TECHNOLOGY

Automation maximizes
performance for shale wells
Control system

Bob Sherven
Shell International Exploration & Production Inc.
HoustonDavid Mudry
Vinson Process Controls
DallasAl Majek

DRILLING &PRODUCTION

Emerson
HoustonAlthough automation technology has been used for many
years to improve well performance in oil and gas production,
the technology continues to evolve, benefitting both operations and production.
Large drilling programs in the shale plays of North America have created many free-flowing wells. Maintaining optimal performance for so many sites can prove difficult for any
production group.

In the northern Louisiana portion of the Haynesville shaleplay, Shell International Exploration & Production Inc. has
met with success in controlling the free-flow stage of welllifecycles. Each well is equipped with the control system
shown in Fig. 1. Flow from a well is manipulated with a single
automated choke valve.
Measurements taken to obtain this control include delta
pressure (DP) and flow rate from an orifice run feeding a sales
pipeline, and static pressure and temperature of the flowline
feeding a separator.
Several requirements had to be met to obtain the degreeof control needed. The electronic platform must include
customized proportional-integral-derivative (PID) control
loops and coded algorithms; it must also be capable ofperforming American Gas Association style flow computations
and communicating with an existing supervisory control anddata acquisition (scada) system. The units must be rugged
enough for harsh environments and, because of the lack ofelectrical power in the area, capable of functioning on a solarpowered system (Fig. 2).

AUTOMATED CHOKE-CONTROLLED SYSTEM

FIG. 1Lowestflow rate

Greatest
flow rate
Minimumflow
overrideHighpressureoverrideHightemperature
overridePPrimaryflowTHighdifferential
pressureoverride

DP Differential

pressure (black)
Temperature (red)Pressure (blue)

Wellhead

Primary flow valve
ESD

Orifice runz130401OGJdsh01

To salesTECHNOLOGY
For this application, Shell selected theEmerson Remote Operations Controller(ROC) 800 series of equipment.
Production Manager, a software productof Vinson Process Controls, provides theuser interface and enables operators toaccess and modify the system.
The primary focus of the system (Fig.
3) is to maintain a steady flow fromthe well to the sales line, based on an
operator-specified set point. Multiple
overrides come into play, depending onoperating conditions.

Flow ramp
An automated start-up sequence canbe used when a well is first started toachieve minimum flow in a consistent,fast, and easy way. After the well isonline, an operator can gradually ramp
up the flow to the desired rate.
Solar power is often required for remote automation (Fig. 2).
For example, the start-up sequence canbring a well to an initial flowing condition of 2 MMscfd of natuLiquid loadingral gas. An operator may want to reach 10 MMscfd over an 8-hr
Whenever slug flow is present, liquid loading and subsequent
period. After an operator enters a desired end flow rate and time
unloading of the well must be addressed. As the well produces
duration, the valve set point will automatically increase by an inwater, gas flow through the sales line decreases. The system’screment of 1 MMscfd/hr ((10–2 MMscfd)/8 hr) until 10 MMscfd
primary flow control programming responds to this change andis reached. At any time, a set point entered to reduce flow causes
opens the choke to compensate.
prompt reaction and is not subject to a ramping function.
As the well unloads (water decreases), the gas flow

HAYNESVILLE WELL: FLOW RESPONSE*FIG. 3

7
Well flow, MMscfd
Well flow set point, MMscfd
6

5

MMscfd4

32*Primary flow control.

