CN109603408A - A kind of control system of petroleum vapor recovery technique - Google Patents
A kind of control system of petroleum vapor recovery technique Download PDFInfo
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- CN109603408A CN109603408A CN201811603291.8A CN201811603291A CN109603408A CN 109603408 A CN109603408 A CN 109603408A CN 201811603291 A CN201811603291 A CN 201811603291A CN 109603408 A CN109603408 A CN 109603408A
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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
- B01D53/002—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 condensation
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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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Oil, Petroleum & Natural Gas (AREA)
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- Separation Of Gases By Adsorption (AREA)
Abstract
A kind of control system of petroleum vapor recovery technique of disclosure of the invention, multiple adsorption towers, any one adsorption tower may be in the state of VOC absorption, remaining adsorption tower is adsorbed accordingly, is replaced, being heated, cooled down, multiple adsorption tower alternating cycle works realize oil gas non-pollution discharge.The present invention uses condensation+TSA(temp.-changing adsorption), adsorbent is regenerated using heating regeneration method, can effectively solve the problems, such as that larger molecular organics regeneration is difficult.
Description
Technical field
The present invention relates to petroleum vapor recovery fields, and in particular to a kind of control system of petroleum vapor recovery technique.
Background technique
In petroleum storage tank in petroleum vapor recovery, existing technology mostly uses pressure-variable adsorption or condensation+PSA(pressure-variable adsorption)
There is underproof situation after operation a period of time in technique, device, the reason is that larger molecular organics are regenerated using vacuumizing
Method, desorption are not thorough, and adsorption effect is bad after larger molecular organics accumulate on the sorbent, empty organic concentration in tail gas
The technical problems such as exceeded.
Summary of the invention
It is an object of the invention to overcome the deficiencies of the prior art and provide a kind of control systems of petroleum vapor recovery technique.It adopts
With condensation+TSA(temp.-changing adsorption), adsorbent is regenerated using heating regeneration method, effectively solution larger molecular organics
Regenerate difficult problem.
The purpose of the present invention is achieved through the following technical solutions: a kind of petroleum vapor recovery technique, recovery process equipment
Including multiple adsorption towers, nitrogen circulating system unit, refrigeration systems units, heating system unit, the nitrogen circulating system list
Member, heating system unit, passes through pipeline between multiple adsorption towers and connects refrigeration systems units, the nitrogen circulating system
Unit is to provide nitrogen source, and the refrigeration control unit and heating system unit are to control nitrogen temperature；
Steps are as follows for recovery process:
S1. raw material oil gas is passed through when being adsorbed in wherein adsorption tower a, replaced respectively in remaining adsorption tower, regenerate it is pre-
Absorption, regeneration preheating, regeneration precooling, regenerative adsorption, displacement, heating, cooling；
S2. when the adsorption tower a is replaced, absorption and regenerative adsorption are carried out in remaining adsorption tower respectively；
S3. it when the adsorption tower a is heated, adsorbed respectively in remaining adsorption tower, regenerate precooling, regeneration preheating；
S4. it when the adsorption tower a is cooled down, adsorbed respectively in remaining adsorption tower, regenerate pre- absorption, regeneration preheating；
S5. it when the adsorption tower a carries out regenerative adsorption, replaced, adsorbed, regenerative adsorption respectively in remaining adsorption tower；
S6. it when the adsorption tower a carries out regenerating pre- absorption, is respectively heated in remaining adsorption tower, adsorbs, regenerates precooling；
S7. it when the adsorption tower a carries out regeneration preheating, carries out cooling down respectively in remaining adsorption tower, adsorbs, regenerates pre- absorption；
S8. when the adsorption tower a carries out regenerative adsorption, absorption, displacement, absorption are respectively regenerated in remaining adsorption tower；
S9. when the adsorption tower a carries out regeneration precooling, pre- absorption, heating, absorption are respectively regenerated in remaining adsorption tower；
S10. when the adsorption tower a carries out regenerating pre- absorption, preheating, cooling, absorption are respectively regenerated in remaining adsorption tower；
S11. S1-S10 step cycle is operated.
Preferably, the S1-S11 step is all made of automatic control mode control.
Preferably, in the entire processing step of the S1-S11, when adsorption tower carries out regeneration heating step, oxygen in adsorption tower
Content is no more than standard value.
