CN114276846B - Method and system for preparing LNG and co-producing synthetic ammonia by using coke oven gas - Google Patents
Method and system for preparing LNG and co-producing synthetic ammonia by using coke oven gas Download PDFInfo
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- CN114276846B CN114276846B CN202111541645.2A CN202111541645A CN114276846B CN 114276846 B CN114276846 B CN 114276846B CN 202111541645 A CN202111541645 A CN 202111541645A CN 114276846 B CN114276846 B CN 114276846B
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 92
- 239000000571 coke Substances 0.000 title claims abstract description 44
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims abstract description 10
- 239000001257 hydrogen Substances 0.000 claims abstract description 154
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 154
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 111
- 239000007789 gas Substances 0.000 claims abstract description 111
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 102
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 75
- 239000007788 liquid Substances 0.000 claims abstract description 57
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 44
- 238000004821 distillation Methods 0.000 claims abstract description 42
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 38
- 238000005406 washing Methods 0.000 claims abstract description 29
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 23
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 23
- 238000004519 manufacturing process Methods 0.000 claims abstract description 11
- 150000002431 hydrogen Chemical class 0.000 claims description 33
- 239000002994 raw material Substances 0.000 claims description 5
- 230000002194 synthesizing effect Effects 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 2
- 239000000203 mixture Substances 0.000 abstract description 5
- 238000001816 cooling Methods 0.000 description 11
- 239000000047 product Substances 0.000 description 8
- 238000004939 coking Methods 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000012797 qualification Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen(.) Chemical compound [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- -1 nitrogen-hydrogen Chemical class 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention discloses a method and a system for preparing LNG and co-producing synthetic ammonia by using coke oven gas, wherein the method comprises the following steps: distilling coke oven gas by using a distillation tower to obtain hydrogen-rich and methane-rich liquid, separating the hydrogen-rich gas by using a pre-tower separator to obtain hydrogen and CO-rich gas, rectifying the methane-rich liquid by using a rectifying tower to obtain LNG (liquefied natural gas) products and CO-rich gas, preparing the hydrogen and medium-pressure liquid nitrogen by using a washing tower to obtain nitrogen and hydrogen and CO-rich gas, and catalyzing the nitrogen and hydrogen by using an ammonia synthesis tower to synthesize liquid ammonia; the invention uses the low temperature of the liquid nitrogen in the washing tower to remove CO in the hydrogen-rich gas, prepares qualified nitrogen and hydrogen to be sent to the synthesis ammonia tower to synthesize liquid ammonia, the CO is changed into a gas-liquid mixture, the production and manufacturing process of the synthesis ammonia has short chain, little consumption in the production and manufacturing process and low cost; the invention can simultaneously produce CO, liquid ammonia and LNG; fully utilizes coke oven gas, is environment-friendly and energy-saving, and has no pollution.
Description
Technical Field
The invention belongs to the field of coke oven gas deep processing, and particularly relates to a method and a system for preparing LNG and co-producing synthetic ammonia by using coke oven gas.
Background
Along with the continuous enhancement of the requirements of China on energy conservation, emission reduction and environmental protection, how to improve the utilization rate of coking byproducts becomes the key of energy conservation, emission reduction and economic benefit improvement for coking enterprises with high pollution and high energy consumption. In coking pairsIn the product, the coke oven gas with importance being inferior to that of coke is up to 4.8 hundred million tons according to the annual coke yield of 2014, and the coke yield per ton is 430Nm 3 The coke oven gas is estimated, and the annual coke oven gas yield can reach 2064 hundred million Nm 3 For such a large amount of valuable resources, the utilization efficiency plays a crucial role in the enterprise benefit of coking.
The coke oven gas composition (volume%) is: 55-60% of hydrogen, 23-27% of methane, 5-8% of carbon monoxide, 2-4% of unsaturated hydrocarbon with more than 2C, 1.5-3% of carbon dioxide, 3-7% of nitrogen and 0.3-0.8% of oxygen. In the prior art, the utilization rate of coke oven gas is low, and a great amount of waste is caused.
