CN102757016B - Method and device for cogeneration of synthesis ammonia gas and liquefied natural gas prepared through pressure gasification of crushed coal in fixed bed - Google Patents
Method and device for cogeneration of synthesis ammonia gas and liquefied natural gas prepared through pressure gasification of crushed coal in fixed bed Download PDFInfo
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- CN102757016B CN102757016B CN201210254264.0A CN201210254264A CN102757016B CN 102757016 B CN102757016 B CN 102757016B CN 201210254264 A CN201210254264 A CN 201210254264A CN 102757016 B CN102757016 B CN 102757016B
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Abstract
The invention discloses a method for cogeneration of synthesis ammonia gas and liquefied natural gas prepared through pressure gasification of crushed coal in a fixed bed. In the method, through appropriate allocation of the processes among a high-pressure nitrogen gas cooler, raw material gas coolers, a nitrogen gas expander, a nitrogen washing column, flash tanks and methane rectifying columns, the cogeneration of the liquefied natural gas is achieved, so that the effects of low investment, low energy consumption, high heating value and high efficiency are achieved. The invention further discloses a device for cogeneration of synthesis ammonia gas and liquefied natural gas prepared through pressure gasification of crushed coal in the fixed bed.
Description
Technical field
The present invention relates to synthetic ammonia gas purification technique field, especially BGL(British Gas-Lurgi is utilized for one) 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, in particular to one low temperature liquid nitrogen as absorption agent, remove CO in mixed gas, Ar, CH4, and isolated methane fraction is refined as the fixed bed broken coal pressurized coal gasification ammonia synthesis gas of high purity liquefied natural gas product and high purity natural gas liquids co-production and device in this treating processes, the method and device are applicable to synthetic gas (hydrogen, carbon monoxide, nitrogen, methane, argon) the purification less energy-consumption new type low temperature liquid nitrogen washing (gas removal) in synthetic ammonia field processed and high purity natural gas liquids co-production technology.
Background technology
At present, the unstripped gas after BGL or the Lurgi gasification of many coal chemical industry enterprises, basal component also has portion of methane except carbon monoxide, hydrogen.Need to remove the rare gas element such as methane or the gas harmful to catalyzer through liquid nitrogen washing operation in synthetic ammonia process of producing product, then get back to again liquid nitrogen washing operation after methane rich cut is delivered to the workshop sections such as methane conversion, most Zhongdao synthesis procedure produces ammonia.
Synthetic ammonia process like this based on BGL or Lurgi stove constitutes a loop chain during the course, this chain as shown in Figure 1, itself BGL or Lurgi stove raw gas of coming is sent into low-temperature rectisol and liquid nitrogen washing operation and is removed the rare gas elementes such as methane or produce ammonia to being sent to synthesis procedure after the harmful gas of catalyzer after CO conversion, gets back to again liquid nitrogen washing operation after the methane rich cut of liquid nitrogen washing operation delivers to the workshop section such as methane conversion, CO conversion.This flow process exists following not enough: 1, this process energy consumption is high, waste resource; 2, the variable effect methane conversion workshop section of the CH4 cut that liquid nitrogen washing workshop section is next; 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, improving calorific value and the rate of recovery of methane, the methane fraction in liquid nitrogen washing process can be refined as high purity natural gas liquids, exporting as byproduct, will very important economic results in society be produced.
Natural gas liquids is the clean energy developed rapidly in recent years, have pollution-free, calorific value is high, be convenient to transport, remote mountain areas can be solved or be not easy to cloth pipe network area combustion gas use.Along with the development of society, the progress of science and technology and the mankind strengthen the consciousness of environment protection, in recent years, natural gas liquids receives much concern as clean energy.
Be gasification process with BGL or Lurgi vapourizing furnace, can produce synthetic ammonia and high purity natural gas liquids will be a brand-new problem simultaneously, can realize the coproduction of synthetic ammonia and high purity natural gas liquids, and the key problem of this coproduction is that the energy consumption as how lower realizes gas cleaning and is separated.
Summary of the invention
One of technical problem to be solved by this invention is for the problem existing for prior art and provides a kind of fixed bed broken coal pressurized coal gasification ammonia synthesis gas and high purity natural gas liquids co-production, the method is by liquid nitrogen washing device and low ternperature separation process technology, eliminate the methane conversion workshop section of complex procedures in Conventional synthesis gas production process, in removing synthetic gas while indifferent gas, be highly purified natural gas liquids by methane fraction concentrate.And unstripped gas is through purification and methane separation, has both reduced the impact of synthesis loop indifferent gas, and has decreased discharge amount of exhaust gas, and achieved synthetic ammonia and the coproduction of high purity natural gas liquids, have significant economic and social benefit.
Two of technical problem to be solved by this invention is for the problem existing for prior art and provides a kind of fixed bed broken coal pressurized coal gasification ammonia synthesis gas and high-purity device.