Preferably, in the entire processing step of the S1-S11, when adsorption tower carries out displacement step, by detecting adsorption tower
When gas outlet, the oxygen content displaced in gas is exceeded, then control valve c is closed, and high temperature regeneration gas is forbidden to enter recovery process
In equipment, the oxygen content in gas out to be replaced is up to standard, then control valve c is opened, and high temperature regeneration gas is allowed to enter recovery process
In equipment.
Preferably, it in the entire processing step of the S1-S11, by the way that temperature sensor is arranged on adsorption tower, supervises in real time
The temperature for controlling entire technique, when temperature is excessively high, control valve c is closed, and high temperature regeneration gas is forbidden to go successively to recovery process equipment
In.
Preferably, in the entire processing step of the S1-S11, the nitrogen gas purity in nitrogen circulating system unit is not less than
99.99%, nitrogen dew-point temperature is -60 DEG C, and nitrogen pressure is not less than 0.2MPaG, and temperature is room temperature.
Preferably, in the entire processing step of the S1-S11, in the refrigeration systems units, coolant media selects -30
DEG C ethylene glycol, refrigerant pressure 0.25MPaG.
Preferably, multiple adsorption towers are respectively adsorption tower A, adsorption tower B, adsorption tower C, adsorption tower D, recovery process step
It is rapid as follows:
S1. VOC is passed through when being adsorbed in adsorption tower A, is replaced respectively in remaining adsorption tower, regenerates pre- absorption, regeneration
Preheating, regeneration precooling, regenerative adsorption, displacement, heating, cooling；
S2. when the adsorption tower A is replaced, adsorption tower B, adsorption tower C, adsorbed in adsorption tower D respectively, regenerative adsorption with
And regenerative adsorption；
S3. it when the adsorption tower A is heated, adsorption tower B, adsorption tower C, adsorbed in adsorption tower D respectively, regenerate pre-cooling
But, regeneration preheating；
S4. it when the adsorption tower A is cooled down, adsorption tower B, adsorption tower C, adsorbed in adsorption tower D respectively, regenerate pre-suction
Attached, regeneration preheating；
S5. when the adsorption tower A carries out regenerative adsorption, adsorption tower B, adsorption tower C, replaced in adsorption tower D, adsorbed respectively,
Regenerative adsorption；
S6. it when the adsorption tower A carries out regenerating pre- absorption, adsorption tower B, adsorption tower C, is respectively heated in adsorption tower D, inhales
Attached, regeneration precools；
S7. when the adsorption tower A carries out regeneration preheating, adsorption tower B, adsorption tower C, carried out in adsorption tower D respectively it is cooling, inhale
Attached, the pre- absorption of regeneration；
S8. when the adsorption tower A carries out regenerative adsorption, adsorption tower B, adsorption tower C, absorption is respectively regenerated in adsorption tower D, is set
It changes, adsorb；
S9. when the adsorption tower A carries out regeneration and precools, pre-suction adsorption tower B, adsorption tower C, is respectively regenerated in adsorption tower D
Attached, heating, absorption；
S10. when the adsorption tower A carries out regenerating pre- absorption, pre-add adsorption tower B, adsorption tower C, is respectively regenerated in adsorption tower D
Heat, cooling, absorption；
S11. S1-S10 step cycle is operated.
Preferably, in the S1, when being adsorbed in adsorption tower A, remaining adsorption tower undergoes first stage, respectively
Two-stage, phase III, when the first stage, adsorption tower B, adsorption tower C, be respectively regenerated absorption in adsorption tower D, regeneration is inhaled
Attached, displacement, when second stage, adsorption tower B, adsorption tower C, be respectively regenerated in adsorption tower D precooling, the pre- absorption of regeneration plus
Heat when the phase III, adsorption tower B, adsorption tower C, is respectively regenerated pre- absorption in adsorption tower D, is regeneration preheating, cooling.
The beneficial effects of the present invention are:
1. use condensation+TSA(temp.-changing adsorption), adsorbent is regenerated using heating regeneration method, can effectively be solved
The difficult problem of larger molecular organics regeneration；
2. protecting system safe present invention employs oxygen on-line checking and interlocking and temperature online detection and interlocking.
3. the present invention uses multiple adsorption towers, any one adsorption tower may be in the attached state of feedstock oil aspiration,
Remaining adsorption tower is adsorbed accordingly, is replaced, being heated, being cooled down, by the Adsorption and desorption of unstripped gas and nitrogen system knot
It is combined, reduces equipment investment, while reducing nitrogen usage amount.
