METHOD AND DEVICE FOR FISCHER-TROPSCH SYNTHESIS

Abstract

A method for Fischer-Tropsch synthesis, the method including: 1) gasifying a raw material to obtain a crude syngas including H.sub.2, CO and CO.sub.2; 2) electrolyzing a saturated NaCl solution using a chloralkali process to obtain a NaOH solution, H.sub.2 and H.sub.2; 3) removing the CO.sub.2 in the crude syngas using the NaOH solution obtained in 2) to obtain a pure syngas; and 4) insufflating the H.sub.2 obtained in 2) to the pure syngas to adjust a mole ratio of CO/H.sub.2 in the pure syngas, and then introducing the pure syngas for Fischer-Tropsch synthesis reaction. A device for Fischer-Tropsch synthesis includes a gasification device, an electrolyzer, a first gas washing device, and a Fischer-Tropsch synthesis reactor.

Claims

1. A method for Fischer-Tropsch synthesis, the method comprising: 1) gasifying a raw material to obtain a crude syngas comprising H.sub.2, CO and CO.sub.2; 2) electrolyzing a saturated NaCl solution using a chloralkali process to obtain a NaOH solution, Cl.sub.2 and H.sub.2; 3) removing the CO.sub.2 in the crude syngas using the NaOH solution obtained in 2) to obtain a pure syngas; and 4) insufflating the H.sub.2 obtained in 2) into the pure syngas to adjust a mole ratio of CO/H.sub.2 in the pure syngas, and then using the pure syngas for Fischer-Tropsch synthesis reaction.

2. The method of claim 1, wherein in 3), the CO.sub.2 in the crude syngas is removed through a direct gas-liquid contact between the NaOH solution and the crude syngas to yield the pure syngas.

3. The method of claim 1, wherein in 3), the CO.sub.2 is first separated from the crude syngas to yield the pure syngas, and then the CO.sub.2 is absorbed using the NaOH solution.

4. The method of claim 1, wherein in 3), a remaining of the NaOH solution after absorbing CO.sub.2 in the crude syngas is condensed and crystallized as a by-product.

5. The method of claim 1, wherein in 3), a remaining of the NaOH solution after absorbing CO.sub.2 in the crude syngas is used for removing CO.sub.2 in an industrial waste gas or gases generated in other processes.

6. The method of claim 1, wherein in 4), a mole ratio of CO/H.sub.2 in the pure syngas is adjusted to 1:1.5 to 2.5.

7. The method of claim 2, wherein in 4), a mole ratio of CO/H.sub.2 in the pure syngas is adjusted to 1:1.5 to 2.5.

8. The method of claim 1, wherein in 1), the crude syngas comprises CO: 5-60 mol. %, H.sub.2: 5-45 mol. %, CO.sub.2: 5-30 mol. % on a dry basis, and the balance is impurity gases.

9. The method of claim 2, wherein in 1), the crude syngas comprises CO: 5-60 mol. %, H.sub.2: 5-45 mol. %, CO.sub.2: 5-30 mol. % on a dry basis, and the balance is impurity gases.

10. The method of claim 1, wherein in 1), the raw material is coal, biomass, heavy oil, natural gas, agroforestry waste, household waste, or a mixture thereof.

11. A device for Fischer-Tropsch synthesis, the device comprising: a gasification device comprising a syngas outlet end; an electrolyzer comprising a hydrogen outlet and a caustic soda solution outlet; a first gas washing device comprising a gas inlet, a gas outlet, and a washing solution inlet; and a Fischer-Tropsch synthesis reactor comprising a feed gas inlet; wherein the syngas outlet end of the gasification device is connected to the gas inlet of the first gas washing device via a pipe system; the gas outlet of the first gas washing device is connected to the feed gas inlet of the Fischer-Tropsch synthesis reactor via the pipe system; the hydrogen outlet of the electrolyzer is connected to the feed gas inlet of the Fischer-Tropsch synthesis reactor via the pipe system; and the caustic soda solution outlet of the electrolyzer is connected to the washing solution inlet of the first gas washing device via the pipe system.

