CN103666585B - Coupling method and system for low-temperature methanol washing technology and CO2 compressing technology - Google Patents

Coupling method and system for low-temperature methanol washing technology and CO2 compressing technology Download PDF

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CN103666585B
CN103666585B CN201310656838.1A CN201310656838A CN103666585B CN 103666585 B CN103666585 B CN 103666585B CN 201310656838 A CN201310656838 A CN 201310656838A CN 103666585 B CN103666585 B CN 103666585B
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methyl alcohol
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interchanger
compression
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CN103666585A (en
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钱宇
刘霞
杨思宇
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South China University of Technology SCUT
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South China University of Technology SCUT
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Abstract

The invention discloses a coupling method and a system for low-temperature methanol washing technology and CO2 compressing technology. A CO2 flash evaporation tower is arranged between the bottom of a CO2 desorption tower and a H2S concentration tower in the low-temperature methanol washing technology. A CO2 multi-stage compression apparatus and a pump pressurizing apparatus are provided for the CO2 compressing technology. The coupling method comprises the following steps: performing coupling on a methanol-rich solution at the CO2 desorption tower bottom and compressed CO2 product gas at the end of the CO2 multi-stage compression apparatus by a heat exchanger, sending the coupled methanol-rich solution into the CO2 flash evaporation tower, and cooling the coupled compressed CO2 product gas to obtain a liquid CO2 product and performing pressurization conveying by the pump pressurizing apparatus. According to the method and the system, the heat generated in the CO2 compressing process is reutilized for providing a methanol-rich solution temperature-raising heat source for enhancing CO2 desorption in the low-temperature methanol washing process, also the cold energy of the methanol-rich solution at the bottom of the CO2 desorption tower is utilized, and thus the refrigeration power consumption in the compressing process is saved and the energy utilization rate is raised.

Description

A kind of low-temp methanol washing process and CO 2the coupling process of compression process and system
Technical field
The present invention relates to field of gas purification and reduction of greenhouse gas discharge field, be specifically related to a kind of low-temp methanol washing process and CO 2the coupling process of compression process and system.
Background technology
CO 2total emission volumn increase substantially in 100 years in the past, cause the whole world temperature on average obviously rise, one of Greenhouse effect the severeest environmental problem having become 21 century facing mankind.The mineral fuel such as coal, oil are utilized in process and produces and the CO discharged 2carry out being separated and reclaim, seal up for safekeeping and utilize (CCS & CCUS) to cause the most attention of countries in the world.
Become an important directions of clean coal utilization with the Modern Coal-based Chemical technology that gasification is leading, the efficiency of utilization with coal is high, and process cost is low, dust, NO x, SO 2deng the feature of pollutent close to zero release.Modern coal gasification course has not only raw material sources, and extensively, efficiency of utilization is high, can realize the front CO that burns simultaneously 2remove and trap, realize CO with lower energy consumption and Financial cost 2reduction of discharging.At the CO in future 2in reduction of discharging process, CO before coal gasification and combustion 2the combination of trapping technique will have a wide range of applications.
Low-temp methanol washing process is a kind of CO of ripe commercial applications 2, H 2s gas removal technology is also have CO before representational burning 2isolation technique.Utilize the physical property that methyl alcohol is large to sour gas solubleness under cryogenic, effectively can remove H from crude synthesis gas 2s, CO 2deng sour gas, make the degree of purification that synthetic gas reaches very high.
Taking coal as raw material, after gasifying process adopts the technological process of chilling process, low-temperature rectisol effectively can remove the CO in thick conversion gas simultaneously 2and H 2the impurity such as S.Low-temperature rectisol gas purifying technique, while being purified synthetic gas, can byproduct gas: rich H 2s gas product and CO 2gas product.High concentration CO 2the gas product rate of recovery in process general about 60%.Residue CO 2major part is in emission, and concentration is roughly 60 ~ 85%, this part CO 2because concentration is lower, obtain high concentration CO 2energy consumption and costly, most processing mode is directly emptying.Also has a small amount of CO 2at rich H 2s gas product, enters Sulfur Recovery Unit process with gas product.
The high concentration CO that technique produces 2gas product needs to carry out processed compressed before carrying out pipe conveying.CO 2the compression section of gas product can be carried out in two steps: first with compressor by CO 2gas compression is the liquid state with certain pressure, then utilize pump further by its pressure-raising to regulation force value.Often by (60bar, the 23 DEG C) dividing point as pump and compressor operating interval in engineering, adopt compressor compresses lower than during 60bar, higher than adopting pump after 60bar to compress.After compressor compresses, CO 2temperature can more than 23 DEG C, in order to ensure by CO during pump 2be in liquid state, must to CO 2carry out cooling process, make its temperature be no more than 23 DEG C.