Detailed description of the invention
Fig. 1 is process flow chart of the invention.
Specific embodiment
Technical solution of the present invention is described in further detail with reference to the accompanying drawing, but protection scope of the present invention is not limited to
It is as described below.
Embodiment
As shown in Figure 1, P101 indicates that lime set delivery pump, J101 indicate that unstripped gas supercharger, E101 indicate pre-cooling in Fig. 1
Device, V101 indicate that lime set basin, C101 indicate that VOC condenser, S101 indicate that gas-liquid separator, T101A indicate adsorption tower A,
T101B indicates that adsorption tower B, T101C indicate that adsorption tower C, T101D indicate that adsorption tower D, E104 indicate nitrogen cooler, E102 table
Show that regeneration gas water cooler, Q101 indicate that electric heater, J102 indicate that nitrogen supercharging machine, E103 indicate regeneration gas forecooler, C102
Indicate that regeneration gas condenser, V101 circular buffering tank, S102 indicate regeneration gas separating device.
As shown in table 1,
Wherein, A indicates absorption in table, and PR indicates displacement, and H indicates heating, and C indicates cooling, and A1 indicates the pre- absorption of regeneration, and H1 is indicated
Regeneration preheating, C1 indicate that regeneration precools, and IS indicates regenerative adsorption.
A kind of control system of petroleum vapor recovery technique,
Including unstripped gas air inlet, unstripped gas supercharger, raw material gas purifying recovery unit, nitrogen circulating system unit, refrigeration system
System unit, lime set storage tank；
The raw material gas purifying recovery unit includes multiple adsorption towers, and any one adsorption tower may be in adsorbed state,
Remaining adsorption tower is adsorbed accordingly, is replaced, being heated, being cooled down, multiple adsorption tower alternating cycle works；
The nitrogen circulating system unit provides nitrogen source for adsorption tower；The system provides regeneration gas when being mainly adsorption tower regeneration
Source, supplement nitrogen parameter request are as follows:
Nitrogen gas purity >=-60 DEG C of 99.99% dew-point temperature
Pressure >=0.2MPaG temperature environment temperature
Flow: interruption supplement, hour flow are not more than 10Nm3/h (average magnitude)
The refrigeration systems units provide refrigerant for raw material gas purifying recovery unit；The system is mainly that compress cell and purification are single
Member provides refrigerant, which is supply in full sets.Parameter request is as follows:
Coolant media: -30 DEG C of ethylene glycol
Refrigerant pressure: refrigerant output pressure~0.25MPaG
The lime set storage tank is to recovering liquid organic matter.
Specifically, the raw material gas purifying recovery unit includes adsorption tower A, adsorption tower B, adsorption tower C, adsorption tower D, institute
State adsorption tower A, adsorption tower B, adsorption tower C, adsorption tower D bottom pass through pipeline a and be connected to unstripped gas feed inlet, the pipeline
A, which is equipped with, enters adsorption tower A, adsorption tower B, adsorption tower C, the valve in adsorption tower D, adsorption tower A, absorption to control unstripped gas
Tower B, adsorption tower C, adsorption tower D bottom pass through pipeline b and be communicated with gas-liquid separator k, the bottom of the gas-liquid separator k with
The connection of lime set storage tank；Adsorption tower A, adsorption tower B, adsorption tower C, adsorption tower D top pass through pipeline d and be communicated with the atmosphere, it is described
Pipeline d is equipped with valve to control system pressure, adsorption tower A, adsorption tower B, adsorption tower C, adsorption tower D bottom pass through
Pipeline e is connected to source nitrogen, and it is slow that nitrogen cooler h, nitrogen supercharging machine i, circulation are successively arranged on the pipeline e from tower bottom to source nitrogen
Rush tank j, adsorption tower A, adsorption tower B, adsorption tower C, adsorption tower D top pass through pipeline p be communicated with nitrogen circulation surge tank and
Source nitrogen.
Wherein, adsorption tower A, adsorption tower B, adsorption tower C, adsorption tower D different time sections can undergo absorption, displacement, plus
Four circulation steps such as heat, cooling, and adsorption tower A, adsorption tower B, adsorption tower C, adsorption tower D can be undergone respectively in the same period
Four steps such as absorption, displacement, heating, cooling.