12. The device of claim 11, further comprising a second gas washing device comprising a gas inlet and a gas outlet, wherein the caustic soda solution outlet of the electrolyzer is connected to the washing solution inlet of the second gas washing device via the pipe system, the gas inlet of the second gas washing device is connected to a pipe conveying flue gas or other CO.sub.2-containing gases, and the gas outlet of the second gas washing device is connected to a downstream process pipe or atmosphere.

13. The device of claim 11, wherein the gas washing device is a packed tower, a sieve plate tower or a spray tower.

14. The device of claim 12, wherein the gas washing device is a packed tower, a sieve plate tower or a spray tower.

15. A device for Fischer-Tropsch synthesis, the device comprising: a gasification device comprising a syngas outlet end, a gas inlet; an electrolyzer comprising a hydrogen outlet, a caustic soda solution outlet; a decarburization device comprising a crude syngas inlet, a pure syngas outlet, a carbon dioxide outlet; a first gas washing device comprising a washing solution inlet; and a Fischer-Tropsch synthesis reactor comprising a feed gas inlet; wherein the syngas outlet end of the gasification device is connected to the crude syngas inlet of the decarburization device via a pipe system the pure syngas outlet of the decarburization device is connected to the feed gas inlet of the Fischer-Tropsch synthesis reactor via the pipe system; the carbon dioxide outlet of the decarburization device is connected to the gas inlet of the first gas washing device via the pipe system; the hydrogen outlet of the electrolyzer is also connected to the feed gas inlet of the Fischer-Tropsch synthesis reactor via the pipe system; and the caustic soda solution outlet of the electrolyzer is connected to the washing solution inlet of the first gas washing device via the pipe system.

16. The device of claim 15, further comprising a second gas washing device comprising a gas inlet and a gas outlet, wherein the caustic soda solution outlet of the electrolyzer is connected to the washing solution inlet of the second gas washing device via the pipe system, the gas inlet of the second gas washing device is connected to a pipe conveying flue gas or other CO.sub.2-containing gases, and the gas outlet of the second gas washing device is connected to a downstream process pipe or atmosphere.

17. The device of claim 15, wherein the gas washing device is a packed tower, a sieve plate tower or a spray tower.

18. The device of claim 16, wherein the gas washing device is a packed tower, a sieve plate tower or a spray tower.

19. The device of claim 15, wherein the decarburization device is a pressure swing adsorption device or a low-temperature methanol washing device.

20. The device of claim 16, wherein the decarburization device is a pressure swing adsorption device or a low-temperature methanol washing device.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0029] FIG. 1 is a structural diagram of a device for Fischer-Tropsch synthesis in accordance with one embodiment of the present invention; and

[0030] FIG. 2 is a modified structure of a device for Fischer-Tropsch synthesis in FIG. 1.

DETAILED DESCRIPTION OF THE EMBODIMENTS

[0031] For further illustrating the invention, experiments detailing a method and device for Fischer-Tropsch synthesis are described below. It should be noted that the following examples are intended to describe and not to limit the invention.