For the consideration to pipe safety, reliability service and comparable economy, CO 2the pressure of Cemented filling design and operation is within the scope of 8.27-17.23MPa, and temperature range is from surface temperature to the highest about 48.9 DEG C.Highly purified CO can be made under such design and operational condition 2under gas product keeps stable overcritical or fine and close phase, thus eliminate the unstable of potential two-phase transport.Table 1 is a large amount of CO 2the requirement of gas product Cemented filling.The CO that low-temperature rectisol trapping system traps 2above requirement can be met, without the need to further purification.The CO of this concentration 2may be used for geological storage or enhanced oil recovery.
The typical CO of table 1 2cemented filling requirement
Application number is disclose a kind of high CO in the application for a patent for invention of 201310247525.0 2the rectisol method of yield and device, as shown in Figure 1.At CO 2at the bottom of desorption tower and H 2cO is increased between S upgrading tower 2flashing tower, by CO 2intensification, the step-down strengthening of the methyl alcohol rich solution at the bottom of desorption tower reach CO 2strengthening desorb, has raising CO 2the effect of product yield, its CO 2gas product yield effectively can be increased to 91.2%.The CO of the high yield obtained in technique 2gas product, by multistage indirect cooled compressed, obtains the CO that liquefies 2product, for Chemical Manufacture, enhanced oil recovery or geological storage.But have the following disadvantages in above-mentioned technology:
(1) CO is improved 2gas product yield, makes methyl alcohol rich solution heat up by additional heat supply.Along with the raising of capture rate, need to increase additional heat input in technique and roll up.
(2) CO is improved 2gas product yield, makes CO by extra cold supply 2the rich CO of flash distillation tower top 2compressed gas cooling is transmitted back to CO 2at the bottom of desorption tower.Along with the raising of capture rate, needing to increase the input of extra cold in technique increases.
(3) CO 2compression process needs certain cold input, and along with CO 2the increase of gas product, the power consumption of cooling process can roll up.
(4) CO 2strengthening desorption process and CO 2it is unreasonable to there is Energy harvesting in compression process, there is the problem that process energy consumption is too high.
Summary of the invention
The object of the invention is to solve the high CO of above-mentioned one 2the low-temp methanol washing process of yield is at raising CO 2the technological problems that during yield, Energy harvesting is unreasonable, process energy consumption is too high, provides a kind of low-temp methanol washing process and CO 2the coupling process of compression process and system, the method and system can at high CO 2under the yield condition of gas product, the cold in Appropriate application system and CO 2heat in compression process, reduces high CO 2system energy consumption under capture rate, reduces running cost.
The technical scheme that the present invention solves the problems of the technologies described above is:
A kind of low-temp methanol washing process and CO 2the coupling process of compression process, wherein, the CO in low-temp methanol washing process 2at the bottom of desorption tower and H 2cO is provided with between S upgrading tower 2flashing tower, CO 2compression process has CO 2multistage compressing device and pump pressure-raising device, this coupling process comprises the following steps:
By described CO 2methyl alcohol rich solution at the bottom of desorption tower tower and described CO 2the compression CO of multistage compressing device end 2gas product is coupled by an interchanger, and described CO sent into by the methyl alcohol rich solution after coupling 2flashing tower, the compression CO after coupling 2gas product cooling liquefaction becomes liquefaction CO 2product is carried to Cemented filling pressure by pump pressure-raising device pressure-raising.
A preferred version of coupling process of the present invention, wherein, as CO in described low-temp methanol washing process 2when yield is 60.4% ~ 79%, this coupling process comprises the following steps:
(1) methyl alcohol lean solution and the H of generation is regenerated in low-temp methanol washing process 2methyl alcohol rich solution at the bottom of S upgrading tower tower and CO 2acid gas absorption tower tower top is delivered to after methyl alcohol rich solution at the bottom of desorption tower tower carries out heat exchange cooling respectively;
(2) CO 2after methyl alcohol rich solution at the bottom of desorption tower tower and the heat exchange of methyl alcohol lean solution heat up, then with CO 2the rich CO of flashing tower tower top 2gas carries out heat exchange intensification, then with CO 2the compression CO of multistage compressing device end 2gas product carries out coupling by interchanger and heats up, and finally sends into described CO 2flashing tower.