z130401OGJDSH02

0

6:56:46 p.m.
7:21:38 a.m.
7:51:38 p.m.
8:21:39 a.m.
8:51:38 p.m.
9:21:38 a.m.
9:51:38 p.m.
10:21:38 a.m.
10:51:38 p.m.
11:21:38 a.m.
11:51:38 p.m.
12:21:38 p.m.
12:51:38 a.m.
1:17:44 p.m.
1:47:45 a.m.
2:17:44 p.m.
2:47:44 a.m.
3:17:45 p.m.
3:47:44 a.m.
4:17:45 p.m.
4:47:44 a.m.
5:17:44 p.m.
5:47:44 a.m.
6:17:44 p.m.
6:47:44 a.m.
7:17:45 p.m.
7:47:44 a.m.
8:17:45 p.m.
8:47:44 a.m.
9:47:22 p.m.
10:17:23 a.m.
10:47:22 p.m.
11:17:22 a.m.
11:47:22 p.m.
12:17:23 p.m.
12:47:22 a.m.
1:17:22 p.m.
1:47:22 a.m.
2:17:22 p.m.
2:47:22 a.m.
3:17:22 p.m.
3:47:22 a.m.
4:17:22 p.m.
4:47:22 a.m.
5:17:22 p.m.
5:47:22 a.m.
6:17:22 p.m.
6:47:22 a.m.
7:17:22 p.m.
7:47:22 a.m.
8:17:22 p.m.

1

TECHNOLOGY
it can return the well to normal flow
control rapidly.
Another issue associated with producing water is ensuring that the well flowrate exceeds critical velocity. Critical velocity, determined by Turner and Coleman equations,1 2 implies the minimum
rate of flow required from the well to lift
liquids. Flow at less than critical velocity
enables water to collect in the well, eventually curtailing production. In this case,a flow rate value can be entered manuallyor automatically calculated by the ROC
unit using tubing ID, as well as real-timetubing and flowline pressure values.
The programming instructions
within the ROC will select between
the greater of the primary flow control
and the critical velocity set points. In
this way, flow will be maintained at theGas-driven cooler reduces temperature to an acceptable range (Fig. 4).
operator-specified set point until thecritical velocity is reached. The control
system then works to maintain the flow at sufficient rate toincreases quickly. The primary flow control programming willcontinue extracting liquids.
compensate and begin to close the choke; the reaction time,
however, tends to be too slow. It is best to return production
to an optimal level quickly and avoid tripping the well offline
Transient flow conditions
as a result of a high sales line pressure.
Wells in the Haynesville shale play tend to reach vertical depths
To accomplish this, the DP of the orifice run is monitored.
of up to 13,000 ft. Bottomhole pressures reach 10,000 psig withThe DP override can be tuned for faster response; therefore,
temperatures around 325° F. The maximum-allowed tempera-

1,280

10

1,250

8

1,220

6

1,190

4

1,160

0

Well flow, MMscfd
Well flow set point, MMscfd
Flowline pressure, psig
Flowline pressure override set point, psig

1,130

1,100z130401OGJdsh03

2

psig

FIG. 512

8:44:27 p.m.
1:29:27 a.m.
6:14:27 a.m.
10:59:27 a.m.
3:44:27 p.m.
8:29:27 p.m.
1:14:27 a.m.
5:59:27 a.m.
10:44:27 a.m.
3:29:27 p.m.
8:14:27 p.m.
12:59:27 a.m.
5:44:27 a.m.
10:59:27 a.m.
3:44:27 p.m.
8:29:27 p.m.
1:14:27 a.m.
5:59:27 a.m.
6:03:57 p.m.
10:51:38 p.m.
3:36:38 a.m.
8:21:38 a.m.
1:06:38 p.m.
5:51:38 p.m.
10:36:38 p.m.
3:21:38 a.m.
8:06:38 a.m.
12:51:38 p.m.
5:36:38 p.m.
10:21:38 p.m.
3:06:38 a.m.
7:51:39 a.m.
12:36:38 p.m.
5:21:38 p.m.
10:06:39 p.m.
2:51:38 a.m.
7:36:38 a.m.
12:21:38 p.m.
5:06:38 p.m.
9:51:38 p.m.
2:36:38 a.m.
7:21:38 a.m.
12:06:38 p.m.
4:51:38 p.m.
9:36:38 p.m.
2:21:38 a.m.
7:06:38 a.m.

