CN202988709U - Device for co-producing ammonia synthesis gas and liquefied natural gas by conny pressurization and gasification by fixed bed - Google Patents
Device for co-producing ammonia synthesis gas and liquefied natural gas by conny pressurization and gasification by fixed bed Download PDFInfo
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- CN202988709U CN202988709U CN 201220355622 CN201220355622U CN202988709U CN 202988709 U CN202988709 U CN 202988709U CN 201220355622 CN201220355622 CN 201220355622 CN 201220355622 U CN201220355622 U CN 201220355622U CN 202988709 U CN202988709 U CN 202988709U
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
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Abstract
The utility model discloses a device for co-producing ammonia synthesis gas and liquefied natural gas by conny pressurization and gasification by a fixed bed, comprising: a high pressure nitrogen cooler, a first raw material gas cooler, a first nitrogen expander, a nitrogen washing column, a first flash evaporation pot, a second flash evaporation pot and a methane rectifying tower, which are connected by pipes. The device of the utility model implements coproduction of liquefied natural gas while purifies ammonia synthesis gas, thereby achieving the effects of low investment, low energy consumption, high calorific value and high benefit.
Description
Technical field
the utility model relates to synthetic ammonia gas purification technique field, especially for a kind of BGL(BritishGas-Lurgi that utilizes) synthetic gas of broken coal slag pressurized-gasification furnace and Lu Qi (Lurgi) crushed coal pressurized-gasification furnace produces synthetic ammonia and by-product high purity LNG Technology field, be particularly related to a kind of low temperature liquid nitrogen of using as absorption agent, remove CO in mixed gas, Ar, CH4, and be the fixed bed broken coal pressing gas ammonia synthesis gas processed of high purity liquefied natural gas product and high purity natural gas liquids combination preparing device with isolated methane fraction is refining in this treating processes, this device is applicable to synthetic gas (hydrogen, carbon monoxide, nitrogen, methane, argon) purify less energy-consumption new type low temperature liquid nitrogen washing (gas removal) and the high purity natural gas liquids co-production technology in synthetic ammonia processed field.
Background technology
At present, the BGL of many coal chemical industry enterprises or the unstripped gas after the Lurgi gasification, basal component also has part methane except carbon monoxide, hydrogen.Need to remove through the liquid nitrogen washing operation rare gas element or the gases harmful to catalyzer such as methane in the synthetic ammonia process of producing product, then get back to again the liquid nitrogen washing operation after the methane rich cut being delivered to the workshop section such as methane conversion, Zhongdao synthesis procedure is produced ammonia.
Synthetic ammonia process based on BGL or Lurgi stove has consisted of a loop chain during the course like this, this chain as shown in Figure 1, raw gas that its BGL or Lurgi stove are come is sent into low-temperature rectisol and liquid nitrogen washing operation after through the CO conversion and is removed the rare gas element such as methane or produce ammonia to being sent to synthesis procedure after the harmful gas of catalyzer, and the methane rich cut of liquid nitrogen washing operation is got back to again the liquid nitrogen washing operation after delivering to the workshop sections such as methane conversion, CO conversion.There is following deficiency in this flow process: 1, this process energy consumption is high, the waste resource; 2, the variable effect methane conversion workshop section of the CH4 cut that comes of liquid nitrogen washing workshop section; 3, long flow path, the degree of coupling is high, affects stable, safety, the long period reliability service of factory; 4, in low, the methane fraction of methane recovery, the concentration of methane is low, calorific value is little; 5, product simplification.
In order to open loop chain, improve calorific value and the rate of recovery of methane, the methane fraction in the liquid nitrogen washing process can be made with extra care is the high purity natural gas liquids, as byproduct output, will produce very important economic results in society.
Natural gas liquids is the clean energy that develops rapidly in recent years, have pollution-free, calorific value is high, is convenient to transportation, the combustion gas that can solve the remote mountain areas or be not easy to the area of cloth pipe network is used.Along with the progress of the development of society, science and technology and the mankind strengthen the consciousness of environment protection, in recent years, natural gas liquids receives much concern as clean energy.
Take BGL or Lurgi vapourizing furnace as gasification process, can produce simultaneously synthetic ammonia and high purity natural gas liquids will be a brand-new problem, can realize the coproduction of synthetic ammonia and high purity natural gas liquids, and the key problem of this coproduction is to realize gas cleaning and separate as how lower energy consumption.
The utility model content
Technical problem to be solved in the utility model is to provide a kind of fixed bed broken coal pressing gas ammonia synthesis gas processed and high purity natural gas liquids combination preparing device for the existing problem of prior art, this device is by liquid nitrogen washing device and low ternperature separation process technology, saved the methane conversion workshop section of complex procedures in traditional synthetic gas production process, in indifferent gas, be highly purified natural gas liquids with the methane fraction concentrate in removing synthetic gas.And unstripped gas both reduced the impact of synthesis loop indifferent gas through purifying and methane separation, reduced discharge amount of exhaust gas, realized synthetic ammonia and the coproduction of high purity natural gas liquids, had significant economic and social benefit.
