CN102288008B - Method and device for extracting carbonic oxide (CO) of coal gas feed gas - Google Patents
Method and device for extracting carbonic oxide (CO) of coal gas feed gas Download PDFInfo
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- CN102288008B CN102288008B CN2011102221734A CN201110222173A CN102288008B CN 102288008 B CN102288008 B CN 102288008B CN 2011102221734 A CN2011102221734 A CN 2011102221734A CN 201110222173 A CN201110222173 A CN 201110222173A CN 102288008 B CN102288008 B CN 102288008B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0261—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon monoxide
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0271—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of H2/CO mixtures, i.e. of synthesis gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers
Abstract
The invention provides a method and device for extracting carbonic oxide (CO) of coal gas feed gas. According to the method provided by the invention, CH4 and CO/H2 can be separated in a washing tower, most synthesis gas (mainly comprising CO, H2) can be acquired from the top of the washing tower, the synthesis gas from the top of the washing tower can be reentered to a CO distillation column, and the user-desired liquid state CO product can be obtained from the tower bottom; if CO gas is needed, the synthesis gas only needs to be fed to a heat exchanger for reheating, meanwhile, the synthesis gas obtained from the tower top can be reheated in the heat exchanger and then fed into the follow-up chemical process system. In order to achieve the purposes of environmental protection and energy conservation, the device provided by the invention can simultaneously produce LNG (liquefied natural gas) clean energy and CO, thus meeting the requirement of the CO products for coalification factories.
Description
Technical field
The invention belongs to gas cold separation technology field, in particular, belong to the cryogenic separation field of coal gas.
Background technology
Carbon monoxide can be reduced into metal simple-substance as reducing agent with many metal oxides during high temperature, therefore be usually used in the smelting of metal, and other purposes of carbon monoxide is also in large-scale popularization.Present many coal gasification factory wishes to come unstripped gas from the coal gas device, and (key component contains CO, CH
4, H
2) middle CO gas or the liquid carbon monoxide product of obtaining.But all there is the deficiency on production efficiency and/or output in existing production technology.
Chinese patent (ZL200910058219.6)---" a kind of separation method of coal gasification device feed gas and device " put down in writing a kind of process and device that methane separation in coal gasification device feed gas is gone out, the present invention is by being combined with this patented method, can produce better economic benefit, all quote in this content with this patent specification.
Summary of the invention
The present invention is with CH
4With CO/ H
2Separate in scrubbing tower, (key component contains CO to most of synthesis gas, H
2) take out in scrubber overhead, scrubber overhead synthesis gas out enters the CO rectifying column again, just can obtain the required liquid carbon monoxide product of user at the bottom of tower, if need CO gas only need enter the heat exchanger re-heat get final product, the synthesis gas of tower top acquisition simultaneously enters follow-up chemical process system after the heat exchanger re-heat.In order to reach not only environmental protection but also energy-conservation purpose, the present invention produces LNG clean energy resource and carbon monoxide simultaneously, has satisfied coalification factory to the demand of carbon monoxide product.In order to achieve the above object, the present invention adopts following method:
A kind of coal gas device comes the carbon monoxide extracting method of unstripped gas, and it comprises the following steps:
A, the unstripped gas after purifying carry out precooling through heat exchanger;
Unstripped gas after B, precooling passes through CH
4The first evaporimeter of-CO rectifier bottoms is further cooled;
C, further cooled unstripped gas are sent in scrubbing tower, draw H in scrubber overhead
2-CO gaseous mixture is drawn CH at the bottom of the scrubbing tower tower
4-CO mixed liquor;
D, above-mentioned H
2The part of-CO gaseous mixture is introduced into the CO rectifying column, draws CO liquid in the CO rectifying column after rectifying at the bottom of tower;
The part of E, above-mentioned CO liquid is sent into the CO liquid storage vessel after the further mistake of above-mentioned heat exchanger is cold, another part forms CO gas after re-heat.