[0032] FIG. 1 shows a device for Fischer-Tropsch synthesis, comprising a gasification device 1, an electrolyzer 2, a first gas washing device 3 and a Fischer-Tropsch synthesis reactor 4, where the gasification device 1 is a gasifier, which may be a Luigi gasifier, a Texaco gasifier, a Shell gasifier or a Hangtian gasifier, and comprises a raw material inlet 1-2, an oxidant inlet 1-3, a water inlet 1-4 and a syngas outlet end 1-1; the electrolyzer 2 comprises a hydrogen outlet 2-1, a caustic solution outlet 2-2, a chlorine outlet 2-3 and a saturated NaCl solution inlet 2-4; the Fischer-Tropsch synthesis reactor 4 comprises a feed gas inlet 4-1, a synthetic product outlet 4-2, an effluent and waste outlet 4-3 and an flue gas outlet 4-4; the first gas washing device 3 comprises a gas inlet 3-1, a gas outlet 3-2, a washing solution inlet 3-3 and a byproduct outlet 3-4; a second gas washing device 5 comprises a gas inlet 5-1, a gas outlet 5-2 and a washing solution inlet 5-3. The syngas outlet end 1-1 of the gasification device 1 is connected to the gas inlet 3-1 of the first gas washing device 3 via the pipe system, and the gas outlet 3-2 of the first gas washing device 3 is connected to the feed gas inlet 4-1 of the Fischer-Tropsch synthesis reactor 4 via the pipe system; the hydrogen outlet 2-1 of the electrolyzer 2 is also connected to the feed gas inlet 4-1 of the Fischer-Tropsch synthesis reactor 4 via the pipe system, and the caustic soda solution outlet 2-2 of the electrolyzer 2 is connected to the washing solution inlet 3-3 of the first gas washing device 3 via the pipe system; the caustic soda solution outlet 2-2 of the electrolyzer 2 is further connected to a washing solution inlet 5-3 of the second gas washing device 5 via the pipe system, the gas inlet 5-1 of the second gas washing device is connected to a pipe 7 of waste gas or other CO.sub.2-containing gases, and the gas outlet 5-2 of the second gas washing device 5 is connected to a downstream process pipe 8 or atmosphere. The first gas washing device 3 and the second gas washing device 5 therein are respectively a packed tower, a sieve plate tower or a spray tower.

[0033] FIG. 2 shows another device for Fischer-Tropsch synthesis, which is a modified structure of FIG. 1, and comprises a gasification device 1, an electrolyzer 2, a decarburization device 6, a first gas washing device 3 and a Fischer-Tropsch synthesis reactor 4, where a syngas outlet end 1-1 of the gasification device 1 is connected to a crude syngas inlet 6-1 of the decarburization device 6 via the pipe system, a pure syngas outlet 6-3 of the decarburization device 6 is connected to a feed gas inlet 4-1 of the Fischer-Tropsch synthesis reactor 4 via the pipe system, a carbon dioxide outlet 6-2 of the decarburization device 6 is connected to a gas inlet 3-1 of the first gas washing device 3 via the pipe system; a hydrogen outlet 2-1 of the electrolyzer 2 is also connected to the feed gas inlet 4-1 of the Fischer-Tropsch synthesis reactor 4 via the pipe system, and a caustic soda solution outlet 2-2 of the electrolyzer 2 is connected to a washing solution inlet 3-3 of the first gas washing device 3 via the pipe system; the caustic soda solution outlet 2-2 of the electrolyzer 2 is further connected to a washing solution inlet 5-3 of a second gas washing device 5 via the pipe system, a gas inlet 5-1 of the second gas washing device 5 is connected to a pipe 7 of waste gas or other CO.sub.2-containing gases, and a gas outlet 5-2 of the second gas washing device 5 is connected to a downstream process pipe 8 or atmosphere. The first gas washing device 3 and the second gas washing device 5 therein are respectively a packed tower, a sieve plate tower or a spray tower; and the decarburization device 6 is a pressure swing adsorption device or a low-temperature methanol washing device.

