CN103666585A - 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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CN103666585A
CN103666585A CN201310656838.1A CN201310656838A CN103666585A CN 103666585 A CN103666585 A CN 103666585A CN 201310656838 A CN201310656838 A CN 201310656838A CN 103666585 A CN103666585 A CN 103666585A
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tower
interchanger
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methyl alcohol
methanol washing
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CN103666585B (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 gas sweetening field 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 in 100 years, increase substantially in the past, cause global temperature on average obviously to rise, Greenhouse effect have become one of the severeest environmental problem of 21 century facing mankind.The mineral fuel such as coal, oil are utilized to the CO that produces and discharge in process 2carry out separation and reclaim, seal up for safekeeping and utilize (CCS & CCUS) to cause the generally attention of countries in the world.
An important directions that has become clean coal utilization with the leading Modern Coal-based Chemical technology of gasification, the efficiency of utilization with coal is high, and process cost is low, dust, NO x, SO 2deng pollutent, approach the feature of zero release.Modern coal gasification course has that not only raw material sources are wide, and efficiency of utilization is high, can realize CO before burning simultaneously 2remove and trap, with lower energy consumption and Financial cost, realize CO 2reduction of discharging.At following CO 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 to have the front CO of representational burning 2isolation technique.Utilize methyl alcohol physical property large to sour gas solubleness under cold condition, can effectively from crude synthesis gas, remove H 2s, CO 2deng sour gas, make synthetic gas reach very high degree of purification.
Take coal as raw material, and after gasifying process adopts the technological process of chilling process, low-temperature rectisol can effectively remove the CO in thick conversion gas simultaneously 2and H 2the impurity such as S.Low-temperature rectisol gas purifying technique, when being purified synthetic gas, can byproduct gas: rich H 2s gas product and CO 2gas product.High concentration CO 2general 60% left and right of the rate of recovery of gas product in technique.Residue CO 2most of in emission, concentration is roughly 60～85%, this part CO 2because concentration is lower, obtain high concentration CO 2energy consumption and expense high, most processing modes are for 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 enters before pipe is carried needs to carry out processed compressed.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 utilizes the further force value to regulation by its pressure-raising of pump.The normal dividing point as pump and compressor operating interval by (60bar, 23 ℃) in engineering, adopts compressor compresses, higher than adopting pump to compress after 60bar during lower than 60bar.After compressor compresses, CO 2temperature can surpass 23 ℃, the CO when by pump 2in liquid state, must be to CO 2carry out cooling process, make its temperature be no more than 23 ℃.
For the consideration to pipe safety, reliability service and comparable economy, CO 2the pressure of pipeline transfer designs and operation is within the scope of 8.27-17.23MPa, and temperature range is from surface temperature to the highest approximately 48.9 ℃.Under such design and operational condition, can make highly purified CO 2gas product keeps under stable overcritical or fine and close phase, thereby has eliminated the unstable of potential two-phase transportation.Table 1 is a large amount of CO 2gas product pipeline is carried requirement.The CO that low-temperature rectisol trapping system traps 2can meet above requirement, without further purification.The CO of this concentration 2can be for geological storage or enhanced oil recovery.
The typical CO of table 1 2pipeline is carried requirement
Figure BDA0000431618650000021
Application number is to disclose a kind of high CO in 201310247525.0 application for a patent for invention 2low-temp methanol washing method and the device of yield, as shown in Figure 1.At CO 2at the bottom of desorption tower and H 2between S upgrading tower, increase CO 2flashing tower, by CO 2the intensification of the methyl alcohol rich solution at the bottom of desorption tower, step-down strengthening reach CO 2strengthening desorb, has raising CO 2the effect of product yield, its CO 2gas product yield can effectively be increased to 91.2%.The CO of the high yield obtaining 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) improve CO 2gas product yield, is supplied with methyl alcohol rich solution is heated up by additional heat.Along with the raising of capture rate, in technique, need to increase additional heat input and roll up.
(2) improve CO 2gas product yield, is supplied with and is made CO by extra cold 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, in technique, needing to increase extra cold input increases.