Technical problem to be solved in the utility model can be achieved through the following technical solutions:
Fixed bed broken coal pressing gas ammonia synthesis gas processed and natural gas liquids combination preparing device is characterized in that, comprising:
High pressure nitrogen water cooler, this high pressure nitrogen water cooler have the first high pressure nitrogen entrance, the first high pressure nitrogen outlet, the first fuel gas outlet, the first fuel gas entrance, the first nitrogen inlet, the first nitrogen outlet, the first synthetic gas entrance, the first syngas outlet;
The first unstripped gas water cooler, this first unstripped gas water cooler have the first unstripped gas entrance, the first unstripped gas outlet, the second nitrogen inlet, the second nitrogen outlet, the second high pressure nitrogen entrance, the second high pressure nitrogen outlet, the second fuel gas entrance, the second fuel gas outlet, the second synthetic gas entrance, the second syngas outlet;
The second unstripped gas water cooler, this second unstripped gas water cooler have the 3rd nitrogen inlet, the 3rd nitrogen outlet, the second unstripped gas entrance, the second unstripped gas outlet, third high pressure nitrogen inlet, third high pressure nitrogen outlet, the first flashed liquid entrance, the 3rd fuel gas outlet, the 3rd synthetic gas entrance, the 3rd syngas outlet, the first natural gas liquids entrance, the first natural gas liquids outlet and the first flash gas entrance;
The first nitrogen expansion machine;
The second nitrogen expansion machine;
Nitrogen wash column, this nitrogen wash column top have a liquid nitrogen entrance, and the top has a nitrogen gas washing outlet, and the bottom has a unstripped gas entrance, and the bottom has a cut outlet;
The first flash tank, this first flash tank top have a unstripped gas entrance, and the top has a unstripped gas outlet, and the bottom has a liquid exit;
The second flash tank, this second flash tank top have gas inlet and the cut entrance after a rectifying, and the top has a flash gas outlet, and the bottom has a flashed liquid outlet;
Methane rectifying tower, this methane rectifying tower middle and upper part have a unstripped gas entrance, and the top has the pneumatic outlet after a rectifying, and the bottom has a reboiler, and the bottom has a natural gas liquids outlet;
the high pressure nitrogen that divides from sky is connected with the first high pressure nitrogen entrance on the high pressure nitrogen cooling apparatus by the first high pressure nitrogen line of pipes, the first high pressure nitrogen entrance and the outlet of the first high pressure nitrogen connect, the second high pressure nitrogen line of pipes is told in the first high pressure nitrogen outlet and third high is pressed the nitrogen line of pipes, the second high pressure nitrogen line of pipes is connected with the entrance of the first nitrogen expansion machine, and third high presses the nitrogen line of pipes to be connected with the second high pressure nitrogen entrance on the first unstripped gas water cooler, the second high pressure nitrogen entrance is communicated with the second high pressure nitrogen outlet, the 4th high pressure nitrogen line of pipes is told in the second high pressure nitrogen outlet, the 5th high pressure nitrogen line of pipes and the 6th high pressure nitrogen line of pipes, the 4th high pressure nitrogen line of pipes is connected with the reboiler entrance of methane rectifying tower bottom, the 5th high pressure nitrogen line of pipes is connected with the entrance of the second nitrogen expansion machine, the 6th high pressure nitrogen line of pipes presses nitrogen inlet to be connected with the third high of the second unstripped gas water cooler, third high presses nitrogen inlet and third high to press nitrogen outlet to be communicated with, third high presses nitrogen outlet to be connected with the liquid nitrogen entrance on nitrogen wash column top by the first liquid nitrogen line of pipes,
Be connected with the first unstripped gas entrance of the first unstripped gas water cooler by the first unstripped gas line of pipes by the unstripped gas out of the molecular sieve in low-temperature rectisol, the first unstripped gas entrance is communicated with the first unstripped gas outlet, the first unstripped gas outlet is connected with the second unstripped gas entrance on the second unstripped gas water cooler by the second unstripped gas export pipeline, the second unstripped gas entrance is communicated with the second unstripped gas outlet, and the second unstripped gas outlet is passed through the 3rd unstripped gas line of pipes and is connected with the unstripped gas entrance on the first flash tank top;
The unstripped gas line of pipes of the unstripped gas of the first flash drum overhead outlet by being rich in methane is connected with the unstripped gas entrance of nitrogen wash column bottom, and the liquid exit bottom the first flash tank is connected with the unstripped gas entrance of methane rectifying tower middle and upper part by fluid-carrying lines;
the nitrogen gas washing outlet at nitrogen wash column top is connected with the first entrance of a constant enthalpy current regulator by nitrogen gas washing line of pipes, the second entrance of isenthalpic throttling device is connected with the first liquid nitrogen line of pipes by the second liquid nitrogen line of pipes, the outlet of isenthalpic throttling device is connected with the 3rd synthetic gas entrance on the second unstripped gas water cooler, the 3rd synthetic gas entrance is communicated with the 3rd syngas outlet, the 3rd syngas outlet is connected with the second synthetic gas entrance on the first unstripped gas water cooler by the first synthetic gas line of pipes, the second synthetic gas entrance is communicated with the second syngas outlet, the second syngas outlet is told the second synthetic gas line of pipes and the 3rd synthetic gas line of pipes, the second synthetic gas line of pipes is connected with the low-temperature rectisol operation, the 3rd synthetic gas line of pipes is connected with the first synthetic gas entrance on the high pressure nitrogen water cooler, the first synthetic gas entrance is communicated with the first syngas outlet, the first syngas outlet is connected with the ammonia synthesis operation by the 4th synthetic gas line of pipes, wherein the 4th synthetic gas line of pipes also becomes the letter shoot line to be connected with the low-temperature rectisol operation by pentahapto,
