CN107890748A - A kind of pre- extracting and concentrating technology of medium temperature sour gas - Google Patents
A kind of pre- extracting and concentrating technology of medium temperature sour gas Download PDFInfo
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- CN107890748A CN107890748A CN201711029997.3A CN201711029997A CN107890748A CN 107890748 A CN107890748 A CN 107890748A CN 201711029997 A CN201711029997 A CN 201711029997A CN 107890748 A CN107890748 A CN 107890748A
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- tower
- flash column
- stripping tower
- hot recycling
- sulfur
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/005—Carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
Abstract
The present invention relates to a kind of pre- extracting and concentrating technology of medium temperature sour gas, by effectively being exchanged heat with the lean absorbent from hot recycling tower before sulfur-rich absorbent carries out hot recycling, sulfur-rich absorbent is warming up to 70~110 DEG C after heat exchange, then flashing operation and air lift operation are carried out again, can cause the CO in sulfur-rich absorbent2Further desorbed Deng gas, so as to significantly improve H therein2S concentration, realize the sour gas concentrate operation under medium temperature condition；Sulfur-rich absorbent before concentrate is entered effectively is exchanged heat by heat exchanger and the lean absorbent from hot recycling tower, realizes effective utilization of energy, reduces production cost；Bypass regulation is additionally provided with the process, the temperature for the sulfur-rich absorbent for entering flash column can be efficiently controlled, it ensure that sulfur-rich absorbent carries out different degrees of concentrate at a suitable temperature, and then cause it to produce the requirement that Crouse's gas of various concentrations meets downstream sulfur recovery workshop section after hot recycling.
Description
Technical field
The present invention relates to purified synthesis gas field, refers specifically to a kind of pre- extracting and concentrating technology of medium temperature sour gas.
Background technology
Purified synthesis gas is mainly used in removing the H in crude synthesis gas2S、COS、CO2, meet the net of technological requirement so as to produce
Change gas.The purified synthesis gas technique commonly used in industry is generally divided into Re Fa and cold process according to the difference for absorbing temperature.In hot method with
Selexol techniques and MDEA techniques are the most famous, and cold process is then using low-temp methanol washing process as representative.Low-temp methanol washing process is 50
A kind of purified synthesis gas technique developed jointly at the beginning of age by German Linde Co and LURGI.The technique is using methanol as absorption
Solvent, using methanol at low temperature to the great good characteristic of sour gas solubility, removed using Physical Absorption in unstripped gas
Sour gas.
The above method is also lacked to H in outlet sour gas at present2The Effective Regulation means of S concentration.In production operation, no
Same sulfur recovery technology is to H in sour gas2S concentration has different requirements.As H in sour gas2When S concentration is relatively low, sulfur recovery dress
Put and will be unable to long-term normal operation.It is to increase by the way of by partially acidic gas recycled back up-stream system in the prior art
H in sour gas2S concentration, but for the built purified synthesis gas device in part, it is limited to its flow setting, entrance synthesis
The factors such as gas sulfur content fluctuation, H in sour gas is improved by increasing sour gas internal circulating load2Extra increased investment needed for S concentration,
Energy consumption is higher, and economy is bad.
The content of the invention
The technical problem to be solved by the invention for the present situation of prior art is to provide a kind of energy consumption is low, and can
Significantly improve H in system outlet sour gas2S concentration, it is easy to adjust H2The pre- extracting and concentrating technology of medium temperature sour gas of S concentration.
Technical scheme is used by the present invention solves above-mentioned technical problem：A kind of pre- extracting and concentrating technology of medium temperature sour gas,
Comprise the following steps：
The temperature of sulfur-rich absorbent from upstream is -20~-60 DEG C, pressure is 0.6~1.5MPaG, H2S's mole contains
Measure as 0.05~5%, carry out heat exchange with the lean absorbent from hot recycling tower and be warming up to 70~110 DEG C, preferably 90~100 DEG C,
It is then sent to flash column and carries out vacuum flashing, it is 0.15~0.45MPaG to control the pressure in the flash column；
What is flashed off contains CO2With part H2S flashed vapour, from flash column top fed downstream process, the tower of flash column
The sulfur-rich absorbent in bottom is sent to stripping tower and carries out air lift operation；
It is 10~110 DEG C of nitrogen that stripping tower bottom, which is passed through temperature, control the air lift tower pressure interior force for 0.15~
0.45MPaG；In air lift operation, the CO in sulfur-rich absorbent2With a small amount of H2S is further desorbed, the gas stripped out with
Above-mentioned flashed vapour converges, fed downstream process in the lump after cooling, and the sulfur-rich absorbent after air lift is discharged from air lift tower bottom；
Hot recycling tower is delivered to from the sulfur-rich absorbent of air lift tower bottom discharge and carries out hot recycling, controls the hot recycling tower
Operation temperature is 80~105 DEG C, and operating pressure is 0.20~0.30MPaG；The sour gas sulfide dissolved in rich absorbent is solved
Suck out, form Crouse's gas, exported by hot recycling top of tower, it is 30 DEG C to be cooled to temperature, wherein H in Crouse's gas2S
Molar content be 40~80%, gas fed downstream sulfur recovery process, after condensate liquid separation as phegma return to it is hot again
Raw top of tower；
Lean absorbent after hot recycling exports from the bottom of hot recycling tower, is sent to after being exchanged heat with the sulfur-rich absorbent
Downstream acidity aspiration process；Aqueous solutions of absorbent exports fed downstream by the bottom of hot recycling tower.