MMscfdHAYNESVILLE: FLOW WITH PRESSURE OVERRIDETECHNOLOGY
ture of a typical sales pipeline is 140° F. A gas engine-driven
cooler (Fig. 4) reduces the surface temperature of the product.
To prevent the well from tripping offline because of awave of high temperature production, a high-temperature
override PID loop responds rapidly to reduce the set point.
Reducing the flow through the heat exchanger helps tomaintain the average temperature at an acceptable level.
Other issues may exist away from the wellsite.
Downstream gas-treating plants sometimes experienceproblems that cause the pipeline to back up. A PID loop will
reduce flow and prevent high-pressure surges from tripping
the well. PID loops in both cases can be tuned as necessary
to adjust the flow to an acceptable rate. The reaction time ismuch less than that possible with the primary flow controlloop configuration.
Fig. 5 shows a response to high pressure. In this example,
the well was flowing at about 10 MMscfd when a pressure spiketo around 1,250 psig caused a sudden flow reduction. The flow
eventually resettled around the primary flow set point with a
new pressure control point determined by the operator.
The following four factors affect the preferred well flow rate:
1. High DP detected on the sales meter.
2. Water production, which may require that the primary
flow rate set point be set to reflect critical velocity.
3. High temperature to the separator, which requires thatthe temperature be reduced to remain within the allowabletemperature range of the sales pipeline.
4. High pressure to the separator, which requires that theflow rate be reduced to avoid high pressure shutdowns.
The programmed instructions of the ROC select the lower
rate of these competing approaches to control the automatedchoke, ensuring that the well is maintained under control
without violating any of the other conditions.
To assist safe operation, switches on site and a remotescada command can initiate an emergency shutdown (ESD)
mode, overriding all other programmed instructions, andattempt immediate closure of the choke.

Economic benefits
The shale boom has greatly intensified the need to hire
personnel in the oil patch. Work is sometimes delayed until
skilled personnel can be hired or contracted or until other
employees can be trained. In addition, local infrastructuresare stressed by the influx of vehicles and people into the
producing areas.
Consequential traffic problems have become a major
incentive to reduce driving time. In this case, the control
system both reduces time spent on the road and frees trained
personnel from hours of rote effort, enabling them to tend toother wells.
Benefits of the control system include the following:• Eliminates driving to restart a well that otherwise

would have tripped offline because of high temperature orhigh pressure short term conditions.
• Enables personnel to get a well online in a faster andsafer manner.
• Eliminates extensive time at a wellsite to perform
actions to achieve an optimal flow rate.
Avoiding deferred production is another benefit. Because
gas production flows to a pipeline, downstream problems ofany type require reducing flow or shutting down the well.
This automated system makes it possible to remotely modify
set points and quickly return wells to operation.

References
1. Coleman, S.B., Clay, H.B., McCurdy, D.G., and Norris,
H.L. III, “A New Look at Predicting Gas-Well Load Up,” Journal ofPetroleum Technology, Vol. 43, No. 3 (March 1991), pp. 329-333.
2. Turner, R.G., Hubbard, M.G., and Dukler, A.E., “Analysisand Prediction of Minimum Flow Rate for the Continuous
Removal of Liquids from Gas Wells,” Journal of Petroleum
Technology, Vol. 21, No. 11 (November 1969), pp. 1475-1482.

The authors
Bob Sherven (bob.sherven@shell.com) is acontrol and automation engineer with Shell
International Exploration & Production Inc. He
has more than 25 years of industry experience
with extensive exposure to instrumentation andcontrol systems. Sherven has been acting as acontrol and automation technical authority supporting onshore gas assets in the US. He has a BS in chemicalengineering from the University of California, Davis and is a
registered professional engineer in California.
David Mudry (david.mudry@vinsonprocess.com)
is an applications specialist for Vinson Process
Controls in Dallas and has more than 20 years ofproduct development experience. He is the architect and developer of Production Manager, anapplication designed for the Emerson ROC andFloBoss product lines specifically to facilitate wellhead optimization and product measurement. Mudry has an AAS
in electronics technology from Odessa College (Odessa, Tex.).
Al Majek (al.majek@emerson.com) is the Oil &Gas Production Area Technical Manager with theEmerson Remote Automation Solutions business
unit. He has more than 30 years of experiencein design, manufacture, and deployment of automation in the oil and gas industry. Majek has aBS in electrical engineering from Rice University.
He is a Six Sigma Green Belt, certified project management
professional, and a registered professional engineer in Texas.

Eprinted and posted with permission to Emerson Process Management from Oil & Gas Financial Journal
April 1 © 2013 PennWell Corporation