(3) CO 2compression process needs certain cold input, and along with CO 2the increase of gas product, the power consumption meeting of cooling process rolls up.
(4) CO 2strengthening desorption process and CO 2it is unreasonable that compression process exists energy to utilize, and has the too high problem of process energy consumption.
Summary of the invention
The object of the invention is to solve above-mentioned a kind of high CO 2the low-temp methanol washing process of yield is improving CO 2during yield, energy utilizes the technological problems unreasonable, process energy consumption is too high, and a kind of low-temp methanol washing process and CO are provided 2the coupling process of compression process and system, the method and system can be at high CO 2under the yield condition of gas product, rationally utilize cold and CO in system 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 2between S upgrading tower, be provided with CO 2flashing tower, CO 2compression process has CO 2stage compression 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 stage compression device end 2gas product is coupled by an interchanger, and the methyl alcohol rich solution after coupling is sent into described CO 2flashing tower, the compression CO after coupling 2gas product cooling liquefaction becomes liquefaction CO 2product is carried by pump pressure-raising device pressure-raising to pipeline transfer pressure.
A preferred version of coupling process of the present invention, wherein, CO in described low-temp methanol washing process 2when yield is 60.4%～79%, this coupling process comprises the following steps:
(1) in low-temp methanol washing process, regeneration produces methyl alcohol lean solution and H 2methyl alcohol rich solution and CO at the bottom of S upgrading tower tower 2methyl alcohol rich solution at the bottom of desorption tower tower carries out being respectively delivered to acid gas absorption tower tower top after heat exchange cooling;
(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 stage compression device end 2gas product, by the interchanger intensification that is coupled, is finally sent into described CO 2flashing tower.
A preferred version of coupling process of the present invention, wherein, CO in described low-temp methanol washing process 2when yield is 80%～91.2%, this coupling process comprises the following steps:
(1) in low-temp methanol washing process, regeneration produces methyl alcohol lean solution and H 2methyl alcohol rich solution and CO at the bottom of S upgrading tower tower 2methyl alcohol rich solution at the bottom of desorption tower tower carries out being respectively delivered to acid gas absorption tower tower top after heat exchange cooling;
(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 stage compression device end 2gas product is by the intensification that is coupled of an interchanger, then with CO 2heat exchange intensification is carried out in recirculated water hot junction in stage compression device, finally sends into described CO 2flashing tower.
A preferred version of coupling process of the present invention, wherein, 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 ℃; Again with CO 2the rich CO of flashing tower tower top 2gas carries out after heat exchange intensification, and service temperature is-31～-28 ℃; Again with CO 2the compression CO of stage compression device end 2gas product is coupled after intensification by an interchanger, and service temperature is-26～-6 ℃.
A preferred version of coupling process of the present invention, wherein, 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 ℃; Again with CO 2the compression CO of stage compression device end 2gas product is coupled after intensification by an interchanger, and service temperature is-6～18 ℃; Again with CO 2carry out after heat exchange intensification in recirculated water hot junction in stage compression device, and service temperature is-6～35 ℃.
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 2between S upgrading tower, be provided with CO 2flashing tower, CO 2compression process has CO 2stage compression device and pump pressure-raising device, described CO 2at the bottom of desorption tower tower, by pipeline, be connected in after First Heat Exchanger again and described CO 2flashing tower connects, described CO 2stage compression device end is connected with pump pressure-raising device after being connected in described First Heat Exchanger by pipeline again.
A preferred version of coupled system of the present invention, wherein, described CO 2stage compression device comprises compressor and a plurality of interchanger with stage compression cylinder, and described every grade of compression cylinder is outside equipped with interchanger, and each interchanger is connected with rising pipe with water inlet pipe respectively.