the cut outlet of nitrogen wash column bottom is connected by the cut entrance of cut line of pipes with the second flash tank top, gas inlet after the rectifying on the air shooter line of the pneumatic outlet after the rectifying at methane rectifying tower top after by rectifying and the second flash tank top is connected, the outlet of the flash gas of the second flash drum overhead is connected with the first flash gas entrance on the second unstripped gas water cooler by the flash gas line of pipes, the gas outlet of methane rectifier bottoms is connected with the first natural gas liquids entrance on the second unstripped gas water cooler by the first natural gas liquids line of pipes, the first natural gas liquids outlet on the second unstripped gas water cooler is communicated with the first natural gas liquids entrance and the first flash gas entrance, the first natural gas liquids outlet is connected with LNG tank by the second natural gas liquids line of pipes,
the flashed liquid outlet of the second flash tank bottom is connected with the first flashed liquid entrance on the second unstripped gas water cooler by the flashed liquid line of pipes, the 3rd fuel gas outlet on the second unstripped gas water cooler is communicated with the first flashed liquid entrance and the first flash gas entrance, the 3rd fuel gas outlet is connected with the second fuel gas entrance on the first unstripped gas water cooler by the first fuel gas line of pipes, the second fuel gas entrance is communicated with the second fuel gas outlet, the second fuel gas outlet is connected with the first fuel gas entrance on the high pressure nitrogen water cooler by the second fuel gas line of pipes, the first fuel gas entrance is communicated with the first fuel gas outlet, the first fuel gas outlet is connected with fuel gas system by the 3rd fuel gas line of pipes,
the outlet of the second nitrogen expansion machine is connected with the 3rd nitrogen inlet on the second unstripped gas water cooler by the first nitrogen line of pipes, the 3rd nitrogen inlet is communicated with the 3rd nitrogen outlet, the 3rd nitrogen outlet is told the second nitrogen line of pipes and the 3rd nitrogen line of pipes, the second nitrogen line of pipes is connected with the outlet of the first nitrogen expansion machine, the 3rd nitrogen line of pipes is connected with the second nitrogen inlet on the first unstripped gas water cooler, the second nitrogen inlet is communicated with the second nitrogen outlet, the second nitrogen outlet is connected with the first nitrogen inlet on the high pressure nitrogen water cooler by the 4th nitrogen line of pipes, the first nitrogen inlet is communicated with the first nitrogen outlet, nitrogen compressor entrance during the first nitrogen outlet passes through the 5th nitrogen line of pipes and sky divides is connected.
In a preferred embodiment of the utility model device, the 5th high pressure nitrogen line of pipes and the 6th high pressure nitrogen line of pipes are told in the second high pressure nitrogen outlet, the 5th high pressure nitrogen line of pipes is connected with entrance with the second nitrogen expansion machine, and the 6th high pressure nitrogen line of pipes presses nitrogen inlet to be connected with the third high of the second unstripped gas water cooler; The second unstripped gas export pipeline and the second unstripped gas output by-pass line are told in the first unstripped gas outlet, the second unstripped gas export pipeline is connected with the second unstripped gas entrance on the second unstripped gas water cooler, and the second unstripped gas output by-pass line is connected with the reboiler entrance of methane rectifying tower bottom.
Owing to having adopted technical scheme as above, the utlity model has following functions:
1. the methane rectifying tower is set, the methane rich of cooling box is formed reach the highly purified natural gas liquids of LNG() specification, farthest reclaimed methane in unstripped gas.
2. liquid-mixing nitrogen and gas are set join two kinds, nitrogen and slightly join the nitrogen mode, give full play to efficiency of heat exchanger.
3. the adjustable mode of methane rectifying tower tower bottom reboiler thermal load is set, guarantees the highly purified natural gas liquids of LNG() product specification.
4. nitrogen wash column is set, and the synthetic gas specification of using liquid nitrogen washing cold box is qualified.
5. the decompression of fuel gas stream is set, cold is provided.
6. the decompression of methane-rich stream is set, cold is provided.
7. the staged nitrogen expansion is set, cold is provided.
According to idiographic flow, the utility model also can have following functions:
1. the synthetic gas essence of only selecting liquid-mixing nitrogen slightly to join nitrogen and cooling box is joined nitrogen.
2. arrange from the sky mode that liquid nitrogen replenishes cold of assigning to.
The ammonia synthesis gas field of purification is developed a kind of fixed bed broken coal pressing gasization and high purity natural gas liquids coproduction flow process of being applicable at home, realize synthetic ammonia and the coproduction of high purity natural gas liquids in this flow process, novel low temperature separation process and the purification techniques of low investment, less energy-consumption.The modified flow configuration, by-product high purity natural gas liquids when reaching decontamination effect improving, thus reach low effect of investing less energy-consumption high heating value high benefit.