As an improvement, the entrance connection of the flash column conveys the first water influent pipeline of pending sulfur-rich absorbent, it is described
First Heat Exchanger and the second heat exchanger have been sequentially connected in series in first water influent pipeline, the flash column is provided with the first gaseous phase outlet,
First gaseous phase outlet connects the first outlet pipe, and the first outlet pipe, which is provided with, is used for adjusting flash distillation pressure in the flash column
The control valve of power；The entrance of the liquid-phase outlet connection stripping tower of the flash column；The bottom connection gas stripping gas of the stripping tower is defeated
Pipeline is sent, the top of the stripping tower is provided with the second gaseous phase outlet, and the liquid-phase outlet of the stripping tower connects the hot recycling tower
Entrance.Sulfur-rich absorbent is continuous by the First Heat Exchanger and second heat exchanger and the lean absorbent from hot recycling tower
After carrying out heat exchange heating twice, it is directly entered flash column and carries out flashing operation, realize effective utilization of energy.
As an improvement, the hot recycling tower includes the I sections and II section two parts of upper and lower setting, the hot recycling tower I sections it is upper
Portion is connected with the liquid-phase outlet of the stripping tower by the second water influent pipeline, and the I pars infrasegmentalises of hot recycling tower are connected with the poor absorption of output
The first drain pipe of agent road, the bottom of the II sections of the hot recycling tower is provided with the reboiler of hot recycling heat, and the heat is again
The bottom of raw tower is connected with the second drain pipe road of conveying aqueous solutions of absorbent.
Preferably, the molar flow of sulfur-rich absorbent of the molar flow of the air lift nitrogen with entering the stripping tower
Ratio is 1: 10000~450: 10000.
As an improvement, the first drain pipe road is provided with the first bypass, the two-port of first bypass is located at respectively
The upstream and downstream of second heat exchanger, first bypass are provided with the first valve；On the sulfur-rich absorbent conveyance conduit
Provided with the second bypass, the two-port of second bypass is located at the upstream and downstream of the First Heat Exchanger respectively, and described
Second bypass is provided with the second valve, and first valve and second valve are respectively intended to control lean absorbent to enter described first
The flow of heat exchanger and sulfur-rich absorbent enter the flow of second heat exchanger, and then control and enter the sulfur-rich of flash column
The flash temperature of absorbent.By setting above-mentioned bypass to adjust, the sulfur-rich absorbent for entering flash column can be efficiently controlled
Temperature, carry out different degrees of flash distillation concentrate, and then it is produced Crouse's gas of various concentrations after hot recycling and is expired
The requirement of foot trip sulfur recovery workshop section.
Preferably, first bypass and the flow-rate ratio on total road where first bypass are 0~1: 3；Described second
Bypass and the flow-rate ratio on total road where second bypass are 0~1: 3.Can be according to the production status of reality, the bypass of control first
With the uninterrupted of the second bypass, the first valve of the first bypass and the second valve of the second bypass can be closed when necessary,
To reach maximum heat exchange.
As an improvement, the flash column and the stripping tower share same tower body, it is separated by between the two using the first end socket
From, and the flash column is located at the top of the stripping tower, and the liquid-phase outlet of the flash column and the entrance of stripping tower pass through
Exterior line connects, and the liquid-phase outlet of the stripping tower connects the entrance of the hot recycling tower, flash column by first circulation pump
Interior operation temperature is 90~100 DEG C, and flashing pressure is 0.30~0.40MPaG, 90~100 DEG C of operation temperature in stripping tower,
Operating pressure is 0.30~0.40MPaG.Steam pressure of the sulfur-rich absorbent after flash distillation process in self gravitation and flash column
Under effect, stripping tower is flowed into by exterior line, after stripping is handled, liquid phase imports hot recycling after the pressurization of first circulation pump
Tower, the conveying cost of fluid is thus eliminated, save energy；Meanwhile two equipment are stacked together, floor space is small,
On the other hand flashing operation and stripping operation can be enabled to carry out step by step；Certainly, when the operating pressure in flash column is enough
Gao Shi, can also save first circulation pump, and liquid phase can be fed directly to hot recycling tower entrance.
Or the flash column and the stripping tower share same tower body, are isolated between the two using tower tray, the sudden strain of a muscle
Steam the top that tower is located at the stripping tower；
The tower tray is provided with the riser for entering the flash column for gas phase in the stripping tower, and the riser constitutes
Second gaseous phase outlet on the stripping tower top, it is additionally provided with the tower tray and enters the air lift for the liquid phase in the flash column
The downspout of tower, the downspout have connected the liquid-phase outlet of the flash column and the entrance of the stripping tower, the stripping tower
Liquid-phase outlet connects the entrance of the hot recycling tower by first circulation pump, wherein, the operation temperature in flash column is 90~100
DEG C, flashing pressure is 0.30~0.40MPaG, 90~100 DEG C of operation temperature in stripping tower, operating pressure is 0.30~
0.40MPaG.Flash column uses same housing structure with stripping tower, between the two using the tower tray provided with riser and downspout
It is isolated, has both eliminated the conveying cost of fluid, save energy, enables flashing operation and stripping operation in flash column same again
Shi Jinhang.