A preferred version of coupled system of the present invention, wherein, the transfer lime of the methyl alcohol lean solution that in described low-temp methanol washing process, regeneration produces respectively with H 2at the bottom of S upgrading tower tower, be connected on the second interchanger and CO 2at the bottom of desorption tower tower, be connected on the 3rd interchanger;
Described CO 2after being connected on described the 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 of the methyl alcohol lean solution that in described low-temp methanol washing process, regeneration produces respectively with H 2at the bottom of S upgrading tower tower, be connected on the second interchanger and CO 2at the bottom of desorption tower tower, be connected on the 3rd interchanger;
Described CO 2after being connected on described the 3rd interchanger by pipeline at the bottom of desorption tower tower, then be connected with described First Heat Exchanger, be then connected on the 5th interchanger with described rising pipe, 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 2between S upgrading tower, increase CO 2flashing tower, CO 2low-temp methanol rich solution at the bottom of desorption tower need enter CO after intensification, step-down again 2flashing tower is strengthened desorb; And at CO 2in compression process, CO 2gas, after repeatedly compressing, need to be cooled to certain temperature to be just convenient to follow-up pumping; The present invention utilize dexterously in above-mentioned two technological processs one need to heat up, a feature that needs are cooling, both are coupled, realize the mutual utilization of energy, make above-mentioned treating processes in two techniques without providing separately heat or cold by outside again, save power consumption, improved the capacity usage ratio of total system.
Accompanying drawing explanation
Fig. 1 is a kind of high CO of the prior art 2the low-temp methanol washing process schema of yield, wherein: 4 absorption towers; 14CO 2desorption tower; 19H 2s upgrading tower; The hot regenerator column of 28 methyl alcohol; 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, 66 is compression CO 2gas product, 67,69 is liquefaction CO 2product; Remaining parts numbering represents identical parts or material with the identical parts numbering in Fig. 1; And in interchanger, 60 is First Heat Exchanger, 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 represents identical parts or material with the identical parts numbering in Fig. 1; And in interchanger, 60 is First Heat Exchanger, 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 to this.
Referring to Fig. 1～Fig. 3, low-temp methanol washing process and CO 2in the coupling process and system of compression process, disclosed a kind of high CO in the application for a patent for invention that the basic comprising of the low temperature washing device for methanol in described low-temp methanol washing process (referring to Fig. 2 and Fig. 3) and application number are 201310247525.0 2(referring to Fig. 1) is identical for the low temperature washing device for methanol of yield, specifically by absorption tower 4, CO 2desorption tower 14, H 2the compositions such as S upgrading tower 19, the hot regenerator column 28 of methyl alcohol, methanol rectifying tower 43, a plurality of flashing tower, a plurality of interchanger, a plurality of pump and a plurality of compressors, CO 214 ends of desorption tower and H 2between S upgrading tower 19, be provided with CO 2flashing tower 50, and Fig. 2, Fig. 3 represent identical parts or material with piece mark identical in Fig. 1, therefore for identical part, application number is, in 201310247525.0 application for a patent for invention, the description of the technical process of Fig. 1 and device is applicable to the description of the present embodiment to Fig. 2, Fig. 3, 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 towers is not to heat by outside thermal source, but and CO 2thermal source in compression process is coupled, thereby obtains heat.
CO of the present invention 2compression process has CO 2stage compression device and pump pressure-raising device, be CO with the difference of prior art 2the compression CO of stage compression device end 2gas product is not by the liquefaction of lowering the temperature of outside low-temperature receiver, but is coupled with the low-temperature receiver in low-temp methanol washing process, thereby 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 towers and described CO 2the compression CO of stage compression device end 2gas product is coupled by an interchanger, and the methyl alcohol rich solution 16 after coupling is sent into described CO 2flashing tower 50, the compression CO after coupling 2gas product cooling liquefaction becomes liquefaction CO 2product is carried by pump pressure-raising device pressure-raising to pipeline transfer pressure 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 towers, by pipeline, be connected in after First Heat Exchanger 60 again and described CO 2flashing tower 50 connects, described CO 2stage compression device end is connected with pump pressure-raising device after being connected in described First Heat Exchanger 60 by pipeline again.