As fixed bed broken coal pressurized coal gasification ammonia synthesis gas and the natural gas liquids co-production of first aspect present invention, it is characterized in that,
After entering the liquid nitrogen washing cold box of liquid nitrogen washing operation by the first unstripped gas out of the molecular sieve in low-temperature rectisol, first in the first unstripped gas water cooler, heat exchange is carried out with the second crude synthesis gas entered in the first unstripped gas water cooler that backflows, the second fuel gas, the second unstripped gas after heat exchange again carries out heat exchange with the first crude synthesis gas, the first fuel gas and the methane rich cut entered in the second unstripped gas water cooler that backflow again in the 3rd unstripped gas water cooler, and after going out the second unstripped gas water cooler, the 3rd unstripped gas enters in the first flash tank and carries out gas-liquid separation, first flash tank out isolate the bottom that the 4th unstripped gas being rich in methane enters nitrogen wash column, in nitrogen wash column, the middle hydraulic fluid nitrogen that the 4th unstripped gas and the nitrogen wash column tower top of rising come becomes counter current contact, and carries out mass transfer, heat transfer, the gaseous impurities condensation of CO, CH4, Ar in the 4th unstripped gas is dissolved in liquid nitrogen, and the first nitrogen gas washing containing a small amount of nitrogen after purification leaves nitrogen wash column by nitrogen wash column tower top, by nitrogen wash column tower top out containing the first nitrogen gas washing of a small amount of nitrogen be incorporated to a part by the second unstripped gas water cooler out in form the second nitrogen gas washing after hydraulic fluid nitrogen, second nitrogen gas washing backflows and enters in the second unstripped gas water cooler and the first crude synthesis gas entered in the second unstripped gas water cooler that backflows, first fuel gas and methane rich cut carry out heat exchange, the 3rd nitrogen gas washing going out the 3rd unstripped gas water cooler after heat exchange allocates the first crude synthesis gas that a part of high pressure nitrogen formation H2/N2 volume ratio reaches 3 into, first crude synthesis gas enters in the first unstripped gas water cooler and carries out heat exchange and form the second crude synthesis gas and send the first unstripped gas water cooler, the second crude synthesis gas going out the first unstripped gas water cooler is divided into two strands, one is that the 3rd crude synthesis gas enters in high pressure nitrogen water cooler, cool the first high pressure nitrogen entered in high pressure nitrogen water cooler together with the 3rd fuel gas entering high pressure nitrogen water cooler, going out the 5th crude synthesis gas after high pressure nitrogen water cooler is normal temperature, another strand is that the 4th crude synthesis gas send low-temperature rectisol operation to return the cold brought from low-temperature rectisol operation by Purge gas to form purified gas, purified gas return to converge with the 5th crude synthesis gas of high pressure nitrogen cooler outlet accurate adjustment become H2/N2 volume ratio be 3 synthetic gas send into ammonia synthesis operation,
The high pressure nitrogen entering liquid nitrogen washing operation, in high pressure nitrogen water cooler, is divided into two portions after being cooled by the 3rd crude synthesis gas, the 3rd fuel gas and the 3rd nitrogen entered in high pressure nitrogen water cooler: a part is obtain the first nitrogen after the first high pressure nitrogen enters the first nitrogen expansion machine expansion acquisition cold; Another part is that the second high pressure nitrogen enters in the first unstripped gas water cooler, forms formation second high pressure nitrogen after being cooled further by the second crude synthesis gas, the second fuel gas and the second nitrogen entered in the first unstripped gas water cooler again; Three parts are divided into by the first unstripped gas water cooler the second high pressure nitrogen out, wherein a part is third high pressure nitrogen, third high pressure nitrogen then enters in the second unstripped gas water cooler, is cooled hydraulic fluid nitrogen in described in rear formation further by the first crude synthesis gas, the first fuel gas and the second nitrogen entered in the second unstripped gas water cooler; A part is the 4th high pressure nitrogen, and the 4th high pressure nitrogen enters the second nitrogen expansion machine expansion acquisition cold and forms the second nitrogen; Part III is the thermal source of reboiler as reboiler that the 5th high pressure nitrogen sends into methane rectifier bottoms; Reboiler the 6th high pressure nitrogen out with mixed by the first unstripped gas water cooler the second unstripped gas out after send in the 3rd unstripped gas water cooler; The 3rd nitrogen is formed after re-heat in second nitrogen flow back into second unstripped gas water cooler, sends into after 3rd nitrogen mixes with the first nitrogen and to send in high pressure nitrogen water cooler re-heat further after carrying out re-heat in the first unstripped gas water cooler again and forms the 4th nitrogen, after entering the nitrogen compressor supercharging that sky divides after the 4th nitrogen goes out high pressure nitrogen water cooler, return high pressure nitrogen water cooler; A described middle hydraulic fluid nitrogen part enters nitrogen wash column tower top, and another part mixes with the first nitrogen gas washing containing a small amount of nitrogen after the purification sent here by nitrogen wash column tower top, becomes the second described nitrogen gas washing;
Sent in methane rectifying tower carried out rectifying by the described first flash tank methane liquid that is rich in out, gas after rectifying is sent by methane rectifying tower tower top and is sent in the second flash tank after decompression, with together with cut out bottom described nitrogen wash column, carry out gas-liquid separation, send into after the second unstripped gas water cooler carries out mixing re-heat through the isolated gas of the second flash tank and liquid and form the first fuel gas, the second fuel gas formed after first fuel gas re-heat is sent into the further re-heat of the first unstripped gas water cooler and is formed the 3rd fuel gas, 3rd fuel gas feeding high pressure nitrogen water cooler further re-heat formation fuel gas is sent to fuel gas system,
The methane rich cut of described methane rectifier bottoms discharge is sent into after the second unstripped gas water cooler carries out cooling further and is formed natural gas liquids feeding LNG tank.
In a preferred embodiment of the inventive method, two parts are divided into by the first unstripped gas water cooler the second high pressure nitrogen out, wherein a part is third high pressure nitrogen, third high pressure nitrogen then enters in the second unstripped gas water cooler, is cooled hydraulic fluid nitrogen in described in rear formation further by the first crude synthesis gas, the first fuel gas and the second nitrogen entered in the second unstripped gas water cooler; A part is the 4th high pressure nitrogen, and the 4th high pressure nitrogen enters the second nitrogen expansion machine expansion acquisition cold and forms the second nitrogen; The second unstripped gas after heat exchange is divided into two portions, a part again carries out heat exchange with the first crude synthesis gas, the first fuel gas and the methane rich cut entered in the second unstripped gas water cooler that backflow again in the 3rd unstripped gas water cooler, and another part sends into the thermal source of reboiler as reboiler of methane rectifier bottoms.
