CN107686741A

CN107686741A - The oil gas reclaiming technical technology that VOCs zero-emissions save again

Info

Publication number: CN107686741A
Application number: CN201610663824.6A
Authority: CN
Inventors: 王建基
Original assignee: Individual
Current assignee: Individual
Priority date: 2016-08-04
Filing date: 2016-08-04
Publication date: 2018-02-13

Abstract

The oil gas reclaiming technical technology that VOCs zero-emissions save again, VOCs VOCs condensed recyclable 90%, residue 10% plus air enter combustion furnace burning, with combustion heat ammonia absorption refrigeration, can reach energy-conservation 60%.This technology is mainly made up of refrigeration unit, ice chest, combustion furnace, RTO (heat accumulating type heating power incinerator), ammonia refrigeration, electric meter etc..

Description

The oil gas reclaiming technical technology that VOCs zero-emissions save again

One technical field：This technology is to belong to Investigation of Petroleum Vapor Recovery Technology field

Two background technologies：Current domestic oil gas reclaiming technical technology mainly has：Condensing, condensation film separate type, condensation are lived Property charcoal absorption type, compression condensing type, compression condensation UF membrane formula etc..The above Investigation of Petroleum Vapor Recovery Technology process can only achieve Current national standard (GB20950-2007 non-methane hydrocarbon emission ＜ 25g/m3 and NMHC rate of recovery ＞ 95%) and The oil gas reclaiming technical technology in the U.S. mainly uses active carbon absorption technology and combustion power generation technique.

In order to adapt to the requirement for issuing execution of the tighter standard of country, for this, we have developed condensation, burning, ammonia refrigeration oil Gas new recovering technology technology, the technology can realize that zero-emission saves 50%-60% while realizes NMHC rate of recovery ＞ again 90%

Three content of the invention：

1st, oil gas composition is shown in Table 1

The oil gas of table 1 forms table

Sequence number	Component	Content mol%
			1	C1	0.25
2	C2	0.35
			3	C3=	0.25
4	C3	0.54
			5	IC4=	2.93
6	TC4=	3.24
			7	iC4	2.89
8	nC4	6.16
			9	C5=	0.53
10	iC5	2.16
			11	nC5	4.23
12	C6	6.88
			13	AIR	69.59

2nd, petroleum vapor recovery process chart Fig. 1

Four flows describe：(use example 2000nm³/ h petroleum vapor recoveries example describes)

4.1 petroleum vapor recovery parts

2000Nm first³/ h oil gas (30 DEG C/0.1MPa) changes by heat exchanger E101, E201 and oil recovery and tail gas successively After heat, oil gas is cooled to -3.9 DEG C.It is cold that oil gas after cooling enters one-level refrigerator E103 (ammonia absorption type refrigerating evaporator) But to about -27.0 DEG C, one-level refrigerating capacity is 104.4kW.Oil gas after cooling enters primary separator V101 and carries out gas-liquid separation, Separate fuel-displaced 1110.2kg/h.Uncooled oil gas enters extremely -70.0 DEG C of two level refrigerator (compression refigerating machine) refrigeration, refrigerating capacity For 101.6kW, gas-liquid separation is carried out subsequently into second-stage separator V102, second-stage separator about isolates oily 562.4kg/h.Through Non-methane after two-stage refrigeration

Total hydrocarbon yield is up to 91.41%.

4.2 ammonia absorption type refrigerating parts

18.5% (wt) dense ammoniacal liquor separates into rectifying column C201, and tower top goes out pure ammoniacal liquor, and bottom of towe is 11.5% (wt's) Dilute ammoniacal liquor.Rectifying tower bottom is by the flue gas heat supply of RTO devices, and tower top cooled down by air cooler A201, and rectifying column operating pressure is 1760kPa.Pure ammonia sequentially enters ammonia from pressure from return tank of top of the tower and crosses cold air E201, E202 and uncooled tail gas and cold ammonia steam Heat exchange, is cooled to about -0.8 DEG C.The ammoniacal liquor of supercooling throttles by throttling arrangement XV201 and is down to -31.8 DEG C to 110kPa, temperature, Gas-liquid separation is carried out subsequently into ammoniacal liquor flash tank V203, the ammonia steam that gas phase comes out with evaporator is mixed into subcooler E202, it is ammonia steam that liquid phase, which enters evaporator E103 gasifications, releases cold.

Dilute ammoniacal liquor of rectifying column C201 bottom of towe is with after the heat exchange of dense ammoniacal liquor, absorbing the next ammonia of E202 into absorber X201 and steaming Vapour, absorb and release substantial amounts of heat, 45.0 DEG C are cooled to by air cooler A202, to ensure that it is complete that ammonia is absorbed.After absorption Dense ammoniacal liquor enters dense ammoniacal liquor storage tank V202.Then it is forced into by ammoniacal liquor pump P201 after 1780kPa and squeezes into E203 and rectifying column bottom Dilute ammoniacal liquor heat exchange, heat exchange final temperature are 132.5 DEG C.Dense ammoniacal liquor is again introduced into rectifying column rectifying afterwards.Complete a kind of refrigeration cycle.Such as This goes round and begins again, you can ensures device normal operation.