Or the flash column, the stripping tower and the hot recycling tower share same tower body, the flash column and described
It is isolated by the first end socket between stripping tower, is isolated between the stripping tower and the hot recycling tower by the second end socket,
And stripping tower described in the flash column and the hot recycling tower are sequentially arranged from top to bottom；The liquid-phase outlet of the flash column with
Connected between the entrance of stripping tower by exterior line；Wherein, the operation temperature in flash column is~90~100 DEG C, flash distillation pressure
Power is 0.30~0.40MPaG, and 90~100 DEG C of operation temperature in stripping tower, operating pressure is 0.30~0.40MPaG, and heat is again
Sheng Tanei operation temperature is 87~104 DEG C, and operating pressure is 0.22~0.28MPaG.Sulfur-rich absorbent after flashing operation
Under steam pressure effect in self gravitation and flash column, stripping tower is flowed into by exterior line, after air lift operates, liquid phase is led
Enter the hot recycling tower of lower section, eliminate above-mentioned first circulation pump, save production cost.
Or the flash column, the stripping tower and the hot recycling tower share same tower body；Gas described in the flash column
Stripper and the hot recycling tower are sequentially arranged from top to bottom；
It is isolated between the flash column and the stripping tower by tower tray, between the stripping tower and the hot recycling tower
It is isolated by the second end socket；The tower tray is provided with the riser for entering the flash column for gas phase in the stripping tower, should
Riser constitutes second gaseous phase outlet on the stripping tower top, is additionally provided with the tower tray for the liquid phase in the flash column
Into the downspout of the stripping tower, the downspout has connected the liquid-phase outlet of the flash column and the entrance of the stripping tower,
Wherein, the operation temperature in flash column is 90~100 DEG C, and flashing pressure is 0.30~0.40MPaG, the operation temperature in stripping tower
90~100 DEG C of degree, operating pressure is 0.30~0.40MPaG.Flash column, stripping tower and hot recycling tower share the knot of same tower body
Structure, the fluid pressure conveyer device of the first circulation pump between stripping tower and hot recycling tower can be saved, in drop to a certain degree
The low conveying cost of fluid, has reached energy-saving purpose, meanwhile, three equipment are stacked together, greatly saved
Floor space.
Compared with prior art, advantages of the present invention：By with carrying out self-heating again before sulfur-rich absorbent carries out hot recycling
The lean absorbent of raw tower is effectively exchanged heat, and sulfur-rich absorbent is warming up to 70~110 DEG C after heat exchange, then carries out flashing operation again
Operated with air lift, the CO in sulfur-rich absorbent can be caused2Further desorbed Deng gas, so as to significantly improve H therein2S
Concentration, realize under medium temperature condition sour gas concentrate operation；On the other hand, the sulfur-rich absorbent before concentrate is entered leads to
Cross First Heat Exchanger and the second heat exchanger effectively to be exchanged heat with the lean absorbent from hot recycling tower, realize energy has
Effect utilizes, and reduces production cost；The first bypass is provided with the first water influent pipeline respectively, the second water influent pipeline is provided with by the of second
Road and be provided with the first valve in the first bypass, the second bypass can efficiently control provided with the second valve enters flash column
It the temperature of sulfur-rich absorbent, ensure that sulfur-rich absorbent carries out different degrees of concentrate at a suitable temperature, and then cause it
Crouse's gas that various concentrations are produced after hot recycling meets the requirement of downstream sulfur recovery workshop section；Finally, the flash column, gas
Stripper and the hot recycling tower share the structure of same tower body, on the one hand considerably reduce floor space, on the other hand can be with
First circulation pump installation is saved, the conveying cost of fluid is being reduced to a certain degree, is reaching energy-saving purpose.
Disclosure is particularly well suited to the use of supporting gas purifying technique, the regeneration for its absorbent in gas purifying technique.
Brief description of the drawings
Fig. 1 is the schematic diagram of the embodiment of the present invention 1；
Fig. 2 is the schematic diagram of the embodiment of the present invention 2；
Fig. 3 is the schematic diagram of the embodiment of the present invention 3；
Fig. 4 is the schematic diagram of the embodiment of the present invention 4.
Embodiment
The present invention is described in further detail below in conjunction with accompanying drawing embodiment.
Handled gas is to be rich in CO from upstream aerogenesis apparatus in following each embodiments2And H2The sour gas such as S
Non- purified gas, its predominant gas composition be H2Content 75%~8%, CO contents 75%~0.1%, CO2Content 60%~2%,
H2S contents 5%~0.0001%, used absorbent can be the physical absorbents such as Selexol, NHD, MDEA and methanol.