As fixed bed broken coal pressurized coal gasification ammonia synthesis gas and the natural gas liquids combination preparing device of second aspect present invention, it is characterized in that, comprising:
High pressure nitrogen water cooler, this high pressure nitrogen water cooler has 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;
First unstripped gas water cooler, this first unstripped gas water cooler has 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;
Second unstripped gas water cooler, this second unstripped gas water cooler has 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;
First nitrogen expansion machine;
Second nitrogen expansion machine;
Nitrogen wash column, this nitrogen wash column top has a liquid nitrogen entrance, and top has a nitrogen gas washing outlet, and bottom has the unstripped gas entrance that is rich in methane, and bottom has a fraction outlets;
First flash tank, this first flash tank top has a unstripped gas entrance, and top has the unstripped gas outlet that is rich in methane, and bottom has one and is rich in methane liquid outlet;
Second flash tank, this second flash tank top has the gas inlet after a rectifying and a cut entrance, and top has a flash gas outlet, and bottom has a flashed liquid outlet;
Methane rectifying tower, this methane rectifying tower middle and upper part has the unstripped gas entrance that is rich in methane, and top has the pneumatic outlet after a rectifying, and bottom has a reboiler, and bottom has a natural gas liquids outlet;
The high pressure nitrogen divided from sky is connected with the first high pressure nitrogen entrance on high pressure nitrogen cooling apparatus by the first high pressure nitrogen line of pipes, first high pressure nitrogen entrance and the first high pressure nitrogen export through, first high pressure nitrogen outlet separates the second high pressure nitrogen line of pipes and third high pressure nitrogen line of pipes, second high pressure nitrogen line of pipes is connected with the entrance of the first nitrogen expansion machine, and third high pressure nitrogen line of pipes is connected with the second high pressure nitrogen entrance on the first unstripped gas water cooler, second high pressure nitrogen entrance and the second high pressure nitrogen outlet, second high pressure nitrogen outlet separates the 4th high pressure nitrogen line of pipes, 5th high pressure nitrogen line of pipes and the 6th high pressure nitrogen line of pipes, 4th high pressure nitrogen line of pipes is connected with the reboiler entrance of methane rectifying tower bottom, 5th high pressure nitrogen line of pipes is connected with the entrance of the second nitrogen expansion machine, 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 pressure nitrogen inlet presses nitrogen outlet to be communicated with third high, third high pressure nitrogen outlet is 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, first unstripped gas entrance and the first unstripped gas outlet, 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, second unstripped gas entrance and the second unstripped gas outlet, the second unstripped gas outlet is connected by the unstripped gas entrance of the 3rd unstripped gas line of pipes with the first flash tank top;
The unstripped gas outlet of being rich in methane of the first flash drum overhead is connected by the unstripped gas entrance being rich in methane of the unstripped gas line of pipes with nitrogen wash column bottom that are rich in methane, and the methane liquid outlet of being rich in bottom the first flash tank is connected with the unstripped gas entrance being rich in methane of methane rectifying tower middle and upper part by being rich in methane liquid line of pipes;
The nitrogen gas washing outlet at nitrogen wash column top is connected by first entrance of nitrogen gas washing line of pipes with a constant enthalpy current regulator, 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, 3rd synthetic gas entrance is communicated with the 3rd syngas outlet, 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, second synthetic gas entrance is communicated with the second syngas outlet, second syngas outlet separates the second synthetic gas line of pipes and the 3rd synthetic gas line of pipes, second synthetic gas line of pipes is connected with low-temperature rectisol operation, 3rd synthetic gas line of pipes is connected with the first synthetic gas entrance on high pressure nitrogen water cooler, first synthetic gas entrance is communicated with the first syngas outlet, first syngas outlet is connected with ammonia synthesis operation by the 4th synthetic gas line of pipes, wherein the 4th synthetic gas line of pipes also becomes letter shoot line to be connected with low-temperature rectisol operation by pentahapto,
Fraction outlets bottom nitrogen wash column is connected with the cut entrance on the second flash tank top by cut line of pipes, pneumatic outlet after the rectifying at methane rectifying tower top is connected with the gas inlet after the rectifying on the second flash tank top by the air shooter line after rectifying, the flash gas outlet of the second flash drum overhead is connected with the first flash gas entrance on the second unstripped gas water cooler by 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 second unstripped gas water cooler is communicated with the first flash gas entrance with the first natural gas liquids entrance, first natural gas liquids outlet is connected with LNG tank by the second natural gas liquids line of pipes,
Flashed liquid outlet bottom second flash tank is connected with the first flashed liquid entrance on the second unstripped gas water cooler by flashed liquid line of pipes, the 3rd fuel gas outlet on second unstripped gas water cooler is communicated with the first flash gas entrance with the first flashed liquid entrance, 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, second fuel gas entrance and the second fuel gas outlet, second fuel gas outlet is connected with the first fuel gas entrance on high pressure nitrogen water cooler by the second fuel gas line of pipes, first fuel gas entrance and the first fuel gas outlet, 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, 3rd nitrogen inlet is communicated with the 3rd nitrogen outlet, 3rd nitrogen outlet separates the second nitrogen line of pipes and the 3rd nitrogen line of pipes, second nitrogen line of pipes is connected with the outlet of the first nitrogen expansion machine, 3rd nitrogen line of pipes is connected with the second nitrogen inlet on the first unstripped gas water cooler, second nitrogen inlet is communicated with the second nitrogen outlet, second nitrogen outlet is connected with the first nitrogen inlet on high pressure nitrogen water cooler by the 4th nitrogen line of pipes, first nitrogen inlet is communicated with the first nitrogen outlet, first nitrogen outlet is connected with the nitrogen compressor entrance in empty point by the 5th nitrogen line of pipes.
In a preferred embodiment of apparatus of the present invention, second high pressure nitrogen outlet only separates the 5th high pressure nitrogen line of pipes and the 6th high pressure nitrogen line of pipes, 5th high pressure nitrogen line of pipes is connected with the entrance of 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; First unstripped gas outlet separates the second unstripped gas export pipeline and the second unstripped gas exports by-pass line, 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 exports by-pass line and is connected with the reboiler entrance of methane rectifying tower bottom.
Owing to have employed technical scheme as above, the present invention has following functions:
1. methane rectifying tower is set, make the methane rich of cooling box form reach the highly purified natural gas liquids of LNG() specification, farthest reclaimed methane in unstripped gas.
2. arrange liquid-mixing nitrogen and gas to join two kinds, nitrogen and slightly join nitrogen mode, give full play to efficiency of heat exchanger.
3. the mode that at the bottom of methane rectifying tower, reboiler heat duty is adjustable is set, ensures the highly purified natural gas liquids of LNG() product specification.
4. arrange nitrogen wash column, the synthetic gas specification 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. staged nitrogen expansion is set, cold is provided.
According to idiographic flow, the present invention also can have following functions:
1. the synthetic gas essence only selecting liquid-mixing nitrogen slightly to join nitrogen and cooling box joins nitrogen.
2. arrange and supplement the mode of cold from sky liquid nitrogen of assigning to.
Ammonia synthesis gas field of purification is developed one and is applicable to fixed bed broken coal pressurized coal gasification and high purity natural gas liquids coproduction flow process at home, synthetic ammonia and the coproduction of high purity natural gas liquids is realized, the novel low temperature separation process of Low investment, less energy-consumption and purification techniques in this flow process.Modified flow configures, by-product high purity natural gas liquids while reaching decontamination effect improving, thus reaches the effect of Low investment less energy-consumption high heating value high benefit.
Compared with joining methane conversion with traditional liquid nitrogen washing device, apparatus of the present invention have the following advantages:
1. static equipment investment is lower.Only increase a rectifying tower, miscellaneous equipment such as the size of interchanger, nitrogen wash column can remain unchanged.