Join methane conversion with traditional liquid nitrogen washing device and compare, the utility model device has the following advantages:
1. the static equipment investment is lower.Only increase a rectifying tower, the size of miscellaneous equipment such as interchanger, nitrogen wash column can remain unchanged.
2. increased the refrigeration cycle of nitrogen expansion, the highly purified natural gas liquids of by-product.
3. the synthesic gas compressor power consumption can not increase.Though by-product the product of high purity natural gas liquids, the cold in ice chest is redistributed and is utilized, and remains unchanged can guarantee that synthetic gas channel resistance in ice chest falls, and therefore can not increase the power consumption of synthetic compressor.
4. the product of the natural specification of by-product high purity liquefaction.Methane recovery can bring up to 88%.Improve the environment protection of life of urban resident environment and near cities manufacturing district; Solution can't be laid the industrial and mining enterprises of gas distributing system for the requirement of clean fuel simultaneously away from neutralizing gas.
5. strict guarantee synthetic gas specification.Though by-product the product of high purity natural gas liquids specification, do not increase again extra cold, resistance drop remains unchanged again, can guarantee that synthetic gas goes the specification of synthesis loop.
Description of drawings
Fig. 1 is the synthetic ammonia process block diagram of existing BGL or Lurgi stove.
Fig. 2 is the utility model fixed bed broken coal pressing gas ammonia synthesis gas processed and natural gas liquids coproduction FB(flow block).
Fig. 3 is fixed bed broken coal pressing gas ammonia synthesis gas processed and the natural gas liquids combination preparing device schematic diagram of the utility model embodiment 1.
Fig. 4 is fixed bed broken coal pressing gas ammonia synthesis gas processed and the natural gas liquids combination preparing device schematic diagram of the utility model embodiment 1.
Embodiment
Further describe the utility model below in conjunction with the drawings and specific embodiments.
Embodiment 1
Referring to Fig. 3, the fixed bed broken coal pressing gas ammonia synthesis gas processed and the natural gas liquids combination preparing device that provide in figure comprise high pressure nitrogen water cooler E-01, the first unstripped gas water cooler E-02, the second unstripped gas water cooler E-03, nitrogen wash column T-01, methane rectifying tower T-02, flash tank V-01, flash tank V-02, nitrogen expansion machine K-01, nitrogen expansion machine K-02.
High pressure nitrogen water cooler E-01 has high pressure nitrogen entrance 11, high pressure nitrogen outlet 12, fuel gas outlet 13, fuel gas entrance 14, nitrogen inlet 15, nitrogen outlet 16, synthetic gas entrance 17, syngas outlet 18.
The first unstripped gas water cooler E-02 has unstripped gas entrance 20, unstripped gas outlet 21, nitrogen inlet 22, nitrogen outlet 23, high pressure nitrogen entrance 24, high pressure nitrogen outlet 25, fuel gas entrance 26, fuel gas outlet 27, synthetic gas entrance 28, syngas outlet 29;
The second unstripped gas water cooler E-03 has nitrogen inlet 30, nitrogen outlet 31, unstripped gas entrance 32, unstripped gas outlet 33, high pressure nitrogen entrance 34, high pressure nitrogen outlet 35, flashed liquid entrance 36, fuel gas outlet 37, synthetic gas entrance 38, syngas outlet 39, natural gas liquids entrance 40, natural gas liquids outlet 41 and flash gas entrance 42;
Nitrogen wash column T-01 top has a liquid nitrogen entrance 50, and the top has a nitrogen gas washing outlet 51, and the bottom has a unstripped gas entrance 52 that is rich in methane, and the bottom has a cut outlet 53.
Flash tank V-01 top has a unstripped gas entrance 61, and the top has a unstripped gas outlet 62 of being rich in methane, and the bottom has one and is rich in methane liquid exit 63; Flash tank V-02 top has gas inlet 70 and the cut entrance 71 after a rectifying, and the top has a flash gas outlet 72, and the bottom has a flashed liquid outlet 73;
Methane rectifying tower T-02 middle and upper part has a unstripped gas entrance 80 that is rich in methane, and the top has the pneumatic outlet 81 after a rectifying, and the bottom has a reboiler 82, and the bottom has a natural gas liquids outlet 83.
the high pressure nitrogen 100 that divides from sky is connected with high pressure nitrogen entrance 11 on high pressure nitrogen water cooler E-01 by high pressure nitrogen line of pipes 90, high pressure nitrogen entrance 11 connects with high pressure nitrogen outlet 12, high pressure nitrogen line of pipes 91 and 92 are told in high pressure nitrogen outlet 12, high pressure nitrogen line of pipes 91 is connected with the entrance of nitrogen expansion machine K-01, and high pressure nitrogen line of pipes 92 is connected with high pressure nitrogen entrance 24 on the first unstripped gas water cooler E-02, high pressure nitrogen entrance 24 is communicated with high pressure nitrogen outlet 25, high pressure nitrogen line of pipes B1 is told in high pressure nitrogen outlet 25, 93, 94, high pressure nitrogen line of pipes B1 is connected with reboiler 82 entrances of methane rectifying tower T-02 bottom, high pressure nitrogen line of pipes 93 is connected with the entrance of nitrogen expansion machine K-02, high pressure nitrogen line of pipes 94 is connected with the high pressure nitrogen entrance 34 of the second unstripped gas water cooler E-03, high pressure nitrogen entrance 34 is communicated with high pressure nitrogen outlet 35, high pressure nitrogen outlet 34 is connected with the liquid nitrogen entrance 50 on nitrogen wash column T-01 top by liquid nitrogen line of pipes 95.