Using the state description that adsorption tower A is adsorbed as main feed,
S1. adsorption process: unstripped gas passes through adsorption bed from bottom to top, and the organic matter in gas is adsorbed removing and falls, and is not inhaled
The components such as attached nitrogen are continuously expelled to purified gas surge tank at the top of adsorption tower, and emptying system is gone to after pressure regulating system pressure stabilizing
System, i.e. acceptable gas exclude atmosphere.
Regenerate process:
S2. it replaces: purging displacement being carried out to bed with high-purity nitrogen (flow control) after the completion of absorption, until in exit gas
Oxygen content terminates in Con trolling index, replaces pneumatic transmission pretreatment unit；
S3. heat: the nitrogen come out from adsorption tower C cold blowing enters the tower after electric heater is warming up to high temperature, to adsorbent bed
Layer is heated, until bed temperature, which reaches Con trolling index, to be terminated, hot gas out is water cooled-and forecooling heat exchanger-condenser
It is preheated to entering what D tower absorption-came out after room temperature through regeneration gas separating device separation lime set-gas phase after being cooled to -20~-25 DEG C
Gas enters nitrogen circulation surge tank；
S4. it cools down: introducing circulation cold nitrogen and adsorption bed is cooled down, be down to room temperature；
S5. the pre- absorption of regeneration: it is mainly used for coming out adsorption tower B regeneration nitrogen progress preliminary clearning, organic matter in gas is adsorbed
After-purification gas returns to nitrogen circulation surge tank；
S6. regeneration preheats: being heated with circulating nitrogen gas, carries out heating regeneration to adsorbent；
S7. regeneration precools: being cooled down with circulating nitrogen gas, is cooled down to adsorption bed；
S8. regenerative adsorption: the nitrogen for being mainly used for the regeneration preheating outlet come out to adsorption tower B purifies, will be in nitrogen
Organic matter adsorbing and removing；
S9. when the adsorption tower A carries out regeneration and precools, pre-suction adsorption tower B, adsorption tower C, is respectively regenerated in adsorption tower D
Attached, heating, absorption；
S10. when the adsorption tower A carries out regenerating pre- absorption, pre-add adsorption tower B, adsorption tower C, is respectively regenerated in adsorption tower D
Heat, cooling, absorption；
S11. S1-S10 step cycle is operated.
The S1-S11 step is all made of automatic control mode control, i.e., controls beating for valve on pipeline by controller
Open and close are closed, and realization accordingly adsorbs adsorption tower A, adsorption tower B, adsorption tower C, adsorption tower D, replaces, heating, cooling step
Control.
So far, adsorption tower A completes the cyclic process of a complete adsorption-regeneration, and can enter absorption next time and follow
Ring.The adsorption-regeneration operating process of other three adsorption towers is identical with adsorption tower A.
Four tower alternating cycle works, so that the components such as the organic matter in continuous separation removal oil gas are realized, after up to standard
Purification gas directly empty.
Furthermore, it is understood that the adsorption tower A, adsorption tower B, adsorption tower C, the top exit of adsorption tower D and forecooler import
Between be equipped with pipeline g, the pipeline g be equipped with valve, the pipeline g be equipped with oxygen on-line detector, detection adsorption tower A,
Adsorption tower B, adsorption tower C, adsorption tower D displacement the stage, detect whether the oxygen in tower up to standard, it is up to standard just can be carried out it is next
Step.
Furthermore, it is understood that in the entire processing step of the S1-S11, it is real by the way that temperature sensor is arranged on adsorption tower
When monitor the temperature of entire technique, when temperature is excessively high, control valve c is closed, and VOC is forbidden to enter in recovery process equipment.
Furthermore, it is understood that between the adsorption tower A, adsorption tower B, adsorption tower C, adsorption tower D and unstripped gas feed inlet also
Equipped with feed gas preprocessing unit, the feed gas preprocessing unit includes forecooler, VOC condenser and gas-liquid separator m,
The bottom of the gas-liquid separator m is connected to lime set storage tank.Lime set storage tank is to the liquid after tentatively recycling gas-liquid separator b separation
State organic matter.Wherein, forecooler, VOC condensation are also successively arranged on the pipeline between the unstripped gas feed inlet and lime set storage tank
Device.VOC condenser further condenses VOC, improves the efficiency of lime set storage tank recovering liquid organic matter.