2. add the refrigeration cycle of nitrogen expansion, the highly purified natural gas liquids of by-product.
3. synthesic gas compressor power consumption can not increase.Though the by-product product of high purity natural gas liquids, the cold in ice chest is redistributed and is utilized, and remains unchanged, therefore can not increase the power consumption of synthetic compressor can the synthetic gas channel resistance ensureing in ice chest falls.
4. by-product high purity liquefies the product of natural specification.Methane recovery can bring up to 88%.Improve the environment protection of life of urban resident environment and near cities manufacturing district; Solve the requirement of industrial and mining enterprises for clean fuel simultaneously cannot laying gas distributing system away from neutralizing gas.
5. strict guarantee synthetic gas specification.Though the by-product product of high purity natural gas liquids specification, do not increase extra cold again, resistance drop remains unchanged again, can ensure that synthetic gas goes the specification of synthesis loop.
Accompanying drawing explanation
Fig. 1 is the synthetic ammonia process block diagram of existing BGL or Lurgi stove.
Fig. 2 is fixed bed broken coal pressurized coal gasification ammonia synthesis gas of the present invention and natural gas liquids coproduction FB(flow block).
Fig. 3 is fixed bed broken coal pressurized coal gasification ammonia synthesis gas and the natural gas liquids combination preparing device schematic diagram of the embodiment of the present invention 1.
Fig. 4 is fixed bed broken coal pressurized coal gasification ammonia synthesis gas and the natural gas liquids combination preparing device schematic diagram of the embodiment of the present invention 1.
Embodiment
The present invention is further described below in conjunction with the drawings and specific embodiments.
Embodiment 1
See Fig. 3, the fixed bed broken coal pressurized coal gasification ammonia synthesis gas provided in figure and natural gas liquids combination preparing device, 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.
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;
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 top has a nitrogen gas washing outlet 51, and bottom has the unstripped gas entrance 52 that is rich in methane, and bottom has a fraction outlets 53.
Flash tank V-01 top has a unstripped gas entrance 61, and top has the unstripped gas outlet 62 that is rich in methane, and bottom has one and is rich in methane liquid outlet 63; Flash tank V-02 top has the gas inlet after a rectifying 70 and a cut entrance 71, and top has a flash gas outlet 72, and bottom has a flashed liquid outlet 73;
Methane rectifying tower T-02 middle and upper part has the unstripped gas entrance 80 that is rich in methane, and top has the pneumatic outlet 81 after a rectifying, and bottom has a reboiler 82, and bottom has a natural gas liquids outlet 83.
The high pressure nitrogen 100 divided from sky is connected with the 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 and high pressure nitrogen export 12 through, high pressure nitrogen outlet 12 separates high pressure nitrogen line of pipes 91 and 92, 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 the high pressure nitrogen entrance 24 on the first unstripped gas water cooler E-02, high pressure nitrogen entrance 24 and high pressure nitrogen export 25 and are communicated with, high pressure nitrogen outlet 25 separates high pressure nitrogen line of pipes B1, 93, 94, high pressure nitrogen line of pipes B1 is connected with reboiler 82 entrance 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 and high pressure nitrogen export 35 and are communicated with, high pressure nitrogen outlet 34 is connected by the liquid nitrogen entrance 50 of liquid nitrogen line of pipes 95 with nitrogen wash column T-01 top.
Be connected by the unstripped gas entrance 20 of unstripped gas line of pipes 96 with the first unstripped gas water cooler E-02 by the unstripped gas 110 out of the molecular sieve in low-temperature rectisol, unstripped gas entrance 20 and unstripped gas export 21 and are communicated with, unstripped gas outlet 21 is connected with the 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 export 33 and are communicated with, and unstripped gas outlet 33 is connected by the unstripped gas entrance 61 of unstripped gas line of pipes 98 with flash tank V-01 top.
The unstripped gas outlet 62 of being rich in methane at flash tank V-01 top is connected by the unstripped gas entrance 52 being rich in methane of the unstripped gas line of pipes 99 with nitrogen wash column T-01 bottom that are rich in methane, and the methane liquid outlet 63 of being rich in bottom flash tank V-01 is connected with the unstripped gas entrance 80 being rich in methane of methane rectifying tower T-02 middle and upper part by being rich in methane liquid line of pipes 101.
The nitrogen gas washing outlet 51 at nitrogen wash column T-01 top is connected by the entrance 84 of nitrogen gas washing line of pipes 102 with a constant enthalpy current regulator M-01, 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 the 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 the 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 separates 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 the 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 is also connected with low-temperature rectisol operation 120 by synthetic gas line of pipes 108.
Fraction outlets 53 bottom nitrogen wash column T-01 is connected by the cut entrance 71 of cut line of pipes 109 with flash tank V-02 top, pneumatic outlet 81 after the rectifying at methane rectifying tower T-02 top is connected with the gas inlet 70 after the rectifying on flash tank V-02 top by the air shooter line 111 after rectifying, the flash gas outlet 72 at flash tank V-02 top is connected with the flash gas entrance 42 on the second unstripped gas water cooler E-03 by flash gas line of pipes 112, natural gas liquids outlet 83 bottom methane rectifying tower T-02 is connected with the 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 flash gas entrance 42 with natural gas liquids entrance 40, natural gas liquids outlet 41 is connected with LNG tank 140 by natural gas liquids line of pipes 114.
Flashed liquid outlet 73 bottom flash tank V-02 is connected with the 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 second unstripped gas water cooler E-03 is communicated with flash gas entrance 43 with flashed liquid entrance 36, fuel gas outlet 37 is connected with the fuel gas entrance 26 on the first unstripped gas water cooler E-02 by fuel gas line of pipes 116, fuel gas entrance 26 and fuel gas export 27 and are communicated with, fuel gas outlet 27 is connected with the fuel gas entrance 13 on high pressure nitrogen water cooler E-01 by fuel gas line of pipes 117, fuel gas entrance 13 and fuel gas export 14 and are communicated with, 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 the 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 separates nitrogen line of pipes 121, 122, 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 the 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 the 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 outlet 16 is connected with nitrogen compressor 160 entrance in empty point by nitrogen line of pipes 124.