Further, due to CO in low-temp methanol washing process 2yield when different, state CO 2methyl alcohol rich solution 16 at the bottom of desorption tower 14 towers is entering CO 2temperature requirement before flashing tower 50 is different, CO 2yield higher, the temperature needing is also higher.Meanwhile, the principle based on low temperature cold cascade utilization, by described CO 2at the bottom of desorption tower, 14 methyl alcohol rich solution 16 colds carry out step heat exchange, successively with recycle methanol lean solution 37, CO 2the rich CO of compression of flashing tower 50 tower tops 2the CO of gas 51, stage compression process 2gas product heat exchange, thereby the technical scheme of acquisition Fig. 2.But along with CO 2the raising of yield, CO 2the working pressure of flashing tower 50 reduces, and compressor 52 power consumptions increase, rich CO 2after gas 51 compressions, temperature obviously improves, at CO 2when yield is 79-80%, rich CO 2after gas 51 compressions, temperature is between 42-60 ℃, at CO 2yield during higher than 80% scope, compresses rich CO 2gas 51 needs to cool through recirculated cooling water, and is not suitable for directly utilizing CO 214 methyl alcohol rich solution 16 colds at the bottom of desorption tower; And, along with CO 2the raising of yield, CO 2the service temperature of flashing tower 50 is corresponding improve also, enters CO 2the methyl alcohol rich solution temperature of flashing tower heats up obviously, therefore the CO after stage compression 2the shortage of heat of gas product is to reach operational requirement, and CO 2the recirculated water hot junction producing in stage compression device can supplement more heat, in conjunction with this feature, forms the technical scheme shown in Fig. 3.
Embodiment when embodiment 1 and embodiment 2 are 60.4%～79% for yield below, embodiment when embodiment 3 and embodiment 4 are 80%～91.2% for yield.
Embodiment 1
Referring to 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) in low-temp methanol washing process, regeneration produces methyl alcohol lean solution 37 and H 2methyl alcohol rich solution 22 and CO at the bottom of S upgrading tower 19 towers 2methyl alcohol rich solution 16 at the bottom of desorption tower 14 towers carries out being respectively delivered to acid gas absorption tower 4 tower tops after heat exchange cooling;
(2) CO 2after methyl alcohol rich solution at the bottom of desorption tower 14 towers 16 heats up with 37 heat exchanges of methyl alcohol lean solution, then with CO 2the rich CO of flashing tower 50 tower tops 2gas 51 carries out heat exchange intensification, then with CO 2the compression CO of stage compression device end 2gas product 66, by the intensification that is coupled of an interchanger, is finally sent 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 of the methyl alcohol lean solution 37 that in described low-temp methanol washing process, regeneration produces respectively with at the bottom of H2S upgrading tower 19 towers, be connected on the second interchanger 27 and CO 2at the bottom of desorption tower 14 towers, be connected on the 3rd interchanger 56; Described CO 2after desorption tower 14 is connected on described the 3rd interchanger 56 by pipeline, then with CO 2flashing tower 50 tower tops are connected on the 4th interchanger 53, are then connected with described First Heat Exchanger 60, last and described CO 2flashing tower 50 connects.
Described CO 2stage compression device comprises compressor 61 and a plurality of interchanger 62,63,64,65 with four compression cylinders, on described each compression cylinder, be provided with an interchanger, each interchanger is connected with rising pipe with water inlet 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 working process of the coupling process of the present embodiment and coupled system is described in further detail:
Referring to Fig. 2, enter the crude synthesis gas 1 of technique of the present invention from take coal as raw material, the sulfur-resisting transformation synthetic gas that texaco gasification obtains, the gas flow coming 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
Enter the unstripped gas 1 of flow process enter flashing tower 3 after interchanger 2 is cooling, at the bottom of tower, isolate water methanol solution 48.The dehydration synthetic gas going out from flashing tower 3 tower tops enters 4 bottoms, absorption tower, and low-temp methanol liquid 47, flow 168.2t/hr, service temperature-50 ℃, working pressure 35bar are injected in 4 tops, absorption tower.On absorption tower, 4 tower tops are purified synthetic gas 5.Not containing H 2the methyl alcohol rich solution 7 of S and rich H 2s methyl alcohol rich solution 6 after cooling decompression, enters flashing tower 11 and flashing tower 13 respectively, carries out flash separation.