Be connected with the unstripped gas entrance 20 of the first unstripped gas water cooler E-02 by unstripped gas line of pipes 96 by the unstripped gas 110 out of the molecular sieve in low-temperature rectisol, unstripped gas entrance 20 is communicated with unstripped gas outlet 21, unstripped gas outlet 21 is connected with unstripped gas entrance 32 on the second unstripped gas water cooler E-03 by unstripped gas export pipeline 97, unstripped gas entrance 32 and unstripped gas outlet 33 is communicated with, and unstripped gas outlet 33 is passed through unstripped gas line of pipes 98 and is connected with the unstripped gas entrance 61 on flash tank V-01 top.
The unstripped gas line of pipes 99 of the unstripped gas outlet of being rich in methane 62 at flash tank V-01 top by being rich in methane is connected with the unstripped gas entrance 52 that is rich in methane of nitrogen wash column T-01 bottom, and the methane liquid exit 63 that is rich in bottom flash tank V-01 is connected with the unstripped gas entrance 80 that is rich in methane of methane rectifying tower T-02 middle and upper part by being rich in methane fluid-carrying lines 101.
the nitrogen gas washing outlet 51 at nitrogen wash column T-01 top is connected with the entrance 84 of a constant enthalpy current regulator M-01 by nitrogen gas washing line of pipes 102, the entrance 85 of isenthalpic throttling device M-01 is connected with liquid nitrogen line of pipes 95 by liquid nitrogen line of pipes 103, the outlet 86 of isenthalpic throttling device M-01 is connected with synthetic gas entrance 38 on the second unstripped gas water cooler E-03, synthetic gas entrance 38 is communicated with syngas outlet 39, syngas outlet 39 is connected with synthetic gas entrance 28 on the first unstripped gas water cooler E-02 by synthetic gas line of pipes 104, synthetic gas entrance 28 is communicated with syngas outlet 29, syngas outlet 29 is told synthetic gas line of pipes 105, 106, synthetic gas line of pipes 106 is connected with low-temperature rectisol operation 120, synthetic gas line of pipes 105 is connected with synthetic gas entrance 17 on high pressure nitrogen water cooler E-01, synthetic gas entrance 17 is communicated with syngas outlet 18, syngas outlet 18 is connected with ammonia synthesis operation 130 by synthetic gas line of pipes 107, wherein synthetic gas line of pipes 107 also is connected with low-temperature rectisol operation 120 by synthetic gas line of pipes 108.
the cut outlet 53 of nitrogen wash column T-01 bottom is connected with the cut entrance 71 on flash tank V-02 top by cut line of pipes 109, the gas inlet 70 of pneumatic outlet 81 after the rectifying at methane rectifying tower T-02 top after by the rectifying on the air shooter line 111 after rectifying and flash tank V-02 top is connected, the outlet 72 of the flash gas at flash tank V-02 top is connected with flash gas entrance 42 on the second unstripped gas water cooler E-03 by flash gas line of pipes 112, the natural gas liquids outlet 83 of methane rectifying tower T-02 bottom is connected with natural gas liquids entrance 40 on the second unstripped gas water cooler E-03 by natural gas liquids line of pipes 113, natural gas liquids outlet 41 is communicated with natural gas liquids entrance 40 and flash gas entrance 42, natural gas liquids outlet 41 is connected with LNG tank 140 by natural gas liquids line of pipes 114.
the flashed liquid outlet 73 of flash tank V-02 bottom is connected with flashed liquid entrance 36 on the second unstripped gas water cooler E-03 by flashed liquid line of pipes 115, fuel gas outlet 37 on the second unstripped gas water cooler E-03 is communicated with flashed liquid entrance 36 and flash gas entrance 43, fuel gas outlet 37 is connected with fuel gas entrance 26 on the first unstripped gas water cooler E-02 by fuel gas line of pipes 116, fuel gas entrance 26 is communicated with fuel gas outlet 27, fuel gas outlet 27 is connected with fuel gas entrance 13 on high pressure nitrogen water cooler E-01 by fuel gas line of pipes 117, fuel gas entrance 13 is communicated with fuel gas outlet 14, fuel gas outlet 14 is connected with fuel gas system 150 by fuel gas line of pipes 118.
the outlet of nitrogen expansion machine V-02 is connected with nitrogen inlet 30 on the second unstripped gas water cooler E-03 by nitrogen line of pipes 119, nitrogen inlet 30 is communicated with nitrogen outlet 31, nitrogen outlet 31 is told nitrogen line of pipes 121, 122, the second nitrogen line of pipes 121 is connected with the outlet of nitrogen expansion machine V-01, nitrogen line of pipes 122 is connected with nitrogen inlet 22 on the first unstripped gas water cooler E-02, nitrogen inlet 22 is communicated with nitrogen outlet 23, nitrogen outlet 23 is connected with nitrogen inlet 15 on high pressure nitrogen water cooler E-01 by nitrogen line of pipes 123, nitrogen inlet 15 is communicated with nitrogen outlet 16, nitrogen compressor 160 entrances during nitrogen outlet 16 passes through nitrogen line of pipes 124 and sky divides are connected.
