressure process for transforming carbonaceous materials into liquid hydrocarbon products in a high pressure processing system adapted for processing a feed mixture at a temperature of at least 340° C. and a pressure of at least 150 bar, the high pressure processing system comprising a first and a second heat exchanger having a heat transfer fluid comprising at least 90% water, preferably at least 99% water circulating in the external part of the first and the second heat exchanger, the first heat exchanger comprising a cold internal input side and a hot internal output side, the second heat exchanger comprising a hot internal input side and a cold internal output side, the system further comprising a high pressure water heater and a high pressure water cooler between the first and the second heat exchanger, where the pressurized feed mixture is heated by feeding the feed mixture to the cold internal side of the first heat exchanger, heating and pressurizing the heat transfer fluid to a pressure of at least 240 bar and a temperature of at least 400° C. at the input to the hot external side of the first heat exchanger, where the cooled heat transfer fluid from the first heat exchanger having a temperature in the range 150 to 300° C. is further cooled to a temperature of 60 to 150° C. in the high pressure water cooler prior to entering the cold external side of the second heat exchanger, where the pressurized, heated and converted feed mixture is cooled to a temperature in the range 60 to 200° C. by feeding it to the internal side of the second heat exchanger, and where the partly heated heat transfer fluid is further heated in the high pressure water heater before entering the first heat exchanger.

## Claims

### Claim at position 1

1-16. (canceled)

### Claim 17

Method of heating and cooling a feed mixture in a continuous high pressure process for transforming carbonaceous materials into liquid hydrocarbon products in a high pressure processing system adapted for processing a feed mixture at a temperature of at least 340° C. and a pressure of at least 150 bar, the high pressure processing system comprising a first and a second heat exchanger having a heat transfer fluid comprising at least 90% water, preferably at least 99% water circulating in the external part of the first and the second heat exchanger, the first heat exchanger comprising a cold internal input side and a hot internal output side, the second heat exchanger comprising a hot internal input side and a cold internal output side, the system further comprising a high pressure water heater and a high pressure water cooler between the first and the second heat exchanger, where the pressurized feed mixture is heated by feeding the feed mixture to the cold internal side of the first heat exchanger, pressurizing and heating the heat transfer fluid to a pressure of at least 240 bar and a temperature of at least 400° C. at the input to the hot external side of the first heat exchanger, where the cooled heat transfer fluid from the first heat exchanger having a temperature in the range 150 to 300° C. is further cooled to a temperature of 60 to 150° C. in the high pressure water cooler prior to entering the cold external side of the second heat exchanger, where the pressurized, heated and converted feed mixture is cooled to a temperature in the range 60 to 250° C. by feeding it to the internal side of the second heat exchanger, and where the partly heated heat transfer fluid is further heated in the high pressure water heater before entering the first heat exchanger,
where the process is a continuous high pressure process for transforming carbonaceous materials into renewable hydrocarbons comprising:
Providing a carbonaceous material
Preparing a feed mixture at least comprising:
Carbonaceous material,
water,
homogeneous catalyst in the form of potassium or sodium
liquid organic compounds in the form of recycled water soluble organics and/or renewable hydrocarbons produced by the process
Pressurizing the feed mixture to a conversion pressure of at least 150 bars,
Heating the pressurized feed mixture to a conversion temperature of at least 340° C.,
Maintaining the pressurized feed mixture at conversion pressure and conversion temperature for a predefined time,
Cooling the feed mixture to a temperature in the range 60 to 200° C.,
Depressurizing the feed mixture to a pressure in the range 10 to 100 bar;
Separating the feed mixture into a hydrocarbon phase, water phase comprising dissolved salts and water soluble organics, and a gas phase and optionally a solid phase,
Separating the water phase into a dischargeable water phase and a residual phase comprising potassium and sodium salts and water soluble organic compounds;
At least partly introducing the residual phase to the feed preparation step,
where
Heat is extracted from converted feed mixture cooling step in the second heat exchanger and transferred to the heating step in the first heat exchanger using a heat transfer fluid comprising at least 90% water, preferably at least 99%, at a pressure of at least 240 bar and a temperature of at least 400° C. at the inlet to the first heat exchanger, and where the cooled heat transfer fluid from the first heat exchanger having a temperature in the range 150 to 300° C. is further cooled to a temperature of 60 to 150° C. in a high pressure water cooler prior to entering the cold external side of the second heat exchanger, where the pressurized, heated and converted feed mixture is cooled to a temperature in the range 80 to 200° C. by feeding it to the inner side of the heat exchanger tubes in said second heat exchanger, and where the partly heated heat transfer fluid from the cooling step in the second heat exchanger is further heated, before entering the hot external side of the heat transfer tubes in feed mixture heating step in the first heat exchanger.
where the pressure of the heat transfer fluid is at least 300 bar; preferably at least 320 bar, and where the temperature of the heat transfer fluid is at least 410° C.; preferably at least 430° C. such as in the range 420 to 450° C. before entering the first heat exchanger.