A preferred version of coupling process of the present invention, wherein, as CO in described low-temp methanol washing process 2when yield is 80% ~ 91.2%, this coupling process comprises the following steps:
(1) methyl alcohol lean solution and the H of generation is regenerated in low-temp methanol washing process 2methyl alcohol rich solution at the bottom of S upgrading tower tower and CO 2acid gas absorption tower tower top is delivered to after methyl alcohol rich solution at the bottom of desorption tower tower carries out heat exchange cooling respectively;
(2) CO 2after methyl alcohol rich solution at the bottom of desorption tower tower and the heat exchange of methyl alcohol lean solution heat up, then with CO 2the compression CO of multistage compressing device end 2gas product carries out coupling by an interchanger and heats up, then with CO 2heat exchange intensification is carried out in recirculated water hot junction in multistage compressing device, finally sends into described CO 2flashing tower.
A preferred version of coupling process of the present invention, wherein, as CO in described low-temp methanol washing process 2when yield is 60.4% ~ 79%, CO 2after methyl alcohol rich solution at the bottom of desorption tower tower and the heat exchange of methyl alcohol lean solution heat up, service temperature is-33 ~-31 DEG C; Again with CO 2the rich CO of flashing tower tower top 2after gas carries out heat exchange intensification, service temperature is-31 ~-28 DEG C; Again with CO 2the compression CO of multistage compressing device end 2after gas product carries out coupling intensification by an interchanger, service temperature is-26 ~-6 DEG C.
A preferred version of coupling process of the present invention, wherein, as CO in described low-temp methanol washing process 2when yield is 80% ~ 91.2%, CO 2after methyl alcohol rich solution at the bottom of desorption tower tower and the heat exchange of methyl alcohol lean solution heat up, service temperature is-24 ~ 0 DEG C; Again with CO 2the compression CO of multistage compressing device end 2after gas product carries out coupling intensification by an interchanger, service temperature is-6 ~ 18 DEG C; Again with CO 2after heat exchange intensification is carried out in recirculated water hot junction in multistage compressing device, service temperature is-6 ~ 35 DEG C.
A kind of low-temp methanol washing process and CO 2the coupled system of compression process, wherein, the CO in low-temp methanol washing process 2at the bottom of desorption tower and H 2cO is provided with between S upgrading tower 2flashing tower, CO 2compression process has CO 2multistage compressing device and pump pressure-raising device, described CO 2at the bottom of desorption tower tower by pipeline to be connected to after First Heat Exchanger again with described CO 2flashing tower connects, described CO 2multistage compressing device end is connected with pump pressure-raising device after being connected to described First Heat Exchanger by pipeline again.
A preferred version of coupled system of the present invention, wherein, described CO 2multistage compressing device comprises the compressor and multiple interchanger with stage compression cylinder, and described every grade of compression cylinder is outside equipped with interchanger, and each interchanger is connected with water inlet pipe and rising pipe respectively.
A preferred version of coupled system of the present invention, wherein, the transfer lime regenerating the methyl alcohol lean solution of generation in described low-temp methanol washing process respectively with H 2be connected on the second interchanger at the bottom of S upgrading tower tower and CO 2be connected on the 3rd interchanger at the bottom of desorption tower tower;
Described CO 2be connected to after on described 3rd interchanger by pipeline at the bottom of desorption tower tower, then with CO 2flashing tower tower top is connected on the 4th interchanger, is then connected with described First Heat Exchanger, last and described CO 2flashing tower connects.
A preferred version of coupled system of the present invention, wherein, the transfer lime regenerating the methyl alcohol lean solution of generation in described low-temp methanol washing process respectively with H 2be connected on the second interchanger at the bottom of S upgrading tower tower and CO 2be connected on the 3rd interchanger at the bottom of desorption tower tower;
Described CO 2be connected to after on described 3rd interchanger by pipeline at the bottom of desorption tower tower, then be connected with described First Heat Exchanger, be then connected to described rising pipe on the 5th interchanger, last and described CO 2flashing tower connects.
The present invention compared with prior art has following beneficial effect:
In low-temp methanol washing process, in order to improve CO 2product yield, at CO 2at the bottom of desorption tower and H 2cO is increased between S upgrading tower 2flashing tower, CO 2low-temp methanol rich solution at the bottom of desorption tower need enter CO again after intensification, step-down 2flashing tower carries out strengthening desorb; And at CO 2in compression process, CO 2gas, after repeatedly compressing, needs to be cooled to certain temperature to be just convenient to follow-up pumping; The present invention utilizes the feature that in above-mentioned two technological processs, needs intensification, needs cool dexterously, both are coupled, realize the mutual utilization of energy, make the above-mentioned treating processes in two techniques without the need to providing separately heat or cold by outside again, save power consumption, improve the capacity usage ratio of total system.