Embodiment 1,
The pre- extracting and concentrating technology of medium temperature sour gas as shown in Figure 1, the sulfur-rich absorption agent flux from upstream are 274954kg/
H, temperature are -55 DEG C, pressure 1.28MPaG, H2S molar content is 0.318%, passes sequentially through First Heat Exchanger 5 and second
Heat exchanger 4 carries out heat exchange with the lean absorbent from hot recycling tower 1 and is warming up to 95 DEG C, is then sent to flash column 2 and carries out decompression sudden strain of a muscle
Steam；Specifically, First Heat Exchanger 5 can be connected in series with the second heat exchanger 4, sulfur-rich absorbent walk First Heat Exchanger 5 with
The tube side of second heat exchanger 4, correspondingly, lean absorbent walk the shell side of the heat exchanger 4 of First Heat Exchanger 5 and second；Certainly, sulfur-rich suction
The shell side that the heat exchanger 4 of First Heat Exchanger 5 and second is walked in agent is received, lean absorbent walks the pipe of the second heat exchanger 4 and First Heat Exchanger 5
Journey, or sulfur-rich absorbent intersects to walk the tube side of the heat exchanger 4 of First Heat Exchanger 5 and second respectively with lean absorbent and shell side also can
Reach same heat exchange purpose.
The top of flash column 2 is provided with the first gaseous phase outlet, and first gaseous phase outlet is connected with the first outlet pipe, the first outlet
Pipeline is provided with the control valve 14 for being used for adjusting flashing pressure in flash column 2, and the flashing pressure of the present embodiment is 0.35MPaG；Dodge
What is be steamed out contains CO2With part H2S flashed vapour, from the top of flash column 2 by the first outlet pipe fed downstream process, dodge
Sulfur-rich absorbent after steaming is sent to stripping tower 3 from the bottom of towe outflow of flash column 2 and carries out air lift operation.
Flash column 2 and stripping tower 3 share same tower body in the present embodiment, are isolated between the two using the first end socket 21,
And flash column 2 is located at the top of stripping tower 3, the entrance of the liquid-phase outlet and stripping tower 3 of flash column 2 is connected by exterior line
Connect, this mode can cause steam pressure effect of the sulfur-rich absorbent after flash distillation process in self gravitation and flash column 2
Under, stripping tower 3 is flowed into by exterior line, thus eliminates the conveying cost of fluid, saves energy, meanwhile, two are set
It is standby to be stacked together, also save floor space.
The bottom connection gas stripping gas conveyance conduit of stripping tower 3, nitrogen enter stripping tower 3, this reality through gas stripping gas conveyance conduit
The flow for applying the air lift nitrogen in example is 310Nm3/ h, temperature are 40 DEG C, and air lift nitrogen pressure is 0.40MPaG, and air lift operates
In, the CO in sulfur-rich absorbent2With a small amount of H2S is further desorbed, and the top of stripping tower 3 is provided with the second gaseous phase outlet, air lift
Mixed gas afterwards is discharged through the second gaseous phase outlet, fed downstream in the lump after converging with above-mentioned flashed vapour, the sulfur-rich suction after air lift
Receiving agent, hot recycling tower 1 is sent in output from the bottom of stripping tower 3.
The temperature that sulfur-rich absorbent is exported from the bottom of stripping tower 3 is 85 DEG C, and hot recycling tower 1 is delivered to by first circulation pump 11
Top, hot recycling tower 1 include the I sections and II section two parts of upper and lower setting, are separated between two sections by liter gas cap, regenerated
When, the operation temperature of hot recycling tower 1 is 87~104 DEG C, and operating pressure is 0.22~0.28MPaG, under the II sections of hot recycling tower 1
The reboiler 8 of portion's connection can provide the heat that hot recycling tower 1 carries out hot recycling by indirect heat exchange mode, molten in rich absorbent
The sour gas of solution desorbs, and forms Crouse's gas, is exported by the top of hot recycling tower 1, is cooled to temperature as 30 DEG C, wherein gram
H in the gas of Louth2S molar content is 40%, Crouse's gas fed downstream sulfur recovery process after cooling, after condensate liquid separation
The top of hot recycling tower 1 is returned to as phegma.
The bottom of the I sections of hot recycling tower 1 is connected with the first drain pipe road, and the first drain pipe road is defeated by second circulation pump 10
The lean absorbent gone out after hot recycling, the temperature of lean absorbent are 102 DEG C, pressure 0.28MPaG, then pass sequentially through above-mentioned the
Two heat exchangers 4 and First Heat Exchanger 5 are sent to upstream acidity aspiration process after being exchanged heat with above-mentioned sulfur-rich absorbent；Hot recycling
The bottom of the II sections of tower 1 is connected with the second drain pipe road, and aqueous solutions of absorbent is exported from the second drain pipe road, and fed downstream absorbs
The purification ＆ isolation process of agent.
First drain pipe road is provided with the first bypass, and the two-port of the first bypass is respectively positioned at second heat exchanger 4
Upstream and downstream, the first bypass are provided with the first valve 12；Sulfur-rich absorbent conveyance conduit is provided with the second bypass, the second bypass
Two-port is located at the upstream and downstream of First Heat Exchanger 5 respectively, and the second bypass is provided with the second valve 13, the first valve 12 and the
Two valves 13 are respectively intended to control lean absorbent to enter the flow of First Heat Exchanger 5 and sulfur-rich absorbent enters the second heat exchanger
4 flow, and then control enters the flash temperature of the sulfur-rich absorbent of flash column 2, the present embodiment in device load variations
In the first flow of the bypass under normal duty be 0, flow of second bypass under normal duty is 0.