[0034] The technical process of the device for Fischer-Tropsch synthesis shown in FIG. 1 comprises the following steps: the raw material, oxidant and water for Fischer-Tropsch synthesis are introduced to the gasification device 1 for gasification respectively from the raw material inlet 1-2, the oxidant inlet 1-3 and the water inlet 1-4 of the gasification device 1 to obtain a crude syngas with the main components of H.sub.2, CO and CO.sub.2, the compositions of which are CO: 5 to 60%, H.sub.2: 5 to 45% and CO.sub.2: 5 to 30% on a dry basis, and the balance is inevitable impurity gases. Crude syngas output from the syngas outlet end 1-1 of the gasification device 1 enters the first gas washing device 3 from the gas inlet 3-1 of the first gas washing device 3. At the same time, saturated NaCl solution is electrolyzed into hydrogen, chlorine and NaOH solution in the electrolyzer 2, the NaOH solution generated through electrolysis is introduced via the caustic soda solution outlet 2-2 into the first gas washing device 3 from the washing solution inlet 3-3 of the first gas washing device 3 to obtain a pure syngas through removing CO.sub.2 in a crude syngas. At the same time, the generated NaHCO.sub.3 and Na.sub.2CO.sub.3 solution is discharged from the by-product outlet 3-4 of the first gas washing device 3, and is sold or used as a solid product after concentration and crystallization. The remaining NaOH solution after absorbing the crude syngas can be used for removing CO.sub.2 in an industrial waste gas or gases generated in other processes. In addition, at the same time, H.sub.2 obtained through chloralkali is insufflated into the pure syngas to adjust the carbon/hydrogen mole ratio (CO/H.sub.2) in the pure syngas to 1:1.5 to 2.5 according to the requirements of hydrogen flow rate control in Fischer-Tropsch synthesis, and then the pure syngas is input into the Fischer-Tropsch synthesis reactor 4 from the feed gas inlet 4-1 of the Fischer-Tropsch synthesis reactor 4 to produce corresponding liquid hydrocarbons and paraffin products through synthetic reaction. Liquid hydrocarbon products obtained through the reaction are output from the synthetic product outlet 4-2, effluent and waste flow out from the effluent and waste outlet 4-3, and flue gas is emitted from the flue gas outlet 4-4. Please see Examples 1 to 3 for detailed technical operation process.

[0035] The difference between the technical process shown in FIG. 2 and the technical process shown in FIG. 1 is that in FIG. 1, the pure syngas is obtained through removing CO.sub.2 in the crude syngas by direct full gas-liquid contact between the NaOH solution and the crude syngas, while in FIG. 2, the pure syngas is obtained through centralized separation of CO.sub.2 in the crude syngas, and then CO.sub.2 obtained through centralized separation is absorbed using the NaOH solution. Please see Examples 4 to 6 for detailed technical operation process.

[0036] In addition, the NaOH solution generated through electrolysis in the electrolyzer 2 may no longer be used to absorb CO.sub.2 in the crude syngas or flue gas, and the entire set of chloralkali device is only used to adjust the carbon/hydrogen mole ratio in the syngas as a hydrogen source.

Example 1

[0037] A normal pressure biomass gasifier is employed, with biomass as raw material, air as an oxidant, the flow rate of the syngas is 8200 kmol/h, the composition of the syngas on a dry basis is (mol. %): CO: 23.28%, H.sub.2: 8.65%, CO.sub.2: 16.82%, N.sub.2: 50.19%, Ar: 0.65%, and other impurity gases: 0.41%.

[0038] Refer to FIG. 1, the technical process is described as follows: the flow rate of the raw material NaCl solution in the chloralkali process is controlled at 5454.81 kmol/h, the NaOH solution obtained therefrom is used to wash the syngas and absorb CO.sub.2 therein to obtain a pure syngas. 2759.14 kmol/h NaOH solution is consumed in this process, and the remaining NaOH (2695.67 kmol/h) is used to absorb the flue gas; H.sub.2 obtained from the chloralkali process is mixed with the pure syngas after gas washing to adjust the hydrogen/carbon ratio in the syngas, then the mixed gas is used as the feed gas for Fischer-Tropsch synthesis, and Cl.sub.2 obtained from the chloralkali process is converted to liquid chlorine for sale, where the H.sub.2 content (mol. %) is 10.4% in the pure syngas after gas washing, and is 35.99% in the feed gas for Fischer-Tropsch synthesis.

[0039] The CO.sub.2 absorption rate in the syngas reaches 99%, and CO/H.sub.2 is 1:1.8 in the feed gas for Fischer-Tropsch synthesis.