Accompanying drawing explanation
Fig. 1 is the high CO of one of the prior art 2the low-temp methanol washing process schema of yield, wherein: 4 absorption towers; 14CO 2desorption tower; 19H 2s upgrading tower; 28 methyl alcohol hot recycling towers; 43 methanol rectifying towers, 50CO 2flashing tower; 3,11,12,13,30,33 is flashing tower; 2,8,9,10,25,27,29,32,36,42,46,49,53 is interchanger; 26,31,38,41,55 is pump; 43,52 compressors; 1,5,6,7,15,16,17,18,20,22,23,34,35,37,39,40,44,45,47,48,51,54 is stock number.
Fig. 2 is low-temp methanol washing process of the present invention and CO 2in the coupling method, system of compression process, work as CO 2system schematic when yield is 60.4% ~ 78%; Wherein: 56,60,62,63,64,65 is interchanger, 61 is multi-stage compressor, and 68 is pump, 70 recirculated water cold junctions, and 71 is recirculated water hot junction, and 66 is compression CO 2gas product, 67,69 is liquefaction CO 2product; Remaining parts numbering numbers with the identical parts in Fig. 1 the parts or material that represent identical; Further, in interchanger, 60 is First Heat Exchanger, and 27 is the second interchanger, and 56 is the 3rd interchanger, and 53 is the 4th interchanger.
Fig. 3 is low-temp methanol washing process of the present invention and CO 2in the coupling method, system of compression process, work as CO 2system schematic when yield is 79% ~ 91.2%; Wherein: 56,60,62,63,64,65,72 is interchanger, 61 is multi-stage compressor, and 68 is pump, 70 recirculated water cold junctions, and 71,73 is recirculated water hot junction, 66 compression CO 2for gas product, 67,69 is liquefaction CO 2product; Remaining parts numbering numbers with the identical parts in Fig. 1 the parts or material that represent identical; Further, in interchanger, 60 is First Heat Exchanger, and 27 is the second interchanger, and 56 is the 3rd interchanger, and 53 is the 4th interchanger, and 72 is the 5th interchanger.
Embodiment
Below in conjunction with embodiment and accompanying drawing, the present invention is described in further detail, but embodiments of the present invention are not limited thereto.
See Fig. 1 ~ Fig. 3, low-temp methanol washing process and CO 2in the coupling process of compression process and system, basic comprising (see Fig. 2 and Fig. 3) and the application number of the low temperature washing device for methanol in described low-temp methanol washing process are the high CO of one disclosed in the application for a patent for invention of 201310247525.0 2the low temperature washing device for methanol (see Fig. 1) of yield is identical, specifically by absorption tower 4, CO 2desorption tower 14, H 2the compositions such as S upgrading tower 19, methyl alcohol hot recycling tower 28, methanol rectifying tower 43, multiple flashing tower, multiple interchanger, multiple pump and multiple compressors, CO 2desorption tower 14 end and H 2cO is provided with between S upgrading tower 19 2flashing tower 50, and piece mark identical in Fig. 2, Fig. 3 and Fig. 1 represents identical parts or material, therefore for identical part, application number is be applicable to the description of the present embodiment to Fig. 2, Fig. 3 to the technical process of Fig. 1 and the description of device in the application for a patent for invention of 201310247525.0, no longer repeats herein.
Shown in low temperature washing device for methanol of the present invention and Fig. 1, the difference of low temperature washing device for methanol is, in the present invention, and described CO 2methyl alcohol rich solution 16 at the bottom of desorption tower 14 tower is not heated by the thermal source of outside, but and CO 2thermal source in compression process is coupled, thus obtains heat.
CO of the present invention 2compression process has CO 2multistage compressing device and pump pressure-raising device, be with the difference of prior art, CO 2the compression CO of multistage compressing device end 2gas product is not carry out cooling liquefaction by the low-temperature receiver of outside, but is coupled with the low-temperature receiver in low-temp methanol washing process, thus obtains low-temp methanol washing process of the present invention and CO 2the coupling process of compression process and system.
Particularly, low-temp methanol washing process of the present invention and CO 2the coupling process of compression process comprises the following steps: by described CO 2methyl alcohol rich solution 16 at the bottom of desorption tower 14 tower and described CO 2the compression CO of multistage compressing device end 2gas product is coupled by an interchanger, and described CO sent into by the methyl alcohol rich solution 16 after coupling 2flashing tower 50, the compression CO after coupling 2gas product cooling liquefaction becomes liquefaction CO 2product is carried to Cemented filling pressure by pump pressure-raising device pressure-raising again.
