CN216303284U - Coke oven gas synthetic ammonia system - Google Patents
Coke oven gas synthetic ammonia system Download PDFInfo
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- CN216303284U CN216303284U CN202122032994.3U CN202122032994U CN216303284U CN 216303284 U CN216303284 U CN 216303284U CN 202122032994 U CN202122032994 U CN 202122032994U CN 216303284 U CN216303284 U CN 216303284U
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 162
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 77
- 239000000571 coke Substances 0.000 title claims abstract description 39
- 238000001179 sorption measurement Methods 0.000 claims abstract description 93
- 239000007789 gas Substances 0.000 claims abstract description 82
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 45
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 44
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 30
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 26
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000001257 hydrogen Substances 0.000 claims abstract description 24
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 24
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 20
- 238000000605 extraction Methods 0.000 claims abstract description 15
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000000741 silica gel Substances 0.000 claims abstract description 12
- 229910002027 silica gel Inorganic materials 0.000 claims abstract description 12
- 239000003463 adsorbent Substances 0.000 claims abstract description 6
- 239000002808 molecular sieve Substances 0.000 claims abstract description 6
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 25
- 238000002156 mixing Methods 0.000 claims description 20
- 238000003795 desorption Methods 0.000 claims description 15
- 238000004519 manufacturing process Methods 0.000 claims description 13
- 238000004939 coking Methods 0.000 claims description 12
- 238000006477 desulfuration reaction Methods 0.000 claims description 10
- 230000023556 desulfurization Effects 0.000 claims description 10
- 239000002918 waste heat Substances 0.000 claims description 9
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 7
- 230000008929 regeneration Effects 0.000 claims description 3
- 238000011069 regeneration method Methods 0.000 claims description 3
- 238000010926 purge Methods 0.000 claims 1
- 230000008901 benefit Effects 0.000 abstract description 5
- 239000003245 coal Substances 0.000 abstract description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 abstract description 4
- 239000000126 substance Substances 0.000 abstract description 3
- 238000000034 method Methods 0.000 description 16
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 8
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 6
- 238000001816 cooling Methods 0.000 description 6
- 125000001741 organic sulfur group Chemical group 0.000 description 6
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 5
- 238000000746 purification Methods 0.000 description 5
- 229910052717 sulfur Inorganic materials 0.000 description 5
- 239000011593 sulfur Substances 0.000 description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- 230000029936 alkylation Effects 0.000 description 4
- 238000005804 alkylation reaction Methods 0.000 description 4
- 239000011787 zinc oxide Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 230000002194 synthesizing effect Effects 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 238000002955 isolation Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
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- Separation Of Gases By Adsorption (AREA)
Abstract
The utility model relates to the technical field of coal chemical industry, in particular to a coke oven gas ammonia synthesis system, which comprises a temperature swing adsorption unit, a pressure swing adsorption hydrogen extraction unit and an ammonia synthesis unit which are sequentially connected; the temperature swing adsorption unit comprises a plurality of temperature swing adsorption towers which are connected in series, and an activated carbon layer, a silica gel layer, an alumina layer and a coke layer are sequentially arranged on the temperature swing adsorption towers from top to bottom; the pressure swing adsorption hydrogen extraction unit comprises a plurality of pressure swing adsorption towers which are connected in series, and a molecular sieve layer, a CO special adsorbent layer, an activated carbon layer and silica gel are sequentially arranged on the pressure swing adsorption towers from top to bottomThe inlet of the first pressure swing adsorption tower is connected with the purified gas outlet of the last temperature swing adsorption tower; the ammonia synthesis unit comprises an ammonia synthesis tower, and the air inlet of the ammonia synthesis tower is connected with the purified H of the last pressure swing adsorption tower2An outlet and an outlet of the nitrogen supply device. The system has short flow path, high running benefit and stability and good quality of produced products.
Description
Technical Field
The utility model relates to the technical field of coal chemical industry, in particular to a system for synthesizing ammonia from coke oven gas.