Example 2

[0040] A normal pressure biomass gasifier is employed, with biomass as raw material, 98% (mol. %) O.sub.2 as an oxidant, the flow rate of the syngas is 8200 kmol/h, the compositions of the syngas on a dry basis is (mol. %): CO: 48.10%, H.sub.2: 23.29%, CO.sub.2: 20.84%, N.sub.2: 3.56%, and other impurity gases: 4.20%.

[0041] Refer to FIG. 1, the technical process is described as follows: the flow rate of the raw material NaCl solution in the chloralkali process is controlled at 10380.08 kmol/h, the NaOH solution obtained therefrom is used to wash the syngas and absorb CO.sub.2 therein to obtain a pure syngas. 1708.88 kmol/h NaOH solution is consumed in this process, and the remaining NaOH (8671.20 kmol/h) is used to absorb the flue gas; H.sub.2 obtained from the chloralkali process is mixed with the pure syngas after gas washing to adjust the hydrogen/carbon ratio in the syngas, then the mixed gas is used as the feed gas for Fischer-Tropsch synthesis, and Cl.sub.2 obtained from the chloralkali process is converted to liquid chlorine for sale, where the H.sub.2 content (mol. %) is 29.43% in the pure syngas after gas washing, and is 60.78% in the feed gas for Fischer-Tropsch synthesis.

[0042] The CO.sub.2 absorption rate in the syngas reaches 99%, and CO/H.sub.2 is 1:1.8 in the feed gas for Fischer-Tropsch synthesis.

Example 3

[0043] A normal pressure Texaco gasifier is employed. Coarse coal as raw material and 99% (mol. %) O.sub.2 as an oxidant are mixed with water to yield water coal slurry which is then put into the gasifier. The flow rate of the syngas is 23622 kmol/h, the compositions of the syngas on a dry basis is (mol. %): CO: 40.28%, H.sub.2: 48.28%, CO.sub.2: 7.94%, N.sub.2: 3.10%, and other impurity gases: 0.40%.

[0044] Refer to FIG. 1, the technical process is described as follows: the flow rate of the raw material NaCl solution in the chloralkali process is controlled at 13347.37 kmol/h, the NaOH solution obtained therefrom is used to wash the syngas and absorb CO.sub.2 therein to obtain a pure syngas. 3751.17 kmol/h NaOH solution is consumed in this process, and the remaining NaOH (9596.20 kmol/h) is used to absorb the flue gas; H.sub.2 obtained from the chloralkali process is mixed with the pure syngas after gas washing to adjust the hydrogen/carbon ratio in the syngas, then the mixed gas is used as the feed gas for Fischer-Tropsch synthesis, and Cl.sub.2 obtained from the chloralkali process is converted to liquid chlorine for sale, where the H.sub.2 content (mol. %) is 52.44% in the pure syngas after gas washing, and is 63.61% in the feed gas for Fischer-Tropsch synthesis.

[0045] The CO.sub.2 absorption rate in the syngas reaches 99%, and CO/H.sub.2 is 1:1.9 in the feed gas for Fischer-Tropsch synthesis.

Example 4

[0046] A normal pressure biomass gasifier is employed, with biomass as raw material, air as a combustion improver, the flow rate of the syngas is 8200 kmol/h, the compositions of the syngas on a dry basis is (mol. %): CO: 23.28%, H.sub.2: 8.65%, CO.sub.2: 16.82%, N.sub.2: 50.19%, Ar: 0.65%, and other impurity gases: 0.41%.

[0047] Refer to FIG. 2, the technical process is described as follows: the flow rate of the raw material NaCl solution in the chloralkali process is controlled at 5454.81 kmol/h, the NaOH solution obtained therefrom is used to absorb CO.sub.2 resulting from a pressure swing adsorptive decarburization of the syngas to yield a pure syngas. 2759.14 kmol/h NaOH solution is consumed in this process, and the remaining NaOH (2695.67 kmol/h) is used to absorb the flue gas; H.sub.2 obtained from the chloralkali process is mixed with the pure syngas after gas washing to adjust the hydrogen/carbon ratio in the syngas, then the mixed gas is used as the feed gas for Fischer-Tropsch synthesis, and Cl.sub.2 obtained from the chloralkali process is converted to liquid chlorine for sale, where the H.sub.2 content (mol. %) is 10.4% in the pure syngas after gas washing, and is 35.99% in the feed gas for Fischer-Tropsch synthesis.