### Claim 18 (depends on 17)

Method according to claim 17, where the outlet temperature of the heat transfer fluid from the feed heating step in the first heat exchanger is at least 150° C.; preferably at least 200° C.

### Claim 19 (depends on 17)

Method according to claim 17, where the heat transfer fluid from the heating step in the first heat exchanger is cooled to a temperature of 80 to 150° C. before entering the cooling step in the second heat exchanger; preferably to a temperature of 100 to 140° C.

### Claim 20 (depends on 17)

Method according to claim 17, where the converted feed mixture is cooled to a temperature in the range 80 to 200° C. by feeding it to the internal side of the second heat exchanger; preferably the converted feed mixture is cooled to a temperature in the range 120 to 180° C. by feeding it to the internal side of the second heat exchanger.

### Claim 21 (depends on 17)

Method according to claim 17, wherein the feed mixture is heated to a temperature of at least 370° C. by the high pressure water in the first heat exchanger, preferably to a temperature in the range 390 to 425° C. by the high pressure water.

### Claim 22 (depends on 17)

Method according to claim 17, where the average velocity of the feed mixture in the heating step and the average velocity of the processed feed flow during the cooling are in the range 0.4 m/s to 5 m/s, preferably in the range 1.0 m/s to 3 m/s.

### Claim 23 (depends on 17)

Method according to claim 17, where the heat added to the high pressure water before entering the feed mixture heating step in the first heat exchanger is at least partly, preferably fully produced by combustion of byproducts from the process.

### Claim 24 (depends on 22)

Method according to claim 22, where the heat added to the high pressure water before entering the feed mixture heating step in the first heat exchanger is at least partly, preferably fully produced by combustion of gas from the process.

### Claim 25 (depends on 23)

Method according to claim 23, where the heat extracted by cooling the high pressure water between the feed mixture heating step in the first heat exchanger and the product cooling step in the second heat exchanger is transferred to a heat transfer medium comprising hot oil, pressurized water or steam, and distributed to the feed mixture preparation step and/or the recovery step and/or upgrading step.

### Claim 26 (depends on 23)

Method according to claim 23, where the heat extracted by cooling the high pressure water between the feed mixture heating step in the first heat exchanger and the product cooling step in the second heat exchanger is transferred to a heat transfer medium comprising hot oil, pressurized water or steam, is further heated by the offgas from the high pressure water heating step and distributed to the feed mixture preparation step and/or the recovery step and/or upgrading step.

### Claim 27 (depends on 24)

Method according to claim 24, where the heat extracted by cooling the high pressure water between the feed mixture heating step in the first heat exchanger and the product cooling step in the second heat exchanger or by cooling the offgas from the high pressure water heating step is at least partly used for district heating.

### Claim 28 (depends on 17)

Method according to claim 17, where the energy recovered in the hydrocarbon product to the total energy added to the system in the form of the carbonaceous material, electricity and heat is at least 65%; preferably at least 75%.

### Claim 29 (depends on 17)

Method according to claim 17, where the feed mixture being heated have a dry solid content of at 15% by weight such as a dry matter content of least 17.5 by weight; preferably the dry mater content is at least 20% by weight such as at least 25% by weight.

### Claim 30 (depends on 18)

Method according to claim 18, where the heat transfer fluid from the heating step in the first heat exchanger is cooled to a temperature of 80 to 150° C. before entering the cooling step in the second heat exchanger; preferably to a temperature of 100 to 140° C.

### Claim 31 (depends on 18)

Method according to claim 18, where the converted feed mixture is cooled to a temperature in the range 80 to 200° C. by feeding it to the internal side of the second heat exchanger; preferably the converted feed mixture is cooled to a temperature in the range 120 to 180° C. by feeding it to the internal side of the second heat exchanger.

### Claim 32 (depends on 19)

Method according to claim 19, where the converted feed mixture is cooled to a temperature in the range 80 to 200° C. by feeding it to the internal side of the second heat exchanger; preferably the converted feed mixture is cooled to a temperature in the range 120 to 180° C. by feeding it to the internal side of the second heat exchanger.

### Claim 33 (depends on 18)

Method according to claim 18, wherein the feed mixture is heated to a temperature of at least 370° C. by the high pressure water in the first heat exchanger, preferably to a temperature in the range 390 to 425° C. by the high pressure water.

### Claim 34 (depends on 19)

Method according to claim 19, wherein the feed mixture is heated to a temperature of at least 370° C. by the high pressure water in the first heat exchanger, preferably to a temperature in the range 390 to 425° C. by the high pressure water.

### Claim 35 (depends on 20)

Method according to claim 20, wherein the feed mixture is heated to a temperature of at least 370° C. by the high pressure water in the first heat exchanger, preferably to a temperature in the range 390 to 425° C. by the high pressure water.

### Claim 36 (depends on 18)

Method according to claim 18, where the average velocity of the feed mixture in the heating step and the average velocity of the processed feed flow during the cooling are in the range 0.4 m/s to 5 m/s, preferably in the range 1.0 m/s to 3 m/s.