The workflow of above-mentioned fixed bed broken coal pressurized coal gasification ammonia synthesis gas and natural gas liquids combination preparing device is as follows:
From the unstripped gas 100 of molecular sieve after the first unstripped gas water cooler E-02 and the second unstripped gas water cooler E-03 heat exchange, send in flash tank V-01, gas in flash tank V-01 after 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, the first unstripped gas water cooler E-02 is entered after re-heat in the second unstripped gas water cooler E-03, thick synthetic gas specification is formed, this crude synthesis gas part to ammonia synthesis operation 130, arrives ammonia synthesis operation 130 after another part reclaims cold to low-temperature rectisol operation 120 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 cools further, in this liquid, methane content is 95%(mol), CO<1000ppmv, can be used as high purity natural gas liquids and uses.
High pressure nitrogen first all sends into high pressure nitrogen water cooler E-01 step-down, two portions are divided into by high pressure nitrogen water cooler E-01 high pressure nitrogen out, a part enters nitrogen expansion machine K-01, another part enters the first unstripped gas water cooler E-02 and cools, the high pressure nitrogen going out the first unstripped gas water cooler E-02 is divided into two portions again, and a part enters nitrogen expansion machine K-02; Another part enters the second unstripped gas water cooler E-03.The high pressure nitrogen entered after the second unstripped gas water cooler E-03 is liquefied formation liquid nitrogen.
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 washing liquid nitrogen; Another part liquid nitrogen is incorporated in synthetic gas.The nitrogen that nitrogen expansion machine K-02 goes out enters the first unstripped gas water cooler E-02 again after mixing with the nitrogen gone out through nitrogen expansion machine K-01 after the second unstripped gas water cooler E-03 re-heat and carries out re-heat, nitrogen after re-heat sends into further re-heat cooling box in high pressure nitrogen water cooler E-01, then gets back to this cold box system after the nitrogen compressor compression that sky divides.
Send in flash tank V-02 after gas after the rectifying that cut out and methane rectifying tower T-02 tower top come at the bottom of nitrogen wash column T-01 tower merges and carry out gas-liquid separation, gas after flash tank V-02 is separated and liquid send into mixing in the second unstripped gas water cooler E-03 in the lump and re-heat forms thick fuel gas, and thick fuel gas does 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 101490Nm3/h, pressure 4.7MPa(G), synthetic ammonia output is 1050MTPD, and the amount of by-product high purity natural gas liquids is 5,700 ten thousand Nm
3/ y, methane content is 95% (mol), and CO<1000ppmv, the rate of recovery is about 88%.
Embodiment 2
See Fig. 4, this embodiment fixed bed broken coal pressurized coal gasification ammonia synthesis gas and natural gas liquids combination preparing device substantially the same manner as Example 1, just high pressure nitrogen exports 25 and separates high pressure nitrogen line of pipes 93,94, 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 outlet 21 separates unstripped gas export pipeline 97 and unstripped gas exports by-pass line A1, unstripped gas exports by-pass line A1 and is connected with reboiler 82 entrance of methane rectifying tower T-02 bottom, unstripped gas export pipeline 97 is connected with the unstripped gas entrance 32 on the second unstripped gas water cooler E-03, unstripped gas entrance 32 and unstripped gas export 33 and are communicated with, and unstripped gas outlet 33 is connected by the unstripped gas entrance 61 of unstripped gas line of pipes 98 with flash tank V-01 top.
The fixed bed broken coal pressurized coal gasification ammonia synthesis gas of this embodiment and the workflow of natural gas liquids combination preparing device substantially the same manner as Example 1.
Claims (4)
1. fixed bed broken coal pressurized coal gasification ammonia synthesis gas and natural gas liquids co-production, is characterized in that,
After entering the liquid nitrogen washing cold box of liquid nitrogen washing operation by the first unstripped gas out of the molecular sieve in low-temperature rectisol, first in the first unstripped gas water cooler, heat exchange is carried out with the second crude synthesis gas entered in the first unstripped gas water cooler that backflows, the second fuel gas, the second unstripped gas after heat exchange again carries out heat exchange with the first crude synthesis gas, the first fuel gas and the methane rich cut entered in the second unstripped gas water cooler that backflow again in the 3rd unstripped gas water cooler, and after going out the second unstripped gas water cooler, the 3rd unstripped gas enters in the first flash tank and carries out gas-liquid separation; First flash tank out isolate the bottom that the 4th unstripped gas being rich in methane enters nitrogen wash column; In nitrogen wash column, the middle hydraulic fluid nitrogen that the 4th unstripped gas and the nitrogen wash column tower top of rising come becomes counter current contact, and carries out mass transfer, heat transfer; CO, CH in 4th unstripped gas
4, Ar gaseous impurities condensation be dissolved in liquid nitrogen, leave nitrogen wash column containing the first nitrogen gas washing of a small amount of nitrogen by nitrogen wash column tower top after purification; By nitrogen wash column tower top out containing the first nitrogen gas washing of a small amount of nitrogen be incorporated to a part by the second unstripped gas water cooler out in form the second nitrogen gas washing after hydraulic fluid nitrogen, second nitrogen gas washing backflows to enter in the second unstripped gas water cooler again and carries out heat exchange with the first crude synthesis gas, the first fuel gas and the methane rich cut entered in the second unstripped gas water cooler that backflow, and the 3rd nitrogen gas washing going out the 3rd unstripped gas water cooler after heat exchange allocates the high pressure nitrogen formation H of a part into
2/ N
2volume ratio reaches first crude synthesis gas of 3, and the first crude synthesis gas enters in the first unstripped gas water cooler and carries out heat exchange and form the second crude synthesis gas and send the first unstripped gas water cooler; The second crude synthesis gas going out the first unstripped gas water cooler is divided into two strands, one is that the 3rd crude synthesis gas enters in high pressure nitrogen water cooler, cool the first high pressure nitrogen entered in high pressure nitrogen water cooler together with the 3rd fuel gas entering high pressure nitrogen water cooler, going out the 5th crude synthesis gas after high pressure nitrogen water cooler is normal temperature; Another strand is that the 4th crude synthesis gas send low-temperature rectisol operation to return the cold brought from low-temperature rectisol operation by Purge gas to form purified gas, and purified gas returns and converges accurate adjustment with the 5th crude synthesis gas of high pressure nitrogen cooler outlet and become H
2/ N
2volume ratio is the synthetic gas feeding ammonia synthesis operation of 3;
The high pressure nitrogen entering liquid nitrogen washing operation, in high pressure nitrogen water cooler, is divided into two portions after being cooled by the 3rd crude synthesis gas, the 3rd fuel gas and the 3rd nitrogen entered in high pressure nitrogen water cooler: a part is obtain the first nitrogen after the first high pressure nitrogen enters the first nitrogen expansion machine expansion acquisition cold; Another part is that the second high pressure nitrogen enters in the first unstripped gas water cooler, forms second high pressure nitrogen after being cooled further by the second crude synthesis gas, the second fuel gas and the second nitrogen entered in the first unstripped gas water cooler again; Three parts are divided into by the first unstripped gas water cooler the second high pressure nitrogen out, wherein a part is third high pressure nitrogen, third high pressure nitrogen then enters in the second unstripped gas water cooler, is cooled hydraulic fluid nitrogen in described in rear formation further by the first crude synthesis gas, the first fuel gas and the second nitrogen entered in the second unstripped gas water cooler; A part is the 4th high pressure nitrogen, and the 4th high pressure nitrogen enters the second nitrogen expansion machine expansion acquisition cold and forms the second nitrogen; Part III is the thermal source of reboiler as reboiler that the 5th high pressure nitrogen sends into methane rectifier bottoms; Reboiler the 6th high pressure nitrogen out with mixed by the first unstripped gas water cooler the second unstripped gas out after send in the 3rd unstripped gas water cooler; The 3rd nitrogen is formed after re-heat in second nitrogen flow back into second unstripped gas water cooler, sends into after 3rd nitrogen mixes with the first nitrogen and to send in high pressure nitrogen water cooler re-heat further after carrying out re-heat in the first unstripped gas water cooler again and forms the 4th nitrogen, after entering the nitrogen compressor supercharging that sky divides after the 4th nitrogen goes out high pressure nitrogen water cooler, return high pressure nitrogen water cooler; A described middle hydraulic fluid nitrogen part enters nitrogen wash column tower top, and another part mixes with the first nitrogen gas washing containing a small amount of nitrogen after the purification sent here by nitrogen wash column tower top, becomes the second described nitrogen gas washing;