Furthermore, it is understood that the bottom at the top of the gas-liquid separator b and adsorption tower A, adsorption tower B, adsorption tower C, adsorption tower D
Portion is connected to by pipeline, and the pipeline is equipped with forecooler, VOC condenser.
The work process of pretreating process: with normal pressure, room temperature enters VOC supercharger and is forced into 40~50KPa(G gas),
70~80 DEG C of outlet temperature enter forecooler (exchanging heat with cold air), enter condenser after heat exchange cools down to 20~25 DEG C, cool down
Enter gas-liquid separator separates lime set after to -20~-25 DEG C, gas phase portion is warming up to~30 DEG C through pre- heat exchange and send raw material gas purifying list
Member.Organic lime set that pretreating process generates enters lime set storage tank, pumps out battery limit (BL).
The above is only a preferred embodiment of the present invention, it should be understood that the present invention is not limited to described herein
Form should not be regarded as an exclusion of other examples, and can be used for other combinations, modifications, and environments, and can be at this
In the text contemplated scope, modifications can be made through the above teachings or related fields of technology or knowledge.And those skilled in the art institute into
Capable modifications and changes do not depart from the spirit and scope of the present invention, then all should be in the protection scope of appended claims of the present invention
It is interior.
Claims (9)
1. a kind of control system of petroleum vapor recovery technique, it is characterised in that: recovery process equipment includes that multiple adsorption towers, nitrogen follow
Loop system unit, refrigeration systems units, heating system unit, the nitrogen circulating system unit, refrigeration systems units, heating system
It unites and is connected between unit, multiple adsorption towers by pipeline, the nitrogen circulating system unit is to provide nitrogen source, the system
Cold control unit and heating system unit are to control nitrogen temperature；
Steps are as follows for recovery process:
S1. unstripped gas is passed through when being adsorbed in one of adsorption tower a, is replaced, is regenerated respectively in remaining adsorption tower
Pre- absorption, regeneration preheating, regeneration precooling, regenerative adsorption, displacement, heating, cooling；
S2. when the adsorption tower a is replaced, absorption and regenerative adsorption are carried out in remaining adsorption tower respectively；
S3. it when the adsorption tower a is heated, adsorbed respectively in remaining adsorption tower, regenerate precooling, regeneration preheating；
S4. it when the adsorption tower a is cooled down, adsorbed respectively in remaining adsorption tower, regenerate pre- absorption, regeneration preheating；
S5. it when the adsorption tower a carries out regenerative adsorption, replaced, adsorbed, regenerative adsorption respectively in remaining adsorption tower；
S6. it when the adsorption tower a carries out regenerating pre- absorption, is respectively heated in remaining adsorption tower, adsorbs, regenerates precooling；
S7. it when the adsorption tower a carries out regeneration preheating, carries out cooling down respectively in remaining adsorption tower, adsorbs, regenerates pre- absorption；
S8. when the adsorption tower a carries out regenerative adsorption, absorption, displacement, absorption are respectively regenerated in remaining adsorption tower；
S9. when the adsorption tower a carries out regeneration precooling, pre- absorption, heating, absorption are respectively regenerated in remaining adsorption tower；
S10. when the adsorption tower a carries out regenerating pre- absorption, preheating, cooling, absorption are respectively regenerated in remaining adsorption tower；
S11. S1-S10 step cycle is operated.
2. a kind of control system of petroleum vapor recovery technique according to claim 1, it is characterised in that: the S1-S11 step
It is all made of automatic control mode control.
3. a kind of control system of petroleum vapor recovery technique according to claim 1, it is characterised in that: whole in the S1-S11
In a processing step, when adsorption tower carries out regeneration heating step, oxygen content is no more than standard value in adsorption tower.
4. a kind of control system of petroleum vapor recovery technique according to claim 1, it is characterised in that: whole in the S1-S11
In a processing step, when adsorption tower carries out displacement step, when by detection adsorption tower gas outlet, the oxygen content in gas is displaced
Exceeded, then control valve c is closed, and high temperature regeneration gas is forbidden to enter in recovery process equipment, the oxygen content in gas out to be replaced
It is up to standard, then control valve c opening, allow high temperature regeneration gas to enter in recovery process equipment.