Low-temp methanol washing process of the present invention and CO 2the coupled system of compression process is: CO 2at the bottom of desorption tower 14 tower by pipeline to be connected to after First Heat Exchanger 60 again with described CO 2flashing tower 50 connects, described CO 2multistage compressing device end is connected with pump pressure-raising device after being connected to described First Heat Exchanger 60 by pipeline again.
Further, owing to working as CO in low-temp methanol washing process 2yield different time, state CO 2methyl alcohol rich solution 16 at the bottom of desorption tower 14 tower is entering CO 2temperature requirement before flashing tower 50 is different, CO 2yield higher, the temperature of needs is also higher.Meanwhile, based on the principle of low temperature cold cascade utilization, by described CO 2at the bottom of desorption tower, methyl alcohol rich solution 16 cold of 14 carries out step heat exchange, namely successively with recycle methanol lean solution 37, CO 2the rich CO of compression of flashing tower 50 tower top 2the CO of gas 51, stage compression process 2gas product heat exchange, thus the technical scheme obtaining Fig. 2.But along with CO 2the raising of yield, CO 2the working pressure of flashing tower 50 reduces, and compressor 52 power consumption increases, rich CO 2gas 51 compresses rear temperature and significantly improves, at CO 2when yield is 79-80%, rich CO 2gas 51 compresses rear temperature between 42-60 DEG C, at CO 2when yield is higher than 80% scope, compress rich CO 2gas 51 need cool through recirculated cooling water, and is not suitable for directly utilizing CO 2at the bottom of desorption tower 14 methyl alcohol rich solution 16 cold; Further, along with CO 2the raising of yield, CO 2the service temperature also corresponding raising of flashing tower 50, enters CO 2the methyl alcohol rich solution temperature of flashing tower is obvious, the CO therefore after stage compression 2the shortage of heat of gas product is to reach operational requirement, and CO 2the recirculated water hot junction produced in multistage compressing device then can supplement more heat, in conjunction with this feature, forms the technical scheme shown in Fig. 3.
Embodiment 1 and embodiment 2 are embodiment when yield is 60.4% ~ 79% below, and embodiment 3 and embodiment 4 are embodiment when yield is 80% ~ 91.2%.
Embodiment 1
See Fig. 2, the low-temp methanol washing process of the present embodiment and CO 2the coupling process of compression process comprises the following steps:
(1) methyl alcohol lean solution 37 and the H of generation is regenerated in low-temp methanol washing process 2methyl alcohol rich solution 22 at the bottom of S upgrading tower 19 tower and CO 2acid gas absorption tower 4 tower top is delivered to after methyl alcohol rich solution 16 at the bottom of desorption tower 14 tower carries out heat exchange cooling respectively;
(2) CO 2after methyl alcohol rich solution at the bottom of desorption tower 14 tower 16 and methyl alcohol lean solution 37 heat exchange heat up, then with CO 2the rich CO of flashing tower 50 tower top 2gas 51 carries out heat exchange intensification, then with CO 2the compression CO of multistage compressing device end 2gas product 66 carries out coupling by an interchanger and heats up, and finally sends into described CO 2flashing tower 50.
The low-temp methanol washing process of the present embodiment and CO 2the coupled system of compression process is: the transfer lime regenerating the methyl alcohol lean solution 37 of generation in described low-temp methanol washing process respectively be connected on the second interchanger 27 at the bottom of H2S upgrading tower 19 tower and CO 2be connected on the 3rd interchanger 56 at the bottom of desorption tower 14 tower; Described CO 2desorption tower 14 is connected to after on described 3rd interchanger 56 by pipeline, then with CO 2flashing tower 50 tower top is connected on the 4th interchanger 53, is then connected with described First Heat Exchanger 60, last and described CO 2flashing tower 50 connects.
Described CO 2multistage compressing device comprises the compressor 61 and multiple interchanger 62,63,64,65 with four compression cylinders, described each compression cylinder is provided with an interchanger, each interchanger is connected with water inlet pipe and rising pipe respectively, described water inlet pipe forms circulating water cold junction 70, and rising pipe forms recirculated water hot junction 71.Described pump pressure-raising device comprises pump 67 and transport pipe.
Below in conjunction with concrete example, the coupling process of the present embodiment and the working process of coupled system are described in further detail:
See Fig. 2, enter the crude synthesis gas 1 of present invention process from taking coal as raw material, the sulfur-resisting transformation synthetic gas that texaco gasification obtains, the gas flow come from conversion section is 95760Nm 3/ hr, table composed as follows.