The method further comprises:
F, at above-mentioned CH
4-CO rectifying tower top divides gas to separate through the first laggard promoting the circulation of qi liquid of condenser condenses, and uncooled gas is sent to the flashed vapour pipe network after above-mentioned heat exchanger re-heat;
G, the gas at above-mentioned CO rectifying column top separate through the second laggard promoting the circulation of qi liquid of condenser condenses, isolated gas and H from the scrubbing tower top
2Export after being sent to above-mentioned heat exchanger re-heat after another part of-CO gaseous mixture converges.
The method further comprises:
H, after above-mentioned C step, the CO-H that the scrubbing tower tower top is drawn
2At least a portion of synthesis gas is exported after the heat exchanger re-heat;
The CH that draws at the bottom of I, scrubbing tower tower
4-CO mixed liquor is admitted to CH
4Rectifying in-CO rectifying column, and in CH
4Obtain the LNG product at the bottom of-CO rectifying tower, this LNG product is crossed through heat exchanger and is sent to the LNG storage tank after cold.
The method further comprises:
J, at above-mentioned CH
4-CO rectifying tower top divides gas to separate through the first laggard promoting the circulation of qi liquid of condenser condenses, and isolated liquid pressurizes rear portion as CH through the CO cryogenic liquid pump
4The phegma of-CO rectifying column, another part is as the phegma of above-mentioned scrubbing tower.
The method further comprises:
K, the gas at above-mentioned CO rectifying column top separate through the second laggard promoting the circulation of qi liquid of condenser condenses, and isolated liquid is as the phegma of CO rectifying column.
The method further comprises:
L, the H that draws from the scrubbing tower tower top
2-CO gaseous mixture is exported after above-mentioned heat exchanger re-heat.
The method further comprises: the temperature after above-mentioned B step Raw gas enters heat exchanger and is further cooled is-165 ℃～-160 ℃.
The method that another kind of coal gas device comes the carbon monoxide of unstripped gas to extract, it comprises the following steps:
A, the unstripped gas after purifying carry out precooling through heat exchanger;
Unstripped gas after B, precooling passes through CH
4The first evaporimeter of-CO rectifier bottoms is further cooled;
C, further cooled unstripped gas are sent in scrubbing tower, draw H in scrubber overhead
2-CO gaseous mixture is drawn CH at the bottom of the scrubbing tower tower
4-CO mixed liquor;
D, above-mentioned CH
4-CO mixed liquor is admitted to CH
4Rectifying in-CO rectifying column, the tower top portion gas is sent into the first condenser condenses, and the gas of uncooled one-tenth liquid state is sent into the CO rectifying column, draws CO liquid in the CO rectifying column after rectifying at the bottom of tower;
The part of E, above-mentioned CO liquid is sent into the CO liquid storage vessel after the further mistake of above-mentioned heat exchanger is cold, another part forms CO gas after re-heat.
The method further comprises:
H, after above-mentioned C step, the CO-H that the scrubbing tower tower top is drawn
2Synthesis gas is exported after the heat exchanger re-heat;
The CH that draws at the bottom of I, scrubbing tower tower
4-CO mixed liquor is admitted to CH
4Rectifying in-CO rectifying column, and in CH
4Obtain the LNG product at the bottom of-CO rectifying tower, this LNG product is crossed through heat exchanger and is sent to the LNG storage tank after cold.
The method further comprises:
J, at above-mentioned CH
4-CO rectifying tower top divides gas to separate through the first laggard promoting the circulation of qi liquid of condenser condenses, and isolated liquid pressurizes rear portion as CH through the CO cryogenic liquid pump
4The phegma of-CO rectifying column, another part is as the phegma of above-mentioned scrubbing tower.
The method further comprises:
K, the gas at above-mentioned CO rectifying column top separate through the second laggard promoting the circulation of qi liquid of condenser condenses, and isolated liquid is as the phegma of CO rectifying column.
The method further comprises:
L, the H that draws from the scrubbing tower tower top
2-CO gaseous mixture is exported after above-mentioned heat exchanger re-heat.
The method further comprises: the temperature after above-mentioned B step Raw gas enters heat exchanger and is further cooled is-165 ℃～-160 ℃.