5. a kind of control system of petroleum vapor recovery technique according to claim 1, it is characterised in that: whole in the S1-S11
In a processing step, by the way that temperature sensor is arranged on adsorption tower, the temperature of entire regeneration technology is monitored in real time, when temperature mistake
Height, control valve c are closed, and high temperature regeneration gas is forbidden to go successively in recovery process equipment.
6. a kind of control system of petroleum vapor recovery technique according to claim 1, it is characterised in that: whole in the S1-S11
In a processing step, the nitrogen gas purity in nitrogen circulating system unit is not less than 99.99%, and nitrogen dew-point temperature is -60 DEG C, nitrogen
Atmospheric pressure is not less than 0.2MPaG, and temperature is room temperature.
7. a kind of control system of petroleum vapor recovery technique according to claim 6, it is characterised in that: whole in the S1-S11
In a processing step, in the refrigeration systems units, coolant media selects -30 DEG C of ethylene glycol, refrigerant pressure 0.25MPaG.
8. a kind of control system of petroleum vapor recovery technique according to claim 1, it is characterised in that: multiple adsorption towers
Respectively adsorption tower A, adsorption tower B, adsorption tower C, adsorption tower D, steps are as follows for recovery process:
S1. raw material oil gas is passed through when being adsorbed in adsorption tower A, replaced respectively in remaining adsorption tower, regenerate pre- absorption,
Regeneration preheating, regeneration precooling, regenerative adsorption, displacement, heating, cooling；
S2. when the adsorption tower A is replaced, adsorption tower B, adsorption tower C, adsorbed in adsorption tower D respectively, regenerative adsorption with
And regenerative adsorption；
S3. it when the adsorption tower A is heated, adsorption tower B, adsorption tower C, adsorbed in adsorption tower D respectively, regenerate pre-cooling
But, regeneration preheating；
S4. it when the adsorption tower A is cooled down, adsorption tower B, adsorption tower C, adsorbed in adsorption tower D respectively, regenerate pre-suction
Attached, regeneration preheating；
S5. when the adsorption tower A carries out regenerative adsorption, adsorption tower B, adsorption tower C, replaced in adsorption tower D, adsorbed respectively,
Regenerative adsorption；
S6. it when the adsorption tower A carries out regenerating pre- absorption, adsorption tower B, adsorption tower C, is respectively heated in adsorption tower D, inhales
Attached, regeneration precools；
S7. when the adsorption tower A carries out regeneration preheating, adsorption tower B, adsorption tower C, carried out in adsorption tower D respectively it is cooling, inhale
Attached, the pre- absorption of regeneration；
S8. when the adsorption tower A carries out regenerative adsorption, adsorption tower B, adsorption tower C, absorption is respectively regenerated in adsorption tower D, is set
It changes, adsorb；
S9. when the adsorption tower A carries out regeneration and precools, pre-suction adsorption tower B, adsorption tower C, is respectively regenerated in adsorption tower D
Attached, heating, absorption；
S10. when the adsorption tower A carries out regenerating pre- absorption, pre-add adsorption tower B, adsorption tower C, is respectively regenerated in adsorption tower D
Heat, cooling, absorption；
S11. S1-S10 step cycle is operated.
9. a kind of control system of petroleum vapor recovery technique according to claim 8, it is characterised in that: in the S1, when
When adsorption tower A is adsorbed, remaining adsorption tower undergoes first stage, second stage, phase III respectively, when the first stage, inhales
Attached tower B, adsorption tower C, absorption, regenerative adsorption, displacement are respectively regenerated in adsorption tower D, when second stage, adsorption tower B, absorption
It is respectively regenerated precooling, the pre- absorption of regeneration, heating in tower C, adsorption tower D, when the phase III, adsorption tower B, adsorption tower C, inhales
Pre- absorption, regeneration preheating, cooling are respectively regenerated in attached tower D.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115893318A (en) * | 2022-12-19 | 2023-04-04 | 南通星球石墨股份有限公司 | Regeneration system for extracting hydrogen chloride and control method |
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2018
- 2018-12-26 CN CN201811603291.8A patent/CN109603408A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115893318A (en) * | 2022-12-19 | 2023-04-04 | 南通星球石墨股份有限公司 | Regeneration system for extracting hydrogen chloride and control method |
| CN115893318B (en) * | 2022-12-19 | 2024-03-12 | 南通星球石墨股份有限公司 | Regeneration system for extracting hydrogen chloride and control method |
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Application publication date: 20190412 |
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