Background
The coke oven gas is a combustible gas product generated in the thermal decomposition process of low-rank coal at 500-650 ℃ under the condition of air isolation or little air isolation, and generally 300-350m coke oven gas can be produced from each ton of dry coal3The coke oven consumes about half of the coke oven. The coke oven gas is a mixture, the yield and composition of which are different due to the quality of the coal for coking and the different conditions of the coking process, and the main component of which is H2 (55% -70%) and CH4 (15％-30％)、CO (5％-9％)、CO2 (2％-5％)、N2 (2% -6%) and small quantity of other components, and the coke-oven gas can be used for producing hydrogen or preparing ammonia.
The conventional process for synthesizing ammonia by using coke oven gas comprises the following steps:
1. pressurizing coke oven gas from a coking device by a compressor, then entering a fine desulfurization section, converting organic sulfur in the coke oven gas into hydrogen sulfide by hydrogenation, and then removing the hydrogen sulfide by using zinc oxide; the coke oven gas with qualified sulfur content passes through a methane conversion working section to convert methane in the coke oven gas into CO and CO2、H2(ii) a Then sequentially carrying out CO conversion and CO conversion2A removing unit for performing alcohol alkylation (or alcohol alkylation) to remove CO and CO2Thoroughly removing the ammonia gas, and pressurizing the obtained qualified hydrogen and nitrogen gas by a compressor to produce ammonia.
2. Pressurizing coke oven gas from a coking device by a compressor, then entering a fine desulfurization section, converting organic sulfur in the coke oven gas into hydrogen sulfide by hydrogenation, and then removing the hydrogen sulfide by using zinc oxide; the coke oven gas with qualified sulfur content is extracted by PSA to obtain ammoniaRequired hydrogen (CO + CO)2Less than or equal to 10 PPm), supplementing qualified nitrogen, and producing ammonia after pressurization by a compressor.
The two production processes both need organic sulfur hydroconversion, the hydroconversion can be carried out at a certain temperature, and the zinc oxide needs to be replaced periodically, so that the coke oven gas needs to be heated and cooled for many times, the investment cost of device construction can be increased, the operation cost is increased, the popularization of the process for synthesizing ammonia by comprehensively utilizing the coke oven gas is restricted, and the improvement of the overall benefit of the coking device is influenced.
Therefore, the utilization mode of the coke oven gas needs to be optimized, the operation benefit of the ammonia synthesis device by the coke oven gas is improved, and a production system with short process flow route and low production cost is developed.
SUMMERY OF THE UTILITY MODEL
The utility model can shorten the process, reduce the cost and achieve excellent H by arranging the treatment layers of various substances in the temperature swing adsorption tower and the pressure swing adsorption tower respectively according to the specific filling structures2Purification effect, obtaining high-purity H capable of directly carrying out ammonia synthesis2。
In order to achieve the effect, the basic concept of the adopted technical scheme is as follows:
the coke oven gas ammonia synthesis system comprises a temperature swing adsorption unit, a pressure swing adsorption hydrogen extraction unit and an ammonia synthesis unit which are connected in sequence;
the temperature swing adsorption unit comprises a plurality of temperature swing adsorption towers which are connected in series, and the temperature swing adsorption towers are sequentially provided with an activated carbon layer, a silica gel layer, an aluminum oxide layer and a coke layer from top to bottom;
the pressure swing adsorption hydrogen extraction unit comprises a plurality of pressure swing adsorption towers which are connected in series, a molecular sieve layer, a CO special adsorbent layer, an activated carbon layer, a silica gel layer and an aluminum oxide layer are sequentially arranged on the pressure swing adsorption towers from top to bottom, and an inlet of the first pressure swing adsorption tower is connected with a purified gas outlet of the last pressure swing adsorption tower;
the ammonia synthesis unit comprises an ammonia synthesis tower, and the air inlet of the ammonia synthesis tower is connected with the purified H of the last pressure swing adsorption tower2 An outlet and an outlet of the nitrogen supply device.
As one mode, a coke oven gas outlet of the coking production device is connected to an inlet of a first temperature swing adsorption tower of the temperature swing adsorption unit through a screw compressor, a first-stage cooler and a first-stage gas-liquid separator in sequence.
As one mode, the purified gas outlet of the last temperature swing adsorption tower of the temperature swing adsorption unit is connected to the inlet of the first pressure swing adsorption tower through a compressor, a secondary cooler and a secondary gas-liquid separator in sequence.