Disclosure of Invention
The invention aims to provide a method and a system for preparing LNG and co-producing synthetic ammonia by using coke oven gas, which can improve the utilization rate of the coke oven gas.
The invention adopts the following technical scheme: a method for preparing LNG and co-producing synthetic ammonia by using coke oven gas, comprising the following steps:
distilling the coke oven gas by using a distillation tower to obtain hydrogen-rich liquid and methane-rich liquid,
separating the hydrogen-rich gas by a separator in front of the tower to obtain hydrogen and CO-rich gas, rectifying the methane-rich liquid by a rectifying tower to obtain LNG products and CO-rich gas,
the hydrogen and the medium-pressure liquid nitrogen are utilized to prepare nitrogen and hydrogen and CO-rich gas,
and catalyzing the nitrogen and hydrogen to synthesize liquid ammonia by using an ammonia synthesis tower.
Further, the CO-rich gas in the pre-tower separator and the scrubber is subjected to a rectifying tower to obtain CO gas.
Further, the hydrogen-rich gas is separated for the first time by utilizing a hydrogen separator to remove methane, and the methane is refluxed to the distillation tower, and the hydrogen-rich gas is separated again by a pre-tower separator.
A system for producing LNG co-production synthetic ammonia from coke oven gas, comprising:
the distillation tower is provided with a raw gas inlet, a methane outlet and a hydrogen outlet, wherein the raw gas inlet is connected with a coke oven gas source,
a pre-tower separator, which is provided with a hydrogen inlet, a hydrogen outlet and a CO outlet, wherein the hydrogen inlet is communicated with the hydrogen outlet of the distillation tower,
the washing tower is provided with a hydrogen inlet, a liquid nitrogen inlet, a nitrogen-hydrogen outlet and a CO outlet, wherein the hydrogen inlet is communicated with the hydrogen outlet of the separator in front of the tower, the liquid nitrogen inlet is connected with a liquid nitrogen source,
a rectifying tower, which is provided with a methane inlet, a CO inlet, an LNG outlet and a CO outlet, wherein the methane inlet is communicated with the methane outlet of the distilling tower, the CO inlet is communicated with the CO outlet of the pre-tower separator and the washing tower, the CO outlet and the LNG outlet are respectively communicated with a CO storage tank and an LNG storage tank,
an ammonia synthesis tower, which is provided with an inlet and an outlet, wherein the inlet is communicated with a nitrogen-hydrogen outlet of the washing tower,
the distillation tower is used for distilling the coke oven gas to obtain hydrogen-rich liquid and methane-rich liquid, the washing tower is used for exchanging heat between the hydrogen-rich liquid and the medium-pressure liquid nitrogen to obtain nitrogen-hydrogen and CO-rich gas, the rectifying tower is used for rectifying the methane-rich liquid to obtain LNG (liquefied natural gas) products and CO-rich gas, and the ammonia synthesis tower is used for synthesizing liquid ammonia by utilizing the nitrogen-hydrogen.
Further, a hydrogen separator is further connected between the distillation tower and the pre-tower separator, the hydrogen separator is provided with a hydrogen inlet, a hydrogen outlet and a methane outlet, the hydrogen inlet is communicated with the hydrogen outlet of the distillation tower, the methane outlet is communicated with the methane inlet of the distillation tower, and the hydrogen outlet is communicated with the hydrogen inlet of the pre-tower separator.
Further, a hydrogen condenser is also connected between the distillation tower and the hydrogen separator, and a subcooler is also connected between the hydrogen separator and the separator in front of the tower.
Further, the pre-tower separator, the washing tower and the rectifying tower are all connected with each other through a subcooler.
Further, a heat exchanger is also connected between the subcooler and the rectifying tower.
Further, the distillation tower and the coke oven gas source are connected with each other through a heat exchanger, and the heat exchanger is used for removing CO gas in the raw material gas through low temperature.