The composition of the thick gasification gas of table 2
Gas H 2 N 2 CO AR CH 4 CO 2 H 2S H 2O
Molar fraction % 45.6 0.3 19.2 0.1 0.1 34.3 0.2 0.2
The unstripped gas 1 entering flow process enters flashing tower 3 after cooling through interchanger 2, isolates water methanol solution 48 at the bottom of tower.The dehydration synthetic gas gone out from flashing tower 3 tower top enters bottom absorption tower 4, and low-temp methanol liquid 47, flow 168.2t/hr is injected at top, absorption tower 4, service temperature-50 DEG C, working pressure 35bar.On absorption tower 4, tower top is purified synthetic gas 5.Not containing H 2the methyl alcohol rich solution 7 of S and rich H 2s methyl alcohol rich solution 6, respectively through after cooling decompression, enters flashing tower 11 and flashing tower 13, carries out flash separation.
Methyl alcohol rich solution at the bottom of flashing tower 11,13 tower enters CO 2desorption process.CO 2at the bottom of desorption tower 14 tower, methyl alcohol rich solution 16 enters CO 2before flashing tower 50, successively through interchanger 56,53,60, fully to recycle the low temperature cold that desorption process produces, wherein, after interchanger 56, service temperature is-34 DEG C, after interchanger 53, service temperature is-31 DEG C, and after interchanger 60, service temperature is-26 DEG C; CO 2the working pressure of flashing tower 50 is 2.5bar.CO 2the rich CO that flashing tower 50 ejects 2gas 51 is delivered to CO after pressurization cooling 2at the bottom of desorption tower 14 tower, greenhouse cooling-31 DEG C after interchanger 53, compressor 52 working pressure is 4bar.Flashing tower 13 tower top obtains the CO that volumetric concentration is 99.1% 2gas product 15, gas product flow is 20068Nm 3/ hr, CO 2the yield of gas product 15 is 60.4%.
CO 2gas product 15 enters multistage indirect cooled compressed process after interchanger 2, CO 2gas product 15 is cooled to service temperature 40 DEG C indirectly through multistage compressing device, and pressure is 70bar.Compression CO 2gas product 66 obtains through interchanger 60 CO that liquefies 2product, service temperature is 21 DEG C, carries out pressure-raising to Cemented filling pressure 150bar by pump 68.
Embodiment 2
The low-temp methanol washing process of the present embodiment and CO 2the coupling process of compression process is identical with embodiment 1 with system, and difference is: CO 2yield is different, and therefore corresponding service temperature is also different.Specific as follows:
See Fig. 2, CO 2at the bottom of desorption tower 14 tower, methyl alcohol rich solution 16 enters CO 2before flashing tower 50, successively through interchanger 56,53,60, fully to recycle the low temperature cold that desorption process produces, wherein, after interchanger 56, service temperature is-33 DEG C, and after interchanger 53, service temperature is-26 DEG C, after interchanger 60, service temperature is-5 DEG C, CO 2the working pressure of flashing tower 50 is 1.7bar.CO 2the rich CO that flashing tower 50 ejects 2gas 51 is delivered to CO after pressurization cooling 2at the bottom of desorption tower 14 tower, greenhouse cooling-30.5 DEG C after interchanger 53, compressor 52 working pressure is 4bar.Flashing tower 13 tower top obtains the CO that volumetric concentration is 99.0% 2gas product 15, gas product flow is 25357Nm 3/ hr, CO 2the yield of gas product 15 is 78.3%.
CO 2gas product 15 enters multistage indirect cooled compressed process after interchanger 2, CO 2gas product 15 is cooled to service temperature 40 DEG C indirectly through multistage compressing device, and pressure is 65bar.Compression CO 2gas product 66 obtains through interchanger 60 CO that liquefies 2product, service temperature is 15 DEG C, carries out pressure-raising to Cemented filling pressure 150bar by pump 68.
The present embodiment other embodiments other than the above are identical with embodiment 1
Embodiment 3
See Fig. 3, the low-temp methanol washing process of the present embodiment and CO 2the coupling process of compression process comprises the following steps:
(1) methyl alcohol lean solution 37 and the H of generation is regenerated in low-temp methanol washing process 2methyl alcohol rich solution 22 at the bottom of S upgrading tower 19 tower and CO 2acid gas absorption tower 4 tower top is delivered to after methyl alcohol rich solution 16 at the bottom of desorption tower 14 tower carries out heat exchange cooling respectively;
(2) CO 2after methyl alcohol rich solution at the bottom of desorption tower 14 tower 16 and methyl alcohol lean solution 37 heat exchange heat up, then with CO 2the compression CO of multistage compressing device end 2gas product 66 carries out coupling by an interchanger and heats up, then with CO 2heat exchange intensification is carried out in recirculated water hot junction 71 in multistage compressing device, finally sends into described CO 2flashing tower 50.