The present apparatus devises coolers of the evaporator E301 of an ammonia absorption type refrigeration as compression refigerating machine group in addition, So as to save the energy consumption of compressor in compression refigerating machine group.

4.3RTO incinerator

Unrecovered tail gas is heated to 35.0 DEG C after heat exchanger E102, E201 successively.With 13500Nm³/ h sky Gas enters RTO incinerators burning F101 together.A flue gas part after burning is used for heating to regenerator in RTO, another part Thermal source as rectifying column C201 bottoms reboiler E204.

Five brief description of the drawings

The petroleum vapor recovery process chart Fig. 1 of accompanying drawing 1

The 2000Nm3/h petroleum vapor recovery computer art flowsheeting figures Fig. 2 of accompanying drawing 2

Six instantiations

1 2000Nm³/ h petroleum vapor recovery computer art flowsheeting figures Fig. 2

2nd, capital equipment technological parameter

6.1 heat exchanger

The heat exchanger process parameter table of table 3

Note：VF is that gasification divides rate.

6.2.2 rectifying column

Rectifying column technological parameter and hydraulic data are shown in Table 4 and table 5.

The rectifying column main technologic parameters of table 4

Project	Unit	Quantity	Remarks
				Number of theoretical plate	-	13	Including reboiler
Input concentration	% (wt)	18.5
				Inlet amount	kg/h	7800
Feed entrance point (theoretical plate)	-	10
				The dilute ammoniacal liquor concentration of bottom of towe	% (wt)	11.5
Bottom of towe produced quantity	kg/h	7184	Go E203 amounts
				Tower top ammonia density	% (wt)	0.999
Overhead extraction amount	kg/h	616	Go E201 amounts
				Design deflation scope	-	0.07
Rectifying tower top pressure	kPa	1760
				Rectifying tower bottom pressure	kPa	1770
Rectifying tower top temperature	℃	44.97
				Rectifying column bottom temperature	℃	172.6
Rectifier column reflux ratio	-	0.69
				Rectifying tower top cools down load	kW	321.4
Rectifying column bottom heating load	kW	496.4

Note：The non-actual plate of theoretical plate, desirable plate efficiency is 0.5 during design.

The rectifying column theoretical plate hydraulic data of table 5

6.2.3 air cooler

The air cooler process parameter table of table 6

Position number	A201	A202
			Thermic load	321.4	373
Medium	Pure ammonia	Dense ammoniacal liquor
			Flow kg/h	1042	7800
Pressure kPa	1760	90
			Inlet temperature DEG C	45.0	62.1
Import gasification divides rate	1.000	0.054
			Outlet temperature DEG C	45.0	45.0
Outlet gasification divides rate	0.000	0.000

6.2.4 pump

The pump technique parameter list of table 7

6.2.5 throttle device

The throttling arrangement process parameter table of table 8

6.2.6 absorber

This technique absorber can be replaced with a jet pump.

The absorber process parameter table of table 9

6.2.7 storage tank

The storage tank process parameter table of table 10

6.2.8 air blower

The air blower process parameter table of table 11

Position number	Medium	Flow Nm³/h	Temperature DEG C	Operating pressure kPa
					G001	Air	13500	20	100

6.2.9RTO device

The RTO process parameter tables of table 12

Seven technical advantages

7.1 energy-conservation

This technology freezes oil gas point two-stage, and first order refrigeration is freezed using ammonia absorption type, and cryogenic temperature is -27 DEG C, system Cold is 104.4kW.The second level uses compression-type refrigeration, and cryogenic temperature is -70 DEG C, refrigerating capacity 101.6kW.Ammonia absorption type system Cold institute's calorific requirement is provided by not absorbing exhaust combustion, without additional heat.Ammonia absorption type refrigeration can also be the second stage compression type system Cold refrigerant condensation provides cold, so as to save the energy consumption of compressor.It can more directly be saved using compression-type refrigeration using this technique About cold more than 50.7%.

Ammonia absorption type kind of refrigeration cycle needs substantial amounts of cooling hot (rectifying tower top and absorber).The ammonia of present apparatus design absorbs Formula refrigeration can replace recirculated cooling water using air-cooled, so as to save substantial amounts of cooling-water consumption.Additionally by optimization, Wo Menli With the pure ammoniacal liquor before the cold supercooling throttling of unrecovered tail gas, the COP that ammonia absorption type freezes is set to improve to 0.419.

The present apparatus has good energy-saving effect in summary.

7.2 zero-emission

This technique can realize the rate of recovery more than 91.0% of NMHC in oil gas, and unrecovered tail gas and excess Air in RTO incinerators completely burned, following table be burning after smoke components, it can be seen that the present apparatus discharge tail gas in not Containing pollutants such as VOCs and CO, it is possible to achieve the zero-emission of pollutant.

The flue gas of table 13 forms table

Claims

1. condensation, burning, ammonia refrigeration technological process.

2. a technology capital equipment has refrigeration unit, ice chest, combustion furnace (RTO), ammonia refrigeration, petroleum vapor recovery and electric instrument Table.