The beneficial effects of the invention are as follows: the CO in the hydrogen-rich gas is removed by utilizing the low temperature of the liquid nitrogen in the washing tower, qualified nitrogen and hydrogen are prepared and sent to the ammonia synthesizing tower to synthesize liquid ammonia, the CO is changed into a gas-liquid mixture, the production and manufacturing process of the ammonia is short in chain, the consumption is low in the production and manufacturing process, and the cost is low; the invention can simultaneously produce CO, liquid ammonia and LNG; fully utilizes coke oven gas, is environment-friendly and energy-saving, and has no pollution.
Drawings
Fig. 1 is a schematic structural view of the present invention.
Wherein: 1. a distillation column; 2. a pre-column separator; 3. a washing tower; 4. a rectifying tower; 5. an ammonia synthesis tower; 6. a hydrogen separator; 7. a subcooler; 8. a heat exchanger; a co separator; a co condenser; 11. a hydrogen condenser; lng storage tank.
Detailed Description
The invention will be described in detail below with reference to the drawings and the detailed description.
The invention discloses a method for preparing LNG and co-producing synthetic ammonia by using coke oven gas, which comprises the following steps:
step 1: and distilling the coke oven gas by using a distillation tower 1 to obtain hydrogen-rich liquid and methane-rich liquid.
Step 2: the hydrogen-rich gas is separated for the first time by utilizing the hydrogen separator 6 to remove methane, then the hydrogen-rich gas is separated by utilizing the pre-tower separator 2 to obtain hydrogen and CO-rich gas, and the methane-rich liquid is rectified by utilizing the rectifying tower 4 to obtain LNG products and CO-rich gas.
Step 3: and preparing nitrogen and hydrogen and CO-rich gas by using the scrubber 3 to mix the hydrogen with the medium-pressure liquid nitrogen.
Step 4: the ammonia synthesis tower 5 is utilized to catalyze and synthesize the liquid ammonia from the nitrogen and the hydrogen.
Step 5: the CO-rich gas in the pre-tower separator 2 and the scrubber 3 is subjected to a rectification column 4 to obtain CO gas.
Before step 1, the coke oven gas needs to be dried, purified and purified, and in step 2, the hydrogen-rich gas is firstly separated to remove methane from the coke oven gas through a hydrogen separator 6, and the methane is refluxed to a distillation tower 1, and then the hydrogen-rich gas is separated again through a pre-tower separator 2.
The invention also discloses a system for preparing LNG and co-producing synthetic ammonia by using the coke oven gas, which is shown in figure 1 and comprises a distillation tower 1, a pre-tower separator 2, a washing tower 3, a rectifying tower 4 and an ammonia synthesizing tower 5, wherein the distillation tower 1 is provided with a raw material gas inlet, a methane outlet and a hydrogen outlet, the raw material gas inlet of the distillation tower 1 is connected with a coke oven gas source, and the coke oven gas source can be a coke oven or a coke oven gas storage tank so as to supply the coke oven gas to the distillation tower 1, and the distillation tower 1 is used for distilling the coke oven gas to obtain hydrogen-rich liquid and methane-rich liquid.
A hydrogen separator 6 is further connected between the distillation tower 1 and the pre-tower separator 2, hydrogen rich gas coming out of the distillation tower 1 enters the hydrogen separator 6, the hydrogen separator 6 is provided with a hydrogen inlet, a hydrogen outlet and a methane outlet, the hydrogen inlet of the hydrogen separator 6 is communicated with the hydrogen outlet of the distillation tower 1, the methane outlet of the hydrogen separator 6 is communicated with the methane inlet of the distillation tower 1, the hydrogen separator 6 removes methane in the hydrogen rich gas, methane is returned to the distillation tower 1, and the distillation tower 1 distills the methane again to obtain methane rich liquid.
The hydrogen-rich gas separated by the hydrogen separator 6 enters the pre-tower separator 2, the pre-tower separator 2 is provided with a hydrogen inlet, a hydrogen outlet and a CO outlet, the hydrogen outlet of the hydrogen separator 6 is communicated with the hydrogen inlet of the pre-tower separator 2, when the hydrogen separator 6 is not arranged, the hydrogen inlet of the pre-tower separator 2 is communicated with the hydrogen outlet of the distillation tower 1, and the pre-tower separator 2 is used for separating CO gas in the hydrogen-rich gas, removing the CO gas in the hydrogen-rich gas, obtaining pure hydrogen, ensuring the qualification of subsequent synthetic ammonia and producing a CO supplementing gas source.