As H in sour gas2When S concentration is relatively low, used partially acidic gas recycled back up-stream system in the prior art
Mode increase the H in sour gas2S concentration；The H in equal outlet sour gas is met2On the basis of S concentration, compared to by acid
Property gas pressurized circulation to upstream flow, the investment using the sour gas concentrate means of the present invention is less, and energy consumption and operating cost are more
It is low.By taking same size low temperature washing device for methanol in the prior art as an example, when exporting H in sour gas2When S concentration is maintained at 40%,
Using sour gas pressurized circulation flow and the public work consumption using technological process in the present embodiment 1, investment, operating cost pair
Than as follows：
| Comparative run | Embodiment 1 compares existing concentrate technology |
| Power consumption (Kw) | -140 |
| Circulate water consume (t/h) | -20 |
| 0.4MPag steam consumptions (t/h) | -0.4 |
| Nitrogen consumes (Nm3/h) | +310 |
| Plant investment (ten thousand yuan) | -30 |
| Year operating cost (ten thousand yuan) | -55 |
Note：1st, "-" represents to reduce, and "+" represents increase；
2nd, public work consumption unit price：0.6 yuan/kw of electricity；0.3 yuan/ton of recirculated water；100 yuan/ton of steam；0.2 yuan of nitrogen/
Nm3。
Embodiment 2,
The pre- extracting and concentrating technology of medium temperature sour gas as shown in Figure 2, the sulfur-rich absorbent from upstream, flow are
274954kg/h, temperature are -55 DEG C, pressure 1.28MPaG, H2S molar content is 0.318%；
In the present embodiment from embodiment 1 unlike, flash column 2 and stripping tower 3 share same tower body, adopt between the two
It is isolated with tower tray 9, flash column 2 is located at the top of stripping tower 3；Tower tray 9 is provided with gas phase in supply stripper 3 and enters flash column 2
Riser 91, the riser 91 constitutes second gaseous phase outlet on the top of stripping tower 3 described in embodiment 1, on tower tray 9 also
Provided with the downspout 92 for entering stripping tower 3 for the liquid phase in flash column 2, the downspout 92 has connected the liquid-phase outlet of flash column 2
With the entrance of stripping tower 3, the liquid-phase outlet of stripping tower 3 connects the entrance of hot recycling tower 1 by first circulation pump 11；The present embodiment
In other guide it is same as Example 1, be no longer described in detail, its corresponding process operation parameter change is as follows：
The temperature that sulfur-rich absorbent enters flash column 2 after the heat exchange of the heat exchanger 4 of First Heat Exchanger 5 and second is 95 DEG C；
The flashing pressure of flash column 2 is 0.35MPaG；
The flow of air lift nitrogen is 310Nm3/ h, the temperature of air lift nitrogen is 40 DEG C, and the pressure of air lift nitrogen is
0.4MPaG；
Temperature from the sulfur-rich absorbent of the bottom of stripping tower 3 output is 85 DEG C；
The operation temperature of hot recycling tower 1 is 87~104 DEG C, and operating pressure is 0.22~0.28MPaG；
Temperature of the output Crouse's gas in the top of hot recycling tower 1 after cooler cools down is 30 DEG C.
H in Crouse's gas2S molar content is 40%；
By taking same size low temperature washing device for methanol in the prior art as an example, when exporting H in sour gas2S concentration is maintained at
When 40%, in the prior art using sour gas pressurized circulation flow with being disappeared using the public work of technological process in the present embodiment
Consumption, investment, operating cost contrast are as follows：
| Comparative run | Embodiment 2 compares existing concentrate technology |
| Power consumption (Kw) | -140 |
| Circulate water consume (t/h) | -20 |
| 0.4MPag steam consumptions (t/h) | -0.4 |
| Nitrogen consumes (Nm3/h) | +310 |
| Plant investment (ten thousand yuan) | -30 |
| Year operating cost (ten thousand yuan) | -55 |
Note：1st, "-" represents to reduce, and "+" represents increase；
2nd, public work consumption unit price：0.6 yuan/kw of electricity；0.3 yuan/ton of recirculated water；100 yuan/ton of steam；0.2 yuan of nitrogen/
Nm3。
Embodiment 3,
The pre- extracting and concentrating technology of medium temperature sour gas as shown in Figure 3, the sulfur-rich absorbent from upstream, flow are
274954kg/h, temperature are -55 DEG C, pressure 1.28MPaG, H2S molar content is 0.318%；
In the present embodiment from embodiment 1 unlike, flash column 2, stripping tower 3 and hot recycling tower 1 share same tower body,
It is isolated between flash column 2 and stripping tower 3 by the first end socket 21, passes through the second end socket 31 between stripping tower 3 and hot recycling tower 1
It is isolated, and the stripping tower 3 of flash column 2 and hot recycling tower 1 are sequentially arranged from top to bottom；The liquid-phase outlet of flash column 2 passes through outer
The entrance of portion's fluid circuit connection stripping tower 3, the liquid-phase outlet of stripping tower 3 connect hot recycling tower 1 by the second water influent pipeline
Entrance, under self gravitation and the effect of tower body internal pressure, sulfur-rich absorbent enters stripping tower 3 from flash column 2, then enters back into
Hot recycling tower 1 is imported into after the heat exchange of the second heat exchanger 4 carry out hot recycling process in second water influent pipeline.Thus eliminate gas
The fluid pressure conveyer device of first circulation pump 11 between stripper 3 and hot recycling unit, reduces production cost.Except this it
Outside, the other guide in the present embodiment is same as Example 1, is no longer described in detail, and corresponding process operation parameter change is as follows：
The temperature that sulfur-rich absorbent enters flash column 2 after the heat exchange of the heat exchanger 4 of First Heat Exchanger 5 and second is 95 DEG C；
The flashing pressure of flash column 2 is 0.35MPaG；
The flow of air lift nitrogen is 310Nm3/ h, the temperature of air lift nitrogen is 40 DEG C, and the pressure of air lift nitrogen is
0.4MPaG；
Temperature from the sulfur-rich absorbent of the bottom of stripping tower 3 output is 85 DEG C；
The operation temperature of hot recycling tower 1 is 87~104 DEG C, and operating pressure is 0.22~0.28MPaG；
Temperature of the output Crouse's gas in the top of hot recycling tower 1 after cooler cools down is 30 DEG C；
H in Crouse's gas2S molar content is 40%.