In order to reach the foregoing invention purpose, the present invention has also adopted a kind of coal gas device to come the carbon monoxide extraction equipment of unstripped gas, and it mainly comprises:
Heat exchanger;
Scrubbing tower, it is separated into H with unstripped gas
2-CO gaseous mixture and CH
4-CO mixed liquor;
CH
4-CO rectifying column, it is with the CH of scrubbing tower output
4-CO mixed liquor is isolated the LNG product;
The CO rectifying column, it is with the H that receives
2-CO mixed gas separation goes out qualified CO liquid;
Be arranged at CH
4First condenser at-CO rectifying column top is arranged at CH
4The first evaporimeter of-CO rectifier bottoms;
Be arranged at second condenser at CO rectifying column top, be arranged at the second evaporimeter of CO rectifier bottoms;
The first gas-liquid separator, it is with above-mentioned CH
4The gas after the first condenser condenses at-CO rectifying column top carries out gas-liquid separation, and isolated liquid is as above-mentioned scrubbing tower and CH
4The phegma of-CO rectifying column;
The second gas-liquid separator, its gas after the second condenser condenses with CO rectifying column top carries out gas-liquid separation, and isolated liquid is as the phegma of CO rectifying column.
This equipment also comprises:
The CO cryogenic liquid pump, it pressurizes the liquid that the first gas-liquid separator separates goes out.
Description of drawings
Accompanying drawing 1 is the first preparation method's of the present invention flow chart
Accompanying drawing 2 is the second preparation method's of the present invention flow chart
E601: heat exchanger V601: the first vapour liquid separator V602: the second vapour liquid separator
V603: the 3rd gas-liquid separator K603: the second condenser K604: the second evaporimeter
CB601: ice chest T601: scrubbing tower T602:CH4-CO rectifying column T603:CO rectifying column
COP601/2:CO cryogenic liquid pump K602: the first evaporimeter K601: the first condenser
V701 cryogen knockout drum WE701: aftercooler MRC701: azeotrope compressor
The specific embodiment
As shown in Figure 1, the feed gas stream 1(key component CO, the CH that come from the upstream cleaning system
4And H
2) enter the heat exchanger E601 in ice chest CB601, be cooled to uniform temperature and extract feed gas stream 2 out, form feed gas stream 3 after feed gas stream 2 is further cooling through the first evaporimeter K602, it is cooling and be partially condensed to approximately-165 ℃～-160 ℃ and draw feed gas stream 4 to scrubbing tower T601 that logistics 3 enters the feed gas passage of heat-exchange system E601.The phegma 6B on scrubbing tower T601 top is from carbon monoxide under low temperature pump COP601/2, the synthesis gas 9(key component H that scrubbing tower T601 tower top is drawn
2The synthesis gas 10(key component H of a part of 9A and CO) and CO rectifying column T603 tower top
2And CO) converge formation logistics 11, and through forming logistics 12(key component H after heat exchanger E601 re-heat
2And CO) export the synthesis gas output pipe network to.The CH that draws at the bottom of scrubbing tower T601
4-CO mixed liquor 5 is delivered to CH
4-CO rectifying column T602, another part 9B of the synthesis gas of drawing from scrubbing tower T601 tower top sends into CO rectifying column T603.From the logistics 5 of scrubbing tower T601 at CH
4Carry out heat and mass in-CO rectifying column T602, obtain qualified LNG product 14 at the bottom of tower, the LNG product 14A that crosses after cold through heat exchanger E601 sends into the LNG storage tank; Tower top portion gas (key component CO) through the first condensed liquid of condenser K601 after CO cryogenic liquid pump OP601 pressurization as the phegma 6A of CH4-CO rectifying column T602 and the phegma 6B of scrubbing tower, uncooled gas 7(key component CO and H
2) form the flashed vapour pipe network that the user is transported in logistics 8 after the heat exchanger re-heat.