Methyl alcohol rich solution at the bottom of flashing tower 11,13 towers enters CO 2desorption process.CO 2at the bottom of desorption tower 14 towers, methyl alcohol rich solution 16 enters CO 2before flashing tower 50, successively pass through interchanger 56,53,60, the low temperature cold producing fully to recycle desorption process, wherein, after interchanger 56, service temperature is-34 ℃, after interchanger 53, service temperature is-31 ℃, and after interchanger 60, service temperature is-26 ℃; 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 towers, greenhouse cooling-31 ℃ after interchanger 53, compressor 52 working pressures are 4bar.It is 99.1% CO that flashing tower 13 tower tops obtain volumetric concentration 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, CO after interchanger 2 2 gas product 15 is cooled to 40 ℃ of service temperatures indirectly through stage compression device, and pressure is 70bar.Compression CO 2gas product 66 obtains through interchanger 60 CO that liquefies 2product, service temperature is 21 ℃, by pump 68, carries out pressure-raising to pipeline transfer pressure 150bar.
Embodiment 2
The low-temp methanol washing process of the present embodiment and CO 2the coupling process of compression process and system are identical with embodiment 1, and difference is: CO 2yield is different, and therefore corresponding service temperature is also different.Specific as follows:
Referring to Fig. 2, CO 2at the bottom of desorption tower 14 towers, methyl alcohol rich solution 16 enters CO 2before flashing tower 50, successively pass through interchanger 56,53,60, the low temperature cold producing fully to recycle desorption process, wherein, after interchanger 56, service temperature is-33 ℃, and after interchanger 53, service temperature is-26 ℃, after interchanger 60, service temperature is-5 ℃, CO 2the working pressure of flashing tower 50 is 1.7bar.CO 2the rich CO that flashing tower 50 ejects 2 gas 51 is delivered to CO after pressurization cooling 2at the bottom of desorption tower 14 towers, greenhouse cooling-30.5 ℃ after interchanger 53, compressor 52 working pressures are 4bar.It is 99.0% CO that flashing tower 13 tower tops obtain volumetric concentration 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, CO after interchanger 2 2 gas product 15 is cooled to 40 ℃ of service temperatures indirectly through stage compression device, and pressure is 65bar.Compression CO 2gas product 66 obtains through interchanger 60 CO that liquefies 2product, service temperature is 15 ℃, by pump 68, carries out pressure-raising to pipeline transfer pressure 150bar.
Other embodiments beyond the present embodiment is above-mentioned are identical with embodiment 1
Embodiment 3
Referring to 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) in low-temp methanol washing process, regeneration produces methyl alcohol lean solution 37 and H 2methyl alcohol rich solution 22 and CO at the bottom of S upgrading tower 19 towers 2methyl alcohol rich solution 16 at the bottom of desorption tower 14 towers carries out being respectively delivered to acid gas absorption tower 4 tower tops after heat exchange cooling;
(2) CO 2after methyl alcohol rich solution at the bottom of desorption tower 14 towers 16 heats up with 37 heat exchanges of methyl alcohol lean solution, then with CO 2the compression CO of stage compression device end 2gas product 66 is by the intensification that is coupled of an interchanger, then with CO 2heat exchange intensification is carried out in recirculated water hot junction 71 in stage compression 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 of the methyl alcohol lean solution 37 that in described low-temp methanol washing process, regeneration produces respectively with H 2at the bottom of S upgrading tower 19 towers, be connected on the second interchanger 27 and CO 2at the bottom of desorption tower 14 towers, be connected on the 3rd interchanger 56; Described CO 2after being connected on described the 3rd interchanger 56 by pipeline at the bottom of desorption tower 14 towers, then be connected with described First Heat Exchanger 60, be then connected on the 5th interchanger 72 with described rising pipe, last and described CO 2flashing tower 50 connects.