A hydrogen condenser 11 is also connected between the distillation tower 1 and the hydrogen separator 6, the hydrogen rich gas from the distillation tower 1 enters the hydrogen condenser 11 for cooling and then enters the hydrogen separator 6, the hydrogen condenser 11 is used for cooling the hydrogen rich gas, a subcooler 7 is also connected between the hydrogen separator 6 and the pre-tower separator 2, and the subcooler 7 is used for cooling the hydrogen rich gas from the hydrogen separator 6 again.
The hydrogen passing through the pre-tower separator 2 enters a washing tower 3, the washing tower 3 is provided with a hydrogen inlet, a liquid nitrogen inlet, a nitrogen-hydrogen outlet and a CO outlet, the hydrogen inlet of the washing tower 3 is communicated with the hydrogen outlet of the pre-tower separator 2, the liquid nitrogen inlet of the washing tower 3 is connected with a liquid nitrogen source, the hydrogen entering the washing tower 3 exchanges heat with the liquid ammonia entering the washing tower 3 to become a mixture of nitrogen and hydrogen, namely nitrogen-hydrogen, and the mixture is conveyed to the synthesis ammonia tower to synthesize liquid ammonia.
The nitrogen and hydrogen flowing out from the nitrogen and hydrogen outlet of the pre-tower separator 2 enters an ammonia synthesis tower 5, the ammonia synthesis tower 5 is provided with an inlet and an outlet, the inlet of the ammonia synthesis tower 5 is communicated with the nitrogen and hydrogen outlet of a washing tower 3, the washing tower 3 is used for exchanging heat between hydrogen-rich gas and medium-pressure liquid nitrogen to obtain nitrogen and hydrogen-rich gas and CO-rich gas, the rectifying tower 4 is used for rectifying methane-rich liquid to obtain LNG products and CO-rich gas, and the ammonia synthesis tower 5 is used for synthesizing liquid ammonia by using the nitrogen and the hydrogen.
The methane-rich liquid separated from the distillation column 1 enters the rectification column 4, the rectification column 4 is provided with a methane inlet, a CO inlet, an LNG outlet and a CO outlet, the methane inlet of the rectification column 4 is communicated with the methane outlet of the distillation column 1, the CO inlet of the rectification column 4 is communicated with the CO outlet of the pre-column separator 2 and the CO outlet of the washing column 3, the CO outlet and the LNG outlet of the rectification column 4 are respectively communicated with the CO storage tank and the LNG storage tank 12, high-concentration LNG and CO are obtained after the rectification of the methane-rich liquid by the rectification column 4, the LNG flows out of the rectification column 4 from the LNG outlet positioned at the bottom of the rectification column 4, flows into the LNG storage tank 12, and the CO flows out of the rectification column 4 from the CO outlet positioned at the top of the rectification column 4 and flows into the CO storage tank.
The pre-tower separator 2 and the rectifying tower 4 are connected with each other through a subcooler 7, and the subcooler 7 is used for performing primary cooling on CO gas coming out of the pre-tower separator 2. The scrubber 3 and the rectifying column 4 are also connected to each other by a subcooler 7, whereby the subcooler 7 also serves to first cool the CO gas exiting the scrubber 3. The subcooler 7 is therefore used for cooling the CO gas coming out of the scrubber 3, also for cooling the CO gas coming out of the pre-tower separator 2, and also for cooling the hydrogen rich gas coming out of the hydrogen separator 6, with a compact system configuration and low costs.
The scrubber 3 and the ammonia synthesis tower 5 are also connected to each other through a subcooler 7, that is, the nitrogen-hydrogen outlet of the scrubber 3 is connected to the inlet of the subcooler 7, the outlet of the subcooler 7 is connected to the inlet of the ammonia synthesis tower 5, and at this time, the subcooler 7 is used for preheating the nitrogen-hydrogen flowing out of the scrubber 3.