Send into logistics 9B(key component CO and the H of CO rectifying column T603
2), carry out heat and mass in CO rectifying column T603; Obtain qualified CO fluid product 15 at the bottom of tower, the CO fluid product both can be through 16 having sent into liquid CO storage tank after cold, also can be after the heat exchanger re-heat with gaseous state 18 for the user; Send into the second gas-liquid separator V602 at rectifying column T603 tower top portion gas after the second condenser K603 condensation, isolated liquid is as the phegma of CO rectifying column, after a part of 9A of the synthesis gas that isolated uncooled gas 10 and scrubbing tower T601 tower top are drawn converges through after heat exchanger E601 re-heat to the synthesis gas output pipe network.
The low-temperature receiver of the first condenser K601 and the second condenser K603 adopts the liquid nitrogen of independent nitrogen cycle as the low-temperature receiver of condenser, incorporates the circulating nitrogen gas suction port of compressor after the nitrogen re-heat after evaporation into.Nitrogen advances heat exchanger E601 through logistics 19 after cyclic nitrogen press NC601 compression and after cooling and is cooled to uniform temperature and extracts logistics 20 out as the thermal source of the second evaporimeter K604, nitrogen cooling rear logistics 21 therein enters heat exchanger E601 liquefaction again, crosses cold rear formation logistics 21A, cross a liquid nitrogen part 24 after cold as the low-temperature receiver of the first condenser K601, another part liquid nitrogen 22 is as the low-temperature receiver of the second condenser K603; Liquid nitrogen evaporates in condenser.Because evaporating pressure is different, cooling box after nitrogen 25 re-heats that are evaporated from the first condenser K601, nitrogen 26 advances circulating nitrogen gas compressor intergrade entrance; After nitrogen 23 re-heats that are evaporated from the second condenser K603, cooling box 27 enters the circulating nitrogen gas suction port of compressor.
The cold major part of this system is obtained by enclosed azeotrope kind of refrigeration cycle: cryogen is by the cryogen compressor compresses, cooling and condensation in heat exchanger, by azeotrope choke valve (J-T valve) thus expand and in heat exchanger E601 re-heat cold is provided.The mixture that cryogen is comprised of the hydrocarbon of nitrogen and C1 to C5.
azeotrope from heat exchanger E601 re-heat out (cryogen that pressure 2～4bar) and cryogen replenishment system come mixes (pressure is about 40Bar) after laggard azeotrope compressor compresses, if cooler is arranged need set up intersegmental vapor-liquid separation tank and intersegmental cryogen liquor pump through between the cooling admission liquid of cooler WE701 knockout drum V701(compressor section again), gas phase after separation is advanced main heat exchanger E601, liquid phase is advanced the laggard main heat exchanger of cryogenic fluid pump P701 pressurization, vapour, liquid is respectively after different passages enters main heat exchanger E601 and the particular allocation structure of heat exchanger inner one of porch, vapour-liquid evenly mixed, enter each interlayer of main heat exchanger, the cooling liquid and cross in main heat exchanger E601 of the mixed cryogen of vapour-liquid is as cold as～and-150 ℃ by azeotrope J/T valve throttling expansion to 2～4bar, and through vapor-liquid separation tank V702, turn back to main heat exchanger E601 re-heat after mixing and circulate to carrying out the next one.
In the present invention, from scrubbing tower T601 Base top contact, can guarantee that like this pressure of CO rectifying column T603 is substantially equal with the pressure that scrubbing tower T601 pushes up due to the synthesis gas that enters CO rectifying column T603; Thereby guarantee from CO rectifying column T603 tower top synthesis gas (key component CO, H out
2) can with scrubber overhead synthesis gas (key component CO, H out
2) enter after the heat exchanger re-heat cooling box after converging and enter again the subsequent technique system, and the drag losses of synthesis gas stream is as far as possible little, and follow-up synthesic gas compressor power consumption can reduce.
The second condenser K603 low-temperature receiver of CO rectifying column adopts by heat exchanger cold junction overfreezing liquid nitrogen out, evaporates in condenser after the liquid nitrogen throttling, and the nitrogen after evaporation enters the entrance that enters again the circulating nitrogen gas compressor after heat exchanger E601 re-heat;
The second evaporimeter K604 thermal source of CO rectifying column adopts by the nitrogen of releasing in the middle part of heat exchanger E601, enters heat exchanger E601 after nitrogen is cooling in evaporimeter again.