The low-temp methanol washing process of the present embodiment and CO 2the coupled system of compression process is: the transfer lime regenerating the methyl alcohol lean solution 37 of generation in described low-temp methanol washing process respectively with H 2be connected on the second interchanger 27 at the bottom of S upgrading tower 19 tower and CO 2be connected on the 3rd interchanger 56 at the bottom of desorption tower 14 tower; Described CO 2be connected to after on described 3rd interchanger 56 by pipeline at the bottom of desorption tower 14 tower, then be connected with described First Heat Exchanger 60, be then connected to described rising pipe on the 5th interchanger 72, last and described CO 2flashing tower 50 connects.
Below in conjunction with concrete example, the coupling process of the present embodiment and the working process of coupled system are described in further detail:
Enter the unstripped gas of present invention process from taking coal as raw material, the sulfur-resisting transformation synthetic gas that texaco gasification obtains, the gas flow come from conversion section is 104292Nm 3/hr, table composed as follows, Fig. 3 is shown in technical process.
The composition of the thick gasification gas of table 3
Gas H 2 N 2 CO AR CH 4 CO 2 H 2S H 2O
Molar fraction % 45.9 0.2 18.9 0.1 0.1 34.2 0.13 0.3
The unstripped gas 1 entering flow process enters flashing tower 3 after cooling through interchanger 2, isolates water methanol solution 48 at the bottom of tower.The dehydration synthetic gas gone out from flashing tower 3 tower top enters bottom absorption tower 4, and low-temp methanol liquid 47, flow 186.8t/hr is injected at top, absorption tower 4, service temperature-50 DEG C, working pressure 35bar.On absorption tower 4, tower top is purified synthetic gas 5.Not containing H 2the methyl alcohol rich solution 7 of S and rich H 2s methyl alcohol rich solution 6, respectively through after cooling decompression, enters flashing tower 11 and flashing tower 13, carries out flash separation.
Methyl alcohol rich solution at the bottom of flashing tower 11,13 tower enters CO 2desorption process.CO 2at the bottom of desorption tower 14 tower, methyl alcohol rich solution 16 enters CO 2before flashing tower 50, successively through interchanger 56,60,72, fully to recycle the low temperature cold that desorption process produces, wherein, after interchanger 56, service temperature is-25 DEG C, and after interchanger 60, service temperature is 6 DEG C, after interchanger 72, service temperature is-2 DEG C, CO 2the working pressure of flashing tower 50 is 1.5bar.CO 2the rich CO that flashing tower 50 ejects 2gas 51 is delivered to CO after pressurization cooling 2at the bottom of desorption tower 14 tower, greenhouse cooling-31 DEG C after interchanger 53, compressor 52 working pressure is 4bar.Flashing tower 13 tower top obtains the CO that volumetric concentration is 99.1% 2gas product 15, gas product flow is 28883.5Nm 3/ hr, CO 2the yield of gas product 15 is 80.9%.
CO 2gas product 15 enters multistage indirect cooled compressed process after interchanger 2, CO 2gas product 15 is cooled to service temperature 40 DEG C indirectly through multistage compressing device, and pressure is 65bar.Compression CO 2gas product 66 obtains through interchanger 60 CO that liquefies 2product, service temperature is 17 DEG C, carries out pressure-raising to Cemented filling pressure 150bar by pump 68.
Embodiment 4
Specifically be implemented as follows:
See Fig. 3, the low-temp methanol washing process of the present embodiment and CO 2the coupling process of compression process is identical with embodiment 3 with system, and difference is: CO 2yield is different, and therefore corresponding service temperature is also different.Specific as follows:
CO 2at the bottom of desorption tower 14 tower, methyl alcohol rich solution 16 enters CO 2before flashing tower 50, successively through interchanger 56,60,72, fully to recycle the low temperature cold that desorption process produces, wherein, after interchanger 56, service temperature is-2 DEG C, and after interchanger 60, service temperature is 17 DEG C, after interchanger 72, service temperature is 35 DEG C, CO 2the working pressure of flashing tower 50 is 1bar.CO 2the rich CO that flashing tower 50 ejects 2gas 51 is delivered to CO after pressurization cooling 2at the bottom of desorption tower 14 tower, greenhouse cooling-32 DEG C after interchanger 53, compressor 52 working pressure is 4bar.Flashing tower 13 tower top obtains the CO that volumetric concentration is 99.3% 2gas product 15, gas product flow is 32431Nm 3/ hr, CO 2the yield of gas product 15 is 91.2%.