By taking same size low temperature washing device for methanol in the prior art as an example, when exporting H in sour gas2S concentration is maintained at
When 40%, in the prior art using sour gas pressurized circulation flow with being disappeared using the public work of technological process in the present embodiment
Consumption, investment, operating cost contrast are as follows：
| Comparative run | Embodiment 3 compares existing concentrate technology |
| Power consumption (Kw) | -140 |
| Circulate water consume (t/h) | -20 |
| 0.4MPag steam consumptions (t/h) | -0.4 |
| Nitrogen consumes (Nm3/h) | +310 |
| Plant investment (ten thousand yuan) | -30 |
| Year operating cost (ten thousand yuan) | -55 |
Note：1st, "-" represents to reduce, and "+" represents increase；
2nd, public work consumption unit price：0.6 yuan/kw of electricity；0.3 yuan/ton of recirculated water；100 yuan/ton of steam；0.2 yuan of nitrogen/
Nm3。
Embodiment 4,
The pre- extracting and concentrating technology of medium temperature sour gas as shown in Figure 4, the sulfur-rich absorbent from upstream, flow are
274954kg/h, temperature are -55 DEG C, pressure 1.28MPaG, H2S molar content is 0.318%；
In the present embodiment from embodiment 1 unlike, flash column 2, stripping tower 3 and hot recycling tower 1 share same tower body,
It is isolated by tower tray 9 between flash column 2 and stripping tower 3, is separated by between stripping tower 3 and hot recycling tower 1 by the second end socket 31
From, and the stripping tower 3 of flash column 2 and hot recycling tower 1 are sequentially arranged from top to bottom；Tower tray 9 is provided with riser 91 and downspout
92, the gas in stripping tower 3 is entered directly into by riser 91 in the flash column 2 of top, correspondingly, the liquid in flash column 2
Mutually entered by downspout 92 in the stripping tower 3 of lower section, it is gentle so to can be avoided the increase connection flash column 2 outside tower body
The pipeline of stripper 3, flash process is also allowd to be carried out simultaneously with air lift process.The liquid-phase outlet of stripping tower 3 enters by second
The entrance of liquid pipeline connection hot recycling tower 1, under self gravitation and the effect of tower body internal pressure, sulfur-rich absorbent is from flash column 2
Enter stripping tower 3 through downspout 92, then enter back into the second water influent pipeline and imported into hot recycling after the heat exchange of the second heat exchanger 4
Tower 1 carries out hot recycling process.Thus eliminate the fluid pressurization of the first circulation pump 11 between stripping tower 3 and hot recycling unit
Conveying device, reduce production cost.In addition, the other guide in the present embodiment is same as Example 1, is no longer described in detail,
Corresponding process operation parameter change is as follows：
The temperature that sulfur-rich absorbent enters flash column 2 after the heat exchange of the heat exchanger 4 of First Heat Exchanger 5 and second is 95 DEG C；
The flashing pressure of flash column 2 is 0.35MPaG；
The flow of air lift nitrogen is 310Nm3/ h, the temperature of air lift nitrogen is 40 DEG C, and the pressure of air lift nitrogen is
0.4MPaG；
Temperature from the sulfur-rich absorbent of the bottom of stripping tower 3 output is 85 DEG C；
The operation temperature of hot recycling tower 1 is 87~104 DEG C, and operating pressure is 0.22~0.28MPaG；
Temperature of the output Crouse's gas in the top of hot recycling tower 1 after cooler cools down is 30 DEG C；
H in Crouse's gas2S molar content is 40%.