Sent in methane rectifying tower carried out rectifying by the described first flash tank methane liquid that is rich in out, gas after rectifying is sent by methane rectifying tower tower top and is sent in the second flash tank after decompression, with together with cut out bottom described nitrogen wash column, carry out gas-liquid separation, send into after the second unstripped gas water cooler carries out mixing re-heat through the isolated gas of the second flash tank and liquid and form the first fuel gas, the second fuel gas formed after first fuel gas re-heat is sent into the further re-heat of the first unstripped gas water cooler and is formed the 3rd fuel gas, 3rd fuel gas feeding high pressure nitrogen water cooler further re-heat formation fuel gas is sent to fuel gas system,
The methane rich cut of described methane rectifier bottoms discharge is sent into after the second unstripped gas water cooler carries out cooling further and is formed natural gas liquids feeding LNG tank.
2. fixed bed broken coal pressurized coal gasification ammonia synthesis gas and natural gas liquids co-production, is characterized in that,
After entering the liquid nitrogen washing cold box of liquid nitrogen washing operation by the first unstripped gas out of the molecular sieve in low-temperature rectisol, first in the first unstripped gas water cooler with to backflow the second crude synthesis gas entered in the first unstripped gas water cooler, second fuel gas carries out heat exchange, the second unstripped gas after heat exchange is divided into two portions, a part again in the 3rd unstripped gas water cooler with to backflow the first crude synthesis gas entered in the second unstripped gas water cooler, first fuel gas and methane rich cut carry out heat exchange again, another part sends into the thermal source of reboiler as reboiler of methane rectifier bottoms, after going out the second unstripped gas water cooler, the 3rd unstripped gas enters in the first flash tank and carries out gas-liquid separation, first flash tank out isolate the bottom that the 4th unstripped gas being rich in methane enters nitrogen wash column, in nitrogen wash column, the middle hydraulic fluid nitrogen that the 4th unstripped gas and the nitrogen wash column tower top of rising come becomes counter current contact, and carries out mass transfer, heat transfer, CO, CH in 4th unstripped gas
4, Ar gaseous impurities condensation be dissolved in liquid nitrogen, leave nitrogen wash column containing the first nitrogen gas washing of a small amount of nitrogen by nitrogen wash column tower top after purification, by nitrogen wash column tower top out containing the first nitrogen gas washing of a small amount of nitrogen be incorporated to a part by the second unstripped gas water cooler out in form the second nitrogen gas washing after hydraulic fluid nitrogen, second nitrogen gas washing backflows and enters in the second unstripped gas water cooler and the first crude synthesis gas entered in the second unstripped gas water cooler that backflows, first fuel gas and methane rich cut carry out heat exchange, the 3rd nitrogen gas washing going out the 3rd unstripped gas water cooler after heat exchange allocates the first crude synthesis gas that a part of high pressure nitrogen formation H2/N2 volume ratio reaches 3 into, first crude synthesis gas enters in the first unstripped gas water cooler and carries out heat exchange and form the second crude synthesis gas and send the first unstripped gas water cooler, the second crude synthesis gas going out the first unstripped gas water cooler is divided into two strands, one is that the 3rd crude synthesis gas enters in high pressure nitrogen water cooler, cool the first high pressure nitrogen entered in high pressure nitrogen water cooler together with the 3rd fuel gas entering high pressure nitrogen water cooler, going out the 5th crude synthesis gas after high pressure nitrogen water cooler is normal temperature, another strand is that the 4th crude synthesis gas send low-temperature rectisol operation to return the cold brought from low-temperature rectisol operation by Purge gas to form purified gas, and purified gas returns and converges accurate adjustment with the 5th crude synthesis gas of high pressure nitrogen cooler outlet and become H
2/ N
2volume ratio is the synthetic gas feeding ammonia synthesis operation of 3,
The high pressure nitrogen entering liquid nitrogen washing operation, in high pressure nitrogen water cooler, is divided into two portions after being cooled by the 3rd crude synthesis gas, the 3rd fuel gas and the 3rd nitrogen entered in high pressure nitrogen water cooler: a part is obtain the first nitrogen after the first high pressure nitrogen enters the first nitrogen expansion machine expansion acquisition cold; Another part is that the second high pressure nitrogen enters in the first unstripped gas water cooler, forms second high pressure nitrogen after being cooled further by the second crude synthesis gas, the second fuel gas and the second nitrogen entered in the first unstripped gas water cooler again;
Two parts are divided into by the first unstripped gas water cooler the second high pressure nitrogen out, wherein a part is third high pressure nitrogen, third high pressure nitrogen then enters in the second unstripped gas water cooler, is cooled hydraulic fluid nitrogen in described in rear formation further by the first crude synthesis gas, the first fuel gas and the second nitrogen entered in the second unstripped gas water cooler; A part is the 4th high pressure nitrogen, and the 4th high pressure nitrogen enters the second nitrogen expansion machine expansion acquisition cold and forms the second nitrogen;
Reboiler the 6th high pressure nitrogen out with mixed by the first unstripped gas water cooler the second unstripped gas out after send in the 3rd unstripped gas water cooler; The 3rd nitrogen is formed after re-heat in second nitrogen flow back into second unstripped gas water cooler, sends into after 3rd nitrogen mixes with the first nitrogen and to send in high pressure nitrogen water cooler re-heat further after carrying out re-heat in the first unstripped gas water cooler again and forms the 4th nitrogen, after entering the nitrogen compressor supercharging that sky divides after the 4th nitrogen goes out high pressure nitrogen water cooler, return high pressure nitrogen water cooler; A described middle hydraulic fluid nitrogen part enters nitrogen wash column tower top, and another part mixes with the first nitrogen gas washing containing a small amount of nitrogen after the purification sent here by nitrogen wash column tower top, becomes the second described nitrogen gas washing;
Sent in methane rectifying tower carried out rectifying by the described first flash tank methane liquid that is rich in out, gas after rectifying is sent by methane rectifying tower tower top and is sent in the second flash tank after decompression, with together with cut out bottom described nitrogen wash column, carry out gas-liquid separation, send into after the second unstripped gas water cooler carries out mixing re-heat through the isolated gas of the second flash tank and liquid and form the first fuel gas, the second fuel gas formed after first fuel gas re-heat is sent into the further re-heat of the first unstripped gas water cooler and is formed the 3rd fuel gas, 3rd fuel gas feeding high pressure nitrogen water cooler further re-heat formation fuel gas is sent to fuel gas system,
The methane rich cut of described methane rectifier bottoms discharge is sent into after the second unstripped gas water cooler carries out cooling further and is formed natural gas liquids feeding LNG tank.