Synthesis gas 9B(key component CO, H
2) send into CO fractionate T603, ejecting from fractionate the portion gas that comes is condensed among the second condenser K603 of fractionate tower top, the liquid of condensation is as the phegma of fractionate, and another part gas is drawn from tower top and incorporated scrubber overhead synthesis gas pipeline out into and send as synthesis gas after the heat exchanger re-heat; Liquid part evaporation in the second evaporimeter K604 at the bottom of CO fractionate T603 tower, uprising gas and phegma carry out heat and mass in tower.
CO rectifying column T603 can adopt packed tower or sieve-plate tower.
Heat exchanger E601 in this ice chest is comprised of several plate-fin heat exchange units.
The cold of this process system can also adopt following several form to obtain:
A) nitrogen expansion refrigeration and system's isothermal throttle effect;
B) mode of nitrogen expansion refrigeration and the combination of enclosed azeotrope kind of refrigeration cycle;
C) mode of enclosed azeotrope kind of refrigeration cycle and nitrogen kind of refrigeration cycle combination
D) the outside liguefied nitrogen of introducing.
Another embodiment:
As shown in Figure 2, the feed gas stream 101(key component CO, the CH that come from the upstream cleaning system
4And H
2) enter heat exchanger E601 in ice chest CB601 and be cooled to uniform temperature and extract feed gas stream 102 out, forming logistics 103 after unstripped gas 102 is further cooling through the first evaporimeter K602, to be sent to the feed gas passage of heat exchanger E601 cooling and be partially condensed to approximately-165 ℃～-160 ℃, draws afterwards logistics 104 and enter scrubbing tower T601.The phegma 106B on scrubbing tower T601 top is from the carbon monoxide under low temperature pump, the synthesis gas 109(key component H that scrubbing tower T601 tower top is drawn
2And CO) be delivered to the synthesis gas output pipe network through forming logistics 112 after heat exchanger E601 re-heat, the CH4-CO mixed liquor 105 of drawing at the bottom of scrubbing tower T601 is delivered to CH
4-CO rectifying column T602, another part 109B of the synthesis gas of drawing from scrubbing tower T601 tower top sends into CO rectifying column T603.Logistics 105(key component CH from scrubbing tower
4And CO) at CH
4Carry out heat and mass in-CO rectifying column T602, obtain qualified LNG product at the bottom of tower, cross through heat exchanger and form logistics 114 after cold and send into the LNG storage tank; The tower top portion gas through the first condensed liquid of condenser K601 after CO cryogenic liquid pump COP601 pressurization as CH
4The phegma 106A of-CO rectifying column T602 and the phegma 106B of scrubbing tower, uncooled gas 107 is sent into CO rectifying column T603.
Send into logistics 107(key component CO and the H of CO rectifying column T603
2), carry out heat and mass in CO rectifying column T603; Obtain qualified CO fluid product 115 at the bottom of tower, the CO fluid product both can be sent into the CO liquid storage vessel through forming logistics 116 after cold, also can be after the heat exchanger re-heat with gaseous state 118 for the user; , form logistics 108 after uncooled gas 110 process heat exchanger E601 re-heats and go the user as flashed vapour through the phegma 109B of the second condensed liquid of condenser K603 as the CO rectifying column at the tower top portion gas.
The low-temperature receiver of the first condenser K601 and the second condenser K603 adopts the liquid nitrogen of independent nitrogen cycle as the low-temperature receiver of condenser, incorporates the circulating nitrogen gas suction port of compressor after the nitrogen re-heat after evaporation into.Nitrogen is through 119 advancing heat exchanger E601 and be cooled to uniform temperature and extract logistics 120 out as the thermal source of the second evaporimeter K604 after cyclic nitrogen press NC601 compression and after cooling, nitrogen is cooling therein 121 enters heat exchanger E601 liquefaction, the cold formation logistics 121A of mistake afterwards again, cross a liquid nitrogen part 124 after cold as the low-temperature receiver of the first condenser K601, another part 122 is as the low-temperature receiver of the second condenser K603, and liquid nitrogen evaporates in condenser.Because evaporating pressure is different, form logistics 126 after nitrogen 125 re-heats that are evaporated from the first condenser K601, output to circulating nitrogen gas compressor intergrade entrance; Form logistics 127 after nitrogen 123 re-heats that are evaporated from the second condenser K603, output to the circulating nitrogen gas suction port of compressor.