By taking same size low temperature washing device for methanol in the prior art as an example, when exporting H in sour gas2S concentration is maintained at
When 40%, in the prior art using sour gas pressurized circulation flow with being disappeared using the public work of technological process in the present embodiment
Consumption, investment, operating cost contrast are as follows：
| Comparative run | Embodiment 4 compares existing concentrate technology |
| Power consumption (Kw) | -140 |
| Circulate water consume (t/h) | -20 |
| 0.4MPag steam consumptions (t/h) | -0.4 |
| Nitrogen consumes (Nm3/h) | +310 |
| Plant investment (ten thousand yuan) | -30 |
| Year operating cost (ten thousand yuan) | -55 |
Note：1st, "-" represents to reduce, and "+" represents increase；
2nd, public work consumption unit price：0.6 yuan/kw of electricity；0.3 yuan/ton of recirculated water；100 yuan/ton of steam；0.2 yuan of nitrogen/
Nm3。
In summary, as H in sour gas2When S concentration is relatively low, with using partially acidic gas recycled back in the prior art
The mode of up-stream system increases the H in sour gas2The mode of operation of S concentration is compared；The H in equal outlet sour gas is met2S
On the basis of concentration, using the present invention sour gas concentrate means plant investment, production operation expense and energy consumption all significantly
Reduce.
Claims (10)
1. a kind of pre- extracting and concentrating technology of medium temperature sour gas, it is characterised in that comprise the following steps：
The temperature of sulfur-rich absorbent from upstream is -20~-60 DEG C, pressure is 0.6~1.5MPaG, H2S molar content is
0.05~5%, carry out heat exchange with the lean absorbent from hot recycling tower (1) and be warming up to 70~110 DEG C, be then sent to flash column
(2) vacuum flashing is carried out, it is 0.15~0.45MPaG to control the pressure in the flash column (2)；
What is flashed off contains CO2With part H2S flashed vapour, the fed downstream process at the top of the flash column (2), flash column (2)
The sulfur-rich absorbent of bottom of towe is sent to stripping tower (3) and carries out air lift operation；
It is 10~110 DEG C of nitrogen that stripping tower (3) bottom, which is passed through temperature, control the stripping tower (3) interior pressure for 0.15~
0.45MPaG；In air lift operation, the CO in sulfur-rich absorbent2With a small amount of H2S is further desorbed, the gas stripped out with
Above-mentioned flashed vapour converges, fed downstream process in the lump after cooling, and the sulfur-rich absorbent after air lift is discharged from stripping tower (3) bottom；
Hot recycling tower (1) is delivered to from the sulfur-rich absorbent of stripping tower (3) bottom discharge and carries out hot recycling, controls the hot recycling tower
(1) operation temperature is 80~105 DEG C, and operating pressure is 0.20~0.30MPaG；The sour gas vulcanization dissolved in rich absorbent
Thing is desorbed out, forms Crouse's gas, by being exported at the top of hot recycling tower (1), is cooled to temperature as 30 DEG C, wherein Crouse
H in gas2S molar content is 40~80%, gas fed downstream sulfur recovery process, is returned after condensate liquid separation as phegma
Return at the top of hot recycling tower (1)；
Lean absorbent after hot recycling exports from the bottom of hot recycling tower (1), is sent to after being exchanged heat with the sulfur-rich absorbent
Downstream acidity aspiration process；Aqueous solutions of absorbent exports fed downstream by the bottom of hot recycling tower (1).
2. the pre- extracting and concentrating technology of medium temperature sour gas according to claim 1, it is characterised in that：Flash column (2) enter
Mouth connection conveys the first water influent pipeline of pending sulfur-rich absorbent, and the first heat exchange has been sequentially connected in series in first water influent pipeline
Device (5) and the second heat exchanger (4), the flash column (2) are provided with the first gaseous phase outlet, the first gaseous phase outlet connection first
Outlet pipe, the first outlet pipe are provided with the control valve (14) for being used for adjusting the flash column (2) interior flashing pressure；The sudden strain of a muscle
Steam the entrance of the liquid-phase outlet connection stripping tower (3) of tower (2)；The bottom connection gas stripping gas conveyance conduit of the stripping tower (3), institute
The top for stating stripping tower (3) is provided with the second gaseous phase outlet, and the liquid-phase outlet of the stripping tower (3) connects the hot recycling tower (1)
Entrance.
3. the pre- extracting and concentrating technology of medium temperature sour gas according to claim 1, it is characterised in that：Hot recycling tower (1) bag
I section and II section of two parts of upper and lower setting are included, I section of top of the hot recycling tower (1) and the liquid phase of the stripping tower (3) go out
Mouth is connected by the second water influent pipeline, and I pars infrasegmentalis of hot recycling tower (1) is connected with output the first drain pipe of lean absorbent road, the heat
II section of bottom of regenerator (1) is provided with the reboiler (8) of hot recycling heat, the bottom of the hot recycling tower (1)
It is connected with the second drain pipe road of conveying aqueous solutions of absorbent.
4. the pre- extracting and concentrating technology of medium temperature sour gas according to claim 1, it is characterised in that：Mole of the air lift nitrogen
The ratio of the molar flow of sulfur-rich absorbent of the flow with entering the stripping tower (3) is 1：10000~450：10000 .