3. fixed bed broken coal pressurized coal gasification ammonia synthesis gas and a natural gas liquids combination preparing device, is characterized in that, comprising:
High pressure nitrogen water cooler, this high pressure nitrogen water cooler has 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;
First unstripped gas water cooler, this first unstripped gas water cooler has 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;
Second unstripped gas water cooler, this second unstripped gas water cooler has 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;
First nitrogen expansion machine;
Second nitrogen expansion machine;
Nitrogen wash column, this nitrogen wash column top has a liquid nitrogen entrance, and top has a nitrogen gas washing outlet, and bottom has the unstripped gas entrance that is rich in methane, and bottom has a fraction outlets;
First flash tank, this first flash tank top has a unstripped gas entrance, and top has the unstripped gas outlet that is rich in methane, and bottom has one and is rich in methane liquid outlet;
Second flash tank, this second flash tank top has the gas inlet after a rectifying and a cut entrance, and top has a flash gas outlet, and bottom has a flashed liquid outlet;
Methane rectifying tower, this methane rectifying tower middle and upper part has the unstripped gas entrance that is rich in methane, and top has the pneumatic outlet after a rectifying, and bottom has a reboiler, and bottom has a natural gas liquids outlet;
The high pressure nitrogen divided from sky is connected with the first high pressure nitrogen entrance on high pressure nitrogen cooling apparatus by the first high pressure nitrogen line of pipes, first high pressure nitrogen entrance and the first high pressure nitrogen export through, first high pressure nitrogen outlet separates the second high pressure nitrogen line of pipes and third high pressure nitrogen line of pipes, second high pressure nitrogen line of pipes is connected with the entrance of the first nitrogen expansion machine, and third high pressure nitrogen line of pipes is connected with the second high pressure nitrogen entrance on the first unstripped gas water cooler, second high pressure nitrogen entrance and the second high pressure nitrogen outlet, second high pressure nitrogen outlet separates the 4th high pressure nitrogen line of pipes, 5th high pressure nitrogen line of pipes and the 6th high pressure nitrogen line of pipes, 4th high pressure nitrogen line of pipes is connected with the reboiler entrance of methane rectifying tower bottom, 5th high pressure nitrogen line of pipes is connected with the entrance of the second nitrogen expansion machine, 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 pressure nitrogen inlet presses nitrogen outlet to be communicated with third high, third high pressure nitrogen outlet is 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, first unstripped gas entrance and the first unstripped gas outlet, 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, second unstripped gas entrance and the second unstripped gas outlet, the second unstripped gas outlet is connected by the unstripped gas entrance of the 3rd unstripped gas line of pipes with the first flash tank top;
The unstripped gas outlet of being rich in methane of the first flash drum overhead is connected by the unstripped gas entrance being rich in methane of the unstripped gas line of pipes with nitrogen wash column bottom that are rich in methane, and the methane liquid outlet of being rich in bottom the first flash tank is connected with the unstripped gas entrance being rich in methane of methane rectifying tower middle and upper part by being rich in methane liquid line of pipes;
The nitrogen gas washing outlet at nitrogen wash column top is connected by first entrance of nitrogen gas washing line of pipes with a constant enthalpy current regulator, 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, 3rd synthetic gas entrance is communicated with the 3rd syngas outlet, 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, second synthetic gas entrance is communicated with the second syngas outlet, second syngas outlet separates the second synthetic gas line of pipes and the 3rd synthetic gas line of pipes, second synthetic gas line of pipes is connected with low-temperature rectisol operation, 3rd synthetic gas line of pipes is connected with the first synthetic gas entrance on high pressure nitrogen water cooler, first synthetic gas entrance is communicated with the first syngas outlet, first syngas outlet is connected with ammonia synthesis operation by the 4th synthetic gas line of pipes, wherein the 4th synthetic gas line of pipes also becomes letter shoot line to be connected with low-temperature rectisol operation by pentahapto,
Fraction outlets bottom nitrogen wash column is connected with the cut entrance on the second flash tank top by cut line of pipes, pneumatic outlet after the rectifying at methane rectifying tower top is connected with the gas inlet after the rectifying on the second flash tank top by the air shooter line after rectifying, the flash gas outlet of the second flash drum overhead is connected with the first flash gas entrance on the second unstripped gas water cooler by 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 second unstripped gas water cooler is communicated with the first flash gas entrance with the first natural gas liquids entrance, first natural gas liquids outlet is connected with LNG tank by the second natural gas liquids line of pipes,
Flashed liquid outlet bottom second flash tank is connected with the first flashed liquid entrance on the second unstripped gas water cooler by flashed liquid line of pipes, the 3rd fuel gas outlet on second unstripped gas water cooler is communicated with the first flash gas entrance with the first flashed liquid entrance, 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, second fuel gas entrance and the second fuel gas outlet, second fuel gas outlet is connected with the first fuel gas entrance on high pressure nitrogen water cooler by the second fuel gas line of pipes, first fuel gas entrance and the first fuel gas outlet, 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, 3rd nitrogen inlet is communicated with the 3rd nitrogen outlet, 3rd nitrogen outlet separates the second nitrogen line of pipes and the 3rd nitrogen line of pipes, second nitrogen line of pipes is connected with the outlet of the first nitrogen expansion machine, 3rd nitrogen line of pipes is connected with the second nitrogen inlet on the first unstripped gas water cooler, second nitrogen inlet is communicated with the second nitrogen outlet, second nitrogen outlet is connected with the first nitrogen inlet on high pressure nitrogen water cooler by the 4th nitrogen line of pipes, first nitrogen inlet is communicated with the first nitrogen outlet, first nitrogen outlet is connected with the nitrogen compressor entrance in empty point by the 5th nitrogen line of pipes.