Below in conjunction with concrete example, the working process of the coupling process of the present embodiment and coupled system is described in further detail:
Enter the unstripped gas of technique of the present invention from take coal as raw material, the sulfur-resisting transformation synthetic gas that texaco gasification obtains, the gas flow coming 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
Enter the unstripped gas 1 of flow process enter flashing tower 3 after interchanger 2 is cooling, at the bottom of tower, isolate water methanol solution 48.The dehydration synthetic gas going out from flashing tower 3 tower tops enters 4 bottoms, absorption tower, and low-temp methanol liquid 47, flow 186.8t/hr, service temperature-50 ℃, working pressure 35bar are injected in 4 tops, absorption tower.On absorption tower, 4 tower tops are purified synthetic gas 5.Not containing H 2the methyl alcohol rich solution 7 of S and rich H 2s methyl alcohol rich solution 6 after cooling decompression, enters flashing tower 11 and flashing tower 13 respectively, carries out flash separation.
Methyl alcohol rich solution at the bottom of flashing tower 11,13 towers enters CO 2desorption process.CO 2at the bottom of desorption tower 14 towers, methyl alcohol rich solution 16 enters CO 2before flashing tower 50, successively pass through interchanger 56,60,72, the low temperature cold producing fully to recycle desorption process, wherein, after interchanger 56, service temperature is-25 ℃, and after interchanger 60, service temperature is 6 ℃, after interchanger 72, service temperature is-2 ℃, CO 2the working pressure of flashing tower 50 is 1.5bar.CO 2the rich CO that flashing tower 50 ejects 2 gas 51 is delivered to CO after pressurization cooling 2at the bottom of desorption tower 14 towers, greenhouse cooling-31 ℃ after interchanger 53, compressor 52 working pressures are 4bar.It is 99.1% CO that flashing tower 13 tower tops obtain volumetric concentration 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, CO after interchanger 2 2 gas product 15 is cooled to 40 ℃ of service temperatures indirectly through stage compression device, and pressure is 65bar.Compression CO 2gas product 66 obtains through interchanger 60 CO that liquefies 2product, service temperature is 17 ℃, by pump 68, carries out pressure-raising to pipeline transfer pressure 150bar.
Embodiment 4
Specifically be implemented as follows:
Referring to Fig. 3, the low-temp methanol washing process of the present embodiment and CO 2the coupling process of compression process and system are identical with embodiment 3, 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 towers, methyl alcohol rich solution 16 enters CO 2before flashing tower 50, successively pass through interchanger 56,60,72, the low temperature cold producing fully to recycle desorption process, wherein, after interchanger 56, service temperature is-2 ℃, and after interchanger 60, service temperature is 17 ℃, after interchanger 72, service temperature is 35 ℃, CO 2the working pressure of flashing tower 50 is 1bar.CO 2the rich CO that flashing tower 50 ejects 2 gas 51 is delivered to CO after pressurization cooling 2at the bottom of desorption tower 14 towers, greenhouse cooling-32 ℃ after interchanger 53, compressor 52 working pressures are 4bar.It is 99.3% CO that flashing tower 13 tower tops obtain volumetric concentration 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, CO after interchanger 2 2 gas product 15 is cooled to 40 ℃ of service temperatures indirectly through stage compression device, and pressure is 65bar.Compression CO 2gas product 66 obtains through interchanger 60 CO that liquefies 2product, service temperature is 20 ℃, by pump 68, carries out pressure-raising to pipeline transfer pressure 150bar.
Other embodiments beyond the present embodiment is above-mentioned are identical with embodiment 3.
Above-described embodiment is preferably embodiment of the present invention; but embodiments of the present invention are not restricted to the described embodiments; other any do not deviate from change, the modification done under spirit of the present invention and principle, substitutes, combination, simplify; all should be equivalent substitute mode, within being included in protection scope of the present invention.

Claims (9)

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 2between S upgrading tower, be provided with CO 2flashing tower, CO 2compression process has CO 2stage compression device and pump pressure-raising device, 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 stage compression device end 2gas product is coupled by an interchanger, and the methyl alcohol rich solution after coupling is sent into described CO 2flashing tower, the compression CO after coupling 2gas product cooling liquefaction becomes liquefaction CO 2product is carried by pump pressure-raising device pressure-raising to pipeline transfer pressure.