5. the pre- extracting and concentrating technology of medium temperature sour gas according to claim 2, it is characterised in that：On the first drain pipe road
Provided with the first bypass, the two-port of first bypass is located at the upstream and downstream of second heat exchanger (4) respectively, and described the
One bypass is provided with the first valve (12)；The sulfur-rich absorbent conveyance conduit is provided with second and bypassed, and the two of second bypass
Port is located at the upstream and downstream of the First Heat Exchanger (5) respectively, and second bypass is provided with the second valve (13), institute
State the first valve (12) and second valve (13) is respectively intended to the flow that control lean absorbent enters the First Heat Exchanger (5)
The flow of second heat exchanger (4) is entered with sulfur-rich absorbent, and then controls the sulfur-rich absorbent for entering flash column (2)
Flash temperature.
6. the pre- extracting and concentrating technology of medium temperature sour gas according to claim 5, it is characterised in that：First bypass with this
The flow-rate ratio on total road is 0~1 where one bypass:3；The second described bypass and the flow-rate ratio on total road where second bypass are 0
~1:3.
7. the pre- extracting and concentrating technology of medium temperature sour gas according to claim 1-6 any claims, it is characterised in that：It is described
Flash column (2) and the stripping tower (3) share same tower body, are isolated between the two using the first end socket (21), and described
Flash column (2) is located at the top of the stripping tower (3), and the entrance of the liquid-phase outlet and stripping tower (3) of the flash column (2) passes through
Exterior line connects, and the liquid-phase outlet of the stripping tower (3) connects entering for hot recycling tower (1) by first circulation pump (11)
Mouthful, the operation temperature in flash column (2) is 90~100 DEG C, and flashing pressure is 0.30~0.40MPaG, the behaviour in stripping tower (3)
Make 90~100 DEG C of temperature, operating pressure is 0.30~0.40MPaG.
8. the pre- extracting and concentrating technology of medium temperature sour gas according to any claim in claim 1-6, it is characterised in that：Institute
State flash column (2) and the stripping tower (3) shares same tower body, be isolated between the two using tower tray (9), the flash column
(2) it is located at the top of the stripping tower (3)；
The tower tray (9) is provided with the riser (91) for entering the flash column (2) for the stripping tower (3) interior gas phase, the liter
Tracheae (91) constitutes second gaseous phase outlet on the stripping tower (3) top, is additionally provided with the tower tray (9) for the flash column
(2) liquid phase in enters the downspout (92) of the stripping tower (3), and the downspout (92) has connected the liquid of the flash column (2)
Mutually outlet and the entrance of the stripping tower (3), the liquid-phase outlet of the stripping tower (3) pass through described in first circulation pump (11) connection
The entrance of hot recycling tower (1), wherein, operation temperature in flash column (2) is 90~100 DEG C, flashing pressure is 0.30~
0.40MPaG, 90~100 DEG C of operation temperature in stripping tower (3), operating pressure is 0.30~0.40MPaG.
9. the pre- extracting and concentrating technology of medium temperature sour gas according to any claim in claim 1-6, it is characterised in that：Institute
State flash column (2), the stripping tower (3) and the hot recycling tower (1) and share same tower body, the flash column (2) and the gas
It is isolated between stripper (3) by the first end socket (21), passes through second between the stripping tower (3) and the hot recycling tower (1)
End socket (31) is isolated, and the flash column (2) described stripping tower (3) and the hot recycling tower (1) cloth successively from top to bottom
Put；It is connected between the liquid-phase outlet of the flash column (2) and the entrance of stripping tower (3) by exterior line；Wherein, flash column
(2) operation temperature in is 90~100 DEG C, and flashing pressure is 0.30~0.40MPaG, the operation temperature 90 in stripping tower (3)~
100 DEG C, operating pressure is 0.30~0.40MPaG, and the operation temperature in hot recycling tower (1) is 87~104 DEG C, and operating pressure is
0.22~0.28MPaG.
10. the pre- extracting and concentrating technology of medium temperature sour gas according to claim 1-6 any claims, it is characterised in that：Institute
State flash column (2), the stripping tower (3) and the hot recycling tower (1) and share same tower body；The flash column (2) air lift
Tower (3) and the hot recycling tower (1) are sequentially arranged from top to bottom；
It is isolated between the flash column (2) and the stripping tower (3) by tower tray (9), the stripping tower (3) and the heat are again
It is isolated between raw tower (1) by the second end socket (31)；The tower tray (9) is provided with to be entered for the interior gas phase of the stripping tower (3)
The riser (91) of the flash column (2), the riser (91) constitute second gaseous phase outlet on the stripping tower (3) top,
The downspout (92) for entering the stripping tower (3) for the liquid phase in the flash column (2), the drop are additionally provided with the tower tray (9)
Liquid pipe (92) has connected the liquid-phase outlet of the flash column (2) and the entrance of the stripping tower (3), wherein, in flash column (2)
Operation temperature is 90~100 DEG C, and flashing pressure is 0.30~0.40MPaG, 90~100 DEG C of operation temperature in stripping tower (3),
Operating pressure is 0.30~0.40MPaG.
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| CN110548370A (en) * | 2019-09-04 | 2019-12-10 | 大连理工大学 | Acid gas purification process and device for producing hydrogen sulfide with various purities |
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