A same embodiment of the present embodiment remainder.
Process of the present invention is as combination " a kind of separation method of coal gasification device feed gas and device " (patent No.: 200910058219.6), can obtain better economic well-being of workers and staff; Because the precooling of unstripped gas is combined, heat exchanger just can be merged into a cover, and the not enough loss of the cold loss caused by heat inleak of system and re-heat can reduce, and can reduce energy consumption like this.
Above-mentioned heat exchanger E601, scrubbing tower T601, CH
4-CO rectifying column T602, CO rectifying column T603 and vapour liquid separator can be assembled into whole ice chest in manufactory, compact conformation, and the quality that is conducive to control installation also reduces to minimum with the installation workload at scene simultaneously.
What need statement is; content in specification of the present invention is in order better to explain claim and the protection domain of unrestricted claim; the present invention's scope required for protection is as the criterion with claims, and the change that needn't pay creative work made on the basis with reference to description of those skilled in the art also should fall into the present invention's scope required for protection in addition.
Claims (7)
1. a coal gas device comes the carbon monoxide extracting method of unstripped gas, and it comprises the following steps:
A, the unstripped gas after purifying carry out precooling through heat exchanger;
Unstripped gas after B, precooling passes through CH
4The first evaporimeter of-CO rectifier bottoms is further cooled;
C, further cooled unstripped gas are sent in scrubbing tower, draw H in scrubber overhead
2-CO gaseous mixture is drawn CH at the bottom of the scrubbing tower tower
4-CO mixed liquor;
D, above-mentioned H
2The part of-CO gaseous mixture is introduced into the CO rectifying column, draws CO liquid in the CO rectifying column after rectifying at the bottom of tower;
The part of E, above-mentioned CO liquid is sent into the CO liquid storage vessel after the further mistake of above-mentioned heat exchanger is cold, another part forms CO gas after re-heat;
F, at above-mentioned CH
4-CO rectifying tower top divides gas to separate through the first laggard promoting the circulation of qi liquid of condenser condenses, and uncooled gas is sent to the flashed vapour pipe network after above-mentioned heat exchanger re-heat;
G, the gas at above-mentioned CO rectifying column top separate through the second laggard promoting the circulation of qi liquid of condenser condenses, isolated gas and H from the scrubbing tower top
2Export after being sent to above-mentioned heat exchanger re-heat after another part of-CO gaseous mixture converges.
2. a coal gas device comes the carbon monoxide extracting method of unstripped gas, and it comprises the following steps:
A, the unstripped gas after purifying carry out precooling through heat exchanger;
Unstripped gas after B, precooling passes through CH
4The first evaporimeter of-CO rectifier bottoms is further cooled;
C, further cooled unstripped gas are sent in scrubbing tower, draw H in scrubber overhead
2-CO gaseous mixture is drawn CH at the bottom of the scrubbing tower tower
4-CO mixed liquor;
D, above-mentioned CH
4-CO mixed liquor is admitted to CH
4Rectifying in-CO rectifying column, the tower top portion gas is sent into the first condenser condenses, and the gas of uncooled one-tenth liquid state is sent into the CO rectifying column, draws CO liquid in the CO rectifying column after rectifying at the bottom of tower;
The part of E, above-mentioned CO liquid is sent into the CO liquid storage vessel after the further mistake of above-mentioned heat exchanger is cold, another part forms CO gas after re-heat.