The workflow of above-mentioned fixed bed broken coal pressing gas ammonia synthesis gas processed and natural gas liquids combination preparing device is as follows:
From the unstripped gas 100 of molecular sieve through the first unstripped gas water cooler E-02 and the second unstripped gas water cooler E-03 heat exchange after, send in flash tank V-01, gas in flash tank V-01 after the separation of methane cut enters nitrogen wash column T-01 bottom, with the cooled liquid nitrogen of high pressure nitrogen counter current contact on nitrogen wash column T-01 column plate, washing CO, Ar and remaining CH
4After go out tower top, after the nitrogen gas washing of tower top mixes in isenthalpic throttling device M-01 with high-pressure liquid nitrogen, send in the second unstripped gas water cooler E-03, enter the first unstripped gas water cooler E-02 after re-heat in the second unstripped gas water cooler E-03, thick synthetic gas specification forms, to ammonia synthesis operation 130, another part arrives ammonia synthesis operation 130 to this crude synthesis gas part after low-temperature rectisol operation 120 reclaims cold through high pressure nitrogen water cooler E-01 re-heat cooling box.
Flash tank V-01 is isolated to be rich in methane liquid and to enter methane rectifying tower T-02 and carry out rectifying, and the gas after rectifying is out delivered to flash tank V-02 by methane rectifying tower T-02 tower top and carried out gas-liquid separation; Be natural gas liquids at the bottom of methane rectifying tower T-02 tower, send in the second unstripped gas water cooler E-03, cooling box after the second unstripped gas water cooler E-03 is further cooling, in this liquid, methane content is 95%(mol), CO＜1000ppmv can be used as the high purity natural gas liquids and uses.
High pressure nitrogen is at first all sent into high pressure nitrogen water cooler E-01 step-down, be divided into two portions by high pressure nitrogen water cooler E-01 high pressure nitrogen out, a part is advanced nitrogen expansion machine K-01, it is cooling that another part advances the first unstripped gas water cooler E-02, the high pressure nitrogen that goes out the first unstripped gas water cooler E-02 is divided into again two portions, and a part is advanced nitrogen expansion machine K-02; Another part advances the second unstripped gas water cooler E-03.Advance high pressure nitrogen after the second unstripped gas water cooler E-03 formation liquid nitrogen that is liquefied.
The liquid nitrogen of the second unstripped gas water cooler E-03 is further divided into two portions, and a part enters nitrogen wash column T-01 top as the washing liquid nitrogen; Another part liquid nitrogen is incorporated in synthetic gas.The nitrogen that nitrogen expansion machine K-02 goes out through after the second unstripped gas water cooler E-03 re-heat with enter again the first unstripped gas water cooler E-02 after the nitrogen that goes out through nitrogen expansion machine K-01 mixes and carry out re-heat, nitrogen after re-heat is sent in high pressure nitrogen water cooler E-01 further re-heat cooling box, then gets back to this ice chest system after the nitrogen compressor compression that sky divides.
Out cut and the gas after the rectifying that comes of methane rectifying tower T-02 tower top is sent into after merging and is carried out gas-liquid separation in flash tank V-02 at the bottom of the nitrogen wash column T-01 tower, gas after flash tank V-02 separates and liquid are sent into the interior mixing of the second unstripped gas water cooler E-03 in the lump and re-heat forms thick fuel gas, and thick fuel gas is done fuel gas by cooling box after the first unstripped gas water cooler E-02 and high pressure nitrogen water cooler E-01 re-heat successively.
The raw gas flow of this embodiment is 101490Nm
3/ h, pressure 4.7MPa(G), synthetic ammonia output is 1050MTPD, the amount of by-product high purity natural gas liquids is 5,700 ten thousand Nm
3/ y, methane content are 95% (mol), CO＜1000ppmv, and the rate of recovery is about 88%.
Embodiment 2
Referring to Fig. 4, this embodiment fixed bed broken coal pressing gas ammonia synthesis gas processed and natural gas liquids combination preparing device are substantially the same manner as Example 1, just high pressure nitrogen line of pipes 93,94 is told in 25 of high pressure nitrogen outlets, high pressure nitrogen line of pipes 93 is connected with the entrance of nitrogen expansion machine K-02, and high pressure nitrogen line of pipes 94 is connected with the high pressure nitrogen entrance 34 of the second unstripped gas water cooler E-03.And unstripped gas export pipeline 97 and unstripped gas output by-pass line A1 are told in unstripped gas outlet 21, unstripped gas output by-pass line A1 is connected with reboiler 82 entrances of methane rectifying tower T-02 bottom, unstripped gas export pipeline 97 is connected with unstripped gas entrance 32 on the second unstripped gas water cooler E-03, unstripped gas entrance 32 and unstripped gas outlet 33 is communicated with, and unstripped gas outlet 33 is passed through unstripped gas line of pipes 98 and is connected with the unstripped gas entrance 61 on flash tank V-01 top.
The fixed bed broken coal pressing gas ammonia synthesis gas processed of this embodiment and the workflow of natural gas liquids combination preparing device are substantially the same manner as Example 1.