4. fixed bed broken coal pressurized coal gasification ammonia synthesis gas and a natural gas liquids combination preparing device, is characterized in that, comprising:
High pressure nitrogen water cooler, this high pressure nitrogen water cooler has 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;
First unstripped gas water cooler, this first unstripped gas water cooler has 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;
Second unstripped gas water cooler, this second unstripped gas water cooler has 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;
First nitrogen expansion machine;
Second nitrogen expansion machine;
Nitrogen wash column, this nitrogen wash column top has a liquid nitrogen entrance, and top has a nitrogen gas washing outlet, and bottom has the unstripped gas entrance that is rich in methane, and bottom has a fraction outlets;
First flash tank, this first flash tank top has a unstripped gas entrance, and top has the unstripped gas outlet that is rich in methane, and bottom has one and is rich in methane liquid outlet;
Second flash tank, this second flash tank top has the gas inlet after a rectifying and a cut entrance, and top has a flash gas outlet, and bottom has a flashed liquid outlet;
Methane rectifying tower, this methane rectifying tower middle and upper part has the unstripped gas entrance that is rich in methane, and top has the pneumatic outlet after a rectifying, and bottom has a reboiler, and bottom has a natural gas liquids outlet;
The high pressure nitrogen divided from sky is connected with the first high pressure nitrogen entrance on high pressure nitrogen cooling apparatus by the first high pressure nitrogen line of pipes, first high pressure nitrogen entrance and the first high pressure nitrogen export through, first high pressure nitrogen outlet separates the second high pressure nitrogen line of pipes and third high pressure nitrogen line of pipes, second high pressure nitrogen line of pipes is connected with the entrance of the first nitrogen expansion machine, and third high pressure nitrogen line of pipes is connected with the second high pressure nitrogen entrance on the first unstripped gas water cooler; Second high pressure nitrogen entrance and the second high pressure nitrogen outlet, second high pressure nitrogen outlet only separates the 5th high pressure nitrogen line of pipes and the 6th high pressure nitrogen line of pipes, 5th high pressure nitrogen line of pipes is connected with the entrance of 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;
First unstripped gas outlet separates the second unstripped gas export pipeline and the second unstripped gas exports by-pass line, 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 exports by-pass line and is connected with the reboiler entrance of methane rectifying tower bottom;
The unstripped gas outlet of being rich in methane of the first flash drum overhead is connected by the unstripped gas entrance being rich in methane of the unstripped gas line of pipes with nitrogen wash column bottom that are rich in methane, and the methane liquid outlet of being rich in bottom the first flash tank is connected with the unstripped gas entrance being rich in methane of methane rectifying tower middle and upper part by being rich in methane liquid line of pipes;
The nitrogen gas washing outlet at nitrogen wash column top is connected by first entrance of nitrogen gas washing line of pipes with a constant enthalpy current regulator, 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, 3rd synthetic gas entrance is communicated with the 3rd syngas outlet, 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, second synthetic gas entrance is communicated with the second syngas outlet, second syngas outlet separates the second synthetic gas line of pipes and the 3rd synthetic gas line of pipes, second synthetic gas line of pipes is connected with low-temperature rectisol operation, 3rd synthetic gas line of pipes is connected with the first synthetic gas entrance on high pressure nitrogen water cooler, first synthetic gas entrance is communicated with the first syngas outlet, first syngas outlet is connected with ammonia synthesis operation by the 4th synthetic gas line of pipes, wherein the 4th synthetic gas line of pipes also becomes letter shoot line to be connected with low-temperature rectisol operation by pentahapto,
Fraction outlets bottom nitrogen wash column is connected with the cut entrance on the second flash tank top by cut line of pipes, pneumatic outlet after the rectifying at methane rectifying tower top is connected with the gas inlet after the rectifying on the second flash tank top by the air shooter line after rectifying, the flash gas outlet of the second flash drum overhead is connected with the first flash gas entrance on the second unstripped gas water cooler by 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 second unstripped gas water cooler is communicated with the first flash gas entrance with the first natural gas liquids entrance, first natural gas liquids outlet is connected with LNG tank by the second natural gas liquids line of pipes,
Flashed liquid outlet bottom second flash tank is connected with the first flashed liquid entrance on the second unstripped gas water cooler by flashed liquid line of pipes, the 3rd fuel gas outlet on second unstripped gas water cooler is communicated with the first flash gas entrance with the first flashed liquid entrance, 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, second fuel gas entrance and the second fuel gas outlet, second fuel gas outlet is connected with the first fuel gas entrance on high pressure nitrogen water cooler by the second fuel gas line of pipes, first fuel gas entrance and the first fuel gas outlet, 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, 3rd nitrogen inlet is communicated with the 3rd nitrogen outlet, 3rd nitrogen outlet separates the second nitrogen line of pipes and the 3rd nitrogen line of pipes, second nitrogen line of pipes is connected with the outlet of the first nitrogen expansion machine, 3rd nitrogen line of pipes is connected with the second nitrogen inlet on the first unstripped gas water cooler, second nitrogen inlet is communicated with the second nitrogen outlet, second nitrogen outlet is connected with the first nitrogen inlet on high pressure nitrogen water cooler by the 4th nitrogen line of pipes, first nitrogen inlet is communicated with the first nitrogen outlet, first nitrogen outlet is connected with the nitrogen compressor entrance in empty point by the 5th nitrogen line of pipes.
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