[0048] The CO.sub.2 absorption rate in the syngas reaches 99%, and CO/H.sub.2 is 1:1.8 in the feed gas for Fischer-Tropsch synthesis.

Example 5

[0049] A normal pressure biomass gasifier is employed, with biomass as raw material, air as a combustion improver, the flow rate of the syngas is 8200 kmol/h, the compositions of the syngas on a dry basis is (mol. %): CO: 48.10%, H.sub.2: 23.29%, CO.sub.2: 20.84%, N.sub.2: 3.56%, and other impurity gases: 4.20%.

[0050] Refer to FIG. 2, the technical process is described as follows: the flow rate of the raw material NaCl solution in the chloralkali process is controlled at 10380.08 kmol/h, the NaOH solution obtained therefrom is used to absorb CO.sub.2 resulting from a pressure swing adsorptive decarburization of the syngas to obtain a pure syngas. 1708.88 kmol/h NaOH solution is consumed in this process, and the remaining NaOH (8671.2 kmol/h) is used to absorb the flue gas; H.sub.2 obtained from the chloralkali process is mixed with the pure syngas after gas washing to adjust the hydrogen/carbon ratio in the syngas, then the mixed gas is used as the feed gas for Fischer-Tropsch synthesis, and Cl.sub.2 obtained from the chloralkali process is converted to liquid chlorine for sale, where the H.sub.2 content (mol. %) is 29.43% in the pure syngas after gas washing, and is 60.78% in the feed gas for Fischer-Tropsch synthesis.

[0051] The CO.sub.2 absorption rate in the syngas reaches 99%, and CO/H.sub.2 is 1:1.8 in the feed gas for Fischer-Tropsch synthesis.

Example 6

[0052] A normal pressure Texaco gasifier is employed. Coarse coal as raw material and 99% (mol. %) O.sub.2 as an oxidant are mixed with water to yield water coal slurry which is then put into the gasifier, the flow rate of the syngas is 23622 kmol/h, the compositions of the syngas on a dry basis is (mol. %): CO: 40.28%, H.sub.2: 48.28%, CO.sub.2: 7.94%, N.sub.2: 3.1%, and other impurity gases: 0.40%.

[0053] Refer to FIG. 2, the technical process is described as follows: the flow rate of the raw material NaCl solution in the chloralkali process is controlled at 13347.37 kmol/h, the NaOH solution obtained therefrom is used to absorb CO.sub.2 resulting from decarburization of the syngas using low temperature methanol to yield a pure syngas. 3751.17 kmol/h NaOH solution is consumed in this process with, and the remaining NaOH (9596.20 kmol/h) is used to absorb the flue gas; H.sub.2 obtained from the chloralkali process is mixed with the pure syngas after gas washing to adjust the hydrogen/carbon ratio in the syngas, then the mixed gas is used as the feed gas for Fischer-Tropsch synthesis, and Cl.sub.2 obtained from the chloralkali process is converted to liquid chlorine for sale, where the H.sub.2 content (mol. %) is 52.44% in the pure syngas after gas washing, and is 63.61% in the feed gas for Fischer-Tropsch synthesis.

[0054] The CO.sub.2 absorption rate in the syngas reaches 99%, and CO/H.sub.2 is 1:1.9 in the feed gas for Fischer-Tropsch synthesis.

[0055] Unless otherwise indicated, the numerical ranges involved in the invention include the end values. While particular embodiments of the invention have been shown and described, it will be obvious to those skilled in the art that changes and modifications may be made without departing from the invention in its broader aspects, and therefore, the aim in the appended claims is to cover all such changes and modifications as fall within the true spirit and scope of the invention.