Claims (2)
1. fixed bed broken coal pressing gas ammonia synthesis gas processed and natural gas liquids combination preparing device, is characterized in that, comprising:
High pressure nitrogen water cooler, this high pressure nitrogen water cooler have the first high pressure nitrogen entrance, the first high pressure nitrogen outlet, the first fuel gas outlet, the first fuel gas entrance, the first nitrogen inlet, the first nitrogen outlet, the first synthetic gas entrance, the first syngas outlet;
The first unstripped gas water cooler, this first unstripped gas water cooler have the first unstripped gas entrance, the first unstripped gas outlet, the second nitrogen inlet, the second nitrogen outlet, the second high pressure nitrogen entrance, the second high pressure nitrogen outlet, the second fuel gas entrance, the second fuel gas outlet, the second synthetic gas entrance, the second syngas outlet;
The second unstripped gas water cooler, this second unstripped gas water cooler have the 3rd nitrogen inlet, the 3rd nitrogen outlet, the second unstripped gas entrance, the second unstripped gas outlet, third high pressure nitrogen inlet, third high pressure nitrogen outlet, the first flashed liquid entrance, the 3rd fuel gas outlet, the 3rd synthetic gas entrance, the 3rd syngas outlet, the first natural gas liquids entrance, the first natural gas liquids outlet and the first flash gas entrance;
The first nitrogen expansion machine;
The second nitrogen expansion machine;
Nitrogen wash column, this nitrogen wash column top have a liquid nitrogen entrance, and the top has a nitrogen gas washing outlet, and the bottom has a unstripped gas entrance, and the bottom has a cut outlet;
The first flash tank, this first flash tank top have a unstripped gas entrance, and the top has a unstripped gas outlet, and the bottom has a liquid exit;
The second flash tank, this second flash tank top have gas inlet and the cut entrance after a rectifying, and the top has a flash gas outlet, and the bottom has a flashed liquid outlet;
Methane rectifying tower, this methane rectifying tower middle and upper part have a unstripped gas entrance, and the top has the pneumatic outlet after a rectifying, and the bottom has a reboiler, and the bottom has a natural gas liquids outlet;
the high pressure nitrogen that divides from sky is connected with the first high pressure nitrogen entrance on the high pressure nitrogen cooling apparatus by the first high pressure nitrogen line of pipes, the first high pressure nitrogen entrance and the outlet of the first high pressure nitrogen connect, the second high pressure nitrogen line of pipes is told in the first high pressure nitrogen outlet and third high is pressed the nitrogen line of pipes, the second high pressure nitrogen line of pipes is connected with the entrance of the first nitrogen expansion machine, and third high presses the nitrogen line of pipes to be connected with the second high pressure nitrogen entrance on the first unstripped gas water cooler, the second high pressure nitrogen entrance is communicated with the second high pressure nitrogen outlet, the 4th high pressure nitrogen line of pipes is told in the second high pressure nitrogen outlet, the 5th high pressure nitrogen line of pipes and the 6th high pressure nitrogen line of pipes, the 4th high pressure nitrogen line of pipes is connected with the reboiler entrance of methane rectifying tower bottom, the 5th high pressure nitrogen line of pipes is connected with the entrance of the second nitrogen expansion machine, the 6th high pressure nitrogen line of pipes presses nitrogen inlet to be connected with the third high of the second unstripped gas water cooler, third high presses nitrogen inlet and third high to press nitrogen outlet to be communicated with, third high presses nitrogen outlet to be connected with the liquid nitrogen entrance on nitrogen wash column top by the first liquid nitrogen line of pipes,
Be connected with the first unstripped gas entrance of the first unstripped gas water cooler by the first unstripped gas line of pipes by the unstripped gas out of the molecular sieve in low-temperature rectisol, the first unstripped gas entrance is communicated with the first unstripped gas outlet, the first unstripped gas outlet is connected with the second unstripped gas entrance on the second unstripped gas water cooler by the second unstripped gas export pipeline, the second unstripped gas entrance is communicated with the second unstripped gas outlet, and the second unstripped gas outlet is passed through the 3rd unstripped gas line of pipes and is connected with the unstripped gas entrance on the first flash tank top;
The outlet of the unstripped gas of the first flash drum overhead is connected with the unstripped gas entrance of nitrogen wash column bottom by the unstripped gas line of pipes, and the liquid exit bottom the first flash tank is connected with the unstripped gas entrance of methane rectifying tower middle and upper part by fluid-carrying lines;
the nitrogen gas washing outlet at nitrogen wash column top is connected with the first entrance of a constant enthalpy current regulator by nitrogen gas washing line of pipes, the second entrance of isenthalpic throttling device is connected with the first liquid nitrogen line of pipes by the second liquid nitrogen line of pipes, the outlet of isenthalpic throttling device is connected with the 3rd synthetic gas entrance on the second unstripped gas water cooler, the 3rd synthetic gas entrance is communicated with the 3rd syngas outlet, the 3rd syngas outlet is connected with the second synthetic gas entrance on the first unstripped gas water cooler by the first synthetic gas line of pipes, the second synthetic gas entrance is communicated with the second syngas outlet, the second syngas outlet is told the second synthetic gas line of pipes and the 3rd synthetic gas line of pipes, the second synthetic gas line of pipes is connected with the low-temperature rectisol operation, the 3rd synthetic gas line of pipes is connected with the first synthetic gas entrance on the high pressure nitrogen water cooler, the first synthetic gas entrance is communicated with the first syngas outlet, the first syngas outlet is connected with the ammonia synthesis operation by the 4th synthetic gas line of pipes, wherein the 4th synthetic gas line of pipes also becomes the letter shoot line to be connected with the low-temperature rectisol operation by pentahapto,