2. low-temp methanol washing process according to claim 1 and CO 2the coupling process of compression process, is characterized in that, CO in described low-temp methanol washing process 2when yield is 60.4%～79%, this coupling process comprises the following steps:
(1) in low-temp methanol washing process, regeneration produces methyl alcohol lean solution and H 2methyl alcohol rich solution and CO at the bottom of S upgrading tower tower 2methyl alcohol rich solution at the bottom of desorption tower tower carries out being respectively delivered to acid gas absorption tower tower top after heat exchange cooling;
(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 stage compression device end 2gas product, by the intensification that is coupled of an interchanger, is finally sent into described CO 2flashing tower.
3. low-temp methanol washing process according to claim 1 and CO 2the coupling process of compression process, is characterized in that, CO in described low-temp methanol washing process 2when yield is 80%～91.2%, this coupling process comprises the following steps:
(1) in low-temp methanol washing process, regeneration produces methyl alcohol lean solution and H 2methyl alcohol rich solution and CO at the bottom of S upgrading tower tower 2methyl alcohol rich solution at the bottom of desorption tower tower carries out being respectively delivered to acid gas absorption tower tower top after heat exchange cooling;
(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 stage compression device end 2gas product is by the intensification that is coupled of an interchanger, then with CO 2heat exchange intensification is carried out in recirculated water hot junction in stage compression device, finally sends into described CO 2flashing tower.
4. low-temp methanol washing process according to claim 2 and CO 2the coupling process of compression process, is characterized in that, 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 ℃; Again with CO 2the rich CO of flashing tower tower top 2gas carries out after heat exchange intensification, and service temperature is-31～-28 ℃; Again with CO 2the compression CO of stage compression device end 2gas product is coupled after intensification by an interchanger, and service temperature is-26～-6 ℃.
5. low-temp methanol washing process according to claim 3 and CO 2the coupling process of compression process, is characterized in that, 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 ℃; Again with CO 2the compression CO of stage compression device end 2gas product is coupled after intensification by an interchanger, and service temperature is-6～18 ℃; Again with CO 2carry out after heat exchange intensification in recirculated water hot junction in stage compression device, and service temperature is-6～35 ℃.
6. a 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 2between S upgrading tower, be provided with CO 2flashing tower, CO 2compression process has CO 2stage compression device and pump pressure-raising device, is characterized in that described CO 2at the bottom of desorption tower tower, by pipeline, be connected in after First Heat Exchanger again and described CO 2flashing tower connects, described CO 2stage compression device end is connected with pump pressure-raising device after being connected in described First Heat Exchanger by pipeline again.
7. low-temp methanol washing process according to claim 6 and CO 2the coupled system of compression process, is characterized in that, described CO 2stage compression device comprises compressor and a plurality of interchanger with stage compression cylinder, and described every grade of compression cylinder is outside equipped with interchanger, and each interchanger is connected with rising pipe with water inlet pipe respectively.
8. low-temp methanol washing process according to claim 7 and CO 2the coupled system of compression process, is characterized in that, the transfer lime of the methyl alcohol lean solution that in described low-temp methanol washing process, regeneration produces respectively with H 2at the bottom of S upgrading tower tower, be connected on the second interchanger and CO 2at the bottom of desorption tower tower, be connected on the 3rd interchanger;
Described CO 2after being connected on described the 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.
9. low-temp methanol washing process according to claim 7 and CO 2the coupled system of compression process, is characterized in that, the transfer lime of the methyl alcohol lean solution that in described low-temp methanol washing process, regeneration produces respectively with H 2at the bottom of S upgrading tower tower, be connected on the second interchanger and CO 2at the bottom of desorption tower tower, be connected on the 3rd interchanger;
Described CO 2after being connected on described the 3rd interchanger by pipeline at the bottom of desorption tower tower, then be connected with described First Heat Exchanger, be then connected on the 5th interchanger with described rising pipe, last and described CO 2flashing tower connects.
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