3. coal gas device as claimed in claim 1 or 2 comes the carbon monoxide extracting method of unstripped gas, further comprises:
H, after above-mentioned C step, the H that the scrubbing tower tower top is drawn
2At least a portion of-CO gaseous mixture is exported after the heat exchanger re-heat;
The CH that draws at the bottom of I, scrubbing tower tower
4-CO mixed liquor is admitted to CH
4Rectifying in-CO rectifying column, and in CH
4Obtain the LNG product at the bottom of-CO rectifying tower, this LNG product is crossed through heat exchanger and is sent to the LNG storage tank after cold.
4. coal gas device as claimed in claim 1 or 2 comes the carbon monoxide extracting method of unstripped gas, further comprises:
J, at above-mentioned CH
4-CO rectifying tower top divides gas to separate through the first laggard promoting the circulation of qi liquid of condenser condenses, and isolated liquid pressurizes rear portion as CH through the CO cryogenic liquid pump
4The phegma of-CO rectifying column, another part is as the phegma of above-mentioned scrubbing tower.
5. coal gas device as claimed in claim 1 or 2 comes the carbon monoxide extracting method of unstripped gas, further comprises:
K, the gas at above-mentioned CO rectifying column top separate through the second laggard promoting the circulation of qi liquid of condenser condenses, and isolated liquid is as the phegma of CO rectifying column.
6. coal gas device as claimed in claim 2 comes the carbon monoxide extracting method of unstripped gas, further comprises:
L, the H that draws from the scrubbing tower tower top
2-CO gaseous mixture is exported after above-mentioned heat exchanger re-heat.
7. the deep cooling separating method of coal gasification device feed gas as claimed in claim 1 or 2, further comprise: the temperature after above-mentioned B step Raw gas is further cooled is-165 ℃～-160 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011102221734A CN102288008B (en) | 2011-08-04 | 2011-08-04 | Method and device for extracting carbonic oxide (CO) of coal gas feed gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011102221734A CN102288008B (en) | 2011-08-04 | 2011-08-04 | Method and device for extracting carbonic oxide (CO) of coal gas feed gas |
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| CN102288008A CN102288008A (en) | 2011-12-21 |
| CN102288008B true CN102288008B (en) | 2013-06-12 |
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| CN2011102221734A Expired - Fee Related CN102288008B (en) | 2011-08-04 | 2011-08-04 | Method and device for extracting carbonic oxide (CO) of coal gas feed gas |
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| CN102538389A (en) * | 2011-12-19 | 2012-07-04 | 中国海洋石油总公司 | Mixed refrigerant pre-cooling system applied to base-load natural gas liquefaction plant |
| CN104534813B (en) * | 2014-12-24 | 2016-10-05 | 四川科比科油气工程有限公司 | One improves liquefied natural gas and light ends unit and recovery method |
| CN106871576B (en) * | 2017-01-25 | 2019-08-09 | 北京三泰天洁气体净化技术有限公司 | Commercial syngas low temperature front-end demethanization method and system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| GB9800693D0 (en) * | 1998-01-13 | 1998-03-11 | Air Prod & Chem | Separation of carbon monoxide from nitrogen-contaminated gaseous mixtures |
| FR2775276B1 (en) * | 1998-02-20 | 2002-05-24 | Air Liquide | PROCESS AND PLANT FOR THE PRODUCTION OF CARBON MONOXIDE AND HYDROGEN |
| FR2780391B1 (en) * | 1998-06-26 | 2000-10-20 | Air Liquide | PROCESS FOR PRODUCING CARBON MONOXIDE |
| FR2915791B1 (en) * | 2007-05-04 | 2009-08-21 | Air Liquide | METHOD AND APPARATUS FOR SEPARATING A MIXTURE OF HYDROGEN, METHANE AND CARBON MONOXIDE BY CRYOGENIC DISTILLATION |
| CN101476813B (en) * | 2009-01-21 | 2011-06-15 | 成都蜀远煤基能源科技有限公司 | Feed gas separation method and apparatus of coal gasification apparatus |
| CN202254634U (en) * | 2011-08-04 | 2012-05-30 | 成都蜀远煤基能源科技有限公司 | Device for extracting carbon monoxide from feed gas of coal gas |
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