CO 2gas product 15 enters multistage indirect cooled compressed process after interchanger 2, CO 2gas product 15 is cooled to service temperature 40 DEG C indirectly through multistage compressing device, and pressure is 65bar.Compression CO 2gas product 66 obtains through interchanger 60 CO that liquefies 2product, service temperature is 20 DEG C, carries out pressure-raising to Cemented filling pressure 150bar by pump 68.
The present embodiment other embodiments other than the above are identical with embodiment 3.
Above-described embodiment is the present invention's preferably embodiment; but embodiments of the present invention are not restricted to the described embodiments; change, the modification done under other any does not deviate from spirit of the present invention and principle, substitute, combine, simplify; all should be the substitute mode of equivalence, be included within protection scope of the present invention.

Claims (3)

1. a low-temp methanol washing process and CO 2the coupling process of compression process, wherein, the CO in low-temp methanol washing process 2at the bottom of desorption tower and H 2cO is provided with between S upgrading tower 2flashing tower, CO 2compression process has CO 2multistage compressing device and pump pressure-raising device, it is characterized in that, this coupling process comprises the following steps:
By described CO 2methyl alcohol rich solution at the bottom of desorption tower tower and described CO 2the compression CO of multistage compressing device end 2gas product is coupled by an interchanger, and described CO sent into by the methyl alcohol rich solution after coupling 2flashing tower, the compression CO after coupling 2gas product cooling liquefaction becomes liquefaction CO 2product is carried to Cemented filling pressure by pump pressure-raising device pressure-raising;
As CO in described low-temp methanol washing process 2when yield is 60.4% ~ 79%, this coupling process comprises the following steps:
(1) methyl alcohol lean solution and the H of generation is regenerated in low-temp methanol washing process 2methyl alcohol rich solution at the bottom of S upgrading tower tower and CO 2acid gas absorption tower tower top is delivered to after methyl alcohol rich solution at the bottom of desorption tower tower carries out heat exchange cooling respectively;
(2) CO 2after methyl alcohol rich solution at the bottom of desorption tower tower and the heat exchange of methyl alcohol lean solution heat up, then with CO 2the rich CO of flashing tower tower top 2gas carries out heat exchange intensification, then with CO 2the compression CO of multistage compressing device end 2gas product carries out coupling by an interchanger and heats up, and finally sends into described CO 2flashing tower;
As CO in described low-temp methanol washing process 2when yield is 80% ~ 91.2%, this coupling process comprises the following steps:
(1) methyl alcohol lean solution and the H of generation is regenerated in low-temp methanol washing process 2methyl alcohol rich solution at the bottom of S upgrading tower tower and CO 2acid gas absorption tower tower top is delivered to after methyl alcohol rich solution at the bottom of desorption tower tower carries out heat exchange cooling respectively;
(2) CO 2after methyl alcohol rich solution at the bottom of desorption tower tower and the heat exchange of methyl alcohol lean solution heat up, then with CO 2the compression CO of multistage compressing device end 2gas product carries out coupling by an interchanger and heats up, then with CO 2heat exchange intensification is carried out in recirculated water hot junction in multistage compressing device, finally sends into described CO 2flashing tower.
2. low-temp methanol washing process according to claim 1 and CO 2the coupling process of compression process, is characterized in that, as CO in described low-temp methanol washing process 2when yield is 60.4% ~ 79%, CO 2after methyl alcohol rich solution at the bottom of desorption tower tower and the heat exchange of methyl alcohol lean solution heat up, service temperature is-33 ~-31 DEG C; Again with CO 2the rich CO of flashing tower tower top 2after gas carries out heat exchange intensification, service temperature is-31 ~-28 DEG C; Again with CO 2the compression CO of multistage compressing device end 2after gas product carries out coupling intensification by an interchanger, service temperature is-26 ~-6 DEG C.
3. low-temp methanol washing process according to claim 1 and CO 2the coupling process of compression process, is characterized in that, as CO in described low-temp methanol washing process 2when yield is 80% ~ 91.2%, CO 2after methyl alcohol rich solution at the bottom of desorption tower tower and the heat exchange of methyl alcohol lean solution heat up, service temperature is-24 ~ 0 DEG C; Again with CO 2the compression CO of multistage compressing device end 2after gas product carries out coupling intensification by an interchanger, service temperature is-6 ~ 18 DEG C; Again with CO 2after heat exchange intensification is carried out in recirculated water hot junction in multistage compressing device, service temperature is-6 ~ 35 DEG C.
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