As a mode, the system is further provided with a desorption gas mixing tank, a gas inlet of the desorption gas mixing tank is connected with a desorption gas outlet of the pressure swing adsorption tower, a gas outlet of the desorption gas mixing tank is connected with a regeneration gas inlet of the temperature swing adsorption tower, and a desorption gas outlet of the temperature swing adsorption tower is connected with a coking production device.
As a mode, the purification H of the last pressure swing adsorption tower2 The outlet of the hydrogen-nitrogen mixing tank is connected to the inlet of the ammonia synthesis tower through a high-pressure machine, a three-stage cooler, a three-stage gas-liquid separator, a circulator and a heat exchanger before the synthesis tower in sequence, the outlet of the ammonia synthesis tower is connected to the inlet of a waste heat boiler, the outlet of the waste heat boiler is connected to the inlet of the heat exchanger before the synthesis tower, and the outlet of the heat exchanger before the synthesis tower is connected to a condenser.
In one mode, a desulfurization and deoxidation tank is arranged between the outlet of the hydrogen-nitrogen mixing tank and the high-pressure machine.
As one mode, an ammonia separator and a cold exchanger both provided with a liquid ammonia outlet are arranged on a pipeline between the three-stage gas-liquid separator and the circulator;
the outlet of the tertiary gas-liquid separator is connected with the inlet of the ammonia separator, the gas outlet of the ammonia separator and the outlet of the condenser are connected with the inlet of the cold exchanger, the gas outlet of the cold exchanger is connected with the inlet of the ammonia cooler, and the outlet of the ammonia cooler is connected with the inlet of the ammonia separator.
In one mode, the outlet of the three-stage gas-liquid separator and the gas outlet of the ammonia cooler are connected together to the inlet of the ammonia separator through a confluence pipe comprising the same pipe section.
As a mode, the temperature swing adsorption tower is internally provided with 25.0-35.0% of an activated carbon layer, 35.0-45.0% of a silica gel layer, 5.0-10.0% of an aluminum oxide layer and 18.0-25.0% of a coke layer by taking the total mass of each layer as 100%.
In one mode, the pressure swing adsorption tower is internally provided with 74.0-77.0% of a molecular sieve layer, 3.0-5.0% of a CO special adsorbent layer, 12.0-15.0% of an activated carbon layer, 3.0-5.0% of a silica gel layer and 1.5-3.0% of an alumina layer, wherein the total mass of all layers is 100%.
Compared with the prior art, the technical scheme of the utility model has the following advantages:
1. the coke oven gas synthetic ammonia system does not need an organic sulfur hydroconversion procedure of the conventional process, reduces the heating and cooling processes of the coke oven gas, shortens the process flow route, reduces the construction investment of the device, reduces the number of operators, reduces the operation difficulty, the production cost and the energy consumption, improves the operation stability of the device, and improves the operation benefit and the stability.
2. The temperature swing adsorption tower adopts a special filling structure to realize that hydrogen sulfide and most of organic sulfur are basically removed in the process of removing impurities such as naphthalene, tar, benzene and the like by temperature swing adsorption (TSA for short), and the total sulfur content in the product hydrogen is less than or equal to 0.10ppm, CO + CO is realized by adjusting the formula and the filling structure of the filler in the pressure swing adsorption tower under the condition of reducing the organic sulfur hydroconversion process2Less than or equal to 10ppm, and meets the requirement of ammonia synthesis.
3. In order to further avoid the condition that the fluctuation of sulfur content and oxygen content caused by the fluctuation of indexes in the production process affects the long-period stable operation of the device, activated carbon (zinc oxide) is added for desulfurization after the hydrogen and nitrogen are mixed, so that the qualified sulfur content is ensured;
and a deoxidizing tank is further added, and a deoxidizer in the deoxidizing tank is utilized to remove trace oxygen in the hydrogen and the nitrogen until the deoxidizer stably meets the standard of synthetic ammonia requirements.
4. Book (I)The pressure swing adsorption hydrogen extraction unit (PSA hydrogen extraction unit for short) adopted by the utility model can produce hydrogen meeting the ammonia process requirements, and reduces the gas purification procedures in the conventional ammonia synthesis process, such as CO conversion and CO2Removal, alcohol alkylation (alcohol alkylation), and the like.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a schematic structural diagram of a coke oven gas ammonia synthesis system of the present invention.
The figure is marked with: the system comprises a screw compressor 1, a primary cooler 2, a primary gas-liquid separator 3, a temperature swing adsorption unit 4, a compressor 5, a secondary cooler 6, a secondary gas-liquid separator 7, a pressure swing adsorption hydrogen extraction unit 8, a hydrogen-nitrogen mixing tank 9, a desulfurization and deoxidation tank 10, a high-pressure machine 11, a tertiary cooler 12, a tertiary gas-liquid separator 13, an ammonia separator 14, a circulator 15, a pre-converter heat exchanger 16, an ammonia synthesis tower 17, a waste heat boiler 18, a condenser 19, a cold exchanger 20 and an ammonia cooler 21.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings, and it should be understood that the described embodiments are some, but not all embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The following definitions of "primary", "secondary", "first", "last", etc. are only for convenience of distinguishing the same kind of equipment used in different stations for better understanding, and do not limit the technical solution.
The utility model provides a coke oven gas synthetic ammonia system, which comprises a temperature swing adsorption unit 4, a pressure swing adsorption hydrogen extraction unit 8 and an ammonia synthesis unit which are sequentially connected;
the temperature swing adsorption unit 4 comprises a plurality of temperature swing adsorption towers connected in series, and the temperature swing adsorption towers are sequentially provided with an activated carbon layer, a silica gel layer, an aluminum oxide layer and a coke layer from top to bottom;
the pressure swing adsorption hydrogen extraction unit 8 comprises a plurality of pressure swing adsorption towers which are connected in series, a molecular sieve layer, a CO special adsorbent layer, an activated carbon layer, a silica gel layer and an aluminum oxide layer are sequentially arranged on the pressure swing adsorption towers from top to bottom, and an inlet of the first pressure swing adsorption tower is connected with a purified gas outlet of the last pressure swing adsorption tower;
the ammonia synthesis unit comprises an ammonia synthesis tower 17, and the air inlet of the ammonia synthesis tower 17 is connected with the purified H of the last pressure swing adsorption tower2 An outlet and an outlet of the nitrogen supply device.
The above definitions of "first", "last", etc. are determined according to the flow order of the air streams in the respective devices.
As shown in fig. 1, which provides a specific configuration of the above system, a coke oven gas outlet of a coking production unit is connected to an inlet of a first temperature swing adsorption tower of a temperature swing adsorption unit 4 via a screw compressor 1, a primary cooler 2 and a primary gas-liquid separator 3 in sequence.
The purified gas outlet of the last temperature swing adsorption tower of the temperature swing adsorption unit 4 is connected to the inlet of the first pressure swing adsorption tower of the pressure swing adsorption hydrogen extraction unit 8 through a compressor 5, a secondary cooler 6 and a secondary gas-liquid separator 7 in sequence.
Preferably, a desulfurization and deoxidation tank 10 is arranged between the outlet of the hydrogen-nitrogen mixing tank 9 and the high-pressure machine 11, namely, the outlet of the hydrogen-nitrogen mixing tank 9 is connected with the inlet of the desulfurization and deoxidation tank 10, and the outlet of the desulfurization and deoxidation tank 10 is connected with the inlet of the high-pressure machine 11.
As a preferable scheme (not shown in fig. 1), the system is further provided with a desorption gas mixing tank, a gas inlet of the desorption gas mixing tank is connected with a desorption gas outlet of the pressure swing adsorption tower, a gas outlet of the desorption gas mixing tank is connected with a regeneration gas inlet of the temperature swing adsorption tower, and a desorption gas outlet of the temperature swing adsorption tower is connected with a coking production device.
Purification H of the last of said pressure swing adsorption columns2 The outlet of the hydrogen-nitrogen mixing tank 9 is connected with the inlet of the hydrogen-nitrogen mixing tank 9 through the outlet of the nitrogen supply device, the outlet of the hydrogen-nitrogen mixing tank 9 is connected with the inlet of the ammonia synthesis tower 17 through the high-pressure machine 11, the three-stage cooler 12, the three-stage gas-liquid separator 13, the circulator 15 and the heat exchanger 16 in front of the synthesis tower in sequence, the outlet of the ammonia synthesis tower 17 is connected with the inlet of the waste heat boiler 18, the outlet of the waste heat boiler 18 is connected with the inlet of the heat exchanger 16 in front of the synthesis tower, and the outlet of the heat exchanger 16 in front of the synthesis tower is connected with the condenser 19.
An ammonia separator 14 and a cold exchanger 20 both having a liquid ammonia outlet are arranged on the pipeline between the three-stage gas-liquid separator 13 and the circulator 15, the outlet of the three-stage gas-liquid separator 13 is connected with the inlet of the ammonia separator 14, the gas outlet of the ammonia separator 14 and the outlet of the condenser 19 are connected with the inlet of the cold exchanger 20, the gas outlet of the cold exchanger 20 is connected with the inlet of an ammonia cooler 21, and the outlet of the ammonia cooler 21 is connected with the inlet of the ammonia separator 14.
Further, the outlet of the third-stage gas-liquid separator 13 and the outlet of the ammonia cooler 21 are connected together to the inlet of the ammonia separator 14 through a confluence pipe comprising the same pipe section.
The filler structure in the temperature swing adsorption tower is as follows:
the temperature swing adsorption tower is internally provided with 25.0-35.0% of an activated carbon layer, 35.0-45.0% of a silica gel layer, 5.0-10.0% of an alumina layer and 18.0-25.0% of a coke layer by taking the total mass of each layer as 100%.
The packing structure in the pressure swing adsorption tower is as follows:
based on the total mass of all layers as 100%, 74.0-77.0% of a molecular sieve layer, 3.0-5.0% of a CO special adsorbent layer, 12.0-15.0% of an activated carbon layer, 3.0-5.0% of a silica gel layer and 1.5-3.0% of an alumina layer are arranged in the pressure swing adsorption tower.
The following describes a working process of the system in implementation:
1) coke oven gas purification and PSA hydrogen extraction
Coke oven gas from a coking production device enters a screw compressor 1 for pressurization through pipeline connection, is cooled through a primary cooler 2 after being pressurized to 0.20MPa, is separated from water and liquid impurities through a primary gas-liquid separator 3, enters a temperature swing adsorption unit 4 (TSA adsorption unit) for adsorption separation of tar, naphthalene and other impurities carried in the gas, is finally required to have the tar content lower than 2PPm and the naphthalene content lower than 1PPm, is pressurized to 1.60MPa through a compressor 5, is cooled through a secondary cooler 6, enters a secondary gas-liquid separator 7 for removing oil drops and water pollution in the coke oven gas, enters a pressure swing adsorption hydrogen extraction unit 8 (PSA adsorption unit), adopts a flushing flow, and comprises the steps of adsorption, pressure equalization, forward release, reverse release, flushing, final pressure boosting and the like in the technical process, and qualified hydrogen is produced.
2) Ammonia synthesis and production of liquid ammonia
Qualified hydrogen from a pressure swing adsorption hydrogen extraction unit 8 and nitrogen from an air separation device enter a hydrogen-nitrogen mixing tank 9, enter a high-pressure machine 11 after passing through a desulfurization and deoxidation tank 10, enter a three-stage cooler 12 for cooling after being pressurized, enter a three-stage gas-liquid separator 13 for separating oil from water, then enter an ammonia separator 14 together with gas from an outlet of an ammonia cooler 21, enter a cold exchanger 20 for separating liquid ammonia, recycle the cold energy of the mixed gas and raise the temperature of the mixed gas, pressurize the gas after being raised in temperature by a circulator 15, enter a heat exchanger 16 in front of a synthesis tower, enter an ammonia synthesis tower 17 after being subjected to heat exchange and temperature raising with gas from a waste heat boiler 18, enter a waste heat boiler 18 for cooling after reaction, enter the heat exchanger 16 in front of the synthesis tower 16, enter a condenser 19 for cooling the synthesis gas after being subjected to heat exchange to about 40 ℃, enter the cold exchanger 20 for further heat exchange and cooling and separating liquid ammonia, the gas enters an ammonia cooler 21 for further cooling, most of the gas ammonia is condensed, and the gas at the outlet of the ammonia cooler 21 enters the next cycle.
The liquid ammonia separated by the ammonia separator 14 and the cold exchanger 20 is sent for sale.
It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications therefrom are within the scope of the utility model.
Claims (8)
1. The coke oven gas ammonia synthesis system is characterized by comprising a temperature swing adsorption unit, a pressure swing adsorption hydrogen extraction unit and an ammonia synthesis unit which are sequentially connected;
the temperature swing adsorption unit comprises a plurality of temperature swing adsorption towers which are connected in series, and the temperature swing adsorption towers are sequentially provided with an activated carbon layer, a silica gel layer, an aluminum oxide layer and a coke layer from top to bottom;
the pressure swing adsorption hydrogen extraction unit comprises a plurality of pressure swing adsorption towers which are connected in series, a molecular sieve layer, a CO special adsorbent layer, an activated carbon layer, a silica gel layer and an aluminum oxide layer are sequentially arranged on the pressure swing adsorption towers from top to bottom, and an inlet of the first pressure swing adsorption tower is connected with a purified gas outlet of the last pressure swing adsorption tower;
the ammonia synthesis unit comprises an ammonia synthesis tower, and the air inlet of the ammonia synthesis tower is connected with the purified H of the last pressure swing adsorption tower2 An outlet and an outlet of the nitrogen supply device.
2. The system of claim 1, wherein the coke oven gas outlet of the coking production unit is connected to the inlet of the first temperature swing adsorption column of the temperature swing adsorption unit through a screw compressor, a primary cooler, and a primary gas-liquid separator in that order.
3. The system of claim 1, wherein the purified gas outlet of the last temperature swing adsorption column of the temperature swing adsorption unit is connected to the inlet of the first pressure swing adsorption column through a compressor, a secondary cooler, and a secondary gas-liquid separator in that order.
4. The system of claim 1, further comprising a desorption gas mixing tank, wherein a gas inlet of the desorption gas mixing tank is connected with a desorption gas outlet of the pressure swing adsorption tower, a gas outlet of the desorption gas mixing tank is connected with a regeneration gas inlet of the temperature swing adsorption tower, and the desorption gas outlet of the temperature swing adsorption tower is connected with a coking production device.
5. The system of claim 1, wherein the purge H of the last of the pressure swing adsorption columns2 The outlet of the hydrogen-nitrogen mixing tank is connected to the inlet of the ammonia synthesis tower through a high-pressure machine, a three-stage cooler, a three-stage gas-liquid separator, a circulator and a heat exchanger before the synthesis tower in sequence, the outlet of the ammonia synthesis tower is connected to the inlet of a waste heat boiler, the outlet of the waste heat boiler is connected to the inlet of the heat exchanger before the synthesis tower, and the outlet of the heat exchanger before the synthesis tower is connected to a condenser.
6. The system of claim 5, wherein a desulfurization and deoxidation tank is arranged between the outlet of the hydrogen-nitrogen mixing tank and the high-pressure machine.
7. The system according to claim 5, wherein an ammonia separator and a cold exchanger each having an outlet for liquid ammonia are further provided on a line between said three-stage gas-liquid separator and said circulator;
the outlet of the tertiary gas-liquid separator is connected with the inlet of the ammonia separator, the gas outlet of the ammonia separator and the outlet of the condenser are connected with the inlet of the cold exchanger, the gas outlet of the cold exchanger is connected with the inlet of the ammonia cooler, and the outlet of the ammonia cooler is connected with the inlet of the ammonia separator.
8. The system of claim 7, wherein the outlet of the tertiary gas-liquid separator is connected to the inlet of the ammonia separator together with the gas outlet of the ammonia cooler by a converging conduit comprising the same pipe segments.
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| CN202122032994.3U CN216303284U (en) | 2021-08-26 | 2021-08-26 | Coke oven gas synthetic ammonia system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116588897A (en) * | 2023-06-12 | 2023-08-15 | 宁波中科远东催化工程技术有限公司 | Method for producing ammonia from coke oven gas |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN116588897A (en) * | 2023-06-12 | 2023-08-15 | 宁波中科远东催化工程技术有限公司 | Method for producing ammonia from coke oven gas |
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