A heat exchanger 8 is further connected between the subcooler 7 and the rectifying tower 4, the heat exchanger 8 is used for cooling other CO coming out of the pre-tower separator 2 and the washing tower 3, the cooled CO enters the rectifying tower 4 for rectification to obtain pure CO, then the CO is stored by a storage tank, and the CO still needs to be purified by a CO condenser 10 and a CO separator 9 before entering the CO storage tank.
The subcooler 7 and the ammonia synthesis tower 5 are also connected to each other by a heat exchanger 8, and the heat exchanger 8 is used for preheating the nitrogen and hydrogen gas flowing out of the subcooler 7.
The distillation tower 1 and the coke oven gas source are connected with each other through the heat exchanger 8, the rectification tower 4 and the LNG storage tank 12 are also connected through the heat exchanger 8, the heat exchanger 8 is used for removing CO gas in the raw gas through low temperature, at the moment, the temperature of the raw gas passing through the heat exchanger 8 is-160+/-5 ℃, the heat exchanger 8 can also be used for cooling CO gas from the washing tower 3 from the subcooler 7, can also be used for cooling CO gas from the pre-tower separator 2 from the subcooler 7, can also be used for cooling LNG from the rectification tower 4, and has compact system structure and low cost.
The generation flow of the invention is as follows:
the raw material gas is purified by a drying and purifying system, enters a heat exchanger 8, is cooled to-160+/-5 ℃ in the heat exchanger 8, enters a distillation tower 1 for primary rectification, and hydrogen-rich liquid and methane-rich liquid are respectively obtained at the upper part and the lower part of the distillation tower 1.
Throttling the methane-rich liquid, and then feeding the throttled methane-rich liquid into a rectifying tower 4 for re-rectifying to obtain LNG; the hydrogen-rich gas is condensed by a hydrogen condenser 11 and then enters a hydrogen separator 6, is separated by the hydrogen separator 6, is supercooled by a supercooler 7 and then enters a pre-tower separator 2 for gas-liquid separation, hydrogen and CO-rich gas are obtained through separation, the hydrogen is sent into a washing tower 3 for heat exchange with medium-pressure nitrogen from the outside to obtain nitrogen and methane-rich liquid respectively, and after passing through the supercooler 7, the nitrogen and hydrogen enter a heat exchanger 8 for rewarming and then are sent into an ammonia synthesis tower 5 for synthesis to obtain a liquid ammonia product.
The liquid at the bottom of the washing tower 3 and the liquid of the separator 2 in front of the tower are converged by the subcooler 7 and then sent to the rectifying tower 4 for rectification again, an LNG product is formed at the bottom of the rectifying tower 4, and after heat exchange by the heat exchanger 8, the liquid is throttled and cooled again by the extraction valve and then sent to the LNG storage tank 12 for storage.
The CO-rich gas separated from the top of the rectifying tower 4 is sent out of the cold box boundary area after being rewarmed by the cooler 7 and the heat exchanger 8.
Example 1
The device co-produces LNG 67291 tons at the beginning of 9 months of 2019 operation, liquid ammonia 84922 tons, the system operation is stable, various process indexes are normal in operation, the product qualification accords with national standards, the liquid ammonia cost is 1400 yuan/ton, and the tax price is 2500 yuan/ton at present, so that the device becomes a new economic growth point of enterprises.