the cut outlet of nitrogen wash column bottom is connected by the cut entrance of cut line of pipes with the second flash tank top, gas inlet after the rectifying on the air shooter line of the pneumatic outlet after the rectifying at methane rectifying tower top after by rectifying and the second flash tank top is connected, the outlet of the flash gas of the second flash drum overhead is connected with the first flash gas entrance on the second unstripped gas water cooler by the flash gas line of pipes, the gas outlet of methane rectifier bottoms is connected with the first natural gas liquids entrance on the second unstripped gas water cooler by the first natural gas liquids line of pipes, the first natural gas liquids outlet on the second unstripped gas water cooler is communicated with the first natural gas liquids entrance and the first flash gas entrance, the first natural gas liquids outlet is connected with LNG tank by the second natural gas liquids line of pipes,
the flashed liquid outlet of the second flash tank bottom is connected with the first flashed liquid entrance on the second unstripped gas water cooler by the flashed liquid line of pipes, the 3rd fuel gas outlet on the second unstripped gas water cooler is communicated with the first flashed liquid entrance and the first flash gas entrance, the 3rd fuel gas outlet is connected with the second fuel gas entrance on the first unstripped gas water cooler by the first fuel gas line of pipes, the second fuel gas entrance is communicated with the second fuel gas outlet, the second fuel gas outlet is connected with the first fuel gas entrance on the high pressure nitrogen water cooler by the second fuel gas line of pipes, the first fuel gas entrance is communicated with the first fuel gas outlet, the first fuel gas outlet is connected with fuel gas system by the 3rd fuel gas line of pipes,
the outlet of the second nitrogen expansion machine is connected with the 3rd nitrogen inlet on the second unstripped gas water cooler by the first nitrogen line of pipes, the 3rd nitrogen inlet is communicated with the 3rd nitrogen outlet, the 3rd nitrogen outlet is told the second nitrogen line of pipes and the 3rd nitrogen line of pipes, the second nitrogen line of pipes is connected with the outlet of the first nitrogen expansion machine, the 3rd nitrogen line of pipes is connected with the second nitrogen inlet on the first unstripped gas water cooler, the second nitrogen inlet is communicated with the second nitrogen outlet, the second nitrogen outlet is connected with the first nitrogen inlet on the high pressure nitrogen water cooler by the 4th nitrogen line of pipes, the first nitrogen inlet is communicated with the first nitrogen outlet, nitrogen compressor entrance during the first nitrogen outlet passes through the 5th nitrogen line of pipes and sky divides is connected.
2. fixed bed broken coal pressing gas as claimed in claim 1 ammonia synthesis gas processed and natural gas liquids combination preparing device, it is characterized in that, the 5th high pressure nitrogen line of pipes and the 6th high pressure nitrogen line of pipes are told in the second high pressure nitrogen outlet, the 5th high pressure nitrogen line of pipes is connected with entrance with the second nitrogen expansion machine, and the 6th high pressure nitrogen line of pipes presses nitrogen inlet to be connected with the third high of the second unstripped gas water cooler; The second unstripped gas export pipeline and the second unstripped gas output by-pass line are told in the first unstripped gas outlet, the second unstripped gas export pipeline is connected with the second unstripped gas entrance on the second unstripped gas water cooler, and the second unstripped gas output by-pass line is connected with the reboiler entrance of methane rectifying tower bottom.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220355622 CN202988709U (en) | 2012-07-20 | 2012-07-20 | Device for co-producing ammonia synthesis gas and liquefied natural gas by conny pressurization and gasification by fixed bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220355622 CN202988709U (en) | 2012-07-20 | 2012-07-20 | Device for co-producing ammonia synthesis gas and liquefied natural gas by conny pressurization and gasification by fixed bed |
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| Publication Number | Publication Date |
|---|---|
| CN202988709U true CN202988709U (en) | 2013-06-12 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220355622 Withdrawn - After Issue CN202988709U (en) | 2012-07-20 | 2012-07-20 | Device for co-producing ammonia synthesis gas and liquefied natural gas by conny pressurization and gasification by fixed bed |
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| CN (1) | CN202988709U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102757016A (en) * | 2012-07-20 | 2012-10-31 | 上海国际化建工程咨询公司 | Method and device for cogeneration of synthesis ammonia gas and liquefied natural gas prepared through pressure gasification of crushed coal in fixed bed |
-
2012
- 2012-07-20 CN CN 201220355622 patent/CN202988709U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102757016A (en) * | 2012-07-20 | 2012-10-31 | 上海国际化建工程咨询公司 | Method and device for cogeneration of synthesis ammonia gas and liquefied natural gas prepared through pressure gasification of crushed coal in fixed bed |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20130612 Effective date of abandoning: 20150422 |