Claims (4)
1. A method for preparing LNG and co-producing synthetic ammonia by using coke oven gas, which is characterized by comprising the following steps:
the raw material gas enters a heat exchanger (8) after being purified by a drying and purifying system, is cooled to-160+/-5 ℃ in the heat exchanger (8),
the coke oven gas is distilled by a distillation tower (1) to obtain hydrogen-rich liquid and methane-rich liquid,
the hydrogen rich gas enters a hydrogen separator (6) after being condensed by a hydrogen condenser (11), is separated by the hydrogen separator (6), then enters a pre-tower separator (2) for gas-liquid separation after being supercooled by a supercooler (7),
separating the hydrogen-rich gas by a pre-tower separator (2) to obtain hydrogen and CO-rich gas, rectifying the methane-rich liquid by a rectifying tower (4) to obtain LNG products and CO-rich gas,
the washing tower (3) is utilized to prepare the nitrogen-hydrogen and CO-rich gas by hydrogen and medium-pressure liquid nitrogen,
after passing through the cooler (7), the nitrogen and hydrogen enter the heat exchanger (8) for rewarming and then are sent to the ammonia synthesis tower (5) for synthesis,
the ammonia synthesis tower (5) is utilized to catalyze and synthesize the liquid ammonia;
the liquid at the bottom of the washing tower (3) and the liquid of the separator (2) in front of the tower are converged by the subcooler (7) and then sent into the rectifying tower (4) for rectification again, and LNG products are formed at the bottom of the rectifying tower (4).
2. A system for producing LNG co-production synthetic ammonia from coke oven gas, comprising:
a distillation tower (1) provided with a feed gas inlet, a methane outlet and a hydrogen outlet, wherein the feed gas inlet is connected with a coke oven gas source,
a pre-tower separator (2) provided with a hydrogen inlet, a hydrogen outlet and a CO outlet, wherein the hydrogen inlet is communicated with the hydrogen outlet of the distillation tower (1),
the washing tower (3) is provided with a hydrogen inlet, a liquid nitrogen inlet, a nitrogen-hydrogen outlet and a CO outlet, the hydrogen inlet is communicated with the hydrogen outlet of the pre-tower separator (2), the liquid nitrogen inlet is connected with a liquid nitrogen source,
a rectifying tower (4) provided with a methane inlet, a CO inlet, an LNG outlet and a CO outlet, wherein the methane inlet is communicated with the methane outlet of the distilling tower (1), the CO inlet is communicated with the CO outlet of the pre-tower separator (2) and the washing tower (3), the CO outlet and the LNG outlet are respectively communicated with a CO storage tank and an LNG storage tank (12),
an ammonia synthesis column (5) having an inlet and an outlet, the inlet of which is in communication with the nitrogen-hydrogen outlet of the scrubber (3),
the distillation tower (1) is used for distilling coke oven gas to obtain hydrogen-rich liquid and methane-rich liquid, the washing tower (3) is used for exchanging heat between the hydrogen-rich liquid and medium-pressure liquid nitrogen to obtain nitrogen-hydrogen gas and CO-rich gas, the rectifying tower (4) is used for rectifying the methane-rich liquid to obtain LNG (liquefied natural gas) products and CO-rich gas, and the ammonia synthesis tower (5) is used for synthesizing liquid ammonia by utilizing the nitrogen-hydrogen gas;
a hydrogen separator (6) is further connected between the distillation tower (1) and the pre-tower separator (2), the hydrogen separator (6) is provided with a hydrogen inlet, a hydrogen outlet and a methane outlet, the hydrogen inlet is communicated with the hydrogen outlet of the distillation tower (1), the methane outlet is communicated with the methane inlet of the distillation tower (1), and the hydrogen outlet is communicated with the hydrogen inlet of the pre-tower separator (2);
a hydrogen condenser (11) is further connected between the distillation tower (1) and the hydrogen separator (6), and a subcooler (7) is further connected between the hydrogen separator (6) and the pre-tower separator (2);
wherein a heat exchanger (8) is also connected between the subcooler (7) and the rectifying tower (4).
3. The system for preparing LNG and co-producing synthetic ammonia from coke oven gas according to claim 2, wherein the pre-tower separator (2), the washing tower (3) and the rectifying tower (4) are all connected with each other through a subcooler (7).
4. A system for CO-production of synthetic ammonia from coke oven gas according to claim 3, characterized in that the distillation column (1) and the coke oven gas source are connected to each other by a heat exchanger (8), the heat exchanger (8) being adapted to remove CO gas from the feed gas by